WO2002086029A2 - In situ recovery from a relatively low permeability formation containing heavy hydrocarbons - Google Patents

Abstract

A method for treating a relatively low permeability formation (222) containing heavy hydrocarbons in situ may include providing heat from one or more heat sources (2604,2608) to a portion of the formation (222). The heat may be allowed to transfer from the heat sources (2604, 2608) to a selected section of the formtion (222). The transferred heat may pyrolyze at least some hydrocarbons within the selected section. A mixture of hydrocarbons may be produced from the selected section. In some embodiments, the permeability of a portion of the formation (222) may be increased relative to an initial permeability of the portion.

Description

IN SITU RECOVERY FROM A RELATIVELY LOW PERMEABILITY FORMATION CONTAINING HEAVY HYDROCARBONS

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates generally to methods and systems for production of hydrocarbons, hydrogen, and/or other products from various relatively low permeability formations containing heavy hydrocarbons. Certain embodiments relate to in situ conversion of hydrocarbons to produce hydrocarbons, hydrogen, and/or novel product streams from underground relatively low permeability formations containing heavy hydrocarbons.

2. Description of Related Art

Hydrocarbons obtained from subterranean (e.g., sedimentary) formations are often used as energy resources, as feedstocks, and as consumer products. Concerns over depletion of available hydrocarbon resources and over declining overall quality of produced hydrocarbons have led to development of processes for more efficient recovery, processing and/or use of available hydrocarbon resources. In situ processes may be used to remove hydrocarbon materials from subterranean formations. Chemical and/or physical properties of hydrocarbon material within a subterranean formation may need to be changed to allow hydrocarbon material to be more easily removed from the subterranean formation. The chemical and physical changes may include in situ reactions that produce removable fluids, composition changes, solubility changes, density changes, phase changes, and/or viscosity changes of the hydrocarbon material within the formation. A fluid may be, but is not limited to, a gas, a liquid, an emulsion, a slurry, and/or a stream of solid particles that has flow characteristics similar to liquid flow. Examples of in situ processes utilizing downhole heaters are illustrated in U.S. Patent Nos. 2,634,961 to Ljungstrom, 2,732,195 to Ljungstrom, 2,780,450 to Ljungstrom, 2,789,805 to Ljungstrom, 2,923,535 to

Ljungstrom, and 4,886,118 to Van Meurs et al., each of which is incorporated by reference as if fully set forth herein.

A heat source may be used to heat a subterranean formation. Electric heaters may be used to heat the subterranean formation by radiation and or conduction. An electric heater may resistively heat an element. U.S. Patent No. 2,548,360 to Germain, which is incorporated by reference as if fully set forth herein, describes an electric heating element placed within a viscous oil within a wellbore. The heater element heats and thins the oil to allow the oil to be pumped from the wellbore. U.S. Patent No. 4,716,960 to Eastlund et al., which is incorporated by reference as if fully set forth herein, describes electrically heating tubing of a petroleum well by passing a relatively low voltage current through the tubing to prevent formation of solids. U.S. Patent No. 5,065,818 to Van Egmond, which is incorporated by reference as if fully set forth herein, describes an electric heating element that is cemented into a well borehole without a casing surrounding the heating element.

U.S. Patent No. 6,023,554 to Vinegar et al., which is incorporated by reference as if fully set forth herein, describes an electric heating element that is positioned within a casing. The heating element generates radiant energy that heats the casing. A granular solid fill material may be placed between the casing and the formation. The casing may conductively heat the fill material, which in turn conductively heats the formation.

U.S. Patent No. 4,570,715 to Van Meurs et al., which is incorporated by reference as if fully set forth herein, describes an electric heating element. The heating element has an electrically conductive core, a surrounding layer of insulating material, and a surrounding metallic sheath. The conductive core may have a relatively low resistance at high temperatures. The insulating material may have electrical resistance, compressive strength, and heat conductivity properties that are relatively high at high temperatures. The insulating layer may inhibit arcing from the core to the metallic sheath. The metallic sheath may have tensile strength and creep resistance properties that are relatively high at high temperatures.

U.S. Patent No. 5,060,287 to Van Egmond, which is incoφorated by reference as if fully set forth herein, describes an electrical heating element having a copper-nickel alloy core.

Combustion of a fuel may be used to heat a formation. Combusting a fuel to heat a formation may be more economical than using electricity to heat a formation. Several different types of heaters may use fuel combustion as a heat source that heats a formation. The combustion may take place in the formation, in a well, and/or near the surface. Combustion in the formation may be a fireflood. An oxidizer may be pumped into the formation. The oxidizer may be ignited to advance a fire front towards a production well. Oxidizer pumped into the formation may flow through the formation along fracture lines in the formation. Ignition of the oxidizer may not result in the fire front flowing uniformly through the formation. A flameless combustor may be used to combust a fuel within a well. U.S. Patent Nos. 5,255,742 to Mikus,

5,404,952 to Vinegar et al., 5,862,858 to Wellington et al., and 5,899,269 to Wellington et al., which are incorporated by reference as if fully set forth herein, describe flameless combustors. Flameless combustion may be accomplished by preheating a fuel and combustion air to a temperature above an auto-ignition temperature of the mixture. The fuel and combustion air may be mixed in a heating zone to combust. In the heating zone of the flameless combustor, a catalytic surface may be provided to lower the auto-ignition temperature of the fuel and air mixture.

Heat may be supplied to a formation from a surface heater. The surface heater may produce combustion gases that are circulated through wellbores to heat the formation. Alternately, a surface burner may be used to heat a heat transfer fluid that is passed through a wellbore to heat the formation. Examples of fired heaters, or surface burners that may be used to heat a subterranean formation, are illustrated in U.S. Patent Nos. 6,056,057 to Vinegar et al. and 6,079,499 to Mikus et al., which are both incorporated by reference as if fully set forth herein.

Synthesis gas may be produced in reactors or in situ within a subterranean formation. Synthesis gas may be produced within a reactor by partially oxidizing methane with oxygen. In situ production of synthesis gas may be economically desirable to avoid the expense of building, operating, and maintaining a surface synthesis gas production facility. U.S. Patent No. 4,250,230 to Terry, which is incorporated by reference as if fully set forth herein, describes a system for in situ gasification of coal. A subterranean coal seam is burned from a first well towards a production well. Methane, hydrocarbons, H₂, CO, and other fluids may be removed from the formation through the production well. The H₂ and CO may be separated from the remaining fluid. The H₂ and CO may be sent to fuel cells to generate electricity. U.S. Patent No. 4,057,293 to Garrett, which is incorporated by reference as if fully set forth herein, discloses a process for producing synthesis gas. A portion of a rubble pile is burned to heat the rubble pile to a temperature that generates liquid and gaseous hydrocarbons by pyrolysis. After pyrolysis, the rubble is further heated, and steam or steam and air are introduced to the rubble pile to generate synthesis gas.

U.S. Patent No. 5,554,453 to Steinfeld et al., which is incorporated by reference as if fully set forth herein, describes an ex situ coal gasifier that supplies fuel gas to a fuel cell. The fuel cell produces electricity. A catalytic burner is used to burn exhaust gas from the fuel cell with an oxidant gas to generate heat in the gasifier. Carbon dioxide may be produced from combustion of fuel and from many chemical processes. Carbon dioxide may be used for various purposes, such as, but not limited to, a feed stream for a dry ice production facility, supercritical fluid in a low temperature supercritical fluid process, a flooding agent for coal bed demethanation, and a flooding agent for enhanced oil recovery. Although some carbon dioxide is productively used, many tons of carbon dioxide are vented to the atmosphere.

U.S. Patent No. 2,780,450 to Ljungstrom describes heating bituminous geological formations in situ to convert or crack a liquid tar-like substance into oils and gases.

U.S. Patent No. 4,597,441 to Ware et al, which is incorporated by reference as if fully set forth herein, describes contactmg oil, heat, and hydrogen simultaneously in a reservoir. Hydrogenation may enhance recovery of oil from the reservoir.

U.S. Patent No. 5,046,559 to Glandt and 5,060,726 to Glandt et al., are incoφorated by reference as if fully set forth herein.

Substantial reserves of heavy hydrocarbons are known to exist in formations that have relatively low permeability. For example, billions of barrels of oil reserves are known to exist in diatomaceous formations in California. Several methods have been proposed and/or used for producing heavy hydrocarbons from relatively low permeability formations.

U.S. Patent No. 5,415,231 to Northrop et al., which is incoφorated by reference as if fully set forth herein, describes a method for recovering hydrocarbons (e.g., oil) from a low permeability subterranean reservoir of the type comprised primarily of diatomite. A first slug or volume of a heated fluid (e.g., 60% quality steam) is injected into the reservoir at a pressure greater than the fracturing pressure of the reservoir. The well is then shut in and the reservoir is allowed to soak for a prescribed period (e.g., 10 days or more) to allow the oil to be displaced by the steam into the fractures. The well is then produced until the production rate drops below an economical level. A second slug of steam is then injected and the cycles are repeated.

U.S. Patent No. 4,530,401 to Hartman et al., which is incoφorated by reference as if fully set forth herein, describes a method for the recovery of viscous oil from a subterranean, viscous oil-containing formation by injecting steam into the formation.

U.S. Patent No. 5,339,897 to Leaute et al. describes a method and apparatus for recovering and/or upgrading hydrocarbons utilizing in situ combustion and horizontal wells.

U.S. Patent No. 5,431,224 to Laali, which is incoφorated by reference as if fully set forth herein, describes a method for improving hydrocarbon flow from low permeability tight reservoir rock.

U.S. Patent Nos. 5,297,626 Vinegar et al. and 5,392,854 to Vinegar et al., which are incoφorated by reference as if fully set forth herein, describe a process wherein an oil containing subterranean formation is heated. The following patents are incoφorated herein by reference: U.S. Patent Nos. 6,152,987 to Ma et al.; 5,525,322 to Willms; 5,861,137 to Edlund; and 5,229,102 to Minet et al. As outlined above, there has been a significant amount of effort to develop methods and systems to economically produce hydrocarbons, hydrogen, and/or other products from relatively low permeability formations containing heavy hydrocarbons. At present, however, there are still many relatively low permeability formations containing heavy hydrocarbons from which hydrocarbons, hydrogen, and/or other products cannot be economically produced. Thus, there is still a need for improved methods and systems for production of hydrocarbons, hydrogen, and/or other products from various relatively low permeability formations containing heavy hydrocarbons. SUMMARY OF THE INVENTION

In an embodiment, hydrocarbons within a relatively low permeability formation containing heavy hydrocarbons may be converted in situ within the formation to yield a mixture of relatively high quality hydrocarbon products, hydrogen, and/or other products. One or more heat sources may be used to heat a portion of the relatively low permeability formation containing heavy hydrocarbons to temperatures that allow pyrolysis of the hydrocarbons. Hydrocarbons, hydrogen, and other formation fluids may be removed from the formation through one or more production wells. In some embodiments, formation fluids may be removed in a vapor phase. In other embodiments, formation fluids may be removed in liquid and vapor phases or in a liquid phase. Temperature and pressure in at least a portion of the formation may be controlled during pyrolysis to yield improved products from the formation.

In an embodiment, one or more heat sources may be installed into a formation to heat the formation. Heat sources may be installed by drilling openings (well bores) into the formation. In some embodiments, openings may be formed in the formation using a drill with a steerable motor and an accelerometer. Alternatively, an opening may be formed into the formation by geosteered drilling. Alternately, an opening may be formed into the formation by sonic drilling.

One or more heat sources may be disposed within the opening such that the heat sources transfer heat to the formation. For example, a heat source may be placed in an open wellbore in the formation. Heat may conductively and radiatively transfer from the heat source to the formation. Alternatively, a heat source may be placed within a heater well that may be packed with gravel, sand, and/or cement. The cement may be a refractory cement.

In some embodiments, one or more heat sources may be placed in a pattern within the formation. For example, in one embodiment, an in situ conversion process for hydrocarbons may include heating at least a portion of a relatively low permeability formation containing heavy hydrocarbons with an array of heat sources disposed within the formation. In some embodiments, the array of heat sources can be positioned substantially equidistant from a production well. Certain patterns (e.g., triangular arrays, hexagonal arrays, or other array patterns) may be more desirable for specific applications. In addition, the array of heat sources may be disposed such that a distance between each heat source may be less than about 70 feet (21 m). In addition, the in situ conversion process for hydrocarbons may include heating at least a portion of the formation with heat sources disposed substantially parallel to a boundary of the hydrocarbons. Regardless of the arrangement of or distance between the heat sources, in certain embodiments, a ratio of heat sources to production wells disposed within a formation may be greater than about 3, 5, 8, 10, 20, or more.

Certain embodiments may also include allowing heat to transfer from one or more of the heat sources to a selected section of the heated portion. In an embodiment, the selected section may be disposed between one or more heat sources. For example, the in situ conversion process may also include allowing heat to transfer from one or more heat sources to a selected section of the formation such that heat from one or more of the heat sources pyrolyzes at least some hydrocarbons within the selected section. The in situ conversion process may include heating at least a portion of a relatively low permeability formation containing heavy hydrocarbons above a pyrolyzation temperature of hydrocarbons in the formation. For example, a pyrolyzation temperature may include a temperature of at least about 270 °C. Heat may be allowed to transfer from one or more of the heat sources to the selected section substantially by conduction. One or more heat sources may be located within the formation such that supeφosition of heat produced from one or more heat sources may occur. Supeφosition of heat may increase a temperature of the selected section to a temperature sufficient for pyrolysis of at least some of the hydrocarbons within the selected section. Supeφosition of heat may vary depending on, for example, a spacing between heat sources. The spacing between heat sources may be selected to optimize heating of the section selected for treatment. Therefore, hydrocarbons may be pyrolyzed within a larger area of the portion. Spacing between heat sources may be selected to increase the effectiveness of the heat sources, thereby increasing the economic viability of a selected in situ conversion process for hydrocarbons. Supeφosition of heat tends to increase the uniformity of heat distribution in the section of the formation selected for treatment. Various systems and methods may be used to provide heat sources. In an embodiment, a natural distributed combustor system and method may heat at least a portion of a relatively low permeability formation containing heavy hydrocarbons. The system and method may first include heating a first portion of the formation to a temperature sufficient to support oxidation of at least some of the hydrocarbons therein. One or more conduits may be disposed within one or more openings. One or more of the conduits may provide an oxidizing fluid from an oxidizing fluid source into an opening in the formation. The oxidizing fluid may oxidize at least a portion of the hydrocarbons at a reaction zone within the formation. Oxidation may generate heat at the reaction zone. The generated heat may transfer from the reaction zone to a pyrolysis zone in the formation. The heat may transfer by conduction, radiation, and/or convection. A heated portion of the formation may include the reaction zone and the pyrolysis zone. The heated portion may also be located adjacent to the opening. One or more of the conduits may remove one or more oxidation products from the reaction zone and/or the opening in the formation. Alternatively, additional conduits may remove one or more oxidation products from the reaction zone and/or formation.

In certain embodiments, the flow of oxidizing fluid may be controlled along at least a portion of the length of the reaction zone. In some embodiments, hydrogen may be allowed to transfer into the reaction zone.

In an embodiment, a system and a method may include an opening in the formation extending from a first location on the surface of the earth to a second location on the surface of the earth. For example, the opening may be substantially U-shaped. Heat sources may be placed within the opening to provide heat to at least a portion of the formation.

A conduit may be positioned in the opening extending from the first location to the second location. In an embodiment, a heat source may be positioned proximate and/or in the conduit to provide heat to the conduit. Transfer of the heat through the conduit may provide heat to a selected section of the formation. In some embodiments, an additional heater may be placed in an additional conduit to provide heat to the selected section of the formation through the additional conduit.

In some embodiments, an annulus is formed between a wall of the opening and a wall of the conduit placed within the opening extending from the first location to the second location. A heat source may be place proximate and/or in the annulus to provide heat to a portion the opening. The provided heat may transfer through the annulus to a selected section of the formation.

In an embodiment, a system and method for heating a relatively low permeability formation containing heavy hydrocarbons may include one or more insulated conductors disposed in one or more openings in the formation. The openings may be uncased. Alternatively, the openings may include a casing. As such, the insulated conductors may provide conductive, radiant, or convective heat to at least a portion of the formation. In addition, the system and method may allow heat to transfer from the insulated conductor to a section of the formation. In some embodiments, the insulated conductor may include a copper-nickel alloy. In some embodiments, the insulated conductor may be electrically coupled to two additional insulated conductors in a 3 -phase Y configuration.

An embodiment of a system and method for heating a relatively low permeability formation containing heavy hydrocarbons may include a conductor placed within a conduit (e.g., a conductor-in-conduit heat source).

The conduit may be disposed within the opening. An electric current may be applied to the conductor to provide heat to a portion of the formation. The system may allow heat to transfer from the conductor to a section of the formation during use. In some embodiments, an oxidizing fluid source may be placed proximate an opening in the formation extending from the first location on the earth's surface to the second location on the earth's surface. The oxidizing fluid source may provide oxidizing fluid to a conduit in the opening. The oxidizing fluid may transfer from the conduit to a reaction zone in the formation. In an embodiment, an electrical current may be provided to the conduit to heat a portion of the conduit. The heat may transfer to the reaction zone in the relatively low permeability formation containing heavy hydrocarbons. Oxidizing fluid may then be provided to the conduit. The oxidizing fluid may oxidize hydrocarbons in the reaction zone, thereby generating heat. The generated heat may transfer to a pyrolysis zone and the transferred heat may pyrolyze hydrocarbons within the pyrolysis zone.

In some embodiments, an insulation layer may be coupled to a portion of the conductor. The insulation layer may electrically insulate at least a portion of the conductor from the conduit during use.

In an embodiment, a conductor-in-conduit heat source having a desired length may be assembled. A conductor may be placed within the conduit to form the conductor-in-conduit heat source. Two or more conductor- in-conduit heat sources may be coupled together to form a heat source having the desired length. The conductors of the conductor-in-conduit heat sources may be electrically coupled together. In addition, the conduits may be electrically coupled together. A desired length of the conductor-in-conduit may be placed in an opening in the relatively low permeability formation containing heavy hydrocarbons. In some embodiments, individual sections of the conductor-in-conduit heat source may be coupled using shielded active gas welding. In some embodiments, a centralizer may be used to inhibit movement of the conductor within the conduit.

A centralizer may be placed on the conductor as a heat source is made. In certain embodiments, a protrusion may be placed on the conductor to maintain the location of a centralizer.

In certain embodiments, a heat source of a desired length may be assembled proximate the relatively low permeability formation containing heavy hydrocarbons. The assembled heat sources may then be coiled. The heat source may be placed in the relatively low permeability formation containing heavy hydrocarbons by uncoiling the heat source into the opening in the relatively low permeability formation containing heavy hydrocarbons.

In certain embodiments, portions of the conductors may include an electrically conductive material. Use of the electrically conductive material on a portion (e.g., in the overburden portion) of the conductor may lower an electrical resistance of the conductor. A conductor placed in a conduit may be treated to increase the emissivity of the conductor, in some embodiments. The emissivity of the conductor may be increased by roughening at least a portion of the surface of the conductor. In certain embodiments, the conductor may be treated to increase the emissivity prior to being placed within the conduit. In some embodiments, the conduit may be treated to increase the emissivity of the conduit. In an embodiment, a system and method may include one or more elongated members disposed in an opening in the formation. Each of the elongated members may provide heat to at least a portion of the formation. One or more conduits may be disposed in the opening. One or more of the conduits may provide an oxidizing fluid from an oxidizing fluid source into the opening. In certain embodiments, the oxidizing fluid may inhibit carbon deposition on or proximate the elongated member.

In certain embodiments, an expansion mechanism may be coupled to a heat source. The expansion mechanism may allow the heat source to move during use. For example, the expansion mechanism may allow for the expansion of the heat source during use.

In one embodiment, an in situ method and system for heating a relatively low permeability formation containing heavy hydrocarbons may include providing oxidizing fluid to a first oxidizer placed in an opening in the formation. Fuel may be provided to the first oxidizer and at least some fuel may be oxidized in the first oxidizer. Oxidizing fluid may be provided to a second oxidizer placed in the opening in the formation. Fuel may be provided to the second oxidizer and at least some fuel may be oxidized in the second oxidizer. Heat from oxidation of fuel may be allowed to transfer to a portion of the formation.

An opening in a relatively low permeability formation containing heavy hydrocarbons may include a first elongated portion, a second elongated portion, and a third elongated portion. Certain embodiments of a method and system for heating a relatively low permeability formation containing heavy hydrocarbons may include providing heat from a first heater placed in the second elongated portion. The second elongated portion may diverge from the first elongated portion in a first direction. The third elongated portion may diverge from the first elongated portion in a second direction. The first direction may be substantially different than the second direction. Heat may be provided from a second heater placed in the third elongated portion of the opening in the formation. Heat from the first heater and the second heater may be allowed to transfer to a portion of the formation.

An embodiment of a method and system for heating a relatively low permeability formation containing heavy hydrocarbons may include providing oxidizing fluid to a first oxidizer placed in an opening in the formation. Fuel may be provided to the first oxidizer and at least some fuel may be oxidized in the first oxidizer. The method may further include allowing heat from oxidation of fuel to transfer to a portion of the formation and allowing heat to transfer from a heater placed in the opening to a portion of the formation.

In an embodiment, a system and method for heating a relatively low permeability formation containing heavy hydrocarbons may include oxidizing a fuel fluid in a heater. The method may further include providing at least a portion of the oxidized fuel fluid into a conduit disposed in an opening in the formation. In addition, additional heat may be transferred from an electric heater disposed in the opening to the section of the formation. Heat may be allowed to transfer uniformly along a length of the opening.

Energy input costs may be reduced in some embodiments of systems and methods described above. For example, an energy input cost may be reduced by heating a portion of a relatively low permeability formation containing heavy hydrocarbons by oxidation in combination with heating the portion of the formation by an electric heater. The electric heater may be turned down and/or off when the oxidation reaction begins to provide sufficient heat to the formation. Electrical energy costs associated with heating at least a portion of a formation with an electric heater may be reduced. Thus, a more economical process may be provided for heating a relatively low permeability formation containing heavy hydrocarbons in comparison to heating by a conventional method. In addition, the oxidation reaction may be propagated slowly through a greater portion of the formation such that fewer heat sources may be required to heat such a greater portion in comparison to heating by a conventional method. Certain embodiments as described herein may provide a lower cost system and method for heating a relatively low permeability formation containing heavy hydrocarbons. For example, certain embodiments may more uniformly transfer heat along a length of a heater. Such a length of a heater may be greater than about 300 m or possibly greater than about 600 m. In addition, in certain embodiments, heat may be provided to the formation more efficiently by radiation. Furthermore, certain embodiments of systems may have a substantially longer lifetime than presently available systems.

In an embodiment, an in situ conversion system and method for hydrocarbons may include maintaining a portion of the formation in a substantially unheated condition. The portion may provide structural strength to the formation and/or confinement/isolation to certain regions of the formation. A processed relatively low permeability formation containing heavy hydrocarbons may have alternating heated and substantially unheated portions arranged in a pattern that may, in some embodiments, resemble a checkerboard pattern, or a pattern of alternating areas (e.g., strips) of heated and unheated portions.

In an embodiment, a heat source may advantageously heat only along a selected portion or selected portions of a length of the heater. For example, a formation may include several hydrocarbon containing layers. One or more of the hydrocarbon containing layers may be separated by layers containing little or no hydrocarbons.

A heat source may include several discrete high heating zones that may be separated by low heating zones. The high heating zones may be disposed proximate hydrocarbon containing layers such that the layers may be heated. The low heating zones may be disposed proximate layers containing little or no hydrocarbons such that the layers may not be substantially heated. For example, an electric heater may include one or more low resistance heater sections and one or more high resistance heater sections. Low resistance heater sections of the electric heater may be disposed in and/or proximate layers containing little or no hydrocarbons. In addition, high resistance heater sections of the electric heater may be disposed proximate hydrocarbon containing layers. In an additional example, a fueled heater (e.g., surface burner) may include insulated sections. Insulated sections of the fueled heater may be placed proximate or adjacent to layers containing little or no hydrocarbons. Alternately, a heater with distributed air and/or fuel may be configured such that little or no fuel may be combusted proximate or adjacent to layers containing little or no hydrocarbons. Such a fueled heater may include flameless combustors and natural distributed combustors.

In certain embodiments, the permeability of a relatively low permeability formation containing heavy hydrocarbons may vary within the formation. For example, a first section may have a lower permeability than a second section. In an embodiment, heat may be provided to the formation to pyrolyze hydrocarbons within the lower permeability first section. Pyrolysis products may be produced from the higher permeability second section in a mixture of hydrocarbons.

In an embodiment, a heating rate of the formation may be slowly raised through the pyrolysis temperature range. For example, an in situ conversion process for hydrocarbons may include heating at least a portion of a relatively low permeability formation containing heavy hydrocarbons to raise an average temperature of the portion above about 270 °C by a rate less than a selected amount (e.g., about 10 °C, 5 °C, 3 °C, 1 °C, 0.5 °C, or 0.1 °C) per day. In a further embodiment, the portion may be heated such that an average temperature of the selected section may be less than about 375 °C or, in some embodiments, less than about 400 °C.

In an embodiment, a temperature of the portion may be monitored through a test well disposed in a formation. For example, the test well may be positioned in a formation between a first heat source and a second heat source. Certain systems and methods may include controlling the heat from the first heat source and/or the second heat source to raise the monitored temperature at the test well at a rate of less than about a selected amount per day. In addition or alternatively, a temperature of the portion may be monitored at a production well. An in situ conversion process for hydrocarbons may include controlling the heat from the first heat source and/or the second heat source to raise the monitored temperature at the production well at a rate of less than a selected amount per day.

An embodiment of an in situ method of measuring a temperature within a wellbore may include providing a pressure wave from a pressure wave source into the wellbore. The wellbore may include a plurality of discontinuities along a length of the wellbore. The method further includes measuring a reflection signal of the pressure wave and using the reflection signal to assess at least one temperature between at least two discontinuities. Certain embodiments may include heating a selected volume of a relatively low permeability formation containing heavy hydrocarbons. Heat may be provided to the selected volume by providing power to one or more heat sources. Power may be defined as heating energy per day provided to the selected volume. A power (Pwr) required to generate a heating rate (h, in units of, for example, °C/day) in a selected volume (V) of a relatively low permeability formation containing heavy hydrocarbons may be determined by EQN. 1 :

(1) Pwr = h*V*C_v*p_B.

In this equation, an average heat capacity of the formation (C_v) and an average bulk density of the formation (p_B) may be estimated or determined using one or more samples taken from the relatively low permeability formation containing heavy hydrocarbons.

Certain embodiments may include raising and maintaining a pressure in a relatively low permeability formation containing heavy hydrocarbons. Pressure may be, for example, controlled within a range of about 2 bars absolute to about 20 bars absolute. For example, the process may include controlling a pressure within a majority of a selected section of a heated portion of the formation. The controlled pressure may be above about 2 bars absolute during pyrolysis. In an alternate embodiment, an in situ conversion process for hydrocarbons may include raising and maintaining the pressure in the formation within a range of about 20 bars absolute to about 36 bars absolute.

In an embodiment, compositions and properties of formation fluids produced by an in situ conversion process for hydrocarbons may vary depending on, for example, conditions within a relatively low permeability formation containing heavy hydrocarbons.

Certain embodiments may include controlling the heat provided to at least a portion of the formation such that production of less desirable products in the portion may be inhibited. Controlling the heat provided to at least a portion of the formation may also increase the uniformity of permeability within the formation. For example, controlling the heating of the formation to inhibit production of less desirable products may, in some embodiments, include controlling the heating rate to less than a selected amount (e.g., 10 °C, 5 °C, 3 °C, 1 °C, 0.5 °C, or 0.1 °C) per day.

Controlling pressure, heat and/or heating rates of a selected section in a formation may increase production of selected formation fluids. For example, the amount and/or rate of heating may be controlled to produce formation fluids having an American Petroleum Institute ("API") gravity greater than about 25. Heat and/or pressure may be controlled to inhibit production of olefins in the produced fluids. Controlling formation conditions to control the pressure of hydrogen in the produced fluid may result in improved qualities of the produced fluids. In some embodiments, it may be desirable to control formation conditions so that the partial pressure of hydrogen in a produced fluid is greater than about 0.5 bars absolute, as measured at a production well. In one embodiment, a method of treating a relatively low permeability formation containing heavy hydrocarbons in situ may include adding hydrogen to the selected section after a temperature of the selected section is at least about 270 °C. Other embodiments may include controlling a temperature of the formation by selectively adding hydrogen to the formation.

In certain embodiments, a relatively low permeability formation containing heavy hydrocarbons may be treated in situ with a heat transfer fluid such as steam. In an embodiment, a method of formation may include injecting a heat transfer fluid into a formation. Heat from the heat transfer fluid may transfer to a selected section of the formation. The heat from the heat transfer fluid may pyrolyze a substantial portion of the hydrocarbons within the selected section of the formation. The produced gas mixture may include hydrocarbons with an average API gravity greater than about 25°. Furthermore, treating a hydrocarbon-containing formation with a heat transfer fluid may also mobilize hydrocarbons in the formation. In an embodiment, a method of treating a formation may include injecting a heat transfer fluid into a formation, allowing the heat from the heat transfer fluid to transfer to a selected first section of the formation, and mobilizing and pyrolyzing at least some of the hydrocarbons within the selected first section of the formation. At least some of the mobilized hydrocarbons may flow from the selected first section of the formation to a selected second section of the formation. The heat may pyrolyze at least some of the hydrocarbons within the selected second section of the formation. A gas mixture may be produced from the formation.

Another embodiment of treating a formation with a heat transfer fluid may include a moving heat transfer fluid front. A method may include injecting a heat transfer fluid into a formation and allowing the heat transfer fluid to migrate through the formation. A size of a selected section may increase as a heat transfer fluid front migrates through an untreated portion of the formation. The selected section is a portion of the foπnation treated by the heat transfer fluid. Heat from the heat transfer fluid may transfer heat to the selected section. The heat may pyrolyze at least some of the hydrocarbons within the selected section of the formation. The heat may also mobilize at least some of the hydrocarbons at the heat transfer fluid front. The mobilized hydrocarbons may flow substantially parallel to the heat transfer fluid front. The heat may pyrolyze at least a portion of the hydrocarbons in the mobilized fluid and a gas mixture may be produced from the formation.

Simulations may be utilized to increase an understanding of in situ processes. Simulations may model heating of the formation from heat sources and the transfer of heat to a selected section of the formation. Simulations may require the input of model parameters, properties of the formation, operating conditions, process characteristics, and or desired parameters to determine operating conditions. Simulations may assess various aspects of an in situ process. For example, various aspects may include, but not be limited to, deformation characteristics, heating rates, temperatures within the formation, pressures, time to first produced fluids, and/or compositions of produced fluids.

Systems utilized in conducting simulations may include a central processing unit (CPU), a data memory, and a system memory. The system memory and the data memory may be coupled to the CPU. Computer programs executable to implement simulations may be stored on the system memory. Carrier mediums may include program instructions that are computer-executable to simulate the in situ processes. In one embodiment, a computer-implemented method and system of treating a relatively low permeability formation containing heavy hydrocarbons may include providing to a computational system at least one set of operating conditions of an in situ system being used to apply heat to a formation. The in situ system may include at least one heat source. The method may further include providing to the computational system at least one desired parameter for the in situ system. The computational system may be used to determine at least one additional operating condition of the formation to achieve the desired parameter.

In an embodiment, operating conditions may be determined by measuring at least one property of the foπnation. At least one measured property may be input into a computer executable program. At least one property of formation fluids selected to be produced from the foπnation may also be input into the computer executable program. The program may be operable to determine a set of operating conditions from at least the one or more measured properties. The program may also determine the set of operating conditions from at least one property of the selected formation fluids. The determined set of operating conditions may increase production of selected formation fluids from the formation.

In some embodiments, a property of the formation and an operating condition used in the in situ process may be provided to a computer system to model the in situ process to determine a process characteristic.

In an embodiment, a heat input rate for an in situ process from two or more heat sources may be simulated on a computer system. A desired parameter of the in situ process may be provided to the simulation. The heat input rate from the heat sources may be controlled to achieve the desired parameter.

Alternatively, a heat input property may be provided to a computer system to assess heat injection rate data using a simulation. In addition, a property of the formation may be provided to the computer system. The property and the heat injection rate data may be utilized by a second simulation to determine a process characteristic for the in situ process as a function of time.

Values for the model parameters may be adjusted using process characteristics from a series of simulations. The model parameters may be adjusted such that the simulated process characteristics coπespond to process characteristics in situ. After the model parameters have been modified to correspond to the in situ process, a process characteristic or a set of process characteristics based on the modified model parameters may be determined. In certain embodiments, multiple simulations may be run such that the simulated process characteristics correspond to the process characteristics in situ.

In some embodiments, operating conditions may be supplied to a simulation to assess a process characteristic. Additionally, a desired value of a process characteristic for the in situ process may be provided to the simulation to assess an operating condition that yields the desired value.

In certain embodiments, databases in memory on a computer may be used to store relationships between model parameters, properties of the formation, operating conditions, process characteristics, desired parameters, etc. These databases may be accessed by the simulations to obtain inputs. For example, after desired values of process characteristics are provided to simulations, an operating condition may be assessed to achieve the desired values using these databases.

In some embodiments, computer systems may utilize inputs in a simulation to assess information about the in situ process. In some embodiments, the assessed information may be used to operate the in situ process. Alternatively, the assessed information and a desired parameter may be provided to a second simulation to obtain information. This obtained information may be used to operate the in situ process. In an embodiment, a method of modeling may include simulating one or more stages of the in situ process. Operating conditions from the one or more stages may be provided to a simulation to assess a process characteristic of the one or more stages.

In an embodiment, operating conditions may be assessed by measuring at least one property of the formation. At least the measured properties may be input into a computer executable program. At least one property of formation fluids selected to be produced from the formation may also be input into the computer executable program. The program may be operable to assess a set of operating conditions from at least the one or more measured properties. The program may also determine the set of operating conditions from at least one property of the selected formation fluids. The assessed set of operating conditions may increase production of selected formation fluids from the formation.

In one embodiment, a method for controlling an in situ system of treating a relatively low permeability formation containing heavy hydrocarbons may include monitoring at least one acoustic event within the formation using at least one acoustic detector placed within a wellbore in the formation. At least one acoustic event may be recorded with an acoustic monitoring system. The method may also include analyzing the at least one acoustic event to determine at least one property of the formation. The in situ system may be controlled based on the analysis of the at least one acoustic event.

An embodiment of a method of determining a heating rate for treating a relatively low peπneability formation containing heavy hydrocarbons in situ may include conducting an experiment at a relatively constant heating rate. The results of the experiment may be used to determine a heating rate for treating the formation in situ. The determined heating rate may be used to determine a well spacing in the formation.

In an embodiment, a method of predicting characteristics of a formation fluid may include determining an isothermal heating temperature that corresponds to a selected heating rate for the formation. The determined isothermal temperature may be used in an experiment to deteπnine at least one product characteristic of the formation fluid produced from the formation for the selected heating rate. Certain embodiments may include altering a composition of formation fluids produced from a relatively low permeability formation containing heavy hydrocarbons by altering a location of a production well with respect to a heater well. For example, a production well may be located with respect to a heater well such that a non-condensable gas fraction of produced hydrocarbon fluids may be larger than a condensable gas fraction of the produced hydrocarbon fluids.

Condensable hydrocarbons produced from the formation will typically include paraffins, cycloalkanes, mono-aromatics, and di-aromatics as major components. Such condensable hydrocarbons may also include other components such as tri-aromatics, etc.

In certain embodiments, a majority of the hydrocarbons in produced fluid may have a carbon number of less than approximately 25. Alternatively, less than about 15 weight % of the hydrocarbons in the fluid may have a carbon number greater than approximately 25. In other embodiments, fluid produced may have a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, of greater than approximately 1. The non- condensable hydrocarbons may include, but are not limited to, hydrocarbons having carbon numbers less than 5.

In certain embodiments, the API gravity of the hydrocarbons in produced fluid may be approximately 25 or above (e.g., 30, 40, 50, etc.). In certain embodiments, the hydrogen to carbon atomic ratio in produced fluid may be at least approximately 1J (e.g., 1.8, 1.9, etc.). Condensable hydrocarbons of a produced fluid may also include olefins. For example, the olefin content of the condensable hydrocarbons may be from about 0.1 weight % to about 15 weight %. Alternatively, the olefin content of the condensable hydrocarbons may be from about 0.1 weight % to about 2.5 weight % or, in some embodiments, less than about 5 weight %.

Non-condensable hydrocarbons of a produced fluid may also include olefins. For example, the olefin content of the non-condensable hydrocarbons may be gauged using the ethene/ethane molar ratio. In certain embodiments, the ethene/ethane molar ratio may range from about 0.001 to about 0.15.

Fluid produced from the formation may include aromatic compounds. For example, the condensable hydrocarbons may include an amount of aromatic compounds greater than about 20 weight % or about 25 weight % of the condensable hydrocarbons. The condensable hydrocarbons may also include relatively low amounts of compounds with more than two rings in them (e.g., tri-aromatics or above). For example, the condensable hydrocarbons may include less than about 1 weight %, 2 weight %, or about 5 weight % of tri-aromatics or above in the condensable hydrocarbons.

In particular, in certain embodiments, asphaltenes (i.e., large multi-ring aromatics that are substantially insoluble in hydrocarbons) make up less than about 0.1 weight % of the condensable hydrocarbons. For example, the condensable hydrocarbons may include an asphaltene component of from about 0.0 weight % to about 0.1 weight % or, in some embodiments, less than about 0.3 weight %.

Condensable hydrocarbons of a produced fluid may also include relatively large amounts of cycloalkanes. For example, the condensable hydrocarbons may include a cycloalkane component of up to 30 weight % (e.g., from about 5 weight % to about 30 weight %) of the condensable hydrocarbons.

In certain embodiments, the condensable hydrocarbons of the fluid produced from a formation may include compounds containing nitrogen. For example, less than about 1 weight % (when calculated on an elemental basis) of the condensable hydrocarbons is nitrogen (e.g., typically the nitrogen is in nitrogen containing compounds such as pyridines, amines, amides, etc.).

In certain embodiments, the condensable hydrocarbons of the fluid produced from a formation may include compounds containing oxygen. For example, in certain embodiments, less than about 1 weight % (when calculated on an elemental basis) of the condensable hydrocarbons is oxygen (e.g., typically the oxygen is in oxygen containing compounds such as phenols, substituted phenols, ketones, etc.).

In certain embodiments, the condensable hydrocarbons of the fluid produced from a formation may include compounds containing sulfur. For example, less than about 1 weight % (when calculated on an elemental basis) of the condensable hydrocarbons is sulfur (e.g., typically the sulfur is in sulfur containing compounds such as thiophenes, mercaptans, etc.).

Furthermore, the fluid produced from the formation may include ammonia (typically the ammonia condenses with the water, if any, produced from the formation). For example, the fluid produced from the formation may in certain embodiments include about 0.05 weight % or more of ammonia.

Furthermore, a produced fluid from the formation may also include molecular hydrogen (H₂), water, carbon dioxide, hydrogen sulfide, etc. For example, the fluid may include a H₂ content between about 10 volume % and about 80 volume % of the non-condensable hydrocarbons.

In an embodiment, an in situ conversion process for treating a relatively low permeability formation containing heavy hydrocarbons may include providing heat to a section of the formation to yield greater than about 60 weight % of the hydrocarbons. Formation fluids produced from a section of the formation may contain one or more components that may be separated from the formation fluids. In addition, conditions within the formation may be controlled to increase production of a desired component.

In certain embodiments, a method of converting pyrolysis fluids into olefins may include converting formation fluids into olefins. An embodiment may include separating olefins from fluids produced from a formation.

An embodiment of a method of enhancing BTEX compounds (i.e., benzene, toluene, ethylbenzene, and xylene compounds) produced in situ in a relatively low permeability formation containing heavy hydrocarbons may include controlling at least one condition within a portion of the formation to enhance production of BTEX compounds in formation fluid. In another embodiment, a method may include separating at least a portion of the

BTEX compounds from the formation fluid. In addition, the BTEX compounds may be separated from the formation fluids after the formation fluids are produced. In other embodiments, at least a portion of the produced formation fluids may be converted into BTEX compounds.

In one embodiment, a method of enhancing naphthalene production from an in situ relatively low permeability formation containing heavy hydrocarbons may include controlling at least one condition within at least a portion of the formation to enhance production of naphthalene in formation fluid. In another embodiment, naphthalene may be separated from produced formation fluids.

Certain embodiments of a method of enhancing anthracene production from an in situ relatively low permeability formation containing heavy hydrocarbons may include controlling at least one condition within at least a portion of the formation to enhance production of anthracene in formation fluid. In an embodiment, anthracene may be separated from produced formation fluids.

In one embodiment, a method of separating ammonia from fluids produced from an in situ relatively low permeability formation containing heavy hydrocarbons may include separating at least a portion of the ammonia from the produced fluid. Furthermore, an embodiment of a method of generating ammonia from fluids produced from a formation may include hydrotreating at least a portion of the produced fluids to generate ammonia.

In an embodiment, a method of enhancing pyridines production from an in situ relatively low permeability formation containing heavy hydrocarbons may include controlling at least one condition within at least a portion of the formation to enhance production of pyridines in formation fluid. Additionally, pyridines may be separated from produced formation fluids. In certain embodiments, a method of selecting a relatively low permeability formation containing heavy hydrocarbons to be treated in situ such that production of pyridines is enhanced may include examining pyridines concentrations in a plurality of samples from relatively low permeability foπnations containing heavy hydrocarbons. The method may further include selecting a formation for treatment at least partially based on the pyridines concentrations. Consequently, the production of pyridines to be produced from the formation may be enhanced.

In an embodiment, a method of enhancing pyrroles production from an in situ relatively low permeability formation containing heavy hydrocarbons may include controlling at least one condition within at least a portion of the formation to enhance production of pyrroles in formation fluid. In addition, pyπoles may be separated from produced formation fluids. In certain embodiments, a relatively low permeability foπnation containing heavy hydrocarbons to be treated in situ may be selected such that production of pyrroles is enhanced. The method may include examining pyrroles concentrations in a plurality of samples from relatively low permeability formations containing heavy hydrocarbons. The formation may be selected for treatment at least partially based on the pyrroles concentrations, thereby enhancing the production of pyrroles to be produced from such formation.

In one embodiment, thiophenes production from an in situ relatively low permeability formation containing heavy hydrocarbons may be enhanced by controlling at least one condition within at least a portion of the formation to enhance production of thiophenes in formation fluid. Additionally, the thiophenes may be separated from produced formation fluids.

An embodiment of a method of selecting a relatively low permeability formation containing heavy hydrocarbons to be treated in situ such that production of thiophenes is enhanced may include examining thiophenes concentrations in a plurality of samples from relatively low permeability formations containing heavy hydrocarbons. The method may further include selecting a formation for treatment at least partially based on the thiophenes concentrations, thereby enhancing the production of thiophenes from such formations.

Certain embodiments may include providing a reducing agent to at least a portion of the formation. A reducing agent provided to a portion of the formation during heating may increase production of selected formation fluids. A reducing agent may include, but is not limited to, molecular hydrogen. For example, pyrolyzing at least some hydrocarbons in a relatively low permeability formation containing heavy hydrocarbons may include forming hydrocarbon fragments. Such hydrocarbon fragments may react with each other and other compounds present in the formation. Reaction of these hydrocarbon fragments may increase production of olefin and aromatic compounds from the formation. Therefore, a reducing agent provided to the formation may react with hydrocarbon fragments to form selected products and/or inhibit the production of non-selected products.

In an embodiment, a hydrogenation reaction between a reducing agent provided to a relatively low permeability formation containing heavy hydrocarbons and at least some of the hydrocarbons within the formation may generate heat. The generated heat may be allowed to transfer such that at least a portion of the formation may be heated. A reducing agent such as molecular hydrogen may also be autogenously generated within a portion of a relatively low permeability formation containing heavy hydrocarbons during an in situ conversion process for hydrocarbons. The autogenously generated molecular hydrogen may hydrogenate formation fluids within the formation. Allowing formation waters to contact hot carbon in the spent formation may generate molecular hydrogen. Cracking an injected hydrocarbon fluid may also generate molecular hydrogen.

Certain embodiments may also include providing a fluid produced in a first portion of a relatively low permeability formation containing heavy hydrocarbons to a second portion of the formation. A fluid produced in a first portion of a relatively low permeability formation containing heavy hydrocarbons may be used to produce a reducing environment in a second portion of the formation. For example, molecular hydrogen generated in a first portion of a formation may be provided to a second portion of the formation. Alternatively, at least a portion of formation fluids produced from a first portion of the formation may be provided to a second portion of the formation to provide a reducing environment within the second portion.

In an embodiment, a method for hydrotreating a compound in a heated formation in situ may include controlling the H₂ partial pressure in a selected section of the formation, such that sufficient H₂ may be present in the selected section of the formation for hydrotreating. The method may further include providing a compound for hydrotreating to at least the selected section of the formation and producing a mixture from the formation that includes at least some of the hydrotreated compound. In certain embodiments, a mass of at least a portion of the formation may be reduced due, for example, to the production of formation fluids from the foπnation. As such, a permeability and porosity of at least a portion of the formation may increase. In addition, removing water during the heating may also increase the permeability and porosity of at least a portion of the formation. Certain embodiments may include increasing a permeability of at least a portion of a relatively low permeability formation containing heavy hydrocarbons to greater than about 0.01, 0.1, 1, 10, 20, and/or 50 darcy. In addition, certain embodiments may include substantially uniformly increasing a permeability of at least a portion of a relatively low permeability foπnation containing heavy hydrocarbons. Some embodiments may include increasing a porosity of at least a portion of a relatively low permeability formation containing heavy hydrocarbons substantially uniformly.

Certain systems and methods may be used to treat heavy hydrocarbons in at least a portion of a relatively low permeability formation (e.g., in "tight" formations that contain heavy hydrocarbons). Such heavy hydrocarbons may be heated to pyrolyze at least some of the heavy hydrocarbons in a selected section of the formation. Heating may also increase the permeability of at least a portion of the selected section. Fluids generated from pyrolysis may be produced from the formation.

Certain embodiments for treating heavy hydrocarbons in a relatively low permeability formation may include providing heat from one or more heat sources to pyrolyze some of the heavy hydrocarbons and then to vaporize a portion of the heavy hydrocarbons. The heat sources may pyrolyze at least some heavy hydrocarbons in a selected section of the formation and may pressurize at least a portion of the selected section. During the heating, the pressure within the formation may increase substantially. The pressure in the formation may be controlled such that the pressure in the formation may be maintained to produce a fluid of a desired composition. Pyrolyzation fluid may be removed from the formation as vapor from one or more heater wells by using the back pressure created by heating the formation.

Certain embodiments for treating heavy hydrocarbons in at least a portion of a relatively low permeability formation may include heating to create a pyrolysis zone and heating a selected second section to less than the average temperature within the pyrolysis zone. Heavy hydrocarbons may be pyrolyzed in the pyrolysis zone. Heating the selected second section may decrease the viscosity of some of the heavy hydrocarbons in the selected second section to create a low viscosity zone. The decrease in viscosity of the fluid in the selected second section may be sufficient such that at least some heated heavy hydrocarbons within the selected second section may flow into the pyrolysis zone. Pyrolyzation fluid may be produced from the pyrolysis zone. In one embodiment, the density of the heat sources in the pyrolysis zone may be greater than in the low viscosity zone.

In certain embodiments, it may be desirable to create the pyrolysis zones and low viscosity zones sequentially over time. The heat sources in a region near a desired pyrolysis zone may be activated first, resulting in establishment of a substantially uniform pyrolysis zone after a period of time. Once the pyrolysis zone is established, heat sources in the low viscosity zone may be activated sequentially from nearest to farthest from the pyrolysis zone.

A heated formation may also be used to produce synthesis gas. Synthesis gas may be produced from the formation prior to or subsequent to producing a formation fluid from the formation. For example, synthesis gas generation may be commenced before and/or after formation fluid production decreases to an uneconomical level. Heat provided to pyrolyze hydrocarbons within the formation may also be used to generate synthesis gas. For example, if a portion of the formation is at a temperature from approximately 270 °C to approximately 375 °C (or 400 °C in some embodiments) after pyrolyzation, then less additional heat is generally required to heat such portion to a temperature sufficient to support synthesis gas generation.

In certain embodiments, synthesis gas is produced after production of pyrolysis fluids. For example, after pyrolysis of a portion of a foπnation, synthesis gas may be produced from carbon and/or hydrocarbons remaining within the formation. Pyrolysis of the portion may produce a relatively high, substantially uniform permeability throughout the portion. Such a relatively high, substantially uniform permeability may allow generation of synthesis gas from a significant portion of the formation at relatively low pressures. The portion may also have a large surface area and/or surface areavolume. The large surface area may allow synthesis gas producing reactions to be substantially at equilibrium conditions during synthesis gas generation. The relatively high, substantially uniform permeability may result in a relatively high recovery efficiency of synthesis gas, as compared to synthesis gas generation in a relatively low permeability formation containing heavy hydrocarbons that has not been so treated.

Pyrolysis of at least some hydrocarbons may in some embodiments convert about 15 weight % or more of the carbon initially available. Synthesis gas generation may convert approximately up to an additional 80 weight % or more of carbon initially available within the portion. In situ production of synthesis gas from a relatively low permeability formation containing heavy hydrocarbons may allow conversion of larger amounts of carbon initially available within the portion. The amount of conversion achieved may, in some embodiments, be limited by subsidence concerns.

Certain embodiments may include providing heat from one or more heat sources to heat the formation to a temperature sufficient to allow synthesis gas generation (e.g., in a range of approximately 400 °C to approximately

1200 °C or higher). At a lower end of the temperature range, generated synthesis gas may have a high hydrogen

(H₂) to carbon monoxide (CO) ratio. At an upper end of the temperature range, generated synthesis gas may include mostly H₂ and CO in lower ratios (e.g., approximately a 1:1 ratio).

Heat sources for synthesis gas production may include any of the heat sources as described in any of the embodiments set forth herein. Alternatively, heating may include transferring heat from a heat transfer fluid (e.g., steam or combustion products from a burner) flowing within a plurality of wellbores within the formation.

A synthesis gas generating fluid (e.g., liquid water, steam, carbon dioxide, air, oxygen, hydrocarbons, and mixtures thereof) may be provided to the foπnation. For example, the synthesis gas generating fluid mixture may include steam and oxygen. In an embodiment, a synthesis gas generating fluid may include aqueous fluid produced by pyrolysis of at least some hydrocarbons within one or more other portions of the formation. Providing the synthesis gas generating fluid may alternatively include raising a water table of the formation to allow water to flow into it. Synthesis gas generating fluid may also be provided through at least one injection wellbore. The synthesis gas generating fluid will generally react with carbon in the foπnation to form H₂, water, methane, C0₂, and/or CO.

A portion of the carbon dioxide may react with carbon in the formation to generate carbon monoxide. Hydrocarbons such as ethane may be added to a synthesis gas generating fluid. When introduced into the formation, the hydrocarbons may crack to form hydrogen and/or methane. The presence of methane in produced synthesis gas may increase the heating value of the produced synthesis gas.

Synthesis gas generation is, in some embodiments, an endothermic process. Additional heat may be added to the formation during synthesis gas generation to maintain a high temperature within the formation. The heat may be added from heater wells and/or from oxidizing carbon and/or hydrocarbons within the formation. In an embodiment, an oxidant may be added to a synthesis gas generating fluid. The oxidant may include, but is not limited to, air, oxygen enriched air, oxygen, hydrogen peroxide, other oxidizing fluids, or combinations thereof. The oxidant may react with carbon within the formation to exothermically generate heat. Reaction of an oxidant with carbon in the formation may result in production of C0₂ and/or CO. Introduction of an oxidant to react with carbon in the formation may economically allow raising the formation temperature high enough to result in generation of significant quantities of H₂ and CO from hydrocarbons within the formation. Synthesis gas generation may be via a batch process or a continuous process.

Synthesis gas may be produced from the formation through one or more producer wells that include one or more heat sources. Such heat sources may operate to promote production of the synthesis gas with a desired composition.

Certain embodiments may include monitoring a composition of the produced synthesis gas and then controlling heating and/or controlling input of the synthesis gas generating fluid to maintain the composition of the produced synthesis gas within a desired range. For example, in some embodiments (e.g., such as when the synthesis gas will be used as a feedstock for a Fischer-Tropsch process), a desired composition of the produced synthesis gas may have a ratio of hydrogen to carbon monoxide of about 1.8:1 to 2.2:1 (e.g., about 2:1 or about

2.1:1). In some embodiments (such as when the synthesis gas will be used as a feedstock to make methanol), such ratio may be about 3:1 (e.g., about 2.8:1 to 3.2:1).

Certain embodiments may include blending a first synthesis gas with a second synthesis gas to produce synthesis gas of a desired composition. The first and the second synthesis gases may be produced from different portions of the formation.

Synthesis gases may be converted to heavier condensable hydrocarbons. For example, a Fischer-Tropsch hydrocarbon synthesis process may convert synthesis gas to branched and unbranched paraffins. Paraffins produced from the Fischer-Tropsch process may be used to produce other products such as diesel, jet fuel, and naphtha products. The produced synthesis gas may also be used in a catalytic methanation process to produce methane. Alternatively, the produced synthesis gas may be used for production of methanol, gasoline and diesel fuel, ammonia, and middle distillates. Produced synthesis gas may be used to heat the formation as a combustion fuel. Hydrogen in produced synthesis gas may be used to upgrade oil.

Synthesis gas may also be used for other pmposes. Synthesis gas may be combusted as fuel. Synthesis gas may also be used for synthesizing a wide range of organic and/or inorganic compounds, such as hydrocarbons and ammonia. Synthesis gas may be used to generate electricity by combusting it as a fuel, by reducing the pressure of the synthesis gas in turbines, and/or using the temperature of the synthesis gas to make steam (and then run turbines). Synthesis gas may also be used in an energy generation unit such as a molten carbonate fuel cell, a solid oxide fuel cell, or other type of fuel cell.

Certain embodiments may include separating a fuel cell feed stream from fluids produced from pyrolysis of at least some of the hydrocarbons within a formation. The fuel cell feed stream may include H₂, hydrocarbons, and/or carbon monoxide. In addition, certain embodiments may include directing the fuel cell feed stream to a fuel cell to produce electricity. The electricity generated from the synthesis gas or the pyrolyzation fluids in the fuel cell may power electric heaters, which may heat at least a portion of the formation. Certain embodiments may include separating carbon dioxide from a fluid exiting the fuel cell. Carbon dioxide produced from a fuel cell or a formation may be used for a variety of puφoses. In certain embodiments, synthesis gas produced from a heated formation may be transferred to an additional area of the formation and stored within the additional area of the formation for a length of time. The conditions of the additional area of the formation may inhibit reaction of the synthesis gas. The synthesis gas may be produced from the additional area of the formation at a later time. In some embodiments, treating a formation may include injecting fluids into the formation. The method may include providing heat to the formation, allowing the heat to transfer to a selected section of the formation, injecting a fluid into the selected section, and producing another fluid from the formation. Additional heat may be provided to at least a portion of the formation, and the additional heat may be allowed to transfer from at least the portion to the selected section of the formation. At least some hydrocarbons may be pyrolyzed within the selected section and a mixture may be produced from the formation. Another embodiment may include leaving a section of the formation proximate the selected section substantially unleached. The unleached section may inhibit the flow of water into the selected section.

In an embodiment, heat may be provided to the formation. The heat may be allowed to transfer to a selected section of the formation such that dissociation of carbonate minerals is inhibited. At least some hydrocarbons may be pyrolyzed within the selected section and a mixture produced from the formation. The method may further include reducing a temperature of the selected section and injecting a fluid into the selected section. Another fluid may be produced from the formation. Alternatively, subsequent to providing heat and allowing heat to transfer, a method may include injecting a fluid into the selected section and producing another fluid from the formation. Similarly, a method may include injecting a fluid into the selected section and pyrolyzing at least some hydrocarbons within the selected section of the formation after providing heat and allowing heat to transfer to the selected section.

In an embodiment that includes injecting fluids, a method of treating a formation may include providing heat from one or more heat sources and allowing the heat to transfer to a selected section of the formation such that a temperature of the selected section is less than about a temperature at which nahcolite dissociates. A fluid may be injected into the selected section and another fluid may be produced from the formation. The method may further include providing additional heat to the formation, allowing the additional heat to transfer to the selected section of the formation, and pyrolyzing at least some hydrocarbons within the selected section. A mixture may then be produced from the formation.

Certain embodiments that include injecting fluids may also include controlling the heating of the formation. A method may include providing heat to the formation, controlling the heat such that a selected section is at a first temperature, injecting a fluid into the selected section, and producing another fluid from the formation. The method may further include controlling the heat such that the selected section is at a second temperature that is greater than the first temperature. Heat may be allowed to transfer from the selected section, and at least some hydrocarbons may be pyrolyzed within the selected section of the formation. A mixture may be produced from the formation.

A further embodiment that includes injecting fluids may include providing heat to a formation, allowing the heat to transfer to a selected section of the formation, injecting a first fluid into the selected section, and producing a second fluid from the formation. The method may further include providing additional heat, allowing the additional heat to transfer to the selected section of the formation, pyrolyzing at least some hydrocarbons within the selected section of the formation, and producing a mixture from the formation. In addition, a temperature of the selected section may be reduced and a third fluid may be injected into the selected section. A fourth fluid may be produced from the formation.

In some embodiments, migration of fluids into and/or out of a treatment area may be inhibited. Inhibition of migration of fluids may occur before, during, and/or after an in situ treatment process. For example, migration of fluids may be inhibited while heat is provided from one or more heat sources to at least a portion of the treatment area. The heat may be allowed to transfer to at least a portion of the treatment area. Fluids may be produced from the treatment area.

Barriers may be used to inhibit migration of fluids into and/or out of a treatment area in a formation.

Barriers may include, but are not limited to naturally occurring portions (e.g., overburden and/or underburden), frozen barrier zones, low temperature barrier zones, grout walls, sulfur wells, dewatering wells, and/or injection wells. Barriers may define the treatment area. Alternatively, barriers may be provided to a portion of the treatment area.

In an embodiment, a method of treating a relatively low permeability formation containing heavy hydrocarbons in situ may include providing a refrigerant to a plurality of barrier wells to form a low temperature barrier zone. The method may further include establishing a low temperature baπier zone. In some embodiments, the temperature within the low temperature barrier zone may be lowered to inhibit the flow of water into or out of at least a portion of a treatment area in the formation.

Certain embodiments of treating a relatively low permeability formation containing heavy hydrocarbons in situ may include providing a refrigerant to a plurality of barrier wells to form a frozen barrier zone. The frozen barrier zone may inhibit migration of fluids into and/or out of the treatment area. In certain embodiments, a portion of the treatment area is below a water table of the formation. In addition, the method may include controlling pressure to maintain a fluid pressure within the treatment area above a hydrostatic pressure of the formation and producing a mixture of fluids from the formation.

Barriers may be provided to a portion of the formation prior to, during, and after providing heat from one or more heat sources to the treatment area. For example, a baπier may be provided to a portion of the formation that has previously undergone a conversion process.

Fluid may be introduced to a portion of the formation that has previously undergone an in situ conversion process. The fluid may be produced from the formation in a mixture, which may contain additional fluids present in the formation. In some embodiments, the produced mixture may be provided to an energy producing unit. In some embodiments, one or more conditions in a selected section may be controlled during an in situ conversion process to inhibit formation of carbon dioxide. Conditions may be controlled to produce fluids having a carbon dioxide emission level that is less than a selected carbon dioxide level. For example, heat provided to the formation may be controlled to inhibit generation of carbon dioxide, while increasing production of molecular hydrogen. In a similar manner, a method for producing methane from a relatively low permeability formation containing heavy hydrocarbons in situ while minimizing production of C0₂ may include controlling the heat from the one or more heat sources to enhance production of methane in the produced mixture and generating heat via at least one or more of the heat sources in a manner that minimizes C0₂ production. The methane may further include controlling a temperature proximate the production wellbore at or above a decomposition temperature of ethane. In certain embodiments, a method for producing products from a heated formation may include controlling a condition within a selected section of the formation to produce a mixture having a carbon dioxide emission level below a selected baseline carbon dioxide emission level. In some embodiments, the mixture may be blended with a fluid to generate a product having a carbon dioxide emission level below the baseline.

In an embodiment, a method for producing methane from a heated formation in situ may include providing heat from one or more heat sources to at least one portion of the foπnation and allowing the heat to transfer to a selected section of the formation. The method may further include providing hydrocarbon compounds to at least the selected section of the formation and producing a mixture including methane from the hydrocarbons in the foπnation.

One embodiment of a method for producing hydrocarbons in a heated foπnation may include forming a temperature gradient in at least a portion of a selected section of the heated formation and providing a hydrocarbon mixture to at least the selected section of the formation. A mixture may then be produced from a production well.

In certain embodiments, a method for upgrading hydrocarbons in a heated formation may include providing hydrocarbons to a selected section of the heated formation and allowing the hydrocarbons to crack in the heated formation. The cracked hydrocarbons may be a higher grade than the provided hydrocarbons. The upgraded hydrocarbons may be produced from the formation. Cooling a portion of the formation after an in situ conversion process may provide certain benefits, such as increasing the strength of the rock in the formation (thereby mitigating subsidence), increasing absoφtive capacity of the formation, etc.

In an embodiment, a portion of a formation that has been pyrolyzed and/or subjected to synthesis gas generation may be allowed to cool or may be cooled to form a cooled, spent portion within the formation. For example, a heated portion of a formation may be allowed to cool by transference of heat to an adjacent portion of the formation. The transference of heat may occur naturally or may be forced by the introduction of heat transfer fluids through the heated portion and into a cooler portion of the formation. .

In alternate embodiments, recovering thermal energy from a post treatment relatively low permeability formation containing heavy hydrocarbons may include injecting a heat recovery fluid into a portion of the formation. Heat from the formation may transfer to the heat recovery fluid. The heat recovery fluid may be produced from the formation. For example, introducing water to a portion of the formation may cool the portion. Water introduced into the portion may be removed from the formation as steam. The removed steam or hot water may be injected into a hot portion of the formation to create synthesis gas

In an embodiment, hydrocarbons may be recovered from a post treatment relatively low permeability formation containing heavy hydrocarbons by injecting a heat recovery fluid into a portion of the formation. Heat may vaporize at least some of the heat recovery fluid and at least some hydrocarbons in the formation. A portion of the vaporized recovery fluid and the vaporized hydrocarbons may be produced from the formation.

In certain embodiments, fluids in the formation may be removed from a post treatment hydrocarbon formation by injecting a heat recovery fluid into a portion of the formation. Heat may transfer to the heat recovery fluid and a portion of the fluid may be produced from the foπnation. The heat recovery fluid produced from the formation may include at least some of the fluids in the formation.

In one embodiment, a method of recovering excess heat from a heated formation may include providing a product stream to the heated formation, such that heat transfers from the heated formation to the product stream. The method may further include producing the product stream from the heated formation and directing the product stream to a processing unit. The heat of the product stream may then be transferred to the processing unit. In an alternate method for recovering excess heat from a heated formation the heated product stream may be directed to another formation, such that heat transfers from the product stream to the other formation.

In one embodiment, a method of utilizing heat of a heated formation may include placing a conduit in the formation, such that conduit input may be located separately from conduit output. The conduit may be heated by the heated formation to produce a region of reaction in at least a portion of the conduit. The method may further include directing a material through the conduit to the region of reaction. The material may undergo change in the region of reaction. A product may be produced from the conduit.

An embodiment of a method of utilizing heat of a heated foπnation may include providing heat from one or more heat sources to at least one portion of the formation and allowing the heat to transfer to a region of reaction in the formation. Material may be directed to the region of reaction and allowed to react in the region of reaction.

A mixture may then be produced from the formation.

In an embodiment, a portion of a relatively low permeability formation containing heavy hydrocarbons may be used to store and/or sequester materials (e.g., formation fluids, carbon dioxide). The conditions within the portion of the formation may inhibit reactions of the materials. Materials may be may be stored in the portion for a length of time. In addition, materials may be produced from the portion at a later time. Materials stored within the portion may have been previously produced from the portion of the formation, and/or another portion of the formation.

After an in situ conversion process has been completed in a portion of the formation, fluid may be sequestered within the formation. In some embodiments, to store a significant amount of fluid within the fonnation, a temperature of the foπnation will often need to be less than about 100 °C. Water may be introduced into at least a portion of the formation to generate steam and reduce a temperature of the formation. The steam may be removed from the formation. The steam may be utilized for various puφoses, including, but not limited to, heating another portion of the formation, generating synthesis gas in an adjacent portion of the formation, generating electricity, and/or as a steam flood in a oil reservoir. After the formation has cooled, fluid (e.g., carbon dioxide) may be pressurized and sequestered in the formation. Sequestering fluid within the formation may result in a significant reduction or elimination of fluid that is released to the environment due to operation of the in situ conversion process.

In alternate embodiments, carbon dioxide may be injected under pressure into the portion of the formation.

The injected carbon dioxide may adsorb onto hydrocarbons in the formation and/or reside in void spaces such as pores in the formation. The carbon dioxide may be generated during pyrolysis, synthesis gas generation, and/or extraction of useful energy. In some embodiments, carbon dioxide may be stored in relatively deep hydrocarbon containing formations and used to desorb methane.

In one embodiment, a method for sequestering carbon dioxide in a heated foπnation may include precipitating carbonate compounds from carbon dioxide provided to a portion of the formation. In some embodiments, the portion may have previously undergone an in situ conversion process. Carbon dioxide and a fluid may be provided to the portion of the formation. The fluid may combine with carbon dioxide in the portion to precipitate carbonate compounds.

In an alternate embodiment, methane may be recovered from a hydrocarbon containing formation by providing heat to the formation. The heat may desorb a substantial portion of the methane within the selected section of the formation. At least a portion of the methane may be produced from the formation. In an embodiment, a method for purifying water in a spent formation may include providing water to the formation and filtering the provided water in the formation. The filtered water may then be produced from the formation.

. In an embodiment, treating a relatively low permeability formation containing heavy hydrocarbons in situ may include injecting a recovery fluid into the formation. Heat may be provided from one or more heat sources to the formation. The heat may transfer from one or more of the heat sources to a selected section of the formation and vaporize a substantial portion of recovery fluid in at least a portion of the selected section. The heat from the heat sources and the vaporized recovery fluid may pyrolyze at least some hydrocarbons within the selected section. A gas mixture may be produced from the formation. The produced gas mixture may include hydrocarbons with an average API gravity greater than about 25°.

In certain embodiments, a method of shutting-in an in situ treatment process in a relatively low permeability formation containing heavy hydrocarbons may include terminating heating from one or more heat sources providing heat to a portion of the formation. A pressure may be monitored and controlled in at least a portion of the formation. The pressure may be maintained approximately below a fracturing or breakthrough pressure of the formation.

One embodiment of a method of shutting-in an in situ treatment process in a relatively low permeability formation containing heavy hydrocarbons may include terminating heating from one or more heat sources providing heat to a portion of the formation. Hydrocarbon vapor may be produced from the formation. At least a portion of the produced hydrocarbon vapor may be injected into a portion of a storage formation. The hydrocarbon vapor may be injected into a relatively high temperature formation. A substantial portion of injected hydrocarbons may be converted to coke and H₂ in the relatively high temperature formation. Alternatively, the hydrocarbon vapor may be stored in a depleted formation.

BRIEF DESCRIPTION OF THE DRAWINGS Further advantages of the present invention may become apparent to those skilled in the art with the benefit of the following detailed description of the preferred embodiments and upon reference to the accompanying drawings in which:

FIG. 1 depicts an illustration of stages of heating a relatively low permeability formation containing heavy hydrocarbons. FIG. 2 depicts an embodiment of a heat source pattern.

FIG. 3 depicts an embodiment of a heater well. FIG. 4 depicts an embodiment of heater well. FIG. 5 depicts an embodiment of heater well.

FIG. 6 illustrates a schematic view of multiple heaters branched from a single well in a relatively low permeability formation containing heavy hydrocarbons.

FIG. 7 illustrates a schematic of an elevated view of multiple heaters branched from a single well in a relatively low permeability formation containing heavy hydrocarbons.

FIG. 8 depicts an embodiment of heater wells located in a relatively low permeability formation containing heavy hydrocarbons. FIG . 9 depicts an embodiment of a pattern of heater wells in a relatively low permeability formation containing heavy hydrocarbons. FIG. 10 depicts a schematic representation of an embodiment of a magnetostatic drilling operation.

FIG. 11 depicts a schematic of a portion of a magnetic string.

FIG. 12 depicts an embodiment of a heated portion of a relatively low permeability formation containing heavy hydrocarbons. FIG. 13 depicts an embodiment of supeφosition of heat in a relatively low permeability formation containing heavy hydrocarbons.

FIG. 14 illustrates an embodiment of a production well placed in a formation.

FIG. 15 depicts an embodiment of a pattern of heat sources and production wells in a relatively low permeability formation containing heavy hydrocarbons. FIG. 16 depicts an embodiment of a pattern of heat sources and a production well in a relatively low permeability formation containing heavy hydrocarbons.

FIG. 17 illustrates a computational system.

FIG. 18 depicts a block diagram of a computational system.

FIG. 19 illustrates a flow chart of an embodiment of a computer-implemented method for treating a foπnation based on a characteristic of the formation.

FIG. 20 illustrates a schematic of an embodiment used to control an in situ conversion process in a formation.

FIG. 21 illustrates a flowchart of an embodiment of a method for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons using a computer system. FIG. 22 illustrates a plot of a porosity-permeability relationship.

FIG. 23 illustrates a method for simulating heat transfer in a formation.

FIG. 24 illustrates a model for simulating a heat transfer rate in a formation.

FIG. 25 illustrates a flowchart of an embodiment of a method for using a computer system to model an in situ conversion process. FIG. 26 illustrates a flow chart of an embodiment of a method for calibrating model parameters to match laboratory or field data for an in situ process.

FIG. 27 illustrates a flowchart of an embodiment of a method for calibrating model parameters.

FIG. 28 illustrates a flow chart of an embodiment of a method for calibrating model parameters for a second simulation method using a simulation method. FIG. 29 illustrates a flow chart of an embodiment of a method for design and/or control of an in situ process.

FIG. 30 depicts a method of modeling one or more stages of a treatment process.

FIG. 31 illustrates a flow chart of an embodiment of method for designing and controlling an in situ process with a simulation method on a computer system. FIG. 32 illustrates a model of a formation that may be used in simulations of deformation characteristics according to one embodiment.

FIG. 33 illustrates a schematic of a strip development according to one embodiment.

FIG. 34 depicts a schematic illustration of a treated portion that may be modeled with a simulation.

FIG. 35 depicts a horizontal cross section of a model of a formation for use by a simulation method according to one embodiment. FIG. 36 illustrates a flow chart of an embodiment of a method for modeling deformation due to in situ treatment of a relatively low permeability formation containing heavy hydrocarbons.

FIG. 37 depicts a profile of richness versus depth in a model of an oil shale formation.

FIG. 38 illustrates a flow chart of an embodiment of a method for using a computer system to design and control an in situ conversion process.

FIG. 39 illustrates a flow chart of an embodiment of a method for determining operating conditions to obtain desired deformation characteristics.

FIG. 40 illustrates the influence of operating pressure on subsidence in a cylindrical model of a formation from a finite element simulation. FIG. 41 illustrates influence of an untreated portion between two treated portions.

FIG. 42 illustrates influence of an untreated portion between two treated portions.

FIG. 43 represents shear deformation of a formation at the location of selected heat sources as a function of depth.

FIG. 44 illustrates a method for controlling an in situ process using a computer system. FIG. 45 illustrates a schematic of an embodiment for controlling an in situ process in a formation using a computer simulation method.

FIG. 46 illustrates several ways that information may be transmitted from an in situ process to a remote computer system.

FIG. 47 illustrates a schematic of an embodiment for controlling an in situ process in a formation using information.

FIG. 48 illustrates a schematic of an embodiment for controlling an in situ process in a formation using a simulation method and a computer system.

FIG. 49 illustrates a flow chart of an embodiment of a computer-implemented method for determining a selected overburden thickness. FIG. 50 illustrates a schematic diagram of a plan view of a zone being treated using an in situ conversion process.

FIG. 51 illustrates a schematic diagram of a cross-sectional representation of a zone being treated using an in situ conversion process.

FIG. 52 illustrates a flow chart of an embodiment of a method used to monitor treatment of a formation. FIG. 53 depicts an embodiment of a natural distributed combustor heat source.

FIG. 54 depicts an embodiment of a natural distributed combustor system for heating a formation.

FIG. 55 illustrates a cross-sectional representation of an embodiment of a natural distributed combustor having a second conduit.

FIG. 56 depicts a schematic representation of an embodiment of a heater well positioned within a relatively low permeability formation containing heavy hydrocarbons.

FIG. 57 depicts a portion of an overburden of a formation with a natural distributed combustor heat source.

FIG. 58 depicts an embodiment of a natural distributed combustor heat source.

FIG. 59 depicts an embodiment of a natural distributed combustor heat source.

FIG. 60 depicts an embodiment of a natural distributed combustor system for heating a formation. FIG. 61 depicts an embodiment of an insulated conductor heat source.

FIG. 62 depicts an embodiment of a transition section of an insulated conductor assembly. FIG. 63 depicts an embodiment of an insulated conductor heat source. FIG. 64 depicts an embodiment of a wellhead of an insulated conductor heat source. FIG. 65 depicts an embodiment of a conductor-in-conduit heat source in a formation. FIG. 66 depicts an embodiment of three insulated conductor heaters placed within a conduit. FIG. 67 depicts an embodiment of a centralizer.

FIG. 68 depicts an embodiment of a centralizer. FIG. 69 depicts an embodiment of a centralizer.

FIG. 70 depicts a cross-sectional representation of an embodiment of a removable conductor-in-conduit heat source. FIG. 71 depicts an embodiment of a sliding connector.

FIG. 72 depicts an embodiment of a wellhead with a conductor-in-conduit heat source. FIG. 73 illustrates a schematic of an embodiment of a conductor-in-conduit heater, wherein a portion of the heater is placed substantially horizontally within a formation.

FIG. 74 illustrates an enlarged view of an embodiment of a junction of a conductor-in-conduit heater. FIG. 75 illustrates a schematic of an embodiment of a conductor-in-conduit heater, wherein a portion of the heater is placed substantially horizontally within a formation.

FIG. 76 illustrates a schematic of an embodiment of a conductor-in-conduit heater, wherein a portion of the heater is placed substantially horizontally within a formation.

FIG. 77 illustrates a schematic of an embodiment of a conductor-in-conduit heater, wherein a portion of the heater is placed substantially horizontally within a formation.

FIG. 78 depicts a cross-sectional view of a portion of an embodiment of a cladding section coupled to a heater support and a conduit.

FIG. 79 illustrates a cross-sectional representation of an embodiment of a centralizer placed on a conductor. FIG. 80 depicts a portion of an embodiment of a conductor-in-conduit heat source with a cutout view showing a centralizer on the conductor.

FIG. 81 depicts a cross-sectional representation of an embodiment of a centralizer. FIG. 82 depicts a cross-sectional representation of an embodiment of a centralizer. FIG. 83 depicts a top view of an embodiment of a centralizer. FIG. 84 depicts a top view of an embodiment of a centralizer.

FIG. 85 depicts a cross-sectional representation of a portion of an embodiment of a section of a conduit of a conduit-in-conductor heat source with an insulation layer wrapped around the conductor.

FIG. 86 depicts a cross-sectional representation of an embodiment of a cladding section coupled to a low resistance conductor. FIG. 87 depicts an embodiment of a conductor-in-conduit heat source in a formation.

FIG. 88 depicts an embodiment for assembling a conductor-in-conduit heat source and installing the heat source in a formation.

FIG. 89 depicts an embodiment of a conductor-in-conduit heat source to be installed in a formation. FIG. 90 shows a cross-sectional representation of an end of a tubular around which two pairs of diametrically opposite electrodes are arranged.

FIG. 91 depicts an embodiment of ends of two adjacent tubulars before forge welding. FIG. 92 illustrates an end view of an embodiment of a conductor-in-conduit heat source heated by diametrically opposite electrodes.

FIG. 93 illustrates a cross-sectional representation of an embodiment of two conductor-in-conduit heat source sections before forge welding. FIG. 94 depicts an embodiment of heat sources installed in a formation.

FIG. 95 depicts an embodiment of a heat source in a formation.

FIG. 96 illustrates a cross-sectional representation of an embodiment of a heater with two oxidizers.

FIG. 97 illustrates a cross-sectional representation of an embodiment of a heater with an oxidizer and an electric heater. FIG. 98 depicts a cross-sectional representation of an embodiment of a heater with an oxidizer and a flameless distributed combustor heater.

FIG. 99 illustrates a cross-sectional representation of an embodiment of a multilateral downhole combustor heater.

FIG. 100 illustrates a cross-sectional representation of an embodiment of a downhole combustor heater with two conduits.

FIG. 101 illustrates a cross-sectional representation of an embodiment of a downhole combustor.

FIG. 102 depicts an embodiment of a heat source for a relatively low permeability formation containing heavy hydrocarbons.

FIG. 103 depicts a representation of a portion of a piping layout for heating a formation using downhole combustors.

FIG. 104 depicts a schematic representation of an embodiment of a heater well positioned within a relatively low permeability formation containing heavy hydrocarbons.

FIG. 105 depicts an embodiment of a heat source positioned in a relatively low permeability foπnation containing heavy hydrocarbons. FIG. 106 depicts a schematic representation of an embodiment of a heat source positioned in a relatively low permeability formation containing heavy hydrocarbons.

FIG. 107 depicts an embodiment of a surface combustor heat source.

FIG. 108 depicts an embodiment of a conduit for a heat source with a portion of an inner conduit shown cut away to show a center tube. FIG. 109 depicts an embodiment of a flameless combustor heat source.

FIG. 110 illustrates a representation of an embodiment of an expansion mechanism coupled to a heat source in an opening in a formation.

FIG. I l l illustrates a schematic of a thermocouple placed in a wellbore.

FIG. 112 depicts a schematic of a well embodiment for using pressure waves to measure temperature within a wellbore.

FIG. 113 illustrates a schematic of an embodiment that uses wind to generate electricity to heat a formation.

FIG. 114 depicts an embodiment of a windmill for generating electricity.

FIG. 115 illustrates a schematic of an embodiment for using solar power to heat a formation. FIG. 116 depicts a cross-sectional representation of an embodiment for treating a lean zone and a rich zone of a formation. FIG. 117 depicts an embodiment of using pyrolysis water to generate synthesis gas in a formation.

FIG. 118 depicts an embodiment of synthesis gas production in a formation.

FIG. 119 depicts an embodiment of continuous synthesis gas production in a formation.

FIG. 120 depicts an embodiment of batch synthesis gas production in a formation. FIG. 121 depicts an embodiment of producing energy with synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons.

FIG. 122 depicts an embodiment of producing energy with pyrolyzation fluid produced from a relatively low permeability formation containing heavy hydrocarbons.

FIG. 123 depicts an embodiment of synthesis gas production from a formation. FIG. 124 depicts an embodiment of sequestration of carbon dioxide produced during pyrolysis in a hydrocarbon containing formation.

FIG. 125 depicts an embodiment of producing energy with synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons.

FIG. 126 depicts an embodiment of a Fischer-Tropsch process using synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons.

FIG. 127 depicts an embodiment of a Shell Middle Distillates process using synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons.

FIG. 128 depicts an embodiment of a catalytic methanation process using synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons. FIG. 129 depicts an embodiment of production of ammonia and urea using synthesis gas produced from a hydrocarbon containing formation.

FIG. 130 depicts an embodiment of production of ammonia and urea using synthesis gas produced from a hydrocarbon containing formation.

FIG. 131 depicts an embodiment of preparation of a feed stream for an ammonia and urea process. FIG. 132 depicts schematic of an embodiment of a relatively low permeability formation used to produce a first mixture that is blended with a second mixture.FIG. 151 depicts asphaltene content (on a whole oil basis) in a blend versus percent blending agent.

FIG. 133 depicts SARA results (saturate/aromatic ratio versus asphaltene/resin ratio) for several blends.

FIG. 134 illustrates near infrared transmittance versus volume of n-heptane added to a first mixture. FIG. 135 illustrates near infrared transmittance versus volume of n-heptane added to a second mixture.

FIG. 136 illustrates near infrared transmittance versus volume of n-heptane added to a third mixture.

FIG. 137 depicts changes in density with increasing temperature for several mixtures.

FIG. 138 depicts changes in viscosity with increasing temperature for several mixtures.

FIG. 139 depicts an embodiment of heat sources and production wells in a relatively low permeability formation.

FIG. 140 depicts an embodiment of heat sources in a relatively low permeability formation.

FIG. 141 depicts an embodiment of heat sources in a relatively low permeability formation.

FIG. 142 depicts an embodiment of heat sources in a relatively low permeability formation.

FIG. 143 depicts an embodiment of heat sources in a relatively low permeability formation. FIG. 144 depicts an embodiment of heat sources in a relatively low permeability formation.

FIG. 145 depicts an embodiment of a heat source and production well pattern. FIG. 146 depicts an embodiment of a heat source and production well pattern.

FIG. 147 depicts an embodiment of a heat source and production well pattern.

FIG. 148 depicts an embodiment of a heat source and production well pattern.

FIG. 149 depicts an embodiment of a heat source and production well pattern. FIG. 150 depicts an embodiment of a heat source and production well pattern.

FIG. 151 depicts an embodiment of a heat source and production well pattern.

FIG. 152 depicts an embodiment of a heat source and production well pattern.

FIG. 153 depicts an embodiment of a heat source and production well pattern.

FIG. 154 depicts an embodiment of a heat source and production well pattern. FIG. 155 depicts an embodiment of a heat source and production well pattern.

FIG. 156 depicts an embodiment of a heat source and production well pattern.

FIG. 157 depicts an embodiment of a heat source and production well pattern.

FIG. 158 depicts an embodiment of a heat source and production well pattern.

FIG. 159 depicts an embodiment of a square pattern of heat sources and production wells. FIG. 160 depicts an embodiment of a heat source and production well pattern.

FIG. 161 depicts an embodiment of a triangular pattern of heat sources.

FIG. 162 depicts an embodiment of a square pattern of heat sources.

FIG. 163 depicts an embodiment of a hexagonal pattern of heat sources.

FIG. 164 depicts an embodiment of a 12 to 1 pattern of heat sources. FIG. 165 depicts an embodiment of surface facilities for treating a formation fluid.

FIG. 166 depicts an embodiment of a catalytic flameless distributed combustor.

FIG. 167 depicts an embodiment of surface facilities for treating a formation fluid.

FIG. 168 depicts a temperature profile for a triangular pattern of heat sources.

FIG. 169 depicts a temperature profile for a square pattern of heat sources. FIG. 170 depicts a temperature profile for a hexagonal pattern of heat sources.

FIG. 171 depicts a comparison plot between the average pattern temperature and temperatures at the coldest spots for various patterns of heat sources.

FIG. 172 depicts a comparison plot between the average pattern temperature and temperatures at various spots within triangular and hexagonal patterns of heat sources. FIG. 173 depicts a comparison plot between the average pattern temperature and temperatures at various spots within a square pattern of heat sources.

FIG. 174 depicts a comparison plot between temperatures at the coldest spots of various pattern of heat sources.

FIG. 175 depicts in situ temperature profiles for electrical resistance heaters and natural distributed combustion heaters.

FIG. 176 depicts extension of a reaction zone in a heated formation over time.

FIG. 177 depicts the ratio of conductive heat transfer to radiative heat transfer in a formation.

FIG. 178 depicts the ratio of conductive heat transfer to radiative heat transfer in a formation.

FIG. 179 depicts temperatures of a conductor, a conduit, and an opening in a formation versus a temperature at the face of a foπnation. FIG. 180 depicts temperatures of a conductor, a conduit, and an opening in a formation versus a temperature at the face of a formation.

FIG. 181 depicts temperatures of a conductor, a conduit, and an opening in a formation versus a temperature at the face of a formation. FIG. 182 depicts temperatures of a conductor, a conduit, and an opening in a formation versus a temperature at the face of a formation.

FIG. 183 depicts calculated equilibrium gas dry mole fractions for a reaction of coal with water.

FIG. 184 depicts calculated equilibrium gas wet mole fractions for a reaction of coal with water.

FIG. 185 depicts a plot of cumulative adsorbed methane and carbon dioxide versus pressure in a coal formation.

FIG. 186 depicts pressure at a wellhead as a function of time from a numerical simulation.

FIG. 187 depicts production rate of carbon dioxide and methane as a function of time from a numerical simulation.

FIG. 188 depicts cumulative methane produced and net carbon dioxide injected as a function of time from a numerical simulation.

FIG. 189 depicts pressure at wellheads as a function of time from a numerical simulation.

FIG. 190 depicts production rate of carbon dioxide as a function of time from a numerical simulation.

FIG. 191 depicts cumulative net carbon dioxide injected as a function of tune from a numerical simulation.

FIG. 192 depicts an embodiment of in situ synthesis gas production integrated with a Fischer-Tropsch process.

FIG. 193 depicts a schematic of a surface treatment configuration that separates formation fluid as it is being produced from a formation.

FIG. 194 depicts a schematic of a surface facility configuration that heats a fluid for use in an in situ treatment process and/or a surface facility configuration. FIG. 195 depicts a schematic of an embodiment of a fractionator that separates component streams from a synthetic condensate.

FIG. 196 depicts a schematic of an embodiment of a series of separating units used to separate component streams from formation fluid,

FIG. 197 depicts a schematic an embodiment of a series of separating units used to separate formation fluid into fractions.

FIG. 198 depicts a schematic of an embodiment of a surface treatment configuration used to reactively distill a synthetic condensate.

FIG. 199 depicts a schematic of an embodiment of a surface treatment configuration that separates formation fluid through condensation. FIG. 200 depicts a schematic of an embodiment of a surface treatment configuration that hydrotreats untreated formation fluid.

FIG. 201 depicts a schematic of an embodiment of a surface treatment configuration that converts formation fluid into olefins.

FIG. 202 depicts a schematic of an embodiment of a surface treatment configuration that removes a component and converts formation fluid into olefins. FIG. 203 depicts a schematic of an embodiment of a surface treatment configuration that converts formation fluid into olefins using a heating unit and a quenching unit.

FIG. 204 depicts a schematic of an embodiment of a surface treatment configuration that separates ammonia and hydrogen sulfide from water produced in the formation. FIG. 205 depicts a schematic of an embodiment of a surface treatment configuration used to produce and separate ammonia.

FIG. 206 depicts a schematic of an embodiment of a surface treatment configuration that separates ammonia and hydrogen sulfide from water produced in the formation.

FIG. 207 depicts a schematic of an embodiment of a surface treatment configuration that produces ammonia on site.

FIG. 208 depicts a schematic of an embodiment of a surface treatment configuration used for the synthesis of urea.

FIG. 209 depicts a schematic of an embodiment of a surface treatment configuration that synthesizes ammonium sulfate. FIG. 210 depicts a schematic of an embodiment of a surface treatment configuration used to separate

BTEX compounds from formation fluid.

FIG. 211 depicts a schematic of an embodiment of a surface treatment configuration used to recover BTEX compounds from a naphtha fraction.

FIG. 212 depicts a schematic of an embodiment of a surface treatment configuration that separates a component from a heart cut.

FIG. 213 depicts a plan view representation of an embodiment of treatment areas formed by perimeter barriers.

FIG. 214 depicts a side representation of an embodiment of an in situ conversion process system used to treat a thin rich formation. FIG. 215 depicts a side representation of an embodiment of an in situ conversion process system used to treat a thin rich formation.

FIG. 216 depicts a side representation of an embodiment of an in situ conversion process system.

FIG. 217 depicts a side representation of an embodiment of an in situ conversion process system with an installed upper perimeter barrier and an installed lower perimeter barrier. FIG. 218 depicts a plan view representation of an embodiment of treatment areas formed by perimeter barriers having arced portions, wherein the centers of the arced portions are in an equilateral triangle pattern.

FIG. 219 depicts a plan view representation of an embodiment of treatment areas formed by perimeter barriers having arced portions, wherein the centers of the arced portions are in a square pattern.

FIG. 220 depicts a plan view representation of an embodiment of treatment areas formed by perimeter barriers radially positioned around a central point.

FIG. 221 depicts a plan view representation of a portion of a treatment area defined by a double ring of freeze wells.

FIG. 222 depicts a side representation of a freeze well that is directionally drilled in a formation so that the freeze well enters the formation in a first location and exits the formation in a second location. FIG. 223 depicts a side representation of freeze wells that form a barrier along sides and ends of a dipping hydrocarbon containing layer in a foπnation. FIG. 224 depicts a representation of an embodiment of a freeze well and an embodiment of a heat source that may be used during an in situ conversion process.

FIG. 225 depicts an embodiment of a batch operated freeze well.

FIG. 226 depicts an embodiment of a batch operated freeze well having an open wellbore portion. FIG. 227 depicts a plan view representation of a circulated fluid refrigeration system.

FIG. 228 depicts an embodiment of a freeze well for a circulated liquid refrigeration system, wherein a cutaway view of the freeze well is represented below ground surface.

FIG. 229 depicts an embodiment of a freeze well for a circulated liquid refrigeration system. FIG. 230 depicts an embodiment of a freeze well for a circulated liquid refrigeration system. FIG. 231 depicts a plan view representation of low temperature zones formed by freeze wells placed in a formation through which fluid flows slowly enough to allow for formation of an interconnected low temperature zone.

FIG. 232 depicts a plan view representation of low temperature zones formed by freeze wells placed in a formation through which fluid flows at too high a flow rate to allow for formation of an interconnected low temperature zone.

FIG. 233 depicts thermal simulation results of a heat source surrounded by a ring of freeze wells. FIG. 234 depicts a representation of an embodiment of a ground cover. FIG. 235 depicts an embodiment of a treatment area surrounded by a ring of dewatering wells. FIG. 236 depicts an embodiment of a treatment area surrounded by two rings of dewatering wells. FIG. 237 depicts an embodiment of a treatment area surrounded by three rings of dewatering wells.

FIG. 238 illustrates a schematic of an embodiment of an injection wellbore and a production wellbore. FIG. 239 depicts an embodiment of a remediation process used to treat a treatment area. FIG. 240 depicts an embodiment of a heated formation used as a radial distillation column. FIG. 241 depicts an embodiment of a heated formation used for separation of hydrocarbons and contaminants.

FIG. 242 depicts an embodiment for recovering heat from a heated formation and transferring the heat to an above-ground processing unit.

FIG. 243 depicts an embodiment for recovering heat from one formation and providing heat to another formation with an intermediate production step. FIG. 244 depicts an embodiment for recovering heat from one formation and providing heat to another formation in situ.

FIG. 245 depicts an embodiment of a region of reaction within a heated formation. FIG. 246 depicts an embodiment of a conduit placed within a heated foπnation. FIG. 247 depicts an embodiment of a U-shaped conduit placed within a heated formation. FIG. 248 depicts an embodiment for sequestration of carbon dioxide in a heated formation.

FIG. 249 depicts an embodiment for solution mining a formation. FIG. 250 is a flow chart illustrating options for produced fluids from a shut-in foπnation. FIG. 251 illustrates a schematic of an embodiment of an injection wellbore and a production wellbore. FIG. 252 illustrates a cross-sectional representation of in situ treatment of a foπnation with steam injection according to one embodiment. FIG. 253 illustrates a cross-sectional representation of in situ treatment of a formation with steam injection according to one embodiment.

FIG. 254 illustrates a cross-sectional representation of in situ treatment of a foπnation with steam injection according to one embodiment. FIG. 255 illustrates a schematic of an embodiment of in situ treatment of an oil containing formation.

While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof are shown by way of example in the drawings and may herein be described in detail. The drawings may not be to scale. It should be understood, however, that the drawings and detailed description thereto are not intended to limit the invention to the particular form disclosed, but on the contrary, the intention is to cover all modifications, equivalents and alternatives falling within the spirit and scope of the present invention as defined by the appended claims.

DETAILED DESCRIPTION OF THE INVENTION

The following description generally relates to systems and methods for treating a relatively low permeability formation containing heavy hydrocarbons. Such formations may be treated to yield relatively high quality hydrocarbon products, hydrogen, and other products.

"Hydrocarbons" are organic material with molecular structures containing carbon and hydrogen. Hydrocarbons may also include other elements, such as, but not limited to, halogens, metallic elements, nitrogen, oxygen, and/or sulfur. Hydrocarbons may be, but are not limited to, kerogen, bitumen, pyrobitumen, oils, natural mineral waxes, and asphaltites. Hydrocarbons may be located within or adjacent to mineral matrices within the earth. Matrices may include, but are not limited to, sedimentary rock, sands, silicilytes, carbonates, diatomites, and other porous media. "Hydrocarbon fluids" are fluids that include hydrocarbons. Hydrocarbon fluids may include, entrain, or be entrained in non-hydrocarbon fluids (e.g., hydrogen ("H₂"), nitrogen ("N₂"), carbon monoxide, carbon dioxide, hydrogen sulfide, water, and ammonia). A "formation" includes one or more hydrocarbon containing layers, one or more non-hydrocarbon layers, an overburden, and/or an underburden. An "overburden" and/or an "underburden" includes one or more different types of impermeable materials. For example, overburden and/or underburden may include rock, shale, mudstone, or wet/tight carbonate (i.e., an impermeable carbonate without hydrocarbons). In some embodiments of in situ conversion processes, an overburden and/or an underburden may include a hydrocarbon containing layer or hydrocarbon containing layers that are relatively impermeable and are not subjected to temperatures during in situ conversion processing that results in significant characteristic changes of the hydrocarbon containing layers of the overburden and/or underburden. For example, an underburden may contain shale or mudstone. In some cases, the overburden and/or underburden may be somewhat permeable.

"Kerogen" is a solid, insoluble hydrocarbon that has been converted by natural degradation (e.g., by diagenesis) and that principally contains carbon, hydrogen, nitrogen, oxygen, and sulfur. "Bitumen" is a non- crystalline solid or viscous hydrocarbon material that is substantially soluble in carbon disulfide. "Oil" is a fluid containing a mixture of condensable hydrocarbons.

The terms "formation fluids" and "produced fluids" refer to fluids removed from a relatively low permeability foπnation containing heavy hydrocarbons and may include pyrolyzation fluid, synthesis gas, mobilized hydrocarbon, and water (steam). The term "mobilized fluid" refers to fluids within the formation that are able to flow because of thermal treatment of the formation. Formation fluids may include hydrocarbon fluids as well as non-hydrocarbon fluids.

"Carbon number" refers to a number of carbon atoms within a molecule. A hydrocarbon fluid may include various hydrocarbons having varying numbers of carbon atoms. The hydrocarbon fluid may be described by a carbon number distribution. Carbon numbers and/or carbon number distributions may be determined by true boiling point distribution and/or gas-liquid chromatography.

A "heat source" is any system for providing heat to at least a portion of a formation substantially by conductive and/or radiative heat transfer. For example, a heat source may include electric heaters such as an insulated conductor, an elongated member, and a conductor disposed within a conduit, as described in embodiments herein. A heat source may also include heat sources that generate heat by burning a fuel external to or within a formation, such as surface burners, downhole gas burners, flameless distributed combustors, and natural distributed combustors, as described in embodiments herein. In addition, it is envisioned that in some embodiments heat provided to or generated in one or more heat sources may by supplied by other sources of energy. The other sources of energy may directly heat a formation, or the energy may be applied to a transfer media that directly or indirectly heats the formation. It is to be understood that one or more heat sources that are applying heat to a formation may use different sources of energy. Thus, for example, for a given foπnation some heat sources may supply heat from electric resistance heaters, some heat sources may provide heat from combustion, and some heat sources may provide heat from one or more other energy sources (e.g., chemical reactions, solar energy, wind energy, biomass, or other sources of renewable energy). A chemical reaction may include an exothermic reaction (e.g., an oxidation reaction). A heat source may also include a heater that may provide heat to a zone proximate and/or suπounding a heating location such as a heater well.

A "heater" is any system for generating heat in a well or a near wellbore region. Heaters may be, but are not limited to, electric heaters, burners, combustors (e.g., natural distributed combustors) that react with material in or produced from a formation, and/or combinations thereof. A "unit of heat sources" refers to a number of heat sources that form a template that is repeated to create a pattern of heat sources within a formation.

The term "wellbore" refers to a hole in a formation made by drilling or insertion of a conduit into the formation. A wellbore may have a substantially circular cross section, or other cross-sectional shapes (e.g., circles, ovals, squares, rectangles, triangles, slits, or other regular or irregular shapes). As used herein, the terms "well" and "opening," when referring to an opening in the formation may be used interchangeably with the term "wellbore." "Natural distributed combustor" refers to a heater that uses an oxidant to oxidize at least a portion of the carbon in the formation to generate heat, and wherein the oxidation takes place in a vicinity proximate a wellbore. Most of the combustion products produced in the natural disfributed combustor are removed through the wellbore.

"Orifices," refers to openings (e.g., openings in conduits) having a wide variety of sizes and cross-sectional shapes including, but not limited to, circles, ovals, squares, rectangles, triangles, slits, or other regular or irregular shapes.

"Reaction zone" refers to a volume of a relatively low permeability formation containing heavy hydrocarbons that is subjected to a chemical reaction such as an oxidation reaction.

"Insulated conductor" refers to any elongated material that is able to conduct electricity and that is covered, in whole or in part, by an electrically insulating material. The term "self-controls" refers to controlling an output of a heater without external control of any type. "Pyrolysis" is the breaking of chemical bonds due to the application of heat. For example, pyrolysis may include transforming a compound into one or more other substances by heat alone. Heat may be transferred to a section of the formation to cause pyrolysis.

"Pyrolyzation fluids" or "pyrolysis products" refers to fluid produced substantially during pyrolysis of hydrocarbons. Fluid produced by pyrolysis reactions may mix with other fluids in a formation. The mixture would be considered pyrolyzation fluid or pyrolyzation product. As used herein, "pyrolysis zone" refers to a volume of a formation (e.g., a relatively low permeability formation containing heavy hydrocarbons) that is reacted or reacting to form a pyrolyzation fluid.

"Cracking" refers to a process involving decomposition and molecular recombination of organic compounds to produce a greater number of molecules than were initially present. In cracking, a series of reactions take place accompanied by a transfer of hydrogen atoms between molecules. For example, naphtha may undergo a thermal cracking reaction to form ethene and H₂.

"Supeφosition of heat" refers to providing heat from two or more heat sources to a selected section of a formation such that the temperature of the formation at least at one location between the heat sources is influenced by the heat sources.

"Fingering" refers to injected fluids bypassing portions of a formation because of variations in transport characteristics of the formation (e.g., permeability or porosity).

"Fluid pressure" is a pressure generated by a fluid within a formation. "Lithostatic pressure" (sometimes referred to as "lithostatic stress") is a pressure within a formation equal to a weight per unit area of an overlying rock mass. "Hydrostatic pressure" is a pressure within a formation exerted by a column of water.

"Condensable hydrocarbons" are hydrocarbons that condense at 25 °C at one atmosphere absolute pressure. Condensable hydrocarbons may include a mixture of hydrocarbons having carbon numbers greater than 4. "Non-condensable hydrocarbons" are hydrocarbons that do not condense at 25 °C and one atmosphere absolute pressure. Non-condensable hydrocarbons may include hydrocarbons having carbon numbers less than 5. "Olefins" are molecules that include unsaturated hydrocarbons having one or more non-aromatic carbon- to-carbon double bonds.

"Urea" describes a compound represented by the molecular formula of NH₂-CO-NH₂. Urea may be used as a fertilizer.

"Synthesis gas" is a mixture including hydrogen and carbon monoxide used for synthesizing a wide range of compounds. Additional components of synthesis gas may include water, carbon dioxide, nitrogen, methane, and other gases. Synthesis gas may be generated by a variety of processes and feedstocks.

"Reforming" is a reaction of hydrocarbons (such as methane or naphtha) with steam to produce CO and H₂ as major products. Generally, it is conducted in the presence of a catalyst, although it can be performed thermally without the presence of a catalyst. "Sequestration" refers to storing a gas that is a by-product of a process rather than venting the gas to the atmosphere.

"Dipping" refers to a foπnation that slopes downward or inclines from a plane parallel to the earth's surface, assuming the plane is flat (i.e., a "horizontal" plane). A "dip" is an angle that a stratum or similar feature makes with a horizontal plane. A "steeply dipping" relatively low permeability formation containing heavy hydrocarbons refers to a relatively low permeability formation containing heavy hydrocarbons lying at an angle of at least 20° from a horizontal plane. "Down dip" refers to downward along a direction parallel to a dip in a formation. "Up dip" refers to upward along a direction parallel to a dip of a formation. "Strike" refers to the course or bearing of hydrocarbon material that is normal to the direction of dip.

"Subsidence" is a downward movement of a portion of a formation relative to an initial elevation of the surface. "Thickness" of a layer refers to the thickness of a cross section of a layer, wherein the cross section is normal to a face of the layer.

"Coring" is a process that generally includes drilling a hole into a formation and removing a substantially solid mass of the formation from the hole.

A "surface unit" is an ex situ treatment unit. "Middle distillates" refers to hydrocarbon mixtures with a boiling point range that coπesponds substantially with that of kerosene and gas oil fractions obtained in a conventional atmospheric distillation of crude oil material. The middle distillate boiling point range may include temperatures between about 150 °C and about 360 °C, with a fraction boiling point between about 200 °C and about 360 °C. Middle distillates may be refened to as gas oil. A "boiling point cut" is a hydrocarbon liquid fraction that may be separated from hydrocarbon liquids when the hydrocarbon liquids are heated to a boiling point range of the fraction.

"Enriched air" refers to air having a larger mole fraction of oxygen than air in the atmosphere. Enrichment of air is typically done to increase its combustion-supporting ability.

"Heavy hydrocarbons" are viscous hydrocarbon fluids. Heavy hydrocarbons may include highly viscous hydrocarbon fluids such as heavy oil, tar, and/or asphalt. Heavy hydrocarbons may include carbon and hydrogen, as well as smaller concentrations of sulfur, oxygen, and nitrogen. Additional elements may also be present in heavy hydrocarbons in trace amounts. Heavy hydrocarbons may be classified by API gravity. Heavy hydrocarbons generally have an API gravity below about 20°. Heavy oil, for example, generally has an API gravity of about 10- 20°, whereas tar generally has an API gravity below about 10°. The viscosity of heavy hydrocarbons is generally greater than about 100 centipoise at 15 °C. Heavy hydrocarbons may also include aromatics or other complex ring hydrocarbons.

"Relatively low permeability" is defined, with respect to formations or portions thereof, as an average permeability of less than about 10 millidarcy. One darcy is equal to about 0.99 square micrometers. An impermeable layer generally has a permeability of less than about 0.1 millidarcy. "Tar" is a viscous hydrocarbon that generally has a viscosity greater than about 10,000 centipoise at 15 °C.

The specific gravity of tar generally is greater than 1.000. Tar may have an API gravity less than 10°.

A "tar sands formation" is a formation in which hydrocarbons are predominantly present in the form of heavy hydrocarbons and/or tar entrained in a mineral grain framework or other host lithology (e.g., sand or carbonate). In some cases, a portion or all of a hydrocarbon portion of a relatively permeable foπnation may be predominantly heavy hydrocarbons and/or tar with no supporting mineral grain framework and only floating (or no) mineral matter (e.g., asphalt lakes).

Certain types of formations that include heavy hydrocarbons may also be, but are not limited to, natural mineral waxes (e.g., ozocerite), or natural asphaltites (e.g., gilsonite, albertite, impsonite, wurtzilite, grahamite, and glance pitch). "Natural mineral waxes" typically occur in substantially tubular veins that may be several meters wide, several kilometers long, and hundreds of meters deep. "Natural asphaltites" include solid hydrocarbons of an aromatic composition and typically occur in large veins. In situ recovery of hydrocarbons from formations such as natural mineral waxes and natural asphaltites may include melting to form liquid hydrocarbons and/or solution mining of hydrocarbons from the formations.

"Upgrade" refers to increasing the quality of hydrocarbons. For example, upgrading heavy hydrocarbons may result in an increase in the API gravity of the heavy hydrocarbons.

"Off peak" times refers to times of operation when utility energy is less commonly used and, therefore, less expensive.

"Low viscosity zone" refers to a section of a formation where at least a portion of the fluids are mobilized. "Thermal fracture" refers to fractures created in a formation caused by expansion or contraction of a formation and/or fluids within the formation, which is in turn caused by increasing/decreasing the temperature of the formation and/or fluids within the formation, and/or by increasing/decreasing a pressure of fluids within the formation due to heating.

"Vertical hydraulic fracture" refers to a fracture at least partially propagated along a vertical plane in a formation, wherein the fracture is created through injection of fluids into a formation. Hydrocarbons in formations may be freated in various ways to produce many different products. In certain embodiments, such formations may be freated in stages. FIG. 1 illustrates several stages of heating a relatively low permeability formation containing heavy hydrocarbons. FIG. 1 also depicts an example of yield (barrels of oil equivalent per ton) (y axis) of formation fluids from a relatively low permeability formation containing heavy hydrocarbons versus temperature (°C) (x axis) of the formation. Desoφtion of methane and vaporization of water occurs during stage 1 heating. Heating of the formation through stage 1 may be performed as quickly as possible. For example, when a relatively low permeability formation containing heavy hydrocarbons is initially heated, hydrocarbons in the formation may desorb adsorbed methane. The desorbed methane may be produced from the formation. If the relatively low permeability formation containing heavy hydrocarbons is heated further, water within the relatively low permeability formation containing heavy hydrocarbons may be vaporized. Water may occupy, in some relatively low peπneability formations containing heavy hydrocarbons, between about 10 % to about 50 % of the pore volume in the formation. In other formations, water may occupy larger or smaller portions of the pore volume. Water typically is vaporized in a formation between about 160 °C and about 285 °C for pressures of about 6 bars absolute to 70 bars absolute. In some embodiments, the vaporized water may produce wettability changes in the formation and/or increase formation pressure. The wettability changes and/or increased pressure may affect pyrolysis reactions or other reactions in the formation. In certain embodiments, the vaporized water may be produced from the formation. In other embodiments, the vaporized water may be used for steam extraction and/or distillation in the formation or outside the formation. Removing the water from and increasing the pore volume in the formation may increase the storage space for hydrocarbons within the pore volume. After stage 1 heating, the formation may be heated further, such that a temperature within the formation reaches (at least) an initial pyrolyzation temperature (e.g., a temperature at the lower end of the temperature range shown as stage 2). Hydrocarbons within the foπnation may be pyrolyzed throughout stage 2. A pyrolysis temperature range may vary depending on types of hydrocarbons within the formation. A pyrolysis temperature range may include temperatures between about 250 °C and about 900 °C. A pyrolysis temperature range for producing desired products may extend through only a portion of the total pyrolysis temperature range. In some embodiments, a pyrolysis temperature range for producing desired products may include temperatures between about 250 °C to about 400 °C. If a temperature of hydrocarbons in a formation is slowly raised through a temperature range from about 250 °C to about 400 °C, production of pyrolysis products may be substantially complete when the temperature approaches 400 °C. Heating the hydrocarbon formation with a plurality of heat sources may establish thermal gradients around the heat sources that slowly raise the temperature of hydrocarbons in the formation through a pyrolysis temperature range.

In some in situ conversion embodiments, a temperature of the hydrocarbons to be subjected to pyrolysis may not be slowly increased throughout a temperature range from about 250 °C to about 400 °C. The hydrocarbons in the foπnation may be heated to a desired temperature (e.g., about 325 °C). Other temperatures may be selected as the desired temperature. Supeφosition of heat from heat sources may allow the desired temperature to be relatively quickly and efficiently established in the formation. Energy input into the foπnation from the heat sources may be adjusted to maintain the temperature in the formation substantially at the desired temperature. The hydrocarbons may be maintained substantially at the desired temperature until pyrolysis declines such that production of desired formation fluids from the formation becomes uneconomical.

Formation fluids including pyrolyzation fluids may be produced from the formation. The pyrolyzation fluids may include, but are not limited to, hydrocarbons, hydrogen, carbon dioxide, carbon monoxide, hydrogen sulfide, ammonia, nitrogen, water, and mixtures thereof. As the temperature of the formation increases, the amount of condensable hydrocarbons in the produced formation fluid tends to decrease. At high temperatures, the formation may produce mostly methane and/or hydrogen. If a relatively low permeability foπnation containing heavy hydrocarbons is heated throughout an entire pyrolysis range, the formation may produce only small amounts of hydrogen towards an upper limit of the pyrolysis range. After all of the available hydrogen is depleted, a minimal amount of fluid production from the formation will typically occur.

After pyrolysis of hydrocarbons, a large amount of carbon and some hydrogen may still be present in the formation. A significant portion of remaining carbon in the formation can be produced from the formation in the form of synthesis gas. Synthesis gas generation may take place during stage 3 heating depicted in FIG. 1. Stage 3 may include heating a relatively low permeability formation containing heavy hydrocarbons to a temperature sufficient to allow synthesis gas generation. For example, synthesis gas may be produced within a temperature range from about 400 °C to about 1200 °C. The temperature of the foπnation when the synthesis gas generating fluid is introduced to the formation may determine the composition of synthesis gas produced within the formation. If a synthesis gas generating fluid is introduced into a formation at a temperature sufficient to allow synthesis gas generation, synthesis gas may be generated within the formation. The generated synthesis gas may be removed from the formation through a production well or production wells. A large volume of synthesis gas may be produced during generation of synthesis gas.

Total energy content of fluids produced from a relatively low permeability formation containing heavy hydrocarbons may stay relatively constant throughout pyrolysis and synthesis gas generation. During pyrolysis at relatively low foπnation temperatures, a significant portion of the produced fluid may be condensable hydrocarbons that have a high energy content. At higher pyrolysis temperatures, however, less of the formation fluid may mclude condensable hydrocarbons. More non-condensable formation fluids may be produced from the formation. Energy content per unit volume of the produced fluid may decline slightly during generation of predominantly non- condensable formation fluids. During synthesis gas generation, energy content per unit volume of produced synthesis gas declines significantly compared to energy content of pyrolyzation fluid. The volume of the produced synthesis gas, however, will in many instances increase substantially, thereby compensating for the decreased energy content.

Relatively low permeability formations containing heavy hydrocarbons may be selected for in situ conversion based on properties of at least a portion of the formation. For example, a formation may be selected based on richness, thickness, and/or depth (i.e., thickness of overburden) of the formation. In addition, the types of fluids producible from the formation may be a factor in the selection of a formation for in situ conversion. In certain embodiments, the quality of the fluids to be produced may be assessed in advance of treatment. Assessment of the products that may be produced from a formation may generate significant cost savings since only formations that will produce desired products need to be subjected to in situ conversion. Properties that may be used to assess hydrocarbons in a formation include, but are not limited to, an amount of hydrocarbon liquids that may be produced from the hydrocarbons, a likely API gravity of the produced hydrocarbon liquids, an amount of hydrocarbon gas producible from the formation, and/or an amount of carbon dioxide and water that in situ conversion will generate.

In some in situ conversion embodiments, a relatively low permeability formation containing heavy hydrocarbons may be selected for freatment based on a hydrogen content within the hydrocarbons in the formation. For example, a method of treating a relatively low permeability formation containing heavy hydrocarbons may include selecting a portion of the relatively low permeability formation containing heavy hydrocarbons for treatment having hydrocarbons with a hydrogen content greater than about 3 weight %, 3.5 weight %, or 4 weight %. In addition, a selected section of a relatively low permeability formation containing heavy hydrocarbons may include hydrocarbons with an atomic hydrogen to carbon ratio that falls within a range from about 0.5 to about 2, and in many instances from about 0.70 to about 1.65.

Hydrogen content of a relatively low permeability foπnation containing heavy hydrocarbons may significantly influence a composition of hydrocarbon fluids producible from the formation. Pyrolysis of hydrocarbons within heated portions of the formation may generate hydrocarbon fluids that include a double bond or a radical. Hydrogen within the formation may reduce the double bond to a single bond. Reaction of generated hydrocarbon fluids with each other and/or with additional components in the formation may be inhibited. For example, reduction of a double bond of the generated hydrocarbon fluids to a single bond may reduce polymerization of the generated hydrocarbons. Such polymerization may reduce the amount of fluids produced and may reduce the quality of fluid produced from the formation.

Hydrogen within the formation may neutralize radicals in the generated hydrocarbon fluids. Hydrogen present in the formation may inhibit reaction of hydrocarbon fragments by transforming the hydrocarbon fragments into relatively short chain hydrocarbon fluids. The hydrocarbon fluids may enter a vapor phase. Vapor phase hydrocarbons may move relatively easily through the formation to production wells. Increase in the hydrocarbon fluids in the vapor phase may significantly reduce a potential for producing less desirable products within the selected section of the formation. A lack of bound and free hydrogen in the formation may negatively affect the amount and quality of fluids that can be produced from the formation. If too little hydrogen is naturally present, then hydrogen or other reducing fluids may be added to the formation.

Heating a relatively low permeability formation containing heavy hydrocarbons may include providing a large amount of energy to heat sources located within the formation. Relatively low permeability formations containing heavy hydrocarbons may also contain some water. A significant portion of energy initially provided to a formation may be used to heat water within the formation. An initial rate of temperature increase may be reduced by the presence of water in the formation. Excessive amounts of heat and/or time may be required to heat a foπnation having a high moisture content to a temperature sufficient to pyrolyze hydrocarbons in the formation. In certain embodiments, water may be inhibited from flowing into a formation subjected to in situ conversion. A formation to be subjected to in situ conversion may have a low initial moisture content. The formation may have an initial moisture content that is less than about 15 weight %. Some formations that are to be subjected to in situ conversion may have an initial moisture content of less than about 10 weight %. Other formations that are to be processed using an in situ conversion process may have initial moisture contents that are greater than about 15 weight %. Formations with initial moisture contents above about 15 weight % may incur significant energy costs to remove the water that is initially present in the formation during heating to pyrolysis temperatures. A relatively low permeability formation containing heavy hydrocarbons may be selected for treatment based on additional factors such as, but not limited to, thickness of hydrocarbon containing layers within the formation, assessed liquid production content, location of the formation, and depth of hydrocarbon containing layers. A relatively low permeability formation containing heavy hydrocarbons may include multiple layers. Such layers may include hydrocarbon containing layers, as well as layers that are hydrocarbon free or have relatively low amounts of hydrocarbons. Conditions during formation may determine the thickness of hydrocarbon and non- hydrocarbon layers in a relatively low permeability formation containing heavy hydrocarbons. A relatively low permeability formation containing heavy hydrocarbons to be subjected to in situ' conversion will typically include at least one hydrocarbon containing layer having a thickness sufficient for economical production of formation fluids. Richness of a hydrocarbon containing layer may be a factor used to determine if a foπnation will be treated by in situ conversion. A thin and rich hydrocarbon layer may be able to produce significantly more valuable hydrocarbons than a much thicker, less rich hydrocarbon layer. Producing hydrocarbons from a formation that is both thick and rich is desirable.

An in situ conversion process may be used to treat formations with hydrocarbon layers that have thicknesses greater than about 10 m. Thick formations may allow for placement of heat sources so that supeφosition of heat from the heat sources efficiently heats the formation to a desired temperature. Formations having hydrocarbon layers that are less than 10 m thick may also be freated using an in situ conversion process. In some in situ conversion embodiments of thin hydrocarbon layer formations, heat sources may be inserted in or adjacent to the hydrocarbon layer along a length of the hydrocarbon layer (e.g., with horizontal or directional drilling). Heat losses to layers above and below the thin hydrocarbon layer or thin hydrocarbon layers may be offset by an amount and/or quality of fluid produced from the formation.

FIG. 2 shows a schematic view of an embodiment of a portion of an in situ conversion system for treating a relatively low permeability foπnation containing heavy hydrocarbons. Heat sources 100 may be placed within at least a portion of the relatively low permeability formation containing heavy hydrocarbons. Heat sources 100 may include, for example, electric heaters such as insulated conductors, conductor-in-conduit heaters, surface burners, flameless distributed combustors, and/or natural distributed combustors. Heat sources 100 may also include other types of heaters. Heat sources 100 may provide heat to at least a portion of a relatively low permeability foπnation containing heavy hydrocarbons. Energy may be supplied to the heat sources 100 through supply lines 102. The supply lines may be structurally different depending on the type of heat source or heat sources being used to heat the formation. Supply lines for heat sources may transmit electricity for electric heaters, may transport fuel for combustors, or may transport heat exchange fluid that is circulated within the formation. Production wells 104 may be used to remove formation fluid from the formation. Formation fluid produced from production wells 104 may be transported through collection piping 106 to freatment facilities 108. Formation fluids may also be produced from heat sources 100. For example, fluid may be produced from heat sources 100 to control pressure within the formation adjacent to the heat sources. Fluid produced from heat sources 100 may be transported through tubing or piping to collection piping 106 or the produced fluid may be transported through tubing or piping directly to treatment facilities 108. Treatment facilities 108 may include separation units, reaction units, upgrading units, fuel cells, turbines, storage vessels, and other systems and units for processing produced formation fluids.

An in situ conversion system for treating hydrocarbons may include dewatering wells 110 (wells shown with reference number 110 may, in some embodiments, be capture, barrier, and/or isolation wells). Dewatering wells 110 or vacuum wells may remove liquid water and/or inhibit liquid water from entering a portion of a relatively low permeability formation containing heavy hydrocarbons to be heated, or to a formation being heated. A plurality of water wells may surround all or a portion of a formation to be heated. In the embodiment depicted in FIG. 2, dewatering wells 110 are shown extending only along one side of heat sources 100, but dewatering wells typically encircle all heat sources 100 used, or to be used, to heat the formation.

Dewatering wells 110 may be placed in one or more rings surrounding selected portions of the formation. New dewatering wells may need to be installed as an area being treated by the in situ conversion process expands. An outermost row of dewatering wells may inhibit a significant amount of water from flowing into the portion of formation that is heated or to be heated. Water produced from the outermost row of dewatering wells should be substantially clean, and may require little or no treatment before being released. An inneπnost row of dewatering wells may inhibit water that bypasses the outermost row from flowing into the portion of formation that is heated or to be heated. The innermost row of dewatering wells may also inhibit outward migration of vapor from a heated portion of the formation into surrounding portions of the formation. Water produced by the innermost row of dewatering wells may include some hydrocarbons. The water may need to be treated before being released. Alternately, water with hydrocarbons may be stored and used to produce synthesis gas from a portion of the formation during a synthesis gas phase of the in situ conversion process. The dewatering wells may reduce heat loss to surrounding portions of the formation, may increase production of vapors from the heated portion, and/or may inhibit contamination of a water table proximate the heated portion of the formation.

In some embodiments, pressure differences between successive rows of dewatering wells may be minimized (e.g., maintained relatively low or near zero) to create a "no or low flow" boundary between rows.

In some in situ conversion process embodiments, a fluid may be injected in the innermost row of wells. The injected fluid may maintain a sufficient pressure around a pyrolysis zone to inhibit migration of fluid from the pyrolysis zone through the formation. The fluid may act as an isolation barrier between the outermost wells and the pyrolysis fluids. The fluid may improve the efficiency of the dewatering wells. In certain embodiments, wells initially used for one puφose may be later used for one or more other puφoses, thereby lowering project costs and/or decreasing the time required to perform certain tasks. For instance, production wells (and in some circumstances heater wells) may initially be used as dewatering wells (e.g., before heating is begun and/or when heating is initially started). In addition, in some circumstances dewatering wells can later be used as production wells (and in some circumstances heater wells). As such, the dewatering wells may be placed and/or designed so that such wells can be later used as production wells and/or heater wells. The heater wells may be placed and/or designed so that such wells can be later used as production wells and/or dewatering wells. The production wells may be placed and/or designed so that such wells can be later used as dewatering wells and or heater wells. Similarly, injection wells may be wells that initially were used for other puφoses (e.g., heating, production, dewatering, monitoring, etc.), and injection wells may later be used for other puφoses. Similarly, monitoring wells may be wells that initially were used for other puφoses (e.g., heating, production, dewatering, injection, etc.), and monitoring wells may later be used for other proposes.

Hydrocarbons to be subjected to in situ conversion may be located under a large area. The in situ conversion system may be used to treat small portions of the formation, and other sections of the formation may be treated as time progresses. In an embodiment of a system for treating a formation, a field layout for 24 years of development may be divided into 24 individual plots that represent individual drilling years. Each plot may include 120 "tiles" (repeating matrix patterns) wherein each plot is made of 6 rows by 20 columns of tiles. Each tile may include 1 production well and 12 or 18 heater wells. The heater wells may be placed in an equilateral triangle pattern with a well spacing of about 12 m. Production wells may be located in centers of equilateral triangles of heater wells, or the production wells may be located approximately at a midpoint between two adjacent heater wells. In certain embodiments, heat sources will be placed within a heater well formed within a relatively low permeability formation containing heavy hydrocarbons. The heater well may include an opening through an overburden of the formation. The heater may extend into or through at least one hydrocarbon containing section (or hydrocarbon containing layer) of the formation. As shown in FIG. 3, an embodiment of heater well 224 may include an opening in hydrocarbon layer 222 that has a helical or spiral shape. A spiral heater well may increase contact with the formation as opposed to a vertically positioned heater. A spiral heater well may provide expansion room that inhibits buckling or other modes of failure when the heater well is heated or cooled. In some embodiments, heater wells may include substantially straight sections through overburden 220. Use of a straight section of heater well through the overburden may decrease heat loss to the overburden and reduce the cost of the heater well. As shown in FIG. 4, a heat source embodiment may be placed into heater well 224. Heater well 224 may be substantially "U" shaped. The legs of the "U" may be wider or more narrow depending on the particular heater well and formation characteristics. First portion 226 and third portion 228 of heater well 224 may be arranged substantially peφendicular to an upper surface of hydrocarbon layer 222 in some embodiments. In addition, the first and the third portion of the heater well may extend substantially vertically through overburden 220. Second portion 230 of heater well 224 may be substantially parallel to the upper surface of the hydrocarbon layer.

Multiple heat sources (e.g., 2, 3, 4, 5, 10 heat sources or more) may extend from a heater well in some situations. As shown in FIG. 5, heat sources 232, 234, and 236 extend through overburden 220 into hydrocarbon layer 222 from heater well 224. Multiple wells extending from a single wellbore may be used when surface considerations (e.g., aesthetics, surface land use concerns, and/or unfavorable soil conditions near the surface) make it desirable to concentrate well platforms in a small area. For example, in areas where the soil is frozen and/or marshy, it may be more cost-effective to have a minimal number of well platforms located at selected sites.

In certain embodiments, a first portion of a heater well may extend from the ground surface, through an overburden, and into a relatively low permeability formation containing heavy hydrocarbons. A second portion of the heater well may include one or more heater wells in the relatively low permeability formation containing heavy hydrocarbons. The one or more heater wells may be disposed within the relatively low permeability foπnation containing heavy hydrocarbons at various angles. In some embodiments, at least one of the heater wells may be disposed substantially parallel to a boundary of the relatively low permeability formation containing heavy hydrocarbons. In alternate embodiments, at least one of the heater wells may be substantially peφendicular to the relatively low permeability formation containing heavy hydrocarbons. In addition, one of the one or more heater wells may be positioned at an angle between peφendicular and parallel to a layer in the formation. FIG. 6 illustrates a schematic of view of multilateral or side tracked lateral heaters branched from a single well in a relatively low permeability formation containing heavy hydrocarbons. In relatively thin and deep layers found in a relatively low permeability formation containing heavy hydrocarbons, it may be advantageous to place more than one heater substantially horizontally within the relatively thin layer of hydrocarbons. Heat provided to a thin layer with a low thermal conductivity from a horizontal wellbore may be more effectively trapped within the thin layer and reduce heat losses from the layer. Substantially vertical opening 6108 may be placed in hydrocarbon layer 6100. Substantially vertical opening 6108 may be an elongated portion of an opening formed in hydrocarbon layer 6100. Hydrocarbon layer 6100 may be below overburden 540.

One or more substantially horizontal openings 6102 may also be placed in hydrocarbon layer 6100. Horizontal openings 6102 may, in some embodiments, contain perforated liners. The horizontal openings 6102 may be coupled to vertical opening 6108. Horizontal openings 6102 may be elongated portions that diverge from the elongated portion of vertical opening 6108. Horizontal openings 6102 may be formed in hydrocarbon layer 6100 after vertical opening 6108 has been formed. In certain embodiments, openings 6102 maybe angled upwards to facilitate flow of formation fluids towards the production conduit.

Each horizontal opening 6102 may lie above or below an adjacent horizontal opening. In an embodiment, six horizontal openings 6102 may be formed in hydrocarbon layer 6100. Three horizontal openings 6102 may face

180°, or in a substantially opposite direction, from three additional horizontal openings 6102. Two horizontal openings facing substantially opposite directions may lie in a substantially identical vertical plane within the formation. Any number of horizontal openings 6102 may be coupled to a single vertical opening 6108, depending on, but not limited to, a thickness of hydrocarbon layer 6100, a type of formation, a desired heating rate in the formation, and a desired production rate.

Production conduit 6106 may be placed substantially vertically within vertical opening 6108. Production conduit 6106 may be substantially centered within vertical opening 6108. Pump 6107 may be coupled to production conduit 6106. Such pump may be used, in some embodiments, to pump formation fluids from the bottom of the well. Pump 6107 may be a rod pump, progressing cavity pump (PCP), centrifugal pump, jet pump, gas lift pump, submersible pump, rotary pump, etc.

One or more heaters 6104 may be placed within each horizontal opening 6102. Heaters 6104 may be placed in hydrocarbon layer 6100 through vertical opening 6108 and into horizontal opening 6102.

In some embodiments, heater 6104 may be used to generate heat along a length of the heater within vertical opening 6108 and horizontal opening 6102. In other embodiments, heater 6104 may be used to generate heat only within horizontal opening 6102. In certain embodiments, heat generated by heater 6104 may be varied along its length and/or varied between vertical opening 6108 and horizontal opening 6102. For example, less heat may be generated by heater 6104 in vertical opening 6108 and more heat may be generated by the heater in horizontal opening 6102. It may be advantageous to have at least some heating within vertical opening 6108. This may maintain fluids produced from the formation in a vapor phase in production conduit 6106 and/or may upgrade the produced fluids within the production well. Having production conduit 6106 and heaters 6104 installed into a foπnation through a single opening in the foπnation may reduce costs associated with forming openings in the foπnation and installing production equipment and heaters within the formation.

FIG. 7 depicts a schematic view from an elevated position of the embodiment of FIG. 6. One or more vertical openings 6108 may be formed in hydrocarbon layer 6100. Each of vertical openings 6108 may lie along a single plane in hydrocarbon layer 6100. Horizontal openings 6102 may extend in a plane substantially peφendicular to the plane of vertical openings 6108. Additional horizontal openings 6102 may lie in a plane below the horizontal openings as shown in the schematic depiction of FIG. 6. A number of vertical openings 6108 and/or a spacing between vertical openings 6108 may be determined by, for example, a desired heating rate or a desired production rate. In some embodiments, spacing between vertical openings may be about 4 m to about 30 m. Longer or shorter spacings may be used to meet specific formation needs. A length of a horizontal opening 6102 may be up to about 1600 m. However, a length of horizontal openings 6102 may vary depending on, for example, a maximum installation cost, an area of hydrocarbon layer 6100, or a maximum producible heater length.

In an in situ conversion process embodiment, a formation having one or more thin hydrocarbon layers may be treated. In some in situ conversion process embodiments, such formations may be freated with heat sources that are positioned substantially horizontal within and/or adjacent to the thin hydrocarbon layer or thin hydrocarbon layers. A relatively thin hydrocarbon layer may be at a substantial depth below a ground surface. For example, a formation may have an overburden of up to about 650 m in depth. The cost of drilling a large number of substantially vertical wells within a formation to a significant depth may be expensive. It may be advantageous to place heaters horizontally within these formations to heat large portions of the formation for lengths up to about 1600 m. Using horizontal heaters may reduce the number of vertical wells that are needed to place a sufficient number of heaters within the formation.

FIG. 8 illustrates an embodiment of hydrocarbon containing layer 200 that may be at a near-horizontal angle with respect to an upper surface of ground 204. An angle of hydrocarbon containing layer 200, however, may vary. For example, hydrocarbon containing layer 200 may dip or be steeply dipping. Economically viable production of a steeply dipping hydrocarbon containing layer may not be possible using presently available mining methods.

A dipping or relatively steeply dipping hydrocarbon containing layer may be subjected to an in situ conversion process. For example, a set of production wells may be disposed near a highest portion of a dipping hydrocarbon layer of a relatively low permeability formation containing heavy hydrocarbons. Hydrocarbon portions adjacent to and below the production wells may be heated to pyrolysis temperature. Pyrolysis fluid may be produced from the production wells. As production from the top portion declines, deeper portions of the formation may be heated to pyrolysis temperatures. Vapors may be produced from the hydrocarbon containing layer by transporting vapor through the previously pyrolyzed hydrocarbons. High permeability resulting from pyrolysis and production of fluid from the upper portion of the formation may allow for vapor phase transport with minimal pressure loss. Vapor phase transport of fluids produced in the formation may eliminate a need to have deep production wells in addition to the set of production wells. A number of production wells required to process the formation may be reduced. Reducing the number of production wells required for production may increase economic viability of an in situ conversion process. hi steeply dipping formations, directional drilling may be used to form an opening in the formation for a heater well or production well. Directional drilling may include drilling an opening in which the route/course of the opening may be planned before drilling. Such an opening may usually be drilled with rotary equipment. In directional drilling, a route/course of an opening may be controlled by deflection wedges, etc.

A wellbore may be formed using a drill equipped with a steerable motor and an accelerometer. The steerable motor and accelerometer may allow the wellbore to follow a layer in the relatively low permeability formation containing heavy hydrocarbons. A steerable motor may maintain a substantially constant distance between heater well 202 and a boundary of hydrocarbon containing layer 200 throughout drilling of the opening.

In some in situ conversion embodiments, geosteered drilling may be used to drill a wellbore in a relatively low permeability formation containing heavy hydrocarbons. Geosteered drilling may include determining or estimating a distance from an edge of hydrocarbon containing layer 200 to the wellbore with a sensor. The sensor may monitor variations in characteristics or signals in the formation. The characteristic or signal variance may allow for determination of a desired drill path. The sensor may monitor resistance, acoustic signals, magnetic signals, gamma rays, and/or other signals within the formation. A drilling apparatus for geosteered drilling may include a steerable motor. The steerable motor may be controlled to maintain a predetermined distance from an edge of a hydrocarbon containing layer based on data collected by the sensor. In some in situ conversion embodiments, wellbores may be formed in a formation using other techniques.

Wellbores may be formed by impaction techniques and/or by sonic drilling techniques. The method used to form wellbores may be determined based on a number of factors. The factors may include, but are not limited to, accessibility of the site, depth of the wellbore, properties of the overburden, and properties of the hydrocarbon containing layer or layers. FIG. 9 illustrates an embodiment of a plurality of heater wells 210 formed in hydrocarbon layer 212.

Hydrocarbon layer 212 may be a steeply dipping layer. One or more of heater wells 210 may be formed in the formation such that two or more of the heater wells are substantially parallel to each other, and/or such that at least one heater well is substantially parallel to a boundary of hydrocarbon layer 212. For example, one or more of heater wells 210 may be formed in hydrocarbon layer 212 by a magnetic steering method. An example of a magnetic steering method is illustrated in U.S. Patent No. 5,676,212 to Kuckes, which is incoφorated by reference as if fully set forth herein. Magnetic steering may include drilling heater well 210 parallel to an adjacent heater well. The adjacent well may have been previously drilled. In addition, magnetic steering may include directing the drilling by sensing and/or determining a magnetic field produced in an adjacent heater well. For example, the magnetic field may be produced in the adjacent heater well by flowing a current through an insulated current- carrying wireline disposed in the adjacent heater well.

Magnetic steering may include directing the drilling by sensing and/or determining a magnetic field produced in an adjacent well. For example, the magnetic field may be produced in the adjacent well by flowing a current through an insulated cuπent-caπying wireline disposed in the adjacent well. In some embodiments, magnetostatic steering may be used to form openings adjacent to a first opening. U.S. Patent No. 5,541,517, issued to Hartmann et al., which is incoφorated by reference as if fully set forth herein, describes a method for drilling a wellbore relative to a second wellbore that has magnetized casing portions.

When drilling a wellbore (opening), a magnet or magnets may be inserted into a first opening to provide a magnetic field used to guide a drilling mechanism that forms an adjacent opening or adjacent openings. The magnetic field may be detected by a 3-axis fluxgate magnetometer in the opening being drilled. A control system may use information detected by the magnetometer to determine and implement operation parameters needed to form an opening that is a selected distance away (e.g., parallel) from the first opening (within desired tolerances). Some types of wells may require or need close tolerances. For example, freeze wells may need to be positioned parallel to each other with small or no variance in parallel alignment to allow for formation of a continuous frozen barrier around a freatment area. Also, vertical and/or horizontally positioned heater wells and/or production wells may need to be positioned parallel to each other with small or no variance in parallel alignment to allow for substantially unifonn heating and/or production from a treatment area in a formation.

FIG. 10 depicts a schematic representation of an embodiment of a magnetostatic drilling operation to form an opening that is a selected distance away from (e.g., substantially parallel to) a drilled opening. Opening 514 may be formed in formation 6100. Opening 514 may be a cased opening or an open hole opening. Magnetic sfring 9678 may be inserted into opening 514. Magnetic string 9678 may be unwound from a reel into opening 514. In an embodiment, magnetic string includes several segments 9680 of magnets within casing 6152.

In some embodiments, casing 6152 may be a conduit made of a material that is not significantly influenced by a magnetic field (e.g., non-magnetic alloy such as non-magnetic stainless steel (e.g., 304, 310, 316 stainless steel), reinforced polymer pipe, or brass tubing). The casing may be a conduit of a conductor-in-conduit heater, or it may be perforated liner or casing. If the casing is not significantly influenced by a magnetic field, then the magnetic flux will not be shielded. In other embodiments, the casing may be made of a material that is influenced by a magnetic field (e.g., carbon steel). The use of a material that is influenced by a magnetic field may weaken the strength of the magnetic field to be detected by drilling apparatus 9684 in adjacent opening 9685.

Magnets may be inserted in conduits 9681 in segments 9680. Conduits 9681 may be threaded or seamless coiled tubing (e.g., tubing having an inside diameter of about 5 cm). Members 9682 (e.g., pins) may be placed between segments 9680 to inhibit movement of segments 9680 relative to conduit 9681. Magnets from adjoining segments of conduit may be close to each other or touch each other as, for example, threaded sections of conduit are ^' tightened together. A segment may be made of several north-south aligned magnets. Alignment of the magnets allows each segment to effectively be a long magnet. In an embodiment, a segment may include one magnet. Magnets may be Alnico magnets or other types of magnets having significant magnetic strength. Two adjacent segments may be oriented to have opposite polarities so that the segments repel each other.

The magnetic string may include 2 or more magnetic segments. Segments may range in length from about 1.5 m to about 15 m. Magnetic segments may be formed from several magnets. Magnets used to form segments may have diameters greater than about 1 cm (about 4.5 cm). The magnets may be oriented so that the magnets are attracted to each other. For example, a segment may be made of 40 magnets each having a length of about 0.15 m. FIG. 11 depicts a schematic of a portion of magnetic string. Segments 9680 may be positioned such that adjacent segments 9680 have opposing polarities. In some embodiments, force may be applied to minimize distance 9692 between segments 9680. Additional segments may be added to increase a length of magnetic string 9678. Magnetic strings may be coiled after assembling. Installation of the magnetic string may include uncoiling the magnetic string. For example, first segment 9697 may be positioned north-south in the conduit and second segment 9698 may be positioned south-north such that the south poles of segments 9697, 9698 are proximate each other. Third segment 9696 may positioned in the conduit may be positioned in a north-south orientation such that the north poles of segments 9697, 9696 are proximate each other. Magnet strings may include multiple south-south and north- north interfaces. As shown in FIG. 11, this configuration may induce a series of magnetic fields 9694. Alternating the polarity of the segments within a magnetic string may provide several magnetic field differentials that allow for reduction in the amount of deviation that is a selected distance between the openings. Increasing a length of the segments within the magnetic string may increase the radial distance at which the magnetometer may detect a magnetic field. In some embodiments, the length of segments within the magnetic sfring may be varied. For example, more magnets may be used in the segment proximate the earth's surface than in segments positioned in the formation. In an embodiment, when the separation distance between two wellbores increases, then the segment length of the magnetic strings may also be increased, and vice versa. With shorter segment lengths, while the overall strength of the magnetic field is decreased, variations in the magnetic field occur more frequently, thus providing more guidance to the drilling operation. For example, segments having a length of about 6 m may induce a magnetic field sufficient to allow drilling of adjacent openings at distances of less than about 16 m. This configuration may allow a desired tolerance between the adjacent openings to be achieved.

In alternate embodiments, the strength of the magnets used may affect a strength of the magnetic field induced. For example, when using magnets having a lower strength than those in the example above, a segment length of about 6 m may induce a magnetic field sufficient to drill adjacent openings at distances of less than about 6 m. In some embodiments, a segment length of about 6 m may induce a magnetic field sufficient to drill adjacent openings at distances of less than about 10 m

A length of the magnetic string may be based on an economic balance between cost of the string and the cost of having to reposition the sfring during drilling. A string length may range from about 30 m to about 500 m. In an embodiment, a magnetic sfring may have a length of about 150 m. Thus, in some embodiments, the magnetic string may need to be repositioned if the openings being drilled are longer than the length of the string. When multiple wellbores are to be drilled, it is possible to initially drill a center wellbore, and then use magnetic strings in that center wellbore to guide the drilling of the other wellbores substantially surrounding the center wellbore. In this manner cumulative eπors may be limited since, for example, movement of the magnetic string may be minimized. In addition, only the center well in this embodiment will include a more expensive nonmagnetic liner. In some embodiments, heated portion 310 may extend radially from heat source 300, as shown in FIG. 12.

For example, a width of heated portion 310, in a direction extending radially from heat source 300, may be about 0 m to about 10 m. A width of heated portion 310 may vary, however, depending upon, for example, heat provided by heat source 300 and the characteristics of the formation. Heat provided by heat source 300 will typically transfer through the heated portion to create a temperature gradient within the heated portion. For example, a temperature proximate the heater well will generally be higher than a temperature proximate an outer lateral boundary of the heated portion. A temperature gradient within the heated portion may vary within the heated portion depending on various factors (e.g., thermal conductivity of the formation, density, and porosity).

As heat transfers through heated portion 310 of the relatively low permeability formation containing heavy hydrocarbons, a temperature within at least a section of the heated portion may be within a pyrolysis temperature range. As the heat transfers away from the heat source, a front at which pyrolysis occurs will in many instances travel outward from the heat source. For example, heat from the heat source may be allowed to transfer into a selected section of the heated portion such that heat from the heat source pyrolyzes at least some of the hydrocarbons within the selected section. Pyrolysis may occur within selected section 315 of the heated portion, and pyrolyzation fluids will be generated in the selected section. Selected section 315 may have a width radially extending from the inner lateral boundary of the selected section. For a single heat source as depicted in FIG. 12, width of the selected section may be dependent on a number of factors. The factors may include, but are not limited to, time that heat source 300 is supplying energy to the fonnation, thermal conductivity properties of the formation, extent of pyrolyzation of hydrocarbons in the formation. A width of selected section 315 may expand for a significant time after initialization of heat source 300. A width of selected section 315 may initially be zero and may expand to 10 m or more after initialization of heat source 300.

An inner boundary of selected section 315 may be radially spaced from the heat source. The inner boundary may define a volume of spent hydrocarbons 317. Spent hydrocarbons 317 may include a volume of hydrocarbon material that is transformed to coke due to the proximity and heat of heat source 300. Coking may occur by pyrolysis reactions that occur due to a rapid increase in temperature in a short time period. Applying heat to a formation at a controlled rate may allow for avoidance of significant coking, however, some coking may occur in the vicinity of heat sources. Spent hydrocarbons 317 may also include a volume of material that has been subjected to pyrolysis and the removal of pyrolysis fluids. The volume of material that has been subjected to pyrolysis and the removal of pyrolysis fluids may produce insignificant amounts or no additional pyrolysis fluids with increases in temperature. The inner lateral boundary may advance radially outwards as time progresses during operation of an in situ conversion process.

In some embodiments, a plurality of heated portions may exist within a unit of heat sources. A unit of heat sources refers to a minimal number of heat sources that form a template that is repeated to create a pattern of heat sources within the formation. The heat sources may be located within the formation such that supeφosition (overlapping) of heat produced from the heat sources occurs. For example, as illustrated in FIG. 13, transfer of heat from two or more heat sources 330 results in supeφosition of heat to region 332 between the heat sources 330.

Supeφosition of heat may occur between two, three, four, five, six, or more heat sources. Region 332 is an area in which temperature is influenced by various heat sources. Supeφosition of heat may provide the ability to efficiently raise the temperature of large volumes of a formation to pyrolysis temperatures. The size of region 332 may be significantly affected by the spacing between heat sources. Supeφosition of heat may increase a temperature in at least a portion of the formation to a temperature sufficient for pyrolysis of hydrocarbons within the portion. Supeφosition of heat to region 332 may increase the quantity of hydrocarbons in a foπnation that are subjected to pyrolysis. Selected sections of a formation that are subjected to pyrolysis may include regions 334 brought into a pyrolysis temperature range by heat fransfer from substantially only one heat source. Selected sections of a formation that are subjected to pyrolysis may also include regions 332 brought into a pyrolysis temperature range by supeφosition of heat from multiple heat sources.

A pattern of heat sources will often include many units of heat sources. There will typically be many heated portions, as well as many selected sections within the pattern of heat sources. Supeφosition of heat within a pattern of heat sources may decrease the time necessary to reach pyrolysis temperatures within the multitude of heated portions. Supeφosition of heat may allow for a relatively large spacing between adjacent heat sources. In some embodiments, a large spacing may provide for a relatively slow heating rate of hydrocarbon material. The slow heating rate may allow for pyrolysis of hydrocarbon material with minimal coking or no coking within the formation away from areas in the vicinity of the heat sources. Heating from heat sources allows the selected section to reach pyrolysis temperatures so that all hydrocarbons within the selected section may be subject to pyrolysis reactions. In some in situ conversion embodiments, a majority of pyrolysis fluids are produced when the selected section is within a range from about 0 m to about 25 m from a heat source. In an in situ conversion process embodiment, a heating rate may be controlled to minimize costs associated with heating a selected section. The costs may include, for example, input energy costs and equipment costs. In certain embodiments, a cost associated with heating a selected section may be minimized by reducing a heating rate when the cost associated with heating is relatively high and increasing the heating rate when the cost associated with heating is relatively low. For example, a heating rate of about 330 watts/m may be used when the associated cost is relatively high, and a heating rate of about 1640 watts/m may be used when the associated cost is relatively low. The cost associated with heating may be relatively high at peak times of energy use, such as during the daytime. For example, energy use may be high in warm climates during the daytime in the summer due to energy use for air conditioning. Low times of energy use may be, for example, at night or during weekends, when energy demand tends to be lower. In an embodiment, the heating rate may be varied from a higher heating rate during low energy usage times, such as during the night, to a lower heating rate during high energy usage times, such as during the day.

As shown in FIG. 2, in addition to heat sources 100, one or more production wells 104 will typically be placed within the portion of the relatively low permeability formation containing heavy hydrocarbons. Formation fluids may be produced through production well 104. In some embodiments, production well 104 may include a heat source. The heat source may heat the portions of the formation at or near the production well and allow for vapor phase removal of formation fluids. The need for high temperature pumping of liquids from the production well may be reduced or eliminated. Avoiding or limiting high temperature pumping of liquids may significantly decrease production costs. Providing heating at or through the production well may: (1) inhibit condensation and/or refluxing of production fluid when such production fluid is moving in the production well proximate the overburden, (2) increase heat input into the formation, and/or (3) increase foπnation permeability at or proximate the production well. In some in situ conversion process embodiments, an amount of heat supplied to production wells is significantly less than an amount of heat applied to heat sources that heat the formation.

Because permeability and/or porosity increases in the heated formation, produced vapors may flow considerable distances through the formation with relatively little pressure differential. Increases in permeability may result from a reduction of mass of the heated portion due to vaporization of water, removal of hydrocarbons, and or creation of fractures. Fluids may flow more easily through the heated portion. In some embodiments, production wells may be provided in upper portions of hydrocarbon layers. As shown in FIG. 8, production wells 206 may extend into a relatively low permeability formation containing heavy hydrocarbons near the top of heated portion 208. Extending production wells significantly into the depth of the heated hydrocarbon layer may be unnecessary.

Fluid generated within a relatively low permeability formation containing heavy hydrocarbons may move a considerable distance through the relatively low permeability formation containing heavy hydrocarbons as a vapor. The considerable distance may be over 1000 m depending on various factors (e.g., permeability of the formation, properties of the fluid, temperature of the formation, and pressure gradient allowing movement of the fluid). Due to increased permeability in formations subjected to in situ conversion and formation fluid removal, production wells may only need to be provided in every other unit of heat sources or every third, fourth, fifth, or sixth units of heat sources.

Embodiments of a production well may include valves that alter, maintain, and/or control a pressure of at least a portion of the formation. Production wells may be cased wells. Production wells may have production screens or perforated casings adjacent to production zones. In addition, the production wells may be surrounded by sand, gravel or other packing materials adjacent to production zones. Production wells 104 may be coupled to treatment facilities 108, as shown in FIG. 2.

During an in situ process, production wells may be operated such that the production wells are at a lower pressure than other portions of the formation. In some embodiments, a vacuum may be drawn at the production wells. Maintaining the production wells at lower pressures may inhibit fluids in the formation from migrating outside of the in situ freatment area.

FIG. 14 illustrates an embodiment of production well 6108 placed in hydrocarbon layer 6100. Production well 6108 may be used to produce foπnation fluids from hydrocarbon layer 6100. Hydrocarbon layer 6100 may be treated using an in situ conversion process. Production conduit 6106 may be placed within production well 6108. In an embodiment, production conduit 6106 is a hollow sucker rod placed in production well 6108. Production well

6108 may have a casing, or lining, placed along the length of the production well. The casing may have openings, or perforations, to allow formation fluids to enter production well 6108. Foπnation fluids may mclude vapors and/or liquids. Production conduit 6106 and production well 6108 may include non-corrosive materials such as steel. In certain embodiments, production conduit 6106 may include heat source 6105. Heat source 6105 may be a heater placed inside or outside production conduit 6106 or formed as part of the production conduit. Heat source

6105 may be a heater such as an insulated conductor heater, a conductor-in-conduit heater, or a skin-effect heater. A skin-effect heater is an electric heater that uses eddy current heating to induce resistive losses in production conduit 6106 to heat the production conduit. An example of a skin-effect heater is obtainable from Dagang Oil Products (China).

Heating of production conduit 6106 may inhibit condensation and/or refluxing in the production conduit or within production well 6108. In certain embodiments, heating of production conduit 6106 may inhibit plugging of pump 6107 by liquids (e.g., heavy hydrocarbons). For example, heat source 6105 may heat production conduit

6106 to about 35 °C to maintain the mobility of liquids in the production conduit to inhibit plugging of pump 6107 or the production conduit. In certain embodiments (e.g., for formations greater than about 100 m in depth), heat source 6105 may heat production conduit 6106 and/or production well 6108 to temperatures of about 200 °C to about 250 °C to maintain produced fluids substantially in a vapor phase by inhibiting condensation and/or reflux of fluids in the production well.

Pump 6107 may be coupled to production conduit 6106. Pump 6107 may be used to pump formation fluids from hydrocarbon layer 6100 into production conduit 6106. Pump 6107 may be any pump used to pump fluids, such as a rod pump, PCP, jet pump, gas lift pump, centrifugal pump, rotary pump, or submersible pump.

Pump 6107 may be used to pump fluids through production conduit 6106 to a surface of the formation above overburden 540.

In certain embodiments, pump 6107 can be used to pump formation fluids that may be liquids. Liquids may be produced from hydrocarbon layer 6100 prior to production well 6108 being heated to a temperature sufficient to vaporize liquids within the production well. In some embodiments, liquids produced from the formation tend to include water. Removing liquids from the formation before heating the formation, or during early times of heating before pyrolysis occurs, tends to reduce the amount of heat input that is needed to produce hydrocarbons from the formation. In an embodiment, formation fluids that are liquids may be produced through production conduit 6106 using pump 6107. Formation fluids that are vapors may be simultaneously produced through an annulus of production well 6108 outside of production conduit 6106.

Insulation may be placed on a wall of production well 6108 in a section of the production well within overburden 540. The insulation may be cement or any other suitable low heat fransfer material. Insulating the overburden section of production well 6108 may inhibit transfer of heat from fluids being produced from the formation into the overburden.

In an in situ conversion process embodiment, a mixture may be produced from a relatively low permeability formation containing heavy hydrocarbons. The mixture may be produced through a heater well disposed in the formation. Producing the mixture through the heater well may increase a production rate of the mixture as compared to a production rate of a mixture produced through a non-heater well. A non-heater well may include a production well. In some embodiments, a production well may be heated to increase a production rate.

A heated production well may inhibit condensation of higher carbon numbers (C₅ or above) in the production well. A heated production well may inhibit problems associated with producing a hot, multi-phase fluid from a formation.

A heated production well may have an improved production rate as compared to a non-heated production well. Heat applied to the formation adjacent to the production well from the production well may increase formation permeability adjacent to the production well by vaporizing and removing liquid phase fluid adjacent to the production well and/or by increasing the permeability of the formation adjacent to the production well by formation of macro and or micro fractures. A heater in a lower portion of a production well may be turned off when supeφosition of heat from heat sources heats the formation sufficiently to counteract benefits provided by heating from within the production well. In some embodiments, a heater in an upper portion of a production well may remain on after a heater in a lower portion of the well is deactivated. The heater in the upper portion of the well may inhibit condensation and reflux of formation fluid. In some embodiments, heated production wells may improve product quality by causing production through a hot zone in the formation adjacent to the heated production well. A final phase of thermal cracking may exist in the hot zone adjacent to the production well. Producing through a hot zone adjacent to a heated production well may allow for an increased olefin content in non-condensable hydrocarbons and/or condensable hydrocarbons in the formation fluids. The hot zone may produce formation fluids with a greater percentage of non-condensable hydrocarbons due to thermal cracking in the hot zone. The extent of thermal cracking may depend on a temperature of the hot zone and/or on a residence time in the hot zone. A heater can be deliberately run hotter to promote the fiirther in situ upgrading of hydrocarbons. This may be an advantage in the case of heavy hydrocarbons in which some heavy hydrocarbons tend to flow into the production well before sufficient upgrading has occurred.

In an embodiment, heating in or proximate a production well may be controlled such that a desired mixture is produced through the production well. The desired mixture may have a selected yield of non-condensable hydrocarbons. For example, the selected yield of non-condensable hydrocarbons may be about 75 weight % non- condensable hydrocarbons or, in some embodiments, about 50 weight % to about 100 weight %. In other embodiments, the desired mixture may have a selected yield of condensable hydrocarbons. The selected yield of condensable hydrocarbons may be about 75 weight % condensable hydrocarbons or, in some embodiments, about 50 weight % to about 95 weight %. A temperature and a pressure may be controlled within the formation to inhibit the production of carbon dioxide and increase production of carbon monoxide and molecular hydrogen during synthesis gas production. In an embodiment, the mixture is produced through a production well (or heater well), which may be heated to inhibit the production of carbon dioxide. In some embodiments, a mixture produced from a first portion of the formation may be recycled into a second portion of the formation to inhibit the production of carbon dioxide. The mixture produced from the first portion may be at a lower temperature than the mixture produced from the second portion of the formation.

A desired volume ratio of molecular hydrogen to carbon monoxide in synthesis gas may be produced from the formation. The desired volume ratio may be about 2.0:1. In an embodiment, the volume ratio may be maintained between about 1.8:1 and 2.2:1 for synthesis gas.

FIG. 15 illustrates a pattern of heat sources 400 and production wells 402 that may be used to treat a relatively low permeability formation containing heavy hydrocarbons. Heat sources 400 may be arranged in a unit of heat sources such as triangular pattern 401. Heat sources 400, however, may be arranged in a variety of patterns including, but not limited to, squares, hexagons, and other polygons. The pattern may include a regular polygon to promote uniform heating of the formation in which the heat sources are placed. The pattern may also be a line drive pattern. A line drive pattern generally includes a first linear array of heater wells, a second linear array of heater wells, and a production well or a linear array of production wells between the first and second linear aπay of heater wells.

A distance from a node of a polygon to a centroid of the polygon is smallest for a 3 -sided polygon and increases with increasing number of sides of the polygon. The distance from a node to the centroid for an equilateral triangle is (length/2)/(square root(3)/2) or 0.5774 times the length. For a square, the distance from a node to the centroid is (length/2)/(square root(2)/2) or 0.7071 times the length. For a hexagon, the distance from a node to the centroid is (Iength/2)/(l/2) or the length. The difference in distance between a heat source and a midpoint to a second heat source (length/2) and the distance from a heat source to the centroid for an equilateral pattern (0.5774 times the length) is significantly less for the equilateral triangle pattern than for any higher order polygon pattern. The small difference means that supeφosition of heat may develop more rapidly and that the formation may rise to a more uniform temperature between heat sources using an equilateral triangle pattern rather than a higher order polygon pattern.

Triangular patterns tend to provide more uniform heating to a portion of the formation in comparison to other patterns such as squares and/or hexagons. Triangular patterns tend to provide faster heating to a predetermined temperature in comparison to other patterns such as squares or hexagons. The use of triangular patterns may result in smaller volumes of a formation being overheated. A plurality of units of heat sources such as triangular pattern 401 may be aπanged substantially adjacent to each other to form a repetitive pattern of units over an area of the formation. For example, triangular patterns 401 may be arranged substantially adjacent to each other in a repetitive pattern of units by inverting an orientation of adjacent triangles 401. Other patterns of heat sources

400 may also be arranged such that smaller patterns may be disposed adjacent to each other to form larger patterns. Production wells may be disposed in the formation in a repetitive pattern of units. In certain embodiments, production well 402 may be disposed proximate a center of every third triangle 401 arranged in the pattern. Production well 402, however, may be disposed in every triangle 401 or within just a few triangles. In some embodiments, a production well may be placed within every 13, 20, or 30 heater well triangles. For example, a ratio of heat sources in the repetitive pattern of units to production wells in the repetitive pattern of units may be more than approximately 5 (e.g., more than 6, 7, 8, or 9). In some well pattern embodiments, three or more production wells may be located within an area defined by a repetitive pattern of units. For example, as shown in FIG. 15, production wells 410 may be located within an area defined by repetitive pattern of units 412. Production wells 410 may be located in the formation in a unit of production wells. The location of production wells 402, 410 within a pattern of heat sources 400 may be determined by, for example, a desired heating rate of the relatively low permeability formation containing heavy hydrocarbons, a heating rate of the heat sources, the type of heat sources used, the type of relatively low permeability formation containing heavy hydrocarbons (and its thickness), the composition of the relatively low permeability formation containing heavy hydrocarbons, permeability of the formation, the desired composition to be produced from the formation, and/or a desired production rate. One or more injection wells may be disposed within a repetitive pattern of units. For example, as shown in

FIG. 15, injection wells 414 may be located within an area defined by repetitive pattern of units 416. Injection wells 414 may also be located in the formation in a unit of injection wells. For example, the unit of injection wells may be a triangular pattern. Injection wells 414, however, may be disposed in any other pattern. In certain embodiments, one or more production wells and one or more injection wells may be disposed in a repetitive pattern of units. For example, as shown in FIG. 15, production wells 418 and injection wells 420 may be located within an area defined by repetitive pattern of units 422. Production wells 418 may be located in the formation in a unit of production wells, which may be arranged in a first triangular pattern. In addition, injection wells 420 may be located within the formation in a unit of production wells, which are aπanged in a second triangular pattern. The first triangular pattern may be different than the second triangular pattern. For example, areas defined by the first and second triangular patterns may be different.

One or more monitoring wells may be disposed within a repetitive pattern of units. Monitoring wells may include one or more devices that measure temperature, pressure, and/or fluid properties. In some embodiments, logging tools may be placed in monitoring well wellbores to measure properties within a formation. The logging tools may be moved to other monitoring well wellbores as needed. The monitoring well wellbores may be cased or uncased wellbores. As shown in FIG. 15, monitoring wells 424 may be located within an area defined by repetitive pattern of units 426. Monitoring wells 424 may be located in the formation in a unit of monitoring wells, which may be aπanged in a triangular pattern. Monitoring wells 424, however, may be disposed in any of the other patterns within repetitive pattern of units 426.

It is to be understood that a geometrical pattern of heat sources 400 and production wells 402 is described herein by example. A pattern of heat sources and production wells will in many instances vary depending on, for example, the type of relatively low permeability formation containing heavy hydrocarbons to be treated. For example, for relatively thin layers, heater wells may be aligned along one or more layers along strike or along dip. For relatively thick layers, heat sources may be at an angle to one or more layers (e.g., orthogonally or diagonally). A triangular pattern of heat sources may treat a hydrocarbon layer having a thickness of about 10 m or more. For a thin hydrocarbon layer (e.g., about 10 m thick or less) a line and/or staggered line pattern of heat sources may treat the hydrocarbon layer.

For certain thin layers, heating wells may be placed close to an edge of the layer (e.g., in a staggered line instead of a line placed in the center of the layer) to increase the amount of hydrocarbons produced per unit of energy input. A portion of input heating energy may heat non-hydrocarbon portions of the formation, but the staggered pattern may allow supeφosition of heat to heat a majority of the hydrocarbon layers to pyrolysis temperatures. If the thin formation is heated by placing one or more heater wells in the layer along a center of the thickness, a significant portion of the hydrocarbon layers may not be heated to pyrolysis temperatures. In some embodiments, placing heater wells closer to an edge of the layer may increase the volume of layer undergoing pyrolysis per unit of energy input.

Exact placement of heater wells, production wells, etc. will depend on variables specific to the formation (e.g., thickness of the layer or composition of the layer), project economics, etc. In certain embodiments, heater wells may be substantially horizontal while production wells may be vertical, or vice versa. In some embodiments, wells may be aligned along dip or strike or oriented at an angle between dip and strike.

The spacing between heat sources may vary depending on a number of factors. The factors may include, but are not limited to, the type of a relatively low permeability formation, the selected heating rate, and or the selected average temperature to be obtained within the heated portion. In some well pattern embodiments, the spacing between heat sources may be within a range of about 5 m to about 25 m. In some well pattern embodiments, spacing between heat sources may be within a range of about 8 m to about 15 m.

The spacing between heat sources may influence the composition of fluids produced from a relatively low permeability formation containing heavy hydrocarbons. In an embodiment, a computer-implemented simulation may be used to determine optimum heat source spacings within a relatively low permeability formation containing heavy hydrocarbons. At least one property of a portion of relatively low permeability formation containing heavy hydrocarbons can usually be measured. The measured property may include, but is not limited to, hydrogen content, atomic hydrogen to carbon ratio, oxygen content, atomic oxygen to carbon ratio, water content, thickness of the relatively low permeability formation containing heavy hydrocarbons, and/or the amount of stratification of the relatively low permeability formation containing heavy hydrocarbons into separate layers of rock and hydrocarbons.

In certain embodiments, a computer-implemented simulation may include providing at least one measured property to a computer system. One or more sets of heat source spacings in the formation may also be provided to the computer system. For example, a spacing between heat sources may be less than about 30 m. Alternatively, a spacing between heat sources may be less than about 15 m. The simulation may include determining properties of fluids produced from the portion as a function of time for each set of heat source spacings. The produced fluids may include formation fluids such as pyrolyzation fluids or synthesis gas. The determined properties may include, but are not limited to, API gravity, carbon number distribution, olefin content, hydrogen content, carbon monoxide content, and/or carbon dioxide content. The determined set of properties of the produced fluid may be compared to a set of selected properties of a produced fluid. Sets of properties that match the set of selected properties may be determined. Furthermore, heat source spacings may be matched to heat source spacings associated with desired properties.

As shown in FIG. 15, unit cell 404 will often include a number of heat sources 400 disposed within a formation around each production well 402. An area of unit cell 404 may be determined by midlines 406 that may be equidistant and peφendicular to a line connecting two production wells 402. Vertices 408 of the unit cell may be at the intersection of two midlines 406 between production wells 402. Heat sources 400 may be disposed in any arrangement within the area of unit cell 404. For example, heat sources 400 may be located within the formation such that a distance between each heat source varies by less than approximately 10 %, 20 %, or 30 %. In addition, heat sources 400 may be disposed such that an approximately equal space exists between each of the heat sources. Other arrangements of heat sources 400 within unit cell 404 may be used. A ratio of heat sources 400 to production wells 402 may be determined by counting the number of heat sources 400 and production wells 402 within unit cell 404 or over the total field.

FIG. 16 illustrates an embodiment of unit cell 404. Unit cell 404 includes heat sources 400 and production well 402. Unit cell 404 may have six full heat sources 400a and six partial heat sources 400b. Full heat sources 400a may be closer to production well 402 than partial heat sources 400b. In addition, an entirety of each of full heat sources 400a may be located within unit cell 404. Partial heat sources 400b may be partially disposed within unit cell 404. Only a portion of heat source 400b disposed within unit cell 404 may provide heat to a portion of a relatively low permeability formation containing heavy hydrocarbons disposed within unit cell 404. A remaining portion of heat source 400b disposed outside of unit cell 404 may provide heat to a remaining portion of the relatively low permeability formation containing heavy hydrocarbons outside of unit cell 404. To detennine a number of heat sources within unit cell 404, partial heat source 400b may be counted as one-half of full heat source 400a. In other unit cell embodiments, fractions other than 1/2 (e.g., 1/3) may more accurately describe the amount of heat applied to a portion from a partial heat source based on geometrical considerations.

The total number of heat sources 400 in unit cell 404 may include six full heat sources 400a that are each counted as one heat source, and six partial heat sources 400b that are each counted as one-half of a heat source.

Therefore, a ratio of heat sources 400 to production wells 402 in unit cell 404 may be determined as 9:1. A ratio of heat sources to production wells may be varied, however, depending on, for example, the desired heating rate of the relatively low permeability formation containing heavy hydrocarbons, the heating rate of the heat sources, the type of heat source, the type of a relatively low permeability formation, the composition of relatively low peπneability formation containing heavy hydrocarbons, the desired composition of the produced fluid, and/or the desired production rate. Providing more heat source wells per unit area will allow faster heating of the selected portion and thus hasten the onset of production. However, adding more heat sources will generally cost more money in installation and equipment. An appropriate ratio of heat sources to production wells may include ratios greater than about 5:1. In some embodiments, an appropriate ratio of heat sources to production wells may be about 10:1, 20:1, 50:1, or greater. If larger ratios are used, then project costs tend to decrease since less wells and equipment are needed.

A selected section is generally the volume of formation that is within a perimeter defined by the location of the outermost heat sources (assuming that the formation is viewed from above). For example, if four heat sources were located in a single square pattern with an area of about 100 m² (with each source located at a comer of the square), and if the formation had an average thickness of approximately 5 m across this area, then the selected section would be a volume of about 500 m³ (i.e., the area multiplied by the average formation thickness across the area). In many commercial applications, many heat sources (e.g., hundreds or thousands) may be adjacent to each other to heat a selected section, and therefore only the outermost heat sources (i.e., edge heat sources) would define the perimeter of the selected section. FIG. 17 illustrates a typical computational system 6250 that is suitable for implementing various embodiments of the system and method for in situ processing of a formation. Each computational system 6250 typically includes components such as one or more central processing units (CPU) 6252 with associated memory mediums, represented by floppy disks or compact discs (CDs) 6260. The memory mediums may store program instructions for computer programs, wherein the program instructions are executable by CPU 6252. Computational system 6250 may further include one or more display devices such as monitor 6254, one or more alphanumeric input devices such as keyboard 6256, and one or more directional input devices such as mouse 6258. Computational system 6250 is operable to execute the computer programs to implement (e.g., control, design, simulate, and/or operate) in situ processing of formation systems and methods.

Computational system 6250 preferably includes one or more memory mediums on which computer programs according to various embodiments may be stored. The term "memory medium" may include an installation medium, e.g., CD-ROM or floppy disks 6260, a computational system memory such as DRAM, SRAM, EDO DRAM, SDRAM,

DDR SDRAM, Rambus RAM, etc., or a non-volatile memory such as a magnetic media (e.g., a hard drive) or optical storage. The memory medium may include other types of memory as well, or combinations thereof. In addition, the memory medium may be located in a first computer that is used to execute the programs. Alternatively, the memory medium may be located in a second computer, or other computers, connected to the first computer (e.g., over a network). In the latter case, the second computer provides the program instructions to the first computer for execution.

Also, computational system 6250 may take various forms, including a personal computer, mainframe computational system, workstation, network appliance, Internet appliance, personal digital assistant (PDA), television system, or other device. In general, the term "computational system" can be broadly defined to encompass any device, or system of devices, having a processor that executes instructions from a memory medium. The memory medium preferably stores a software program or programs for event-triggered transaction processing. The software program(s) may be implemented in any of various ways, including procedure-based techniques, component-based techniques, and/or object-oriented techniques, among others. For example, the software program may be implemented using ActiveX controls, C++ objects, JavaBeans, Microsoft Foundation Classes (MFC), or other technologies or methodologies, as desired. A CPU, such as host CPU 6252, executing code and data from the memory medium, includes a system/process for creating and executing the software program or programs according to the methods and/or block diagrams described below.

In one embodiment, the computer programs executable by computational system 6250 may be implemented in an object-oriented programming language. In an object-oriented programming language, data and related methods can be grouped together or encapsulated to form an entity known as an object. All objects in an object-oriented programming system belong to a class, which can be thought of as a category of like objects that describes the characteristics of those objects. Each object is created as an instance of the class by a program. The objects may therefore be said to have been instantiated from the class. The class sets out variables and methods for objects that belong to that class. The definition of the class does not itself create any objects. The class may define initial values for its variables, and it normally defines the methods associated with the class (e.g., includes the program code which is executed when a method is invoked). The class may thereby provide all of the program code that will be used by objects in the class, hence maximizing re-use of code that is shared by objects in the class.

Turning now to FIG. 18, a block diagram of one embodiment of computational system 6270 including processor 6293 coupled to a variety of system components through bus bridge 6292 is shown. Other embodiments are possible and contemplated. In the depicted system, main memory 6296 is coupled to bus bridge 6292 through memory bus 6294, and graphics controller 6288 is coupled to bus bridge 6292 through AGP bus 6290. Finally, a plurality of PCI devices 6282 and 6284 are coupled to bus bridge 6292 through PCI bus 6276. Secondary bus bridge 6274 may further be provided to accommodate an electrical interface to one or more EISA or ISA devices 6280 through EISA/ISA bus 6278. Processor 6293 is coupled to bus bridge 6292 through CPU bus 6295 and to optional L2 cache 6297. Bus bridge 6292 provides an interface between processor 6293, main memory 6296, graphics controller

6288, and devices attached to PCI bus 6276. When an operation is received from one of the devices connected to bus bridge 6292, bus bridge 6292 identifies the target of the operation (e.g., a particular device or, in the case of PCI bus 6276, that the target is on PCI bus 6276). Bus bridge 6292 routes the operation to the targeted device. Bus bridge 6292 generally translates an operation from the protocol used by the source device or bus to the protocol used by the target device or bus. In addition to providing an interface to an ISA/EISA bus for PCI bus 6276, secondary bus bridge 6274 may further incoφorate additional functionality, as desired. An input/output confroller (not shown), either external from or integrated with secondary bus bridge 6274, may also be included within computational system 6270 to provide operational support for keyboard and mouse 6272 and for various serial and parallel ports, as desired. An external cache unit (not shown) may further be coupled to CPU bus 6295 between processor 6293 and bus bridge 6292 in other embodhnents. Alternatively, the external cache may be coupled to bus bridge 6292 and cache control logic for the external cache may be integrated into bus bridge 6292. L2 cache 6297 is further shown in a backside configuration to processor 6293. It is noted that L2 cache 6297 may be separate from processor 6293, integrated into a cartridge (e.g., slot 1 or slot A) with processor 6293, or even integrated onto a semiconductor substrate with processor 6293. Main memory 6296 is a memory in which application programs are stored and from which processor 6293 primarily executes. A suitable main memory 6296 comprises DRAM (Dynamic Random Access Memory). For example, a plurality of banks of SDRAM (Synchronous DRAM), DDR (Double Data Rate) SDRAM, or Rambus DRAM (RDRAM) may be suitable.

PCI devices 6282 and 6284 are illustrative of a variety of peripheral devices such as, for example, network interface cards, video accelerators, audio cards, hard or floppy disk drives or drive controllers, SCSI (Small

Computer Systems Interface) adapters, and telephony cards. Similarly, ISA device 6280 is illustrative of various types of peripheral devices, such as a modem, a sound card, and a variety of data acquisition cards such as GPIB or field bus interface cards.

Graphics confroller 6288 is provided to confrol the rendering of text and images on display 6286. Graphics controller 6288 may embody a typical graphics accelerator generally known in the art to render three- dimensional data structures that can be effectively shifted into and from main memory 6296. Graphics controller 6288 may therefore be a master of AGP bus 6290 in that it can request and receive access to a target interface within bus bridge 6292 to thereby obtain access to main memory 6296. A dedicated graphics bus accommodates rapid retrieval of data from main memory 6296. For certain operations, graphics confroller 6288 may generate PCI protocol transactions on AGP bus 6290. The AGP interface of bus bridge 6292 may thus include functionality to support both AGP protocol transactions as well as PCI protocol target and initiator transactions. Display 6286 is any electronic display upon which an image or text can be presented. A suitable display 6286 includes a cathode ray tube ("CRT"), a liquid crystal display ("LCD"), etc.

It is noted that, while the AGP, PCI, and ISA or EISA buses have been used as examples in the above description, any bus architectures may be substituted as desired. It is further noted that computational system 6270 may be a multiprocessing computational system including additional processors (e.g., processor 6291 shown as an optional component of computational system 6270). Processor 6291 may be similar to processor 6293. More particularly, processor 6291 may be an identical copy of processor 6293. Processor 6291 may be connected to bus bridge 6292 via an independent bus (as shown in FIG. 18) or may share CPU bus 6295 with processor 6293. Furthermore, processor 6291 may be coupled to an optional L2 cache 6298 similar to L2 cache 6297. FIG. 19 illustrates a flow chart of a computer-implemented method for treating a hydrocarbon formation based on a characteristic of the formation. At least one characteristic 6370 may be input into computational system 6250. Computational system 6250 may process at least one characteristic 6370 using a software executable to determine a set of operating conditions 6372 for treating the formation with in situ process 6310. The software executable may process equations relating to formation characteristics and/or the relationships between formation characteristics. At least one characteristic 6370 may include, but is not limited to, an overburden thickness, depth of the formation, type of formation, permeability, density, porosity, moisture content, and other organic maturity indicators, oil saturation, water saturation, volatile matter content, oil chemistry, net-to-gross ratio, carbon content, hydrogen content, oxygen content, sulfur content, nitrogen content, mineralology, soluble compound content, elemental composition, hydrogeology, water zones, gas zones, barren zones, mechanical properties, or top seal character. Computational system 6250 may be used to control in situ process 6310 using determined set of operating conditions 6372.

FIG. 20 illustrates a schematic of an embodiment used to control an in situ conversion process (ICP) in formation 6600. Barrier well 6602, monitor well 6604, production well 6606, and heater well 6608 may be placed in formation 6600. Baπier well 6602 may be used to confrol water conditions within formation 6600. Monitoring well 6604 may be used to monitor subsurface conditions in the formation, such as, but not limited to, pressure, temperature, product quality, or fracture progression. Production well 6606 may be used to produce formation fluids (e.g., oil, gas, and water) from the formation. Heater well 6608 may be used to provide heat to the formation. Formation conditions such as, but not limited to, pressure, temperature, fracture progression (monitored, for instance, by acoustical sensor data), and fluid quality (e.g., product quality or water quality) may be monitored through one or more of wells 6602, 6604, 6606, and 6608.

Surface data such as pump status (e.g., pump on or off), fluid flow rate, surface pressure/temperature, and heater power may be monitored by instruments placed at each well or certain wells. Similarly, subsurface data such as pressure, temperature, fluid quality, and acoustical sensor data may be monitored by instruments placed at each well or certain wells. Surface data 6610 from barrier well 6602 may include pump status, flow rate, and surface pressure/temperature. Surface data 6612 from production well 6606 may include pump status, flow rate, and surface pressure/temperature. Subsurface data 6614 from barrier well 6602 may include pressure, temperature, water quality, and acoustical sensor data. Subsurface data 6616 from monitoring well 6604 may include pressure, temperature, product quality, and acoustical sensor data. Subsurface data 6618 from production well 6606 may include pressure, temperature, product quality, and acoustical sensor data. Subsurface data 6620 from heater well

6608 may mclude pressure, temperature, and acoustical sensor data.

Surface data 6610 and 6612 and subsurface data 6614, 6616, 6618, and 6620 may be monitored as analog data 6621 from one or more measuring instruments. Analog data 6621 may be converted to digital data 6623 in analog-to-digital converter 6622. Digital data 6623 may be provided to computational system 6250. Alternatively, one or more measuring instruments may provide digital data to computational system 6250. Computational system

6250 may include a distributed central processing unit (CPU). Computational system 6250 may process digital data 6623 to inteφret analog data 6621. Output from computational system 6250 may be provided to remote display 6624, data storage 6626, display 6628, or to a surface facility 6630. Surface facility 6630 may include, for example, a hydrotreating plant, a liquid processing plant, or a gas processing plant. Computational system 6250 may provide digital output 6632 to digital-to-analog converter 6634. Digital-to-analog converter 6634 may converter digital output 6632 to analog output 6636. Analog output 6636 may include instructions to control one or more conditions of formation 6600. Analog output 6636 may include instructions to control the ICP within formation 6600. Analog output 6636 may include instructions to adjust one or more parameters of the ICP. The one or more parameters may include, but are not limited to, pressure, temperature, product composition, and product quality. Analog output 6636 may include instructions for confrol of pump status 6640 or flow rate 6642 at baπier well 6602. Analog output 6636 may include instructions for control of pump status 6644 or flow rate 6646 at production well 6606. Analog output 6636 may also include instructions for control of heater power 6648 at heater well 6608. Analog output 6636 may include instructions to vary one or more conditions such as pump status, flow rate, or heater power. Analog output 6636 may also include instructions to turn on and/or off pumps, heaters, or monitoring instruments located at each well.

Remote input data 6638 may also be provided to computational system 6250 to control conditions within formation 6600. Remote input data 6638 may include data used to adjust conditions of formation 6600. Remote input data 6638 may include data such as, but not limited to, elecfricity cost, gas or oil prices, pipeline tariffs, data from simulations, plant emissions, or refinery availability. Remote input data 6638 may be used by computational system 6250 to adjust digital output 6632 to a desired value. In some embodiments, surface facility data 6650 may be provided to computational system 6250.

An in situ conversion process (ICP) may be monitored using a feedback confrol process. Conditions within a formation may be monitored and used within the feedback confrol process. A formation being treated using an in situ conversion process may undergo changes in mechanical properties due to the conversion of solids and viscous liquids to vapors, fracture propagation (e.g., to overburden, underburden, water tables, etc.), increases in peπneability or porosity and decreases in density, moisture evaporation, and/or thermal instability of matrix minerals (leading to dehydration and decarbonation reactions and shifts in stable mineral assemblages).

Remote monitoring techniques that will sense these changes in reservoir properties may include, but are not limited to, 4D (4 dimension) time lapse seismic monitoring, 3D/3C (3 dimension/3 component) seismic passive acoustic monitoring of fracturing, time lapse 3D seismic passive acoustic monitoring of fracturing, electrical resistivity, thermal mapping, surface or downhole tilt meters, surveying permanent surface monuments, chemical sniffing or laser sensors for surface gas abundance, and gravimetrics. More direct subsurface-based monitoring techniques may include high temperature downhole instrumentation (such as thermocouples and other temperature sensing mechanisms, stress sensors, or instrumentation in the producer well to detect gas flows on a finely incremental basis).

In certain embodiments, a "base" seismic monitoring may be conducted, and then subsequent seismic results can be compared to determine changes.

Simulation methods on a computer system may be used to model an in situ process for treating a formation. Simulations may determine and/or predict operating conditions (e.g., pressure, temperature, etc.), products that may be produced from the formation at given operating conditions, and/or product characteristics

(e.g., API gravity, aromatic to paraffin ratio, etc.) for the process. In certain embodiments, a computer simulation may be used to model fluid mechanics (including mass fransfer and heat fransfer) and kinetics within the formation to determine characteristics of products produced during heating of the formation. A formation may be modeled using commercially available simulation programs such as STARS, THERM, FLUENT, or CFX. In addition, combinations of simulation programs may be used to more accurately determine or predict characteristics of the in situ process. Results of the simulations may be used to determine operating conditions within the formation prior to actual treatment of the formation. Results of the simulations may also be used to adjust operating conditions during treatment of the formation based on a change in a property of the formation and/or a change in a desired property of a product produced from the formation.

FIG. 21 illustrates a flowchart of an embodiment of method 9470 for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons using a computer system. Method

9470 may include providing at least one property 9472 of the foπnation to the computer system. Properties of the foπnation may include, but are not limited to, porosity, peπneability, saturation, thermal conductivity, volumetric heat capacity, compressibility, composition, and number and types of phases in the formation. Properties may also include chemical components, chemical reactions, and kinetic parameters. At least one operating condition 9474 of the process may also be provided to the computer system. For instance, operating conditions may include, but are not limited to, pressure, temperature, heating rate, heat input rate, process time, weight percentage of gases, production characteristics (e.g., flow rates, locations, compositions), and peripheral water recovery or injection. In addition, operating conditions may include characteristics of the well pattern such as producer well location, producer well orientation, ratio of producer wells to heater wells, heater well spacing, type of heater well pattern, heater well orientation, and distance between an overburden and horizontal heater wells.

Furthermore, a method may include assessing at least one process characteristic 9478 of the in situ process using simulation method 9476 on the computer system. At least one process characteristic may be assessed as a function of time from at least one property of the formation and at least one operating condition. Process characteristics may include properties of a produced fluid such as API gravity, olefin content, carbon number distribution, ethene to ethane ratio, atomic carbon to hydrogen ratio, and ratio of non condensable hydrocarbons to condensable hydrocarbons (gas/oil ratio). Process characteristics may also include a pressure and temperature in the formation, total mass recovery from the formation, and or production rate of fluid produced from the foπnation.

In some embodiments, a simulation method may include a numerical simulation method used/performed on the computer system. The numerical simulation method may employ finite difference methods to solve fluid mechanics, heat transfer, and chemical reaction equations as a function of time. A finite difference method may use a body-fitted grid system with unstructured grids to model a formation. An unstructured grid employs a wide variety of shapes to model a foπnation geometry, in contrast to a structured grid. A body-fitted finite difference simulation method may calculate fluid flow and heat transfer in a formation. Heat transfer mechanisms may include conduction, convection, and radiation. The body-fitted finite difference simulation method may also be used to treat chemical reactions in the formation. Simulations with a finite difference simulation method may employ closed value thermal conduction equations to calculate heat transfer and temperature distributions in the formation. A finite difference simulation method may determine values for heat injection rate data.

In an embodiment, a body-fitted finite difference simulation method may be well suited for simulating systems that include shaφ interfaces in physical properties or conditions. In general, a body-fitted finite difference simulation method may be more accurate, in certain circumstances, than space-fitted methods due to the use of finer, unstructured grids in body-fitted methods. For instance, it may be advantageous to use a body-fitted finite difference simulation method to calculate heat transfer in a heater well and in the region near or close to a heater well. The temperature profile in and near a heater well may be relatively shaφ. A region near a heater well may be refened to as a "near wellbore region." The size or radius of a near wellbore region may depend on the type of formation. A general criteria for determining or estimating the radius of a "near wellbore region" may be a distance at which heat transfer by the mechanism of convection contributes significantly to overall heat transfer. Heat fransfer in the near wellbore region is typically limited to contributions from conductive and/or radiative heat fransfer. Convective heat transfer tends to contribute significantly to overall heat fransfer at locations where fluids flow within the foπnation (i.e., convective heat transfer is significant where the flow of mass contributes to heat fransfer). In general, the radius of a near wellbore region in a formation decreases with both increasing convection and increasing variation of thennal properties with temperature in the formation. For example, a relatively low permeability formation containing heavy hydrocarbons may have a relatively small near wellbore region due to the contribution of convection for heat fransfer and a large variation of thermal properties with temperature. In one embodiment, the near wellbore region in a relatively low permeability formation containing heavy hydrocarbons may have a radius of about 1 m to about 2 m. In other embodiments, the radius may be between about 2 m and about 4 m.

In a simulation of a heater well and near wellbore region, a body-fitted finite difference simulation method may calculate the heat input rate that corresponds to a given temperature in a heater well. The method may also calculate the temperature distributions both inside the wellbore and at the near wellbore region. CFX supplied by AEA Technologies in the United Kingdom is an example of a commercially available body-fitted finite difference simulation method. FLUENT is another commercially available body-fitted finite difference simulation method from FLUENT, Inc. located in Lebanon, New Hampshire. FLUENT may simulate models of a formation that include porous media and heater wells. The porous media models may include one or more materials and/or phases with variable fractions. The materials may have user-specified temperature dependent thermal properties and densities. The user may also specify the initial spatial distribution of the materials in a model. In one modeling scheme of a porous media, a combustion reaction may only involve a reaction between carbon and oxygen. In a model of hydrocarbon combustion, the volume fraction and porosity of the formation tend to decrease. In addition, a gas phase may be modeled by one or more species in FLUENT, for example, nitrogen, oxygen, and carbon dioxide. ' ' In an embodiment, the simulation method may include a numerical simulation method on a computer system that uses a space-fitted finite difference method with structured grids. The space-fitted finite difference simulation method may be a reservoir simulation method. A reservoir simulation method may calculate fluid mechanics, mass balances, heat fransfer, and/or kinetics in the formation. A reservoir simulation method may be particularly useful for modeling multiphase porous media in which convection (e.g., the flow of hot fluids) is a relatively important mechanism of heat transfer.

STARS is an example of a reservoir simulation method provided by Computer Modeling Group, Ltd. of Alberta, Canada. STARS is designed for simulating steam flood, steam cycling, steam-with-additives, dry and wet combustion, along with many types of chemical additive processes, using a wide range of grid and porosity models in both field and laboratory scales. STARS includes options such as thermal applications, steam injection, fireflood, horizontal wells, dual porosity/permeability, directional permeability, and flexible grids. STARS allows for complex temperature dependent models of thermal and physical properties. STARS may also simulate pressure dependent chemical reactions. STARS may simulate a formation using a combination of structured space-fitted grids and unstructured body-fitted grids. Additionally, THERM is an example of a reservoir simulation method provided by Scientific Software Intercomp. , In certain embodiments, a simulation method may use properties of a foπnation. In general, the properties of a formation for a model of an in situ process depend on the type of formation. For example, in a model of an oil shale formation, for example, a porosity value may be used to model an amount of kerogen and hydrated mineral matter in the formation. The kerogen and hydrated mineral matter used in a model may be determined or approximated by the amount of kerogen and hydrated mineral matter necessary to generate the oil, gas and water produced in laboratory experiments. The remainder of the volume of the oil shale may be modeled as inert mineral matter, which may be assumed to remain intact at all simulated temperatures. During a simulation, hydrated mineral matter decomposes to produce water and minerals. In addition, kerogen pyrolyzes during the simulation to produce hydrocarbons and other compounds resulting in a rise in fluid porosity. In some embodiments, the change in porosity during a simulation may be determined by monitoring the amount of solids that are treated/transformed, and fluids that are generated. In an embodiment of a coal formation model, the amount of coal in the formation for the model may be determined by laboratory pyrolysis experiments. Laboratory pyrolysis experiments may determine the amount of coal in an actual formation. The remainder of the volume may be modeled as inert mineral matter or ash. In some embodiments, the porosity of the ash may be between approximately 5% and approximately 10%. Absorbed and/or adsorbed fluid components, such as initial moisture, may be modeled as part of a solid phase. As moisture desorbs, the fluid porosity tends to increase. The value of the fluid porosity affects the results of the simulation since it may be used to model the change in permeability.

An embodiment of a model of a tar sands formation may include an inert mineral matter phase and a fluid phase that includes heavy hydrocarbons. In an embodiment, the porosity of a tar sands formation may be modeled as a function of the pressure of the formation and its mechanical properties. For example, the porosity, φ, at a pressure, P, in a tar sands formation may be given by EQN. 2:

(2) φ = φ_ref exp [c (P- P_reβJ

where P_ref is a reference pressure, φ_refis the porosity at the reference pressure, and c is the formation compressibility.

Some embodiments of a simulation method may require an initial permeability of a formation and a relationship for the dependence of permeability on conditions of the formation. An initial permeability of a formation may be determined from experimental measurements of a sample (e.g., a core sample) of a formation. In some types of formations, a ratio of vertical permeability to horizontal permeability may be adjusted to take into consideration clearing in the formation.

In some embodiments, the porosity of a formation may be used to model the change in permeability of the formation during a simulation. For example, the permeability of oil shale often increases with temperature due to the loss of solid matter from the decomposition of mineral matter and the pyrolysis of kerogen. Similarly, the permeability of a coal formation often increases with temperature due to the loss of solid matter from pyrolysis. In one embodiment, the dependence of porosity on permeability may be described by an analytical relationship. For example, the effect of pyrolysis on permeability, K, may be governed by a Carman-Kozeny type formula shown in EQN. 3:

(3) K(φj) = Ko (φ_f/ φ_f,oX^power [ (1 - φ_f0) / (1 - φβ ϊ where ψfis the current fluid porosity, φ_ffi is the initial fluid porosity, K₀ is the permeability at initial fluid porosity, and CKpower is a user-defined exponent. The value of CKpower may be fitted by matching or approximating the pressure gradient in an experiment in a formation. The porosity-permeability relationship 9350 is plotted in FIG. 22 for a value of the initial porosity of 0.935 millidarcy and CKpower = 0.95. Alternatively, in some formations, such as a tar sands formation, the peπneability dependence may be expressed as shown in EQN. 4:

(4) K(φβ = K₀ x exp [k_mul * ( <p_f - φ_f,o)/(l - φ_f,o) ]

where K₀ and φ ₀ are the initial permeability and porosity, and k_m„ι is a user-defined grid dependent permeability multiplier. In other embodiments, a tabular relationship rather than an analytical expression may be used to model the dependence of permeability on porosity. In addition, the ratio of vertical to horizontal permeability for tar sands formations may be determined from experimental data. In one embodiment, expressions for the dependence of permeability on porosity in a relatively low permeability formation containing heavy hydrocarbons may be used in a simulation method.

In certain embodiments, the thermal conductivity of a model of a formation may be expressed in terms of the theπnal conductivities of constituent materials. For example, the thermal conductivity may be expressed in terms of solid phase components and fluid phase components. The solid phase in oil shale formations and coal formations may be composed of inert mineral matter and organic solid matter. One or more fluid phases in the formations may include, for example, a water phase, an oil phase, and a gas phase. In some embodiments, the dependence of the thermal conductivity on constituent materials in an oil shale formation may be modeled according to EQN. 5:

(5) k_lh (7) = φ_f (k_lhw x S_w + k_th0 x S₀ + k_lllg x S_g) + (1 - φ) x k_lh (T) + (φ - φ_f) x k_th

where φ is the porosity of the formation, φ_f is the instantaneous fluid porosity, k,_hιi is the thermal conductivity of phase z'=(w, o,g)=(water,oil,gas), S* is the saturation of phase i=(w,o,g)=(water,oil,gas), k_lh T) is the thermal conductivity of rock (inert mineral matter), and k^ T) is the thermal conductivity of solid-phase components. The theπnal conductivity, from EQN. 5, may be a function of temperature due to the temperature dependence of the solid phase components. The thermal conductivity also changes with temperature due to the change in composition of the fluid phase and porosity. ^•

In some embodiments, a model may take into account the effect of different geological strata on properties of the formation. A property of a formation may be calculated for a given mineralogical composition. For example, the thermal conductivity of a model of a tar sands formation may be calculated from EQN. 6:

(6) = -^Γ ¹ where A^Φ _f is the thermal conductivity of the fluid phase at porosity φ, k_t is the theπnal conductivity of geological layer z, and is the compressibility of geological layer /'. In other embodiments, the thermal conductivity in a relatively low peπneability foπnation containing heavy hydrocarbons may be modeled with expressions in a simulation method.

In an embodiment, the volumetric heat capacity, P_bC_p, may also be modeled as a direct function of temperature. However, the volumetric heat capacity also depends on the composition of the formation material through the density, which is affected by temperature.

In one embodiment, properties of the formation may include one or more phases with one or more chemical components. For example, fluid phases may include water, oil, and gas. Solid phases may include mineral matter and organic matter. Each of the fluid phases in an in situ process may include a variety of chemical components such as hydrocarbons, H₂, C0₂, etc. The chemical components may be products of one or more chemical reactions, such as pyrolysis reactions, that occur in the formation. Some embodiments of a model of an in situ process may include modeling individual chemical components known to be present in a formation. However, inclusion of chemical components in a model of an in situ process may be limited by available experimental composition and kinetic data for the components. In addition, a simulation method may also place numerical and solution time limitations on the number of components that may be modeled. In some embodiments, one or more chemical components may be modeled as a single component called a pseudo-component. In certain embodiments, the oil phase may be modeled by two volatile pseudo-components, a light oil and a heavy oil. The oil and at least some of the gas phase components are generated by pyrolysis of organic matter in the formation. The light oil and the heavy oil may be modeled as having an API gravity that is consistent with laboratory or experimental field data. For example, the light oil may have an API gravity of between about 20° and about 70°. The heavy oil may have an API gravity less than about 20°.

In some embodiments, hydrocarbon gases in a formation of one or more carbon numbers may be modeled as a single pseudo-component. In other embodiments, non-hydrocarbon gases and hydrocarbon gases may be modeled as a single component. For example, hydrocarbon gases between a carbon number of one to a carbon number of five and nitrogen and hydrogen sulfide may be modeled as a single component. In some embodiments, the multiple components modeled as a single component have relatively similar molecular weights. A molecular weight of the hydrocarbon gas pseudo-component may be set such that the pseudo-component is similar to a hydrocarbon gas generated in a laboratory pyrolysis experiment at a specified pressure.

In some embodiments of an in situ process, the composition of the generated hydrocarbon gas may vary with pressure. As pressure increases, the ratio of a higher molecular weight component to a lower molecular component tends to increase. For example, as pressure increases, the ratio of hydrocarbon gases with carbon numbers between about three and about five to hydrocarbon gases with one and two carbon numbers tends to increase. Consequently, the molecular weight of the pseudo-component that models a mixture of component gases may vary with pressure.

TABLE 1 lists components in a model of in situ process in a coal formation according to one embodiment. Similarly, TABLE 2 lists components in a model of an in situ process in an oil shale formation according to an embodiment. TABLE 1 CHEMICAL COMPONENTS IN A MODEL OF A COAL FORMATION.

TABLE 2 CHEMICAL COMPONENTS IN A MODEL OF AN OIL SHALE FORMATION.

As shown in TABLE 1, the hydrocarbon gases produced by the pyrolysis of coal may be grouped into a pseudo-component, HCgas. The HCgas component may have critical properties intermediate between methane and ethane. Similarly, the pseudo-component, HCgas, generated from pyrolysis in an oil shale formation, as shown in TABLE 2, may have critical properties very close to those of ethane. For both coal and oil shale, the HCgas pseudo-components may model hydrocarbons between a carbon number of about one and a carbon number of about five. The molecular weight of the pseudo-component in TABLE 2 generally reflects the composition of the hydrocarbon gas that was generated in a laboratory experiment at a pressure of about 6.9 bars absolute. In some embodiments, the solid phase in a formation may be modeled with one or more components. For example, in a coal formation the components may include coal and char, as shown in TABLE 1. The components in a kerogen formation may include kerogen and a hydrated mineral phase (hydramin), as shown in TABLE 2. The hydrated mineral component may be included to model water and carbon dioxide generated in an oil shale formation at temperatures below a pyrolysis temperature of kerogen. The hydrated minerals, for example, may include illite and nahcolite.

Kerogen may be the source of most or all of the hydrocarbon fluids generated by the pyrolysis. Kerogen may also be the source of some of the water and carbon dioxide that is generated at temperatures below a pyrolysis temperature. In an embodiment, the solid phase model may also include one or more intermediate components that are artifacts of the reactions that model the pyrolysis. For example, a coal formation may include two intermediate components, coalbtm and prechar, as shown in TABLE 1. An oil shale formation may include at least one intermediate component, prechar, as shown in TABLE 2. The prechar solid-phase components may model carbon residue in a formation that may contain H₂ and low molecular weight hydrocarbons. Coalbtm accounts for intermediate unpyrolyzed compounds that tend to appear and disappear during the course of pyrolysis. In one embodiment, the number of intermediate components may be increased to improve the match or agreement between simulation results and experimental results.

In one embodiment, a model of an in situ process may include one or more chemical reactions. A number of chemical reactions are known to occur in an in situ process for a relatively low permeability formation containing heavy hydrocarbons. The chemical reactions may belong to one of several categories of reactions. The categories may include, but not be limited to, generation of pre-pyrolysis water and carbon dioxide, generation of hydrocarbons, coking and cracking of hydrocarbons, foπnation of synthesis gas, and combustion and oxidation of coke.

In one embodiment, the rate of change of the concentration of species X due to a chemical reaction, for example:

(I) X -> products

may be expressed in terms of a rate law:

(II) d[X] / dt = - k [X]ⁿ

Species X in the chemical reaction undergoes chemical transformation to the products. [X] is the concentration of species X, t is the time, k is the reaction rate constant, and n is the order of the reaction. The reaction rate constant, k, may be defined by the Arrhenius equation:

(III) k = A exp[ -E_a/ RT ]

where A is the frequency factor, E_a is the activation energy, R is the universal gas constant, and T is the temperature. Kinetic parameters, such as k, A, E_a, and n, may be determined from experimental measurements. A simulation method may include one or more rate laws for assessing the change in concentration of species in an in situ process as a function of time. Experimentally determined kinetic parameters for one or more chemical reactions may be used as input to the simulation method.

In some embodiments, the number and categories of reactions in a model of an in situ process may depend on the availability of experimental kinetic data and/or numerical limitations of a simulation method. Generally, chemical reactions and kinetic parameters for a model may be chosen such that simulation results match or approximate quantitative and qualitative experimental trends.

In some embodiments, reactions that model the generation of pre-pyrolysis water and carbon dioxide account for the bound water, carbon dioxide, and carbon monoxide generated in a temperature range below a pyrolysis temperature. For example, pre-pyrolysis water may be generated from hydrated mineral matter. In one embodiment, the temperature range may be between about 100 °C and about 270 °C. In other embodiments, the temperature range may be between about 80 °C and about 300 °C. Reactions in the temperature range below a pyrolysis temperature may account for between about 45% and about 60% of the total water generated and up to about 30% of the total carbon dioxide observed in laboratory experiments of pyrolysis.

In an embodiment, the pressure dependence of the chemical reactions may be modeled. To account for the pressure dependence, a single reaction with variable stoichiometric coefficients may be used to model the generation of pre-pyrolysis fluids. Alternatively, the pressure dependence may be modeled with two or more reactions with pressure dependent kinetic parameters such as frequency factors.

For example, experimental results indicate that the reaction that generates pre-pyrolysis fluids from oil shale is a function of pressure. The amount of water generated generally decreases with pressure while the amount of carbon dioxide generated generally increases with pressure. In an embodiment, the generation of pre-pyrolysis fluids may be modeled with two reactions to account for the pressure dependence. One reaction may be dominant at high pressures while the other may be prevalent at lower pressures. For example, a molar stoichiometry of two reactions according to one embodiment may be written as follows:

(7) 1 mol hydramin ^ 0.5884 mol H₂0 + 0.0962 mol C0₂ + 0.0114 mol CO

(8) 1 mol hydramin -» 0.8234 mol H₂0 + 0.0 mol C0₂ + 0.0114 mol CO

Experimentally determined kinetic parameters for Reactions (7) and (8) are shown in TABLE 3. TABLE 3 shows that pressure dependence of Reactions (7) and (8) is taken into account by the frequency factor. The frequency-factor increases with increasing pressure for Reaction (7), which results in an increase in the rate of product formation with pressure. The rate of product formation increases due to the increase in the rate constant. In addition, the frequency-factor decreases with increasing pressure for Reaction (8), which results in a decrease in the rate of product formation with increasing pressure. Therefore, the values of the frequency-factor in TABLE 3 indicate that Reaction (7) dominates at high pressures while Reaction (8) dominates at low pressures. In addition, the molar balances for Reactions (7) and (8) indicate that Reaction (7) generates less water and more carbon dioxide than Reaction (8).

In one embodiment, a reaction enthalpy may be used by a simulation method such as STARS to assess the thermodynamic properties of a formation. In TABLES 3-8, the reaction enthalpy is a negative number if a chemical reaction is endothermic and positive if a chemical reaction is exothermic. TABLE 3 KINETIC PARAMETERS OF PRE-PYROLYSIS FLUID GENERATION REACTIONS IN AN OIL SHALE

FORMATION.

In other embodiments, the generation of hydrocarbons in a pyrolysis temperature range in a formation may be modeled with one or more reactions. One or more reactions may model the amount of hydrocarbon fluids and carbon residue that are generated in a pyrolysis temperature range. Hydrocarbons generated may include light oil, heavy oil, and non-condensable gases. Pyrolysis reactions may also generate water, H₂, and C0₂. Experimental results indicate that the composition of products generated in a pyrolysis temperature range may depend on operating conditions such as pressure. For example, the production rate of hydrocarbons generally decreases with pressure. In addition, the amount of produced hydrogen gas generally decreases substantially with pressure, the amount of carbon residue generally increases with pressure, and the amount of condensable hydrocarbons generally decreases with pressure. Furthermore, the amount of non-condensable hydrocarbons generally increases with pressure such that the sum of condensable hydrocarbons and non-condensable hydrocarbons generally remains approximately constant with a change in pressure. In addition, the API gravity of the generated hydrocarbons increases with pressure.

In an embodiment, the generation of hydrocarbons in a pyrolysis temperature range in an oil shale formation may be modeled with two reactions. One of the reactions may be dominant at high pressures, the other prevailing at low pressures. For example, the molar stoichiometry of the two reactions according to one embodiment may be as follows:

(9) 1 mol kerogen - 0.02691 mol H₂0 + 0.009588 mol heavy oil + 0.01780 mol light oil + 0.04475 mol HCgas + 0.01049 mol H₂ + 0.00541 mol C0₂ + 0.5827 mol prechar (10) 1 mol kerogen - 0.02691 mol H₂0 + 0.009588 mol heavy oil + 0.01780 mol light oil + 0.04475 mol HCgas + 0.07930 mol H₂ + 0.00541 mol C0₂+ 0.5718 mol prechar

Experimentally determined kinetic parameters are shown in TABLE 4. Reactions (9) and (10) model the pressure dependence of hydrogen and carbon residue on pressure. However, the reactions do not take into account the pressure dependence of hydrocarbon production. In one embodiment, the pressure dependence of the production of hydrocarbons may be taken into account by a set of cracking/coking reactions. Alternatively, pressure dependence of hydrocarbon production may be modeled by hydrocarbon generation reactions without cracking/coking reactions.

TABLE 4 KINETIC PARAMETERS OF PRE-PYROLYSIS GENERATION REACTIONS IN AN OIL SHALE

FORMATION.

En one embodiment, one or more reactions may model the cracking and coking in a formation. Cracking reactions involve the reaction of condensable hydrocarbons (e.g., light oil and heavy oil) to form lighter compounds (e.g., light oil and non-condensable gases) and carbon residue. The coking reactions model the polymerization and condensation of hydrocarbon molecules. Coking reactions lead to foπnation of char, lower molecular weight hydrocarbons, and hydrogen. Gaseous hydrocarbons may undergo coking reactions to form carbon residue and H₂. Coking and cracking may account for the deposition of coke in the vicinity of heater wells where the temperature may be substantially greater than a pyrolysis temperature. For example, the molar stoichiometry of the cracking and coking reactions in an oil shale formation according to one embodiment may be as follows:

(11) 1 mol heavy oil (gasphase) -> 1.8530 mol light oil + 0.045 mol HCgas + 2.4515 mol prechar

(12) 1 mol light oil (gasphase) -> 5.730 mol HCgas (13) 1 mol heavy oil (liquid phase) -> 0.2063 mol light oil + 2.365 mol HCgas + 17.497 mol prechar

(14) 1 mol light oil (liquid phase) -> 0.5730 mol HCgas + 10.904 mol prechar

(15) 1 mol HCgas -» 2.8 mol H₂ + 1.6706 mol char

Kinetics parameters for Reactions 11 to 15 are listed in TABLE 5. The kinetics parameters of the cracking reactions were chosen to match or approximate the oil and gas production observed in laboratory experiments. The kinetics parameter of the coking reaction was derived from experimental data on pyrolysis reactions in a coal experiment.

TABLE 5 KINETIC PARAMETERS OF CRACKING AND COKING REACTIONS IN AN OIL SHALE FORMATION.

In addition, reactions may model the generation of water at a temperature below or within a pyrolysis temperature range and the generation of hydrocarbons at a temperature in a pyrolysis temperature range in a coal formation. For example, according to one embodiment, the reactions may include:

(16) 1 mol coal -» 0.01894 mol H₂0 + 0.0004.91 mol HCgas + 0.000047 mol H₂ + 0.0006.8 mol C0₂ +

0.99883 mol coalbtm

(17) 1 mol coalbtm -> 0.02553 mol H₂0 + 0.00136 mol heavy oil + 0.003174 mol light oil + 0.01618 mol

HCgas + 0.0032 mol H₂ + 0.005599 mol C0₂+ 0.0008.26 mol CO + 0.91306 mol prechar

(18) 1 mol prechar -» 0.02764 mol H₂0 + 0.05764 mol HCgas + 0.02823 mol H₂ + 0.0154 mol C0₂ +

0.006.465 mol CO + 0.90598 mol char The kinetic parameters of the three reactions are tabulated in TABLE 6. Reaction (16) models the generation of water in a temperature range below a pyrolysis temperature. Reaction (17) models the generation of hydrocarbons, such as oil and gas, generated in a pyrolysis temperature range. Reaction (18) models gas generated at temperatures between about 370 °C and about 600°C.

TABLE 6 KINETIC PARAMETERS OF REACTIONS IN A COAL FORMATION.

Coking and cracking in a coal formation may be modeled by one or more reactions in both the liquid phase and the gas phase. For example, the molar stoichiometry of two cracking reactions in the liquid and gas phase may be according to one embodiment:

(19) 1 mol heavy oil -> 0.1879 mol light oil + 2.983 mol HCgas + 16.038 mol char

(20) 1 mol light oil -> 0.7985 mol HCgas + 10.977 mol char

In addition coking in a coal formation may be modeled as

(21) 1 mol HCgas - 2.2 mol H₂ + 1.1853 mol char

Reaction (21) may model the coking of methane and ethane observed in field experiments when low carbon number hydrocarbon gases are injected into a hot coal formation.

The kinetic parameters of reactions 19-21 are tabulated in TABLE 7. The kinetic parameters for cracking were derived from literature data. The kinetic parameters for the coking reaction were derived from laboratory data on cracking.

TABLE 7 KINETIC PARAMETERS OF CRACKING AND COKING REACTIONS IN A COAL FORMATION.

In certain embodiments, the generation of synthesis gas in a formation may be modeled by one or more reactions. For example, the molar stoichiometry of four synthesis gas reactions may be according to one embodiment:

(22) 1 mol 0.9442 char + 1.0 mol C0₂ - 2.0 mol CO

(23) 1.0 mol CO -» 0.5 mol C0₂+ 0.4721 mol char

(24) 0.94426 mol char + 1.0 mol H₂0 -» 1.0 mol H₂ + 1.0 mol CO

(25) 1.0 mol H₂ + 1.0 mol CO -» 0.94426 mol char + 1.0 mol H₂0

The kinetic parameters of the four reactions are tabulated in TABLE 8. Kinetic parameters for Reactions 22-25 were based on literature data that were adjusted to fit the results of a coal cube laboratory experiment. Pressure dependence of reactions in the coal formation is not taken in to account in TABLES 6, 7, and 8. In one embodiment, pressure dependence of the reactions in the coal formation may be modeled, for example, with pressure dependent frequency-factors.

TABLE 8 KINETIC PARAMETERS FOR SYNTHESIS GAS REACTIONS IN A COAL FORMATION.

In one embodiment, a combustion and oxidation reaction of coke to carbon dioxide may be modeled in a formation. For example, the molar stoichiometry of a reaction according to one embodiment may be:

(26) 0.9442 mol char + 1.0 mol 0₂ -» 1.0 mol C0₂

Experimentally derived kinetic parameters include a frequency factor of 1.0 x 10⁴ (day)^"1, an activation energy of 58,614 KJ/mole, an order of 1, and a reaction enthalpy of 427,977 KJ/mole.

In some embodiments, a model of a tar sands formation may be modeled with the following components: bitumen (heavy oil), light oil, HCgas 1, HCgas2, water, char, and prechar. According to one embodiment, an in situ process in a tar sands formation may be modeled by at least two reactions:

(27) Bitumen - light oil + HCgas 1 + H₂0 + prechar

(28) Prechar -> HCgas2 + H₂0 + char Reaction 27 models the pyrolysis of bitumen to oil and gas components. In one embodiment, Reaction (27) may be modeled as a 2^nd order reaction and Reaction (28) may be modeled as a 7^th order reaction. In one embodiment, the reaction enthalpy of Reactions (27) and (28) may be zero.

In other embodiments, a model of a relatively low permeability formation containing heavy hydrocarbons may be include one or more phases, one or more components, and one or more chemical reactions.

In an embodiment, a method of modeling an in situ process of freating a relatively low permeability formation containing heavy hydrocarbons using a computer system may include simulating a heat input rate to the foπnation from two or more heat sources. FIG. 23 illustrates method 9360 for simulating heat transfer in a formation. Simulation method 9361 may simulate heat input rate 9368 from two or more heat sources in the formation. For example, the simulation method may be a body-fitted finite difference simulation method. The heat may be allowed to transfer from the heat sources to a selected section of the formation. In an embodiment, the supeφosition of heat from the two or more heat sources may pyrolyze at least some hydrocarbons within the selected section of the formation. In one embodiment, two or more heat sources may be simulated with a model of heat sources with symmetry boundary conditions. In some embodiments, the method may further include providing at least one desired parameter 9366 of the in situ process to the computer system. For example, the desired parameter may be a desired temperature in the formation. In particular, the desired parameter may be a maximum temperature at specific locations in the formation. In addition, the desired parameter may be a desired heating rate or a desired product composition. Desired parameters may also include other parameters such as a desired pressure, process time, production rate, time to obtain a given production rate, and product composition. Process characteristics 9362 determined by simulation method 9361 may be compared 9364 to at least one desired parameter 9366. The method may further include controlling 9363 the heat input rate from the heat sources (or some other process parameter) to achieve at least one desired parameter. Consequently, the heat input rate from the two or more heat sources during a simulation may be time dependent. In an embodiment, heat injection into a formation may be initiated by imposing a constant flux per unit area at the interface between a heater and the formation. When a point in the formation, such as the interface, reaches a specified maximum temperature, the heat flux may be varied to maintain the maximum temperature. The specified maximum temperature may correspond to the maximum temperature allowed for a heater well casing (e.g., a maximum operating temperature for the metallurgy in the heater well). In one embodiment, the maximum temperature may be between about 600 °C and about 700 °C. In other embodiments, the maximum temperature may be between about 700 °C and about 800 °C. In some embodiments, the maximum temperature may be greater than about 800 °C.

FIG. 24 illustrates a model for simulating a heat fransfer rate in a formation. Model 9370 represents an aerial view of 1112^th of a seven spot heater pattern in a formation. The pattern is composed of body-fitted grid elements 9371. The model includes horizontal heater 9372 and producer 9374. A pattern of heaters in a formation is modeled by imposing symmetry boundary conditions. The elements near the heaters and in the region near the heaters are substantially smaller than other portions of the formation to more effectively model a steep temperature profile.

In one embodiment, an in situ process may be modeled with more than one simulation methods. FIG. 25 illustrates a flowchart of an embodiment of method 8630 for modeling an in situ process for treating a relatively low permeability fonnation containing heavy hydrocarbons using a computer system. At least one heat input property 8632 may be provided to the computer system. The computer system may include first simulation method 8634. At least one heat input property 8632 may include a heat transfer property of the foπnation. For example, the heat transfer property of the formation may include heat capacities or thermal conductivities of one or more components in the formation. In certain embodiments, at least one heat input property 8632 includes an initial heat input property of the foπnation. Initial heat input properties may also include, but are not limited to, volumefric heat capacity, thermal conductivity, porosity, permeability, saturation, compressibility, composition, and the number and types of phases. Properties may also include chemical components, chemical reactions, and kinetic parameters.

In certain embodiments, first simulation method 8634 may simulate heating of the formation. For example, the first simulation method may simulate heating the wellbore and the near wellbore region. Simulation of heating of the formation may assess (i.e., estimate, calculate, or determine) heat injection rate data 8636 for the formation. In one embodiment, heat injection rate data may be assessed to achieve at least one desired parameter of the formation, such as a desired temperature or composition of fluids produced from the formation. First simulation method 8634 may use at least one heat input property 8632 to assess heat injection rate data 8636 for the formation. First simulation method 8634 may be a numerical simulation method. The numerical simulation may be a body- fitted finite difference simulation method. In certain embodiments, first simulation method 8634 may use at least one heat input property 8632, which is an initial heat input property. First simulation method 8634 may use the initial heat input property to assess heat input properties at later times during treatment (e.g., heating) of the formation.

Heat injection rate data 8636 may be used as input into second simulation method 8640. In some embodiments, heat injection rate data 8636 may be modified or altered for input into second simulation method

8640. For example, heat injection rate data 8636 may be modified as a boundary condition for second simulation method 8640. At least one property 8638 of the formation may also be input for use by second simulation method 8640. Heat injection rate data 8636 may include a temperature profile in the formation at any time during heating of the formation. Heat injection rate data 8636 may also include heat flux data for the formation. Heat injection rate data 8636 may also include properties of the formation.

Second simulation method 8640 may be a numerical simulation and/or a reservoir simulation method. In certain embodiments, second simulation method 8640 may be a space-fitted finite difference simulation (e.g., STARS). Second simulation method 8640 may include simulations of fluid mechanics, mass balances, and/or kinetics within the formation. The method may further include providing at least one property 8638 of the formation to the computer system. At least one property 8638 may include chemical components, reactions, and kinetic parameters for the reactions that occur within the formation. At least one property 8638 may also include other properties of the formation such as, but not limited to, permeability, porosities, and/or a location and orientation of heat sources, injection wells, or production wells.

Second simulation method 8640 may assess at least one process characteristic 8642 as a function of time based on heat injection rate data 8636 and at least one property 8638. In some embodiments, second simulation method 8640 may assess an approximate solution for at least one process characteristic 8642. The approximate solution may be a calculated estimation of at least one process characteristic 8642 based on the heat injection rate data and at least one property. The approximate solution may be assessed using a numerical method in second simulation method 8640. At least one process characteristic 8642 may include one or more parameters produced by treating a relatively low permeability formation containing heavy hydrocarbons in situ. For example, at least one process characteristic 8642 may include, but is not limited to, a production rate of one or more produced fluids, an API gravity of a produced fluid, a weight percentage of a produced component, a total mass recovery from the formation, and operating conditions in the formation such as pressure or temperature.

In some embodiments, first simulation method 8634 and second simulation method 8640 may be used to predict process characteristics using parameters based on laboratory data. For example, experimentally based parameters may include chemical components, chemical reactions, kinetic parameters, and one or more formation properties. The simulations may further be used to assess operating conditions that can be used to produce desired properties in fluids produced from the formation. In additional embodiments, the simulations may be used to predict changes in process characteristics based on changes in operating conditions and/or formation properties. In certain embodiments, one or more of the heat input properties may be initial values of the heat input properties. Similarly, one or more of the properties of the formation may be initial values of the properties. The heat input properties and the reservoir properties may change during a simulation of the formation using the first and second simulation methods. For example, the chemical composition, porosity, permeability, volumetric heat capacity, thermal conductivity, and/or saturation may change with time. Consequently, the heat input rate assessed by the first simulation method may not be adequate input for the second simulation method to achieve a desired parameter of the process. In some embodiments, the method may further include assessing modified heat injection rate data at a specified time of the second simulation. At least one heat input property 8641 of the formation assessed at the specified time of the second simulation method may be used as input by first simulation method 8634 to calculate the modified heat input data. Alternatively, the heat input rate may be controlled to achieve a desired parameter during a simulation of the formation using the second simulation method. In some embodiments, one or more model parameters for input into a simulation method may be based on laboratory or field test data of an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons. FIG. 26 illustrates a flow chart of an embodiment of method 9390 for calibrating model parameters to match or approximate laboratory or field data for an in situ process. The method may include providing one or more model parameters 9392 for the in situ process. The model parameters may include properties of the formation. In addition, the model parameters may also include relationships for the dependence of properties on the changes in conditions, such as temperature and pressure, in the formation. For example, model parameters may include a relationship for the dependence of porosity on pressure in the formation. Model parameters may also include an expression for the dependence of permeability on porosity. Model parameters may include an expression for the dependence of thermal conductivity on composition of the foπnation. In addition, model parameters may include chemical components, the number and types of reactions in the formation, and kinetic parameters. Kinetic parameters may include the order of a reaction, activation energy, reaction enthalpy, and frequency factor.

In some embodiments, the method may include assessing one or more simulated process characteristics 9396 based on the one or more model parameters. Simulated process characteristics 9396 may be assessed using simulation method 9394. Simulation method 9394 may be a body-fitted finite difference simulation method. Alternatively, simulation method 9394 may be a reservoir simulation method.

In an embodiment, simulated process characteristics 9396 may be compared 9398 to real process characteristics 9400. Real process characteristics may be process characteristics obtained from laboratory or field tests of an in situ process. Comparing process characteristics may include comparing the simulated process characteristics with the real process characteristics as a function of time. Differences between a simulated process characteristic and a real process characteristic may be associated with one or more model parameters. For example, a higher ratio of gas to oil of produced fluids from a real in situ process may be due to a lack of pressure dependence of kinetic parameters. The method may further include modifying 9399 the one or more model parameters such that at least one simulated process characteristic matches or approximates at least one real process characteristic. One or more model parameters may be modified to account for a difference between a simulated process characteristic and a real process characteristic. For example, an additional chemical reaction may be added to account for pressure dependence or a discrepancy of an amount of a particular component in produced fluids.

Some embodiments may include assessing one or more modified simulated process characteristics from simulation method 9394 based on modified model parameters 9397. Modified model parameters may mclude one or both of model parameters 9392 that have been modified and that have not been modified. In an embodiment, the simulation method may use modified model parameters 9397 to assess at least one operating condition of the in situ process to achieve at least one desired parameter.

Method 9390 may be used to calibrate model parameters for generation reactions of pre-pyrolysis fluids and generation of hydrocarbons from pyrolysis. For example, field test results may show a larger amount of H₂ produced from the formation than the simulation results. The discrepancy may be due to the generation of synthesis gas in the formation in the field test. Synthesis gas may be generated from water in the formation, particularly near heater wells. The temperatures near heater wells may approach a synthesis gas generating temperature range even when the majority of the formation is below synthesis gas generating temperatures. Therefore, the model parameters for the simulation method may be modified to include some synthesis gas reactions.

In addition, model parameters may be calibrated to account for the pressure dependence of the production of low molecular weight hydrocarbons in a formation. The pressure dependence may arise in both laboratory and field scale experiments. As pressure increases, fluids tend to remain in a laboratory vessel or a formation for longer periods of time. The fluids tend to undergo increased cracking and/or coking with increased residence time in the laboratory vessel or the formation. As a result, larger amounts of lower molecular weight hydrocarbons may be generated. Increased cracking of fluids may be more pronounced in a field scale experiment (as compared to a lab experiment, or as compared to calculated cracking) due to longer residence times since fluids may be required to pass through significant distances (e.g., tens of meters) of formation before being produced from a formation.

Simulations may be used to calibrate kinetics parameters that account for the pressure dependence. For example, pressure dependence may be accounted for by introducing cracking and coking reactions into a simulation. The reactions may include pressure dependent kinetic parameters to account for the pressure dependence. Kinetics parameters may be chosen to match or approximate hydrocarbon production reactions parameters from experiments.

In certain embodiments, a simulation method based on a set of model parameters may be used to design an in situ process. A field test of an in situ process based on the design may be used to calibrate the model parameters. FIG. 27 illustrates a flowchart of an embodiment of method 9405 for calibrating model parameters. Method 9405 may include assessing at least one operating condition 9414 of the in situ process using simulation method 9410 based on one or more model parameters. Operating conditions may include pressure, temperature, heating rate, heat input rate, process time, weight percentage of gases, peripheral water recovery or injection. Operating conditions may also include characteristics of the well pattern such as producer well location, producer well orientation, ratio of producer wells to heater wells, heater well spacing, type of heater well pattern, heater well orientation, and distance between an overburden and horizontal heater wells. In one embodiment, at least one operating condition may be assessed such that the in situ process achieves at least one desired parameter. In some embodiments, at least one operating condition 9414 may be used in real in situ process 9418. In an embodiment, the real in situ process may be a field test, or a field operation, operating with at least one operating condition. The real in situ process may have one or more real process characteristics 9420. Simulation method 9410 may assess one or more simulated process characteristics 9412. In an embodiment, simulated process characteristics 9412 may be compared 9416 to real process characteristics 9420. The one or more model parameters may be modified such that at least one simulated process characteristic 9412 from a simulation of the in situ process matches or approximates at least one real process characteristic 9420 from the in situ process. The in situ process may then be based on at least one operating condition. The method may further include assessing one or more modified simulated process characteristics based on the modified model parameters 9417. In some embodiments, simulation method 9410 may be used to control the in situ process such that the in situ process has at least one desired parameter.

In one embodiment, a first simulation method may be more effective than a second simulation method in assessing process characteristics under a first set of conditions. Alternatively, the second simulation method may be more effective in assessing process characteristics under a second set of conditions. A first simulation method may include a body-fitted finite difference simulation method. A first set of conditions may include, for example, a relatively shaφ interface in an in situ process. In an embodiment, a first simulation method may use a finer grid than a second simulation method. Thus, the first simulation method may be more effective in modeling a shaφ interface. A shaφ interface refers to a relatively large change in one or more process characteristics in a relatively small region in the formation. A shaφ interface may include a relatively steep temperature gradient that may exist in a near wellbore region of a heater well. A relatively steep gradient in pressure and composition, due to pyrolysis, may also exist in the near wellbore region. A shaφ interface may also be present at a combustion or reaction front as it propagates through a formation. A steep gradient in temperature, pressure, and composition may be present at a reaction front.

In certain embodiments, a second simulation method may include a space-fitted finite difference simulation method such as a reservoir simulation method. A second set of conditions may include conditions in which heat transfer by convection is significant. In addition, a second set of conditions may also include condensation of fluids in a foπnation.

In some embodiments, model parameters for the second simulation method may be calibrated such that the second simulation method effectively assesses process characteristics under both the first set and the second set of conditions. FIG. 28 illustrates a flow chart of an embodiment of method 9430 for calibrating model parameters for a second simulation method using a first simulation method. Method 9430 may include providing one or more model parameters 9431 to a computer system. One or more first process characteristics 9434 based on one or more model parameters 9431 may be assessed using first simulation method 9432 in memory on the computer system. First simulation method 9432 may be a body-fitted finite difference simulation method. The model parameters may include relationships for the dependence of properties such as porosity, permeability, thermal conductivity, and heat capacity on the changes in conditions (e.g., temperature and pressure) in the formation. In addition, model parameters may include chemical components, the number and types of reactions in the foπnation, and kinetic parameters. Kinetic parameters may include the order of a reaction, activation energy, reaction enthalpy, and frequency factor. Process characteristics may include, but are not limited to, a temperature profile, pressure, composition of produced fluids, and a velocity of a reaction or combustion front. In certain embodiments, one or more second process characteristics 9440 based on one or more model parameters 9431 may be assessed using second simulation method 9438. Second simulation method 9438 may be a space-fitted finite difference simulation method, such as a reservoir simulation method. One or more first process characteristics 9434 may be compared 9436 to one or more second process characteristics 9440. The method may further include modifying one or more model parameters 9431 such that at least one first process characteristic 9434 matches or approximates at least one second process characteristic 9440. For example, the order or the activation energy of the one or more chemical reactions may be modified to account for differences between the first and second process characteristics. In addition, a single reaction may be expressed as two or more reactions. In some embodiments, one or more third process characteristics based on the one or more modified model parameters 9442 may be assessed using the second simulation method.

In one embodiment, simulations of an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons may be used to design and/or control a real in situ process. Design and/or confrol of an in situ process may include assessing at least one operating condition that achieves a desired parameter of the in situ process. FIG. 29 illustrates a flow chart of an embodiment of method 9450 for the design and/or confrol of an in situ process. The method may include providing to the computer system one or more values of at least one operating condition 9452 of the in situ process for use as input to simulation method 9454. The simulation method may be a space-fitted finite difference simulation method such as a reservoir simulation method or it may be a body-fitted simulation method such as FLUENT. At least one operating condition may include, but is not limited to, pressure, temperature, heating rate, heat input rate, process time, weight percentage of gases, peripheral water recovery or injection, production rate, and time to reach a given production rate. In addition, operating conditions may include characteristics of the well pattern such as producer well location, producer well orientation, ratio of producer wells to heater wells, heater well spacing, type of heater well pattern, heater well orientation, and distance between an overburden and horizontal heater wells.

In one embodiment, the method may include assessing one or more values of at least one process characteristic 9456 corresponding to one or more values of at least one operating condition 9452 from one or more simulations using simulation method 9454. In certain embodiments, a value of at least one process characteristic may include the process characteristic as a function of time. A desired value of at least one process characteristic 9460 for the in situ process may also be provided to the computer system. An embodiment of the method may further include assessing 9458 desired value of at least one operating condition 9462 to achieve desired value of at least one process characteristic 9460. Desired value of at least one operating condition 9462 may be assessed from the values of at least one process characteristic 9456 and values of at least one operating condition 9452. For example, desired value 9462 may be obtained by inteφolation of values 9456 and values 9452. In some embodiments, a value of at least one process characteristic may be assessed from the desired value of at least one operating condition 9462 using simulation method 9454. In some embodiments, an operating condition to achieve a desired parameter may be assessed by comparing a process characteristic as a function of time for different operating conditions. In an embodiment, the method may include operating the in situ system using the desired value of at least one additional operating condition.

In an alternate embodiment, a desired value of at least one operating condition to achieve the desired value of at least one process characteristic may be assessed by using a relationship between at least one process characteristic and at least one operating condition of the in situ process. The relationship may be assessed from a simulation method. The relationship may be stored on a database accessible by the computer system. The relationship may include one or more values of at least one process characteristic and coπesponding values of at least one operating condition. Alternatively, the relationship may be an analytical function.

In an embodiment, a desired process characteristic may be a selected composition of fluids produced from a formation. A selected composition may correspond to a ratio of non-condensable hydrocarbons to condensable hydrocarbons. In certain embodiments, increasing the pressure in the formation may increase the ratio of non- condensable hydrocarbons to condensable hydrocarbons of produced fluids. The pressure in the formation may be confrolled by increasing the pressure at a production well in an in situ process. In an alternate embodiment, another operating condition may be confrolled simultaneously (e.g., the heat input rate).

In an embodiment, the pressure coπesponding to the selected composition may be assessed from two or more simulations at two or more pressures. In one embodiment, at least one of the pressures of the simulations may be estimated from EQN. 29:

where p is measured in psia (pounds per square inch absolute), Tis measured in Kelvin, and A and B are parameters dependent on the value of the desired process characteristic for a given type of formation. Values of A and B may be assessed from experimental data for a process characteristic in a given fonnation and may be used as input to EQN. 29. The pressure corresponding to the desired value of the process characteristic may then be estimated for use as input into a simulation. The two or more simulations may provide a relationship between pressure and the composition of produced fluids. The pressure corresponding to the desired composition may be inteφolated from the relationship. A simulation at the inteφolated pressure may be performed to assess a composition and one or more additional process characteristics. The accuracy of the inteφolated pressure may be assessed by comparing the selected composition with the composition from the simulation. The pressure at the production well may be set to the inteφolated pressure to obtain produced fluids with the selected composition.

In certain embodiments, the pressure of a formation may be readily confrolled at certain stages of an in situ process. At some stages of the in situ process, however, pressure control may be relatively difficult. For example, during a relatively short period of time after heating has begun the permeability of the formation may be relatively low. At such early stages, the heat fransfer front at which pyrolysis occurs may be at a relatively large distance from a producer well (i.e., the point at which pressure may be confrolled). Therefore, there may be a significant pressure drop between the producer well and the heat fransfer front. Consequently, adjusting the pressure at a producer well may have a relatively small influence on the pressure at which pyrolysis occurs at early stages of the in situ process. At later stages of the in situ process when permeability has developed relatively uniformly throughout the formation, the pressure of the producer well corresponds to the pressure in the formation. Therefore, the pressure at the producer well may be used to control the pressure at which pyrolysis occurs.

In some embodiments, a similar procedure may be followed to assess heater well pattern and producer well pattern characteristics that correspond to a desired process characteristic. For example, a relationship between the spacing of the heater wells and composition of produced fluids may be obtained from two or more simulations with different heater well spacings. Simulations may use expressions similar to EQNS. 2-6 for modeling the properties of a relatively low permeability formation containing heavy hydrocarbons. Chemical reactions in the formation may be modeled with equations similar to EQNS. 27 and 28, for example. The heat injection rate may be calculated using CFX. A constant heat input rate of about 1640 Watts/m may be imposed at the casing interface. When the interface temperature reaches about 760 °C, the heat input rate may be controlled to maintain the temperature of the interface at about 760 °C. The approximate heat input rate to maintain the interface temperature at about 760 °C may be used as input into STARS. STARS may then be used to simulate in situ treatment of a relatively low permeability formation containing heavy hydrocarbons. Data from simulations may be used to predict or assess operating conditions and/or process characteristics for in situ freatment of relatively low permeability formations containing heavy hydrocarbons.

In one embodiment, a simulation method on a computer system may be used in a method for modeling one or more stages of a process for treating a relatively low permeability formation containing heavy hydrocarbons in situ. The simulation method may be, for example, a reservoir simulation method. The simulation method may simulate heating of the formation, fluid flow, mass transfer, heat fransfer, and chemical reactions in one or more of the stages of the process. In some embodiments, the simulation method may also simulate removal of contaminants from the formation, recovery of heat from the formation, and injection of fluids into the foπnation.

Method 9588 of modeling the one or more stages of a freatment process is depicted in a flow chart in FIG. 30. The one or more stages may include heating stage 9574, pyrolyzation stage 9576, synthesis gas generation stage 9579, remediation stage 9582, and/or shut-in stage 9585. The method may include providing at least one property 9572 of the formation to the computer system. In addition, operating conditions 9573, 9577, 9580, 9583, and/or 9586 for one or more of the stages of the in situ process may be provided to the computer system. Operating conditions may include, but not be limited to, pressure, temperature, heating rates, etc. In addition, operating conditions of a remediation stage may include a flow rate of ground water and injected water into the formation, size of treatment area, and type of drive fluid. In certain embodiments, the method may include assessing process characteristics 9575, 9578, 9581, 9584, and/or 9587 of the one or more stages using the simulation method. Process characteristics may include properties of a produced fluid such as API gravity and gas/oil ratio. Process characteristics may also include a pressure and temperature in the formation, total mass recovery from the formation, and production rate of fluid produced from the formation. In addition, a process characteristic of the remediation stage may include the type and concentration of contaminants remaining in the formation.

In one embodiment, a simulation method may be used to assess operating conditions of at least one of the stages of an in situ process that results in desired process characteristics. FIG. 31 illustrates a flow chart of an embodiment of method 9701 for designing and controlling heating stage 9706, pyrolyzation stage 9708, synthesis gas generating stage 9714, remediation stage 9720, and/or shut-in stage 9726 of an in situ process with a simulation method on a computer system. The method may include providing sets of operating conditions 9702, 9712, 9718,

9724, and or 9730 for at least one of the stages of the in situ process. In addition, desired process characteristics 9704, 9713, 9719, 9725, and/or 9731 for at least one of the stages of the in situ process may also be provided. The method may further include assessing at least one additional operating condition 9707, 9710, 9716, 9722, and/or 9728 for at least one of the stages that achieves the desired process characteristics of one or more stages. In an embodiment, in situ treatment of a relatively low permeability formation containing heavy hydrocarbons may substantially change physical and mechanical properties of the formation. The physical and mechanical properties may be affected by chemical properties of a formation, operating conditions, and process characteristics.

Changes in physical and mechanical properties due to treatment of a formation may result in deformation of the formation. Deformation characteristics may include, but are not limited to, subsidence, compaction, heave, and shear deformation. Subsidence is a vertical decrease in the surface of a formation over a treated portion of a formation. Heave is a vertical increase at the surface above a freated portion of a formation. Surface displacement may result from several concurrent subsurface effects, such as the thermal expansion of layers of the formation, the compaction of the richest and weakest layers, and the constraining force exerted by cooler rock that suπounds the treated portion of the foπnation. hi general, in the initial stages of heating a formation, the surface above the treated portion may show a heave due to thermal expansion of incompletely pyrolyzed formation material in the treated portion of the formation. As a significant portion of formation becomes pyrolyzed, the formation is weakened and pore pressure in the treated portion declines. The pore pressure is the pressure of the liquid and gas that exists in the pores of a formation. The pore pressure may be influenced by the thermal expansion of the organic matter in the formation and the withdrawal of fluids from the formation. The decrease in the pore pressure tends to increase the effective stress in the treated portion. Since the pore pressure affects the effective sfress on the treated portion of a formation, pore pressure influences the extent of subsurface compaction in the formation. Compaction, another deformation characteristic, is a vertical decrease of a subsurface portion above or in the treated portion of the formation. In addition, shear deformation of layers both above and in the treated portion of the formation may also occur. In some embodiments, deformation may adversely affect the in situ treatment process. For example, deformation may seriously damage surface facilities and wellbores.

In certain embodiments, an in situ freatment process may be designed and confrolled such that the adverse influence of deformation is minimized or substantially eliminated. Computer simulation methods may be useful for design and control of an in situ process since simulation methods may predict deformation characteristics. For example, simulation methods may predict subsidence, compaction, heave, and shear deformation in a formation from a model of an in situ process. The models may include physical, mechanical, and chemical properties of a formation. Simulation methods may be used to study the influence of properties of a formation, operating conditions, and process characteristics on deformation characteristics of the formation.

FIG. 32 illustrates model 9518 of a formation that may be used in simulations of deformation characteristics according to one embodiment. The formation model is a vertical cross-section that may include treated portions 9524 with thickness 9532 and width or radius 9528. Treated portion 9524 may include several layers or regions that vary in mineral composition and richness of organic matter. For example, in a model of an oil shale foπnation, treated portion 9524 may include layers of lean kerogenous chalk, rich kerogenous chalk, and silicified kerogenous chalk. In one embodiment, freated portion 9524 may be a dipping coal seam that is at an angle to the surface of the formation. The model may also include untreated portions such as overburden 9521 and base rock 9526. Overburden 9521 may have thickness 9530. Overburden 9521 may also include one or more portions, for example, portion 9520 and portion 9522 that differ in composition. For example, portion 9522 may have a composition similar to freated portion 9524 prior to treatment. Portion 9520 may be composed of organic material, soil, rock, etc. Base rock 9526 may include barren rock with at least some organic material.

In some embodiments, an in situ process may be designed such that it includes an untreated portion or strip between treated portions of the foπnation. FIG. 33 illustrates a schematic of a strip development according to one embodiment. The formation includes freated portion 9523 and treated portion 9525 with thicknesses 9531 and widths 9533 (thicknesses 9531 and widths 9533 may vary between portion 9523 and portion 9525). Untreated portion 9527 with width 9529 separates freated portion 9523 from treated portion 9525. In some embodiments, width 9529 is substantially less than widths 9533 since only smaller sections need to remain untreated to provide structural support. In some embodiments, the use of an untreated portion may decrease the amount of subsidence, heave, compaction, or shear deformation at and above the freated portions of the foπnation.

In an embodiment, an in situ treatment process may be represented by a three-dimensional model. FIG. 34 depicts a schematic illustration of a freated portion that may be modeled with a simulation. The treated portion includes a well pattern with heat sources 9524 and producers 9526. Dashed lines 9528 correspond to three planes of symmetry that may divide the pattern into six equivalent sections. Solid lines between heat sources 9524 merely depict the pattern of heat sources (i.e., the solid lines do not represent actual equipment between the heat sources).

In some embodiments, a geomechanical model of the pattern may include one of the six symmetry segments. FIG. 35 depicts a horizontal cross section of a model of a foπnation for use by a simulation method according to one embodiment. The model includes grid elements 9530. Treated portion 9532 is located in the lower left corner of the model. Grid elements in the freated portion may be sufficiently small to take into account the large variations in conditions in the treated portion. In addition, distance 9537 and distance 9539 may be sufficiently large such that the deformation furthest from the freated portion is substantially negligible. Alternatively, a model may be approximated by a shape, such as a cylinder. The diameter and height of the cylinder may correspond to the size and height of the treated portion.

In certain embodiments, heat sources may be modeled by line sources that inject heat at a fixed rate. The heat sources may generate a reasonably accurate temperature distribution in the vicinity of the heat sources.

Alternatively, a time-dependent temperature distribution may be imposed as an average boundary condition. FIG. 36 illustrates a flow chart of an embodiment of method 9532 for modeling deformation due to freatment of a relatively low permeability formation containing heavy hydrocarbons in situ. The method may include providing at least one property 9534 of the formation to a computer system. The formation may include a freated portion and an untreated portion. Properties may include mechanical, chemical, thermal, and physical properties of the portions of the formation. For example, the mechanical properties may include compressive sfrength, confining pressure, creep parameters, elastic modulus, Poisson's ratio, cohesion stress, friction angle, and cap eccentricity. Thermal and physical properties may include a coefficient of thermal expansion, volumetric heat capacity, and theπnal conductivity. Properties may also include the porosity, permeability, saturation, compressibility, and density of the formation. Chemical properties may include, for example, the richness and/or organic content of the portions of the formation.

In addition, at least one operating condition 9535 may be provided to the computer system. For instance, operating conditions may include, but are not limited to, pressure, temperature, process time, rate of pressure increase, heating rate, and characteristics of the well pattern. In addition, an operating condition may include the overburden thickness and thickness and width or radius of the treated portion of the formation. An operating condition may also include untreated portions between freated portions of the formation, along with the horizontal distance between freated portions of a formation.

In certain embodiments, the properties may include initial properties of the formation. Furthermore, the model may include relationships for the dependence of the mechanical, thermal, and physical properties on conditions such as temperature, pressure, and richness in the portions of the formation. For example, the compressive sfrength in the freated portion of the formation may be a function of richness, temperature, and pressure. The volumefric heat capacity may depend on the richness and the coefficient of thermal expansion may be a function of the temperature and richness. Additionally, the permeability, porosity, and density may be dependent upon the richness of the formation.

In some embodiments, physical and mechanical properties for a model of a formation may be assessed from samples extracted from a geological foπnation targeted for freatment. Properties of the samples may be measured at various temperatures and pressures. For example, mechanical properties may be measured using uniaxial, triaxial, and creep experiments. In addition, chemical properties (e.g., richness) of the samples may also be measured. The dependence of properties on temperature, pressure, and richness may then be assessed from the measurements. In certain embodhnents, the properties may be mapped on to a model using known sample locations. For instance, FIG. 37 depicts a profile of richness versus depth in a model of an oil shale formation. The treated portion is represented by region 9545. Similarly, the overburden and base rock are represented by region 9547 and region 9549, respectively. In FIG. 37, richness is measured in m³ of kerogen per metric ton of oil shale.

In certain embodiments, assessing deformation using a simulation method may require a material or constitutive model. A constitutive model relates the stress in the formation to the strain or displacement. Mechanical properties may be entered into a suitable constitutive model to calculate the deformation of the formation. In one embodiment, the Drucker-Prager-with-cap material model may be used to model the time- independent deformation of the formation.

In an embodiment, the time-dependent creep or secondary creep strain of the formation may also be modeled. For example, the time-dependent creep in a formation may be modeled with a power law in EQN. 30:

where ε is the secondary creep strain, C is a creep multiplier, σi is the axial stress, σ₃ is the confining pressure, D is a stress exponent, and t is the time. The values of C and D may be obtained from fitting experimental data. In one embodiment, the creep rate may be expressed by EQN. 31 :

(31) dε/dt = A ^χ ( σ_!/σ_u)^D

where A is a multiplier obtained from fitting experimental data and σ_u is the ultimate sfrength in uniaxial compression.

Additionally, the method shown in FIG. 36 may further include assessing 9536 at least one process characteristic 9538 of the freated portion of the foπnation. At least one process characteristic 9538 may include a pore pressure disfribution, a heat input rate, or a time dependent temperature disfribution in the treated portion of the foπnation. At least one process characteristic may be assessed by a simulation method. For example, a heat input rate may be estimated using a body-fitted finite difference simulation package such as FLUENT. Similarly, the pore pressure distribution may be assessed from a space-fitted or body-fitted simulation method such as STARS. In other embodiments, the pore pressure may be assessed by a finite element simulation method such as ABAQUS. The finite element simulation method may employ line sinks of fluid to simulate the performance of production wells. Alternatively, process characteristics such as temperature disfribution and pore pressure distribution may be approximated by other means. For example, the temperature disfribution may be imposed as an average boundary condition in the calculation of deformation characteristics. The temperature distribution may be estimated from results of detailed calculations of a heating rate of a formation. For example, a freated portion may be heated to a pyrolyzation temperature for a specified period of time by heat sources and the temperature disfribution assessed during heating of the freated portion. In an embodiment, the heat sources may be uniformly disfributed and inject a constant amount of heat. The temperature distribution inside most of the freated portion may be substantially uniform during the specified period of time. Some heat may be allowed to diffuse from the freated portion into the overburden, base rock, and lateral rock. The freated portion may be maintained at a selected temperature for a selected period of time after the specified period of time by injecting heat from the heat sources as needed.

Similarly, the pore pressure disfribution may also be imposed as an average boundary condition. The initial pore pressure disfribution may be assumed to be lithostatic. The pore pressure distribution may then be gradually reduced to a selected pressure during the remainder of the simulation of the deformation characteristics. In some embodiments, the method may include assessing at least one deformation characteristic 9542 of the formation using simulation method 9540 on the computer system as a function of time. At least one deformation characteristic may be assessed from at least one property 9534, at least one process characteristic 9538, and at least one operating condition 9535. In certain embodiments, process characteristic 9538 may be assessed by a simulation or process characteristic 9538 may be measured. Deformation characteristics may include, but are not limited to, subsidence, compaction, heave, and shear deformation in the formation.

Simulation method 9540 may be a finite element simulation method for calculating elastic, plastic, and time dependent behavior of materials. For example, ABAQUS is a commercially available finite element simulation method from Hibbitt, Karlsson & Sorensen, Inc. located in Pawtucket, Rhode Island. ABAQUS is capable of describing the elastic, plastic, and time dependent (creep) behavior of a broad class of materials such as mineral matter, soils, and metals. In general, ABAQUS may treat materials whose properties may be specified by user-defined constitutive laws. ABAQUS may also calculate heat fransfer and treat the effect of pore pressure variations on rock deformation.

Computer simulations may be used to assess operating conditions of an in situ process in a formation that may result in desired deformation characteristics. FIG. 38 illustrates a flow chart of an embodiment of method 9544 for designing and controlling an in situ process using a computer system. The method may include providing to the computer system at least one set of operating conditions 9546 for the in situ process. For instance, operating conditions may include pressure, temperature, process time, rate of pressure increase, heating rate, characteristics of the well pattern, the overburden thickness, thickness and width of the freated portion of the formation and or untreated portions between treated portions of the formation, and the horizontal distance between freated portions of a formation.

In addition, at least one desired deformation characteristic 9548 for the in situ process may be provided to the computer system. The desfred deformation characteristic may be a selected subsidence, selected heave, selected compaction, or selected shear deformation. In some embodiments, at least one additional operating condition 9551 may be assessed using simulation method 9550 that achieves at least one desired deformation characteristic 9548. A desired deformation characteristic may be a value that does not adversely effect the operation of an in situ process. For example, a minimum overburden necessary to achieve a desired maximum value of subsidence may be assessed. In an embodiment, at least one additional operating condition 9551 may be used to operate an in situ process 9552.

In one embodiment, operating conditions to obtain desired deformation characteristics may be assessed from simulations of an in situ process based on multiple operating conditions. FIG. 39 illustrates a flow chart of an embodiment of method 9554 for assessing operating conditions to obtain desired deformation characteristics. The method may include providing one or more values of at least one operating condition 9556 to a computer system for use as input to simulation method 9558. The simulation method may be a finite element simulation method for calculating elastic, plastic, and creep behavior.

In some embodhnents, the method may further include assessing one or more values of deformation characteristics 9560 using simulation method 9558 based on the one or more values of at least one operating condition 9556. In one embodiment, a value of at least one deformation characteristic may include the deformation characteristic as a function of time. A desired value of at least one deformation characteristic 9564 for the in situ process may also be provided to the computer system. An embodiment of the method may include assessing 9562 desired value of at least one operating condition 9566 to achieve desired value of at least one deformation characteristic 9564.

Desired value of at least one operating condition 9566 may be assessed from the values of at least one deformation characteristic 9560 and the values of at least one operating condition 9556. For example, desired value 9566 may be obtained by inteφolation of values 9560 and values 9556. In some embodiments, a value of at least one deformation characteristic may be assessed 9565 from the desired value of at least one operating condition 9566 using simulation method 9558. In some embodiments, an operating condition to achieve a desired deformation characteristic may be assessed by comparing a deformation characteristic as a function of time for different operating conditions.

In an alternate embodiment, a desired value of at least one operating condition to achieve the desired value of at least one deformation characteristic may be assessed using a relationship between at least one deformation characteristic and at least one operating condition of the in situ process. The relationship may be assessed using a simulation method. Such relationship may be stored on a database accessible by the computer system. The relationship may include one or more values of at least one deformation characteristic and coπesponding values of at least one operating condition. Alternatively, the relationship may be an analytical function.

Simulations have been used to investigate the effect of various operating conditions on the deformation characteristics of an oil shale formation. In one set of simulations, the formation was modeled as either a cylinder or a rectangular slab. In the case of a cylinder, the model of the formation is described by a thickness of the freated portion, a radius, and a thickness of the overburden. The rectangular slab is described by a width rather than a radius and by a thickness of the freated section and overburden. FIG. 40 illustrates the influence of operating pressure on subsidence in a cylindrical model of a formation from a finite element simulation. The thickness of the freated portion is 189 m, the radius of the treated portion is 305 m, and the overburden thickness is 201 m. FIG. 40 shows the vertical surface displacement in meters over a period of years. Curve 9568 corresponds to an operating pressure of 27.6 bars absolute and curve 9569 to an operating pressure of 6.9 bars absolute. It is to be understood that the surface displacements set forth in FIG. 40 are only illustrative (actual surface displacements will generally differ from those shown in FIG. 40). FIG. 40 demonstrates, however, that increasing the operating pressure may substantially reduce subsidence. FIGS. 41 and 42 illustrate the influence of the use of an untreated portion between two freated portions. FIG. 41 is the subsidence in a rectangular slab model with a freated portion thickness of 189 m, freated portion width of 649 m, and overburden thickness of 201 m. FIG. 42 represents the subsidence in a rectangular slab model with two freated portions separated by an untreated portion, as pictured in FIG. 33. The thickness of the freated portion and the overburden are the same as the model corresponding to FIG. 41. The width of each freated portion is one half of the width of the freated portion of the model in FIG. 41. Therefore, the total width of the freated portions is the same for each model. The operating pressure in each case is 6.9 bars absolute. As with FIG. 40, the surface displacements in FIGS. 41 and 42 are only illustrative. A comparison of FIGS. 41 and 42, however, shows that the use of an untreated portion reduces the subsidence by about 25%. In addition, the initial heave is also reduced.

In another set of simulations, the calculation of the shear deformation in a freated oil shale formation was demonstrated. The model included a symmetry element of a pattern of heat sources and producer wells. Boundary conditions imposed in the model were such that the vertical planes bounding the formation were symmetry planes. FIG. 43 represents the shear deformation of the formation at the location of selected heat sources as a function of depth. Curve 9570 and curve 9571 represent the shear deformation as a function of depth at 10 months and 12 months, respectively. The curves, which correspond to the predicted shape of the heat injection wells, show that shear deformation increases with depth in the foπnation.

In certain embodiments, a computer system may be used to operate an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons. The in situ process may include providing heat from one or more heat sources to at least one portion of the formation. In addition, the in situ process may also include allowing the heat to fransfer from the one or more heat sources to a selected section of the formation. FIG. 44 illustrates method 9480 for operating an in situ process using a computer system. The method may include operating in situ process 9482 using one or more operating parameters. Operating parameters may include properties of the formation, such as heat capacity, density, permeability, thermal conductivity, porosity, and/or chemical reaction data. In addition, operating parameters may include operating conditions. Operating conditions may include, but are not limited to, thickness and area of heated portion of the formation, pressure, temperature, heating rate, heat input rate, process time, production rate, time to obtain a given production rate, weight percentage of gases, and/or peripheral water recovery or injection. Operating conditions may also include characteristics of the well pattern such as producer well location, producer well orientation, ratio of producer wells to heater wells, heater well spacing, type of heater well pattern, heater well orientation, and/or distance between an overburden and horizontal heater wells. Operating parameters may also include mechanical properties of the formation. Operating parameters may include deformation characteristics, such as fracture, strain, subsidence, heave, compaction, and/or shear deformation.

In certain embodiments, at least one operating parameter 9484 of in situ process 9482 may be provided to computer system 9486. Computer system 9486 may be at or near in situ process 9482. Alternatively, computer system 9486 may be at a location remote from in situ process 9482. The computer system may include a first simulation method for simulating a model of in situ process 9482. In one embodiment, the first simulation method may include method 9470 illustrated in FIG. 21, method 9360 illustrated in FIG. 23, method 8630 illustrated in FIG. 25, method 9390 illustrated in FIG. 26, method 9405 illustrated in FIG. 27, method 9430 illustrated in FIG. 28, and/or method 9450 illustrated in FIG. 29. The first simulation method may include a body-fitted finite difference simulation method such as FLUENT or space-fitted finite difference simulation method such as STARS. The first simulation method may perform a reservoir simulation. A reservoir simulation method may be used to determine operating parameters including, but not limited to, pressure, temperature, heating rate, heat input rate, process time, production rate, time to obtain a given production rate, weight percentage of gases, and peripheral water recovery or injection. In an embodiment, the first simulation method may also calculate deformation in a foπnation. A simulation method for calculating deformation characteristics may include a finite element simulation method such as ABAQUS. The first simulation method may calculate fracture progression, strain, subsidence, heave, compaction, and shear deformation. A simulation method used for calculating deformation characteristics may include method 9532 illustrated in FIG. 36 and/or method 9554 illustrated in FIG. 39. The method may further include using at least one parameter 9484 with a first simulation method and the computer system to provide assessed information 9488 about in situ process 9482. Operating parameters from the simulation may be compared to operating parameters of in situ process 9482. Assessed information from a simulation may include a simulated relationship between one or more operating parameters with at least one parameter 9484. For example, the assessed information may include a relationship between operating parameters such as pressure, temperature, heating input rate, or heating rate and operating parameters relating to product quality.

In some embodiments, assessed information may include inconsistencies between operating parameters from simulation and operating parameters from in situ process 9482. For example, the temperature, pressure, product quality, or production rate from the first simulation method may differ from in situ process 9482. The source of the inconsistencies may be assessed from the operating parameters provided by simulation. The source of the inconsistencies may include differences between certain properties used in a simulated model of in situ process 9482 and in situ process 9482. Certain properties may include, but are not limited to, thermal conductivity, heat capacity, density, permeability, or chemical reaction data. Certain properties may also include mechanical properties such as compressive sfrength, confining pressure, creep parameters, elastic modulus, Poisson's ratio, cohesion stress, friction angle, and cap eccentricity.

In one embodiment, assessed infoπnation may include adjustments in one or more operating parameters of in situ process 9482. The adjustments may compensate for inconsistencies between simulated operating parameters and operating parameters from in situ process 9482. Adjustments may be assessed from a simulated relationship between at least one parameter 9484 and one or more operating parameters. For example, an in situ process may have a particular hydrocarbon fluid production rate, e.g., 1 m³/day, after a particular period of time (e.g., 90 days). A theoretical temperature at an observation well (e.g., 100 °C) may be calculated using given properties of the formation. However, a measured temperature at an observation well (e.g., 80 °C) may be lower than the theoretical temperature. A simulation on a computer system may be performed using the measured temperature. The simulation may provide operating parameters of the in situ process that correspond to the measured temperature. The operating parameters from simulation may be used to assess a relationship between, for example, temperature or heat input rate and the production rate of the in situ process. The relationship may indicate that the heat capacity or thermal conductivity of the formation used in the simulation is inconsistent with the formation.

In some embodiments, the method may further include using assessed information 9488 to operate in situ process 9482. As used herein, "operate" refers to controlling or changing operating conditions of an in situ process.

For example, the assessed information may indicate that the thermal conductivity of the formation in the above example is lower than the thermal conductivity used in the simulation. Therefore, the heat input rate to in situ process 9482 may be increased to operate at the theoretical temperature.

In other embodiments, the method may include obtaining 9492 information 9494 from a second simulation method and the computer system using assessed information 9488 and desired parameter 9490. In one embodiment, the first simulation method may be the same as the second simulation method. In another embodiment, the first and second simulation methods may be different. Simulations may provide a relationship between at least one operating parameter and at least one other parameter. Additionally, obtained information 9494 may be used to operate in situ process 9482.

Obtained infoπnation 9494 may include at least one operating parameter for use in the in situ process that achieves the desired parameter. In one embodiment, simulation method 9450 illustrated in FIG. 29 may be used to obtain at least one operating parameter that achieves the desired parameter. For example, a desired hydrocarbon fluid production rate for an in situ process may be 6 m³/day. One or more simulations may be used to determine the operating parameters necessary to achieve a hydrocarbon fluid production rate of 6 ffiVday. In some embodiments, model parameters used by simulation method 9450 may be calibrated to account for differences observed between simulations and in situ process 9482. In one embodiment, simulation method 9390 illustrated in FIG. 26 may be used to calibrate model parameters. In another embodiment, simulation method 9554 illustrated in FIG. 39 may be used to obtain at least one operating parameter that achieves a desired deformation characteristic.

FIG. 45 illustrates a schematic of an embodiment for controlling in situ process 9701 in a formation using a computer simulation method. In situ process 9701 may include sensor 9702 for monitoring operating parameters. Sensor 9702 may be located in a baπier well, a monitoring well, a production well, or a heater well. Sensor 9702 may monitor operating parameters such as subsurface and surface conditions in the formation. Subsurface conditions may include pressure, temperature, product quality, and deformation characteristics, such as fracture progression. Sensor 9702 may also monitor surface data such as pump status (i.e., on or off), fluid flow rate, surface pressure/temperature, and heater power. The surface data may be monitored with instruments placed at a well.

In addition, at least one operating parameter 9704 measured by sensor 9702 may be provided to local computer system 9708. Alternatively, operating parameter 9704 may be provided to remote computer system 9706. Computer system 9706 may be, for example, a personal desktop computer system, a laptop, or personal digital assistant such as a palm pilot. FIG. 46 illustrates several ways that information such as operating parameter 9704 may be transmitted from in situ process 9701 to remote computer system 9706. Information may be transmitted by means of internet 9718, hardwire telephone lines 9720, and wireless communications 9722. Wireless communications 9722 may include transmission via satellite 9724.

In some embodiments, operating parameter 9704 may be provided to computer system 9708 or 9706 automatically during the freatment of a formation. Computer systems 9706 and 9708 may include a simulation method for simulating a model of the in situ freatment process 9701. The simulation method may be used to obtain information 9710 about the in situ process.

In an embodiment, a simulation of in situ process 9701 may be performed manually at a desired time. Alternatively, a simulation may be performed automatically when a desired condition is met. For instance, a simulation may be performed when one or more operating parameters reach, or fail to reach, a particular value at a particular time. For example, a simulation may be performed when the production rate fails to reach a particular value at a particular time. In some embodiments, information 9710 relating to in situ process 9701 may be provided automatically by computer system 9706 or 9708 for use in controlling in situ process 9701. Information 9710 may include instructions relating to confrol of in situ process 9701. Information 9710 may be fransmitted from computer system 9706 via internet, hardwire, wireless, or satellite transmission as illustrated in FIG. 46. Information 9710 may be provided to computer system 9712. Computer system 9712 may also be at a location remote from the in situ process. Computer system 9712 may process information 9710 for use in controlling in situ process 9701. For example, computer system 9712 may use information 9710 to determine adjustments in one or more operating parameters. Computer system 9712 may then automatically adjust 9716 one or more operating parameters of in situ process 9701. Alternatively, one or more operating parameters of in situ process 9701 may be displayed and then, optionally, adjusted manually 9714.

FIG. 47 illustrates a schematic of an embodiment for controlling in situ process 9701 in a formation using information 9710. Information 9710 may be obtained using a simulation method and a computer system. Information 9710 may be provided to computer system 9712. Information 9710 may include information that relates to adjusting one or more operating parameters. Output 9713 from computer system 9712 may be provided to display 9722, data storage 9724, or surface facility 9723. Output 9713 may also be used to automatically confrol conditions in the formation by adjusting one or more operating parameters. Output 9713 may include instructions to adjust pump status and flow rate at a barrier well 9726, adjust pump status and flow rate at a production well 9728, and/or adjust the heater power at a heater well 9730. Output 9713 may also include instractions to heating pattern 9732 of in situ process 9701. For example, an instruction may be to add one or more heater wells at particular locations. In addition, output 9713 may include instructions to shut-in the formation 9734.

Alternatively, output 9713 may be viewed by operators of the in situ process on display 9722. The operators may then use output 9713 to manually adjust one or more operating parameters.

FIG. 48 illustrates a schematic of an embodiment for controlling in situ process 9701 in a formation using a simulation method and a computer system. At least one operating parameter 9704 from in situ process 9701 may be provided to computer system 9736. Computer system 9736 may include a simulation method for simulating a model of in situ process 9701. Computer system 9736 may use the simulation method to obtain information 9738 about in situ process 9701. Information 9738 may be provided to data storage 9740, display 9742, and analysis 9743. In an embodiment, information 9738 may be automatically provided to in situ process 9701. Information 9738 may then be used to operate in situ process 9701. Analysis 9743 may include review of infoπnation 9738 and/or use of information 9738 to operate in situ process 9701. Analysis 9743 may include obtaining additional information 9750 using one or more simulations 9746 of in situ process 9701. One or more simulations may be used to obtain additional or modified model parameters of in situ process 9701. The additional or modified model parameters may be used to further assess in situ process 9701. Simulation method 9390 illustrated in FIG. 26 may be used to determine additional or modified model parameters. Method 9390 may use at least one operating parameter 9704 and information 9738 to calibrate model parameters. For example, at least one operating parameter 9704 may be compared to at least one simulated operating parameter. Model parameters may be modified such that at least one simulated operating parameter matches or approximates at least one operating parameter 9704.

In an embodiment, analysis 9743 may include obtaining 9744 additional information 9748 about properties of in situ process 9701. Properties may include, for example, thermal conductivity, heat capacity, porosity, or permeability of one or more portions of the formation. Properties may also include chemical reaction data such as, chemical reactions, chemical components, and chemical reaction parameters. Properties may be obtained from the literature or from field or laboratory experiments. For example, properties of core samples of the freated foπnation may be measured in a laboratory. Additional information 9748 may be used to operate in situ process 9701. Alternatively, additional information 9743 may be used in one or more simulations 9746 to obtain additional information 9750. For example, additional information 9750 may include one or more operating parameters that may be used to operate in situ process 9701 with a desired operating parameter. In one embodiment, method 9450 illustrated in FIG. 29 may be used to determine operating parameters to achieve a desired parameter. The operating parameters may then be used to operate in situ process 9701.

An in situ process for treating a formation may include freating a selected section of the formation with a minimum average overburden thickness. The minimum average overburden thickness may depend on a type of hydrocarbon resource and geological formation surrounding the hydrocarbon resource. An overburden may, in some embodiments, be substantially impermeable so that fluids produced in the selected section are inhibited from passing to the ground surface through the overburden. A minimum overburden thickness may be determined as the minimum overburden needed to inhibit the escape of fluids produced in the formation and to inhibit breakthrough to the surface due to increased pressure within the formation during in the situ conversion process. Determining this minimum overburden thickness may be dependent on, for example, composition of the overburden, maximum pressure to be reached in the formation during the in situ conversion process, permeability of the overburden, composition of fluids produced in the formation, and/or temperatures in the formation or overburden. A ratio of overburden thickness to hydrocarbon resource thickness may be used during selection of resources to produce using an in situ thermal conversion process.

Selected factors may be used to determine a minimum overburden thickness. These selected factors may include overall thickness of the overburden, lithology and/or rock properties of the overburden, earth sfresses, expected extent of subsidence and/or reservoir compaction, a pressure of a process to be used in the formation, and extent and connectivity of natural fracture systems surrounding the formation. FIG. 49 illustrates a flow chart of a computer-implemented method for determining a selected overburden thickness. Selected section properties 6366 may be input into computational system 6250. Properties of the selected section may include type of formation, density, permeability, porosity, earth sfresses, etc. Selected section properties 6366 may be used by a software executable to determine minimum overburden thickness 6368 for the selected section. The software executable may be, for example, ABAQUS. The software executable may incoφorate selected factors. Computational system 6250 may also run a simulation to determine minimum overburden thickness 6368. The minimum overburden thickness may be determined so that fractures that allow formation fluid to pass to the ground surface will not form within the overburden during an in situ process. A formation may be selected for freatment by computational system 6250 based on properties of the formation and/or properties of the overburden as determined herein. Overburden properties 6364 may also be input into computational system 6250. Properties of the overburden may include a type of material in the overburden, density of the overburden, permeability of the overburden, earth sfresses, etc. Computational system 6250 may also be used to determine operating conditions and/or confrol operating conditions for an in situ process of freating a formation. Heating of the formation may be monitored during an in situ conversion process. Monitoring heating of a selected section may include continuously monitoring acoustical data associated with the selected section. Acoustical data may include seismic data or any acoustical data that may be measured, for example, using geophones, hydrophones, or other acoustical sensors. In an embodiment, a continuous acoustical monitoring system can be used to monitor (e.g., intermittently or constantly) the formation. The formation can be monitored (e.g., using geophones at 2 kilohertz, recording measurements every 1/8 of a millisecond) for undesirable formation conditions. In an embodiment, a continuous acoustical monitoring system may be obtained from Oyo Instruments (Houston, TX). Acoustical data may be acquired by recording information using underground acoustical sensors located within and/or proximate a freated formation area. Acoustical data may be used to deteπnine a type and/or location of fractures developing within the selected section. Acoustical data may be input into a computational system to determine the type and/or location of fractures. Also, heating profiles of the formation or selected section may be determined by the computational system using the acoustical data. The computational system may run a software executable to process the acoustical data. The computational system may be used to determine a set of operating conditions for freating the formation in situ. The computational system may also be used to control the set of operating conditions for freating the formation in situ based on the acoustical data. Other properties, such as a temperature of the formation, may also be input into the computational system.

An in situ conversion process may be confrolled by using some of the production wells as injection wells for injection of steam and/or other process modifying fluids (e.g., hydrogen, which may affect a product composition through in situ hydrogenation).

In certain embodiments, it may be possible to use well technologies that may operate at high temperatures. These technologies may include both sensors and confrol mechanisms. The heat injection profiles and hydrocarbon vapor production may be adjusted on a more discrete basis. It may be possible to adjust heat profiles and production on a bed-by-bed basis or in meter-by-meter increments. This may allow the ICP to compensate, for example, for different thermal properties and or organic contents in an interbedded lithology. Thus, cold and hot spots may be inhibited from forming, the formation may not be oveφressurized, and/or the integrity of the formation may not be highly stressed, which could cause deformations and/or damage to wellbore integrity. FIGS. 50 and 51 illustrate schematic diagrams of apian view and a cross-sectional representation, respectively, of a zone being freated using an in situ conversion process (ICP). The ICP may cause microseismic failures, or fractures, within the freatment zone from which a seismic wave may be emitted. Treatment zone 6400 may be heated using heat provided from heater 6410 placed in heater well 6402. Pressure in treatment zone 6400 may be controlled by producing some formation fluid through heater wells 6402 and/or production wells. Heat from heater 6410 may cause failure 6406 in a portion of the foπnation proximate freatment zone 6400. Failure 6406 may be a localized rock failure within a rock volume of the foπnation. Failure 6406 may be an instantaneous failure. Failure 6406 tends to produce seismic disturbance 6408. Seismic disturbance 6408 may be an elastic or microseismic disturbance that propagates as a body wave in the formation surrounding the failure. Magnitude and direction of seismic disturbance as measured by sensors may indicate a type of macro-scale failure that occurs within the formation and/or treatment zone 6400. For example, seismic disturbance 6408 may be evaluated to indicate a location, orientation, and/or extent of one or more macro-scale failures that occurred in the formation due to heat freatment of the freatment zone 6400.

Seismic disturbance 6408 from one or more failures 6406 may be detected with one or more sensors 6412. Sensor 6412 may be a geophone, hydrophone, accelerometer, and/or other seismic sensing device. Sensors 6412 may be placed in monitoring well 6404 or monitoring wells. Monitoring wells 6404 may be placed in the formation proximate heater well 6402 and treatment zone 6400. In certain embodiments, three monitoring wells 6404 are placed in the foπnation such that a location of failure 6406 may be triangulated using sensors 6412 in each monitoring well.

In an in situ conversion process embodiment, sensors 6412 may measure a signal of seismic disturbance 6408. The signal may include a wave or set of waves emitted from failure 6406. The signals may be used to determine an approximate location of failure 6406. An approximate time at which failure 6406 occurred, causing seismic disturbance 6408, may also be determined from the signal. This approximate location and approximate time of failure 6406 may be used to detennine if failure 6406 can propagate into an undesired zone of the formation. The undesired zone may include a water aquifer, a zone of the formation undesired for freatment, overburden 540 of the formation, and/or underburden 6416 of the foπnation. An aquifer may also lie above overburden 540 or below underburden 6416. Overburden 540 and/or underburden 6416 may include one or more rock layers that can be fractured and allow formation fluid to undesirably escape from the in situ conversion process. Sensors 6412 may be used to monitor a progression of failure 6406 (i.e., an increase in extent of the failure) over a period of time.

In certain embodhnents, a location of failure 6406 may be more precisely determined using a vertical disfribution of sensors 6412 along each monitoring well 6404. The vertical disfribution of sensors 6412 may also include at least one sensor above overburden 540 and/or below underburden 6416. The sensors above overburden

540 and/or below underburden 6416 may be used to monitor penetration (or an absence of penetration) of a failure through the overburden or underburden.

If failure 6406 may propagate into an undesired zone of the formation, a parameter for treatment of treatment zone 6400 confrolled through heater well 6402 may be altered to inhibit propagation of the failure. The parameter of freatment may include a pressure in freatment zone 6400, a volume (or flow rate) of fluids injected into the freatment zone or removed from the freatment zone, or a heat input rate from heater 6410 into the treatment zone.

FIG. 52 illustrates a flow chart of an embodiment of a method used to monitor freatment of a formation. Treatment plan 6420 may be provided for a freatment zone (e.g., freatment zone 6400 in FIGS. 50 and 51). Parameters 6422 for treatment plan 6420 may include, but are not limited to, pressure in the freatment zone, heating rate of the treatment zone, and average temperature in the freatment zone. Treatment parameters 6422 may be confrolled to treat through heat sources, production wells, and/or injection wells. A failure or failures may occur during freatment of the treatment zone for a given set of parameters. Seismic disturbances that indicate a failure may be detected by sensors placed in one or more monitoring wells in monitoring step 6424. The seismic disturbances may be used to determine a location, a time, and/or extent of the one or more failures in determination step 6426. Determination step 6426 may include imaging the seismic disturbances to determine a spatial location of a failure or failures and/or a time at which the failure or failures occurred. The location, time, and/or extent of the failure or failures may be processed to determine if freatment parameters 6422 may be altered to inhibit the propagation of a failure or failures into an undesired zone of the formation in inteφretation step 6428. In an in situ conversion process embodiment, a recording system may be used to continuously monitor signals from sensors placed in a formation. The recording system may continuously record the signals from sensors. The recording system may save the signals as data. The data may be permanently saved by the recording system. The recording system may simultaneously monitor signals from sensors. The signals may be monitored at a selected sampling rate (e.g., about once every 0.25 milliseconds). In some embodiments, two recording systems may be used to continuously monitor signals from sensors. A recording system may be used to record each signal from the sensors at the selected sampling rate for a desired time period. A confroller may be used when the recording system is used to monitor a signal. The confroller may be a computational system or computer. In an embodiment using two or more recording systems, the confroller may direct which recording system is used for a selected time period. The confroller may include a global positioning satellite (GPS) clock. The GPS clock may be used to provide a specific time for a recording system to begin monitoring signals (e.g., a trigger time) and a time period for the monitoring of signals. The controller may provide the specific time for the recording system to begin monitoring signals to a trigger box. The trigger box may be used to supply a trigger pulse to a recording system to begin monitoring signals.

A storage device may be used to record signals monitored by a recording system. The storage device may include a tape drive (e.g., a high-speed high-capacity tape drive) or any device capable of recording relatively large amounts of data at very short time intervals. In an embodiment using two recording systems, the storage device may receive data from the first recording system while the second recording system is monitoring signals from one or more sensors, or vice versa. This enables continuous data coverage so that all or substantially all microseismic events that occur will be detected. In some embodiments, heat progress through the formation may be monitored by measuring microseismic events caused by heating of various portions of the formation . In some embodiments, monitoring heating of a selected section of the formation may include electromagnetic monitoring of the selected section. Electromagnetic monitoring may include measuring a resistivity between at least two electrodes within the selected section. Data from electromagnetic monitoring may be input into a computational system and processed as described above.

A relationship between a change in characteristics of formation fluids with temperature in an in situ conversion process may be developed. The relationship may relate the change in characteristics with temperature to a heating rate and temperature for the formation. The relationship may be used to select a temperature which can be used in an isothermal experiment to determine a quantity and quality of a product produced by ICP in a formation without having to use one or more slow heating rate experiments. The isothermal experiment may be conducted in a laboratory or similar test facility. The isothermal experiment may be conducted much more quickly than experiments that slowly increase temperatures. An appropriate selection of a temperature for an isothermal experiment may be significant for prediction of characteristics of formation fluids. The experiment may include conducting an experiment on a sample of a formation. The experiment may include producing hydrocarbons from the sample.

For example, first order kinetics may be generally assumed for a reaction producing a product. Assuming first order kinetics and a linear heating rate, the change in concentration (a characteristic of a formation fluid being the concentration of a component) with temperature may be defined by the equation:

(32) dC/dT = -(k₀/m) x e^("E/RT)C ;

in which C is the concentration of a component, T is temperature in Kelvin, k₀ is the frequency factor of the reaction, m is the heating rate, E is the activation energy, and R is the gas constant.

EQN. 32 may be solved for a concentration at a selected temperature based on an initial concentration at a first temperature. The result is the equation:

in which C is the concenfration of a component at temperature rand C₀ is an initial concenfration of the component. Substituting EQN. 33 into EQN. 32 yields the expression:

_E_ dC koCo (-

(34) = ^■ x e RT mE dT m

which relates the change in concenfration C with temperature T for first-order kinetics and a linear heating rate.

Typically, in application of an ICP to a relatively low permeability formation containing heavy hydrocarbons, the heating rate may not be linear due to temperature limitations in heat sources and/or in heater wells. For example, heating may be reduced at higher temperatures so that a temperature in a heater well is maintained below a desired temperature (e.g., about 650° C). This may provide a non-linear heating rate that is relatively slower than a linear heating rate. The non-linear heating rate may be expressed as:

(35) J = m x t" ;

in which t is time and n is an exponential decay term for the heating rate, and in which n is typically less than 1 (e.g., about 0.75).

Using ΕQN. 35 in a first-order kinetics equation gives the expression:

which is a generalization of ΕQN. 33 for a non-linear heating rate.

An isothermal experiment may be conducted at a selected temperature to determine a quality and a quantity of a product produced using an ICP in a foπnation. The selected temperature may be a temperature at which half the initial concenfration, C₀, has been converted into product (i.e., C/C₀ = Vf). ΕQN. 36 may be solved for this value, giving the expression:

in which Tm is the selected temperature which coπesponds to converting half of the initial concenfration into product. Alternatively, an equation such as ΕQN. 34 may be used with a heating rate that approximates a heating rate expected in a temperature range where in situ conversion of hydrocarbons is expected. ΕQN. 37 may be used to determine a selected temperature based on a heating rate that may be expected for ICP in at least a portion of a formation. The heating rate may be selected based on parameters such as, but not limited to, heater well spacing, heater well installation economics (e.g., drilling costs, heater costs, etc.), and maximum heater output. At least one property of the formation may also be used to determine the heating rate. At least one property may include, but is not limited to, a type of formation, foπnation heat capacity, formation depth, permeability, theπnal conductivity, and total organic content. The selected temperature may be used in an isothermal experiment to determine product quality and/or quantity. The product quality and/or quantity may also be determined at a selected pressure in the isothermal experiment. The selected pressure may be a pressure used for an ICP. The selected pressure may be adjusted to produce a desired product quality and/or quantity in the isothermal experiment. The adjusted selected pressure may be used in an ICP to produce the desired product quality and/or quality from the formation. In some embodiments, EQN. 37 may be used to determine a heating rate (m or m") used in an ICP based on results from an isothermal experiment at a selected temperature (7_//2). For example, isothermal experiments may be performed at a variety of temperatures. The selected temperature may be chosen as a temperature at which a product of desired quality and or quantity is produced. The selected temperature may be used in EQN. 37 to determine the desired heating rate during ICP to produce a product of the desired quality and/or quantity. Alternatively, if a heating rate is estimated, at least in a first instance, by optimizing costs and incomes such as heater well costs and the time required to produce hydrocarbons, then constants for an equation such as EQN. 37 may be determined by data from an experiment when the temperature is raised at a constant rate. With the constants of EQN. 37 estimated and heating rates estimated, a temperature for isothermal experiments may be calculated. Isothermal experiments may be performed much more quickly than experiments at anticipated heating rates (i.e., relatively slow heating rates). Thus, the effect of variables (such as pressure) and the effect of applying additional gases (such as, for example, steam and hydrogen) may be determined by relatively fast experiments.

In an embodiment, a relatively low permeability formation containing heavy hydrocarbons may be heated with a natural distributed combustor system located in the formation. The generated heat may be allowed to fransfer to a selected section of the formation. A natural distributed combustor may oxidize hydrocarbons in a formation in the vicinity of a wellbore to provide heat to a selected section of the formation.

A temperature sufficient to support oxidation may be at least about 200 °C or 250 °C. The temperature sufficient to support oxidation will tend to vary depending on many factors (e.g., a composition of the hydrocarbons in the relatively low permeability formation containing heavy hydrocarbons, water content of the formation, and/or type and amount of oxidant). Some water may be removed from the formation prior to heating. For example, the water may be pumped from the formation by dewatering wells. The heated portion of the formation may be near or substantially adjacent to an opening in the relatively low permeability formation containing heavy hydrocarbons. The opening in the formation may be a heater well formed in the formation. The heated portion of the relatively low permeability formation containing heavy hydrocarbons may extend radially from the opening to a width of about 0.3 m to about 1.2 m. The width, however, may also be less than about 0.9 m. A width of the heated portion may vary with time. In certain embodiments, the variance depends on factors including a width of formation necessary to generate sufficient heat during oxidation of carbon to maintain the oxidation reaction without providing heat from an additional heat source. After the portion of the formation reaches a temperature sufficient to support oxidation, an oxidizing fluid may be provided into the opening to oxidize at least a portion of the hydrocarbons at a reaction zone or a heat source zone within the formation. Oxidation of the hydrocarbons will generate heat at the reaction zone. The generated heat will in most embodiments fransfer from the reaction zone to a pyrolysis zone in the foπnation. In certain embodiments, the generated heat fransfers at a rate between about 650 watts per meter and 1650 watts per meter as measured along a depth of the reaction zone. Upon oxidation of at least some of the hydrocarbons in the formation, energy supplied to the heater for initially heating the foπnation to the temperature sufficient to support oxidation may be reduced or turned off. Energy input costs may be significantly reduced using natural disfributed combustors, thereby providing a significantly more efficient system for heating the foπnation. In an embodiment, a conduit may be disposed in the opening to provide oxidizing fluid into the opening.

The conduit may have flow orifices or other flow control mechanisms (i.e., slits, venturi meters, valves, etc.) to allow the oxidizing fluid to enter the opening. The term "orifices" includes openings having a wide variety of cross-sectional shapes including, but not limited to, circles, ovals, squares, rectangles, triangles, slits, or other regular or irregular shapes. The flow orifices may be critical flow orifices in some embodiments. The flow orifices may provide a substantially constant flow of oxidizing fluid into the opening, regardless of the pressure in the opening.

In some embodiments, the number of flow orifices may be limited by the diameter of the orifices and a desired spacing between orifices for a length of the conduit. For example, as the diameter of the orifices decreases, the number of flow orifices may increase, and vice versa. In addition, as the desired spacing increases, the number of flow orifices may decrease, and vice versa. The diameter of the orifices may be determined by a pressure in the conduit and/or a desired flow rate through the orifices. For example, for a flow rate of about 1.7 standard cubic meters per minute and a pressure of about 7 bars absolute, an orifice diameter may be about 1.3 mm with a spacing between orifices of about 2 m. Smaller diameter orifices may plug more readily than larger diameter orifices. Orifices may plug for a variety of reasons. The reasons may include, but are not limited to, contaminants in the fluid flowing in the conduit and/or solid deposition within or proximate the orifices.

In some embodiments, the number and diameter of the orifices are chosen such that a more even or nearly uniform heating profile will be obtained along a depth of the opening in the formation. A depth of a heated formation that is intended to have an approximately uniform heating profile may be greater than about 300 m, or even greater than about 600 m. Such a depth may vary, however, depending on, for example, a type of formation to be heated and/or a desired production rate.

In some embodiments, flow orifices may be disposed in a helical pattern around the conduit within the opening. The flow orifices may be spaced by about 0.3 m to about 3 m between orifices in the helical pattern. In some embodhnents, the spacing may be about 1 m to about 2 m or, for example, about 1.5 m.

The flow of oxidizing fluid into the opening may be confrolled such that a rate of oxidation at the reaction zone is controlled. Transfer of heat between incoming oxidant and outgoing oxidation products may heat the oxidizing fluid. The fransfer of heat may also maintain the conduit below a maximum operatmg temperature of the conduit.

FIG. 53 illustrates an embodiment of a natural disfributed combustor that may heat a relatively low permeability formation containing heavy hydrocarbons. Conduit 512 may be placed into opening 514 in hydrocarbon layer 516. Conduit 512 may have inner conduit 513. Oxidizing fluid source 508 may provide oxidizing fluid 517 into inner conduit 513. Inner conduit 513 may have critical flow orifices 515 along its length. Critical flow orifices 515 may be disposed in a helical pattern (or any other pattern) along a length of inner conduit 513 in opening 514. For example, critical flow orifices 515 may be arranged in a helical pattern with a distance of about 1 m to about 2.5 m between adjacent orifices. Inner conduit 513 may be sealed at the bottom. Oxidizing fluid 517 may be provided into opening 514 through critical flow orifices 515 of inner conduit 513. Critical flow orifices 515 may be designed such that substantially the same flow rate of oxidizing fluid 517 may be provided through each critical flow orifice. Critical flow orifices 515 may also provide substantially uniform flow of oxidizing fluid 517 along a length of conduit 512. Such flow may provide substantially uniform heating of hydrocarbon layer 516 along the length of conduit 512. Packing material 542 may enclose conduit 512 in overburden 540 of the formation. Packing material 542 may inhibit flow of fluids from opening 514 to surface 550. Packing material 542 may include any material that inhibits flow of fluids to surface 550 such as cement or consolidated sand or gravel. A conduit or opening through the packing may provide a path for oxidation products to reach the surface.

Oxidation products 519 typically enter conduit 512 from opening 514. Oxidation products 519 may include carbon dioxide, oxides of nitrogen, oxides of sulfur, carbon monoxide, and/or other products resulting from a reaction of oxygen with hydrocarbons and/or carbon. Oxidation products 519 may be removed through conduit 512 to surface 550. Oxidation product 519 may flow along a face of reaction zone 524 in opening 514 until proximate an upper end of opening 514 where oxidation product 519 may flow into conduit 512. Oxidation products 519 may also be removed through one or more conduits disposed in opening 514 and/or in hydrocarbon layer 516. For example, oxidation products 519 may be removed through a second conduit disposed in opening

514. Removing oxidation products 519 through a conduit may inhibit oxidation products 519 from flowing to a production well disposed in the formation. Critical flow orifices 515 may also inhibit oxidation products 519 from entering inner conduit 513.

A flow rate of oxidation product 519 may be balanced with a flow rate of oxidizing fluid 517 such that a substantially constant pressure is maintained within opening 514. For a 100 m length of heated section, a flow rate of oxidizing fluid may be between about 0.5 standard cubic meters per minute to about 5 standard cubic meters per minute, or about 1.0 standard cubic meters per minute to about 4.0 standard cubic meters per minute, or, for example, about 1.7 standard cubic meters per minute. A flow rate of oxidizing fluid into the formation may be incrementally increased during use to accommodate expansion of the reaction zone. A pressure in the opening may be, for example, about 8 bars absolute. Oxidizing fluid 517. may oxidize at least a portion of the hydrocarbons in heated portion 518 of hydrocarbon layer 516 at reaction zone 524. Heated portion 518 may have been initially heated to a temperature sufficient to support oxidation by an electric heater, as shown in FIG. 54. In some embodiments, an electric heater may be placed inside or strapped to the outside of conduit 513.

In certain embodiments, controlling the pressure within opening 514 may inhibit oxidation product and/or oxidation fluids from flowing into the pyrolysis zone of the formation. In some instances, pressure within opening

514 may be confrolled to be slightly greater than a pressure in the formation to allow fluid within the opening to pass into the formation but to inhibit formation of a pressure gradient that allows the transport of the fluid a significant distance into the formation.

Although the heat from the oxidation is transfened to the formation, oxidation product 519 (and excess oxidation fluid such as air) may be inhibited from flowing through the formation and/or to a production well within the formation. Instead, oxidation product 519 and/or excess oxidation fluid may be removed from the formation. In some embodiments, the oxidation product and/or excess oxidation fluid are removed through conduit 512. Removing oxidation product and/or excess oxidation fluid may allow heat from oxidation reactions to transfer to the pyrolysis zone without significant amounts of oxidation product and or excess oxidation fluid entering the pyrolysis zone. In certain embodiments, some pyrolysis product near reaction zone 524 may be oxidized in reaction zone 524 in addition to the carbon. Oxidation of the pyrolysis product in reaction zone 524 may provide additional heating of hydrocarbon layer 516. When oxidation of pyrolysis product occurs, oxidation product from the oxidation of pyrolysis product may be removed near the reaction zone (e.g., through a conduit such as conduit 512). Removing the oxidation product of a pyrolysis product may inhibit contamination of other pyrolysis products in the formation with oxidation product.

Conduit 512 may, in some embodiments, remove oxidation product 519 from opening 514 in hydrocarbon layer 516. Oxidizing fluid 517 in inner conduit 513 may be heated by heat exchange with conduit 512. A portion of heat fransfer between conduit 512 and inner conduit 513 may occur in overburden section 540. Oxidation product 519 may be cooled by fransfemng heat to oxidizing fluid 517. Heating the incoming oxidizing fluid 517 tends to improve the efficiency of heating the formation.

Oxidizing fluid 517 may transport through reaction zone 524, or heat source zone, by gas phase diffusion and/or convection. Diffusion of oxidizing fluid 517 through reaction zone 524 may be more efficient at the relatively high temperatures of oxidation. Diffusion of oxidizing fluid 517 may inhibit development of localized overheating and fingering in the formation. Diffusion of oxidizing fluid 517 through hydrocarbon layer 516 is generally a mass fransfer process. In the absence of an external force, a rate of diffusion for oxidizing fluid 517 may depend upon concentration, pressure, and/or temperature of oxidizing fluid 517 within hydrocarbon layer 516. The rate of diffusion may also depend upon the diffusion coefficient of oxidizing fluid 517 through hydrocarbon layer 516. The diffusion coefficient may be determined by measurement or calculation based on the kinetic theory of gases. In general, random motion of oxidizing fluid 517 may transfer the oxidizing fluid tiirough hydrocarbon layer 516 from a region of high concenfration to a region of low concenfration.

With time, reaction zone 524 may slowly extend radially to greater diameters from opening 514 as hydrocarbons are oxidized. Reaction zone 524 may, in many embodiments, maintain a relatively constant width. For example, reaction zone 524 may extend radially at a rate of less than about 0.91 m per year for a relatively low permeability foπnation containing heavy hydrocarbons. Reaction zone 524 may extend at slower rates for richer formations and at faster rates for leaner formations with more inorganic material since more hydrocarbons per volume are available for combustion in the hydrocarbon rich formations.

A flow rate of oxidizing fluid 517 into opening 514 may be increased as a diameter of reaction zone 524 increases to maintain the rate of oxidation per unit volume at a substantially steady state. Thus, a temperature within reaction zone 524 may be maintained substantially constant in some embodiments. The temperature within reaction zone 524 may be between about 650 °C to about 900 °C or, for example, about 760 °C. The temperature may be maintained below a temperature that results in production of oxides of nifrogen (NO_x). Oxides of nifrogen are often produced at temperatures above about 1200 °C.

The temperature within reaction zone 524 may be varied to achieve a desired heating rate of selected section 526. The temperature within reaction zone 524 may be increased or decreased by increasing or decreasing a flow rate of oxidizing fluid 517 into opening 514. A temperature of conduit 512, inner conduit 513, and/or any metallurgical materials within opening 514 may be controlled to not exceed a maximum operating temperature of the material. Maintaining the temperature below the maximum operating temperature of a material may inhibit excessive deformation and/or corrosion of the material. An increase in the diameter of reaction zone 524 may allow for relatively rapid heating of hydrocarbon layer 516. As the diameter of reaction zone 524 increases, an amount of heat generated per time in reaction zone 524 may also increase. Increasing an amount of heat generated per time in the reaction zone will in many instances increase a heating rate of hydrocarbon layer 516 over a period of time, even without increasing the temperature in the reaction zone or the temperature at conduit 513. Thus, increased heating may be achieved over time without installing additional heat sources and without increasing temperatures adjacent to wellbores. In some embodiments, the heating rates may be increased while allowing the temperatures to decrease (allowing temperatures to decrease may often lengthen the life of the equipment used).

By utilizing the carbon in the foπnation as a fuel, the natural disfributed combustor may save significantly on energy costs. Thus, an economical process may be provided for heating formations that would otherwise be economically unsuitable for heating by other types of heat sources. Using natural disfributed combustors may allow fewer heaters to be inserted into a formation for heating a desired volume of the formation as compared to heating the formation using other types of heat sources. Heating a formation using natural disfributed combustors may allow for reduced equipment costs as compared to heating the formation using other types of heat sources.

Heat generated at reaction zone 524 may fransfer by thermal conduction to selected section 526 of hydrocarbon layer 516. In addition, generated heat may fransfer from a reaction zone to the selected section to a lesser extent by convective heat fransfer. Selected section 526, sometimes referred as the "pyrolysis zone," may be substantially adjacent to reaction zone 524. Removing oxidation product (and excess oxidation fluid such as air) may allow the pyrolysis zone to receive heat from the reaction zone without being exposed to oxidation product, or oxidants, that are in the reaction zone. Oxidation product and/or oxidation fluids may cause the formation of undesirable products if they are present in the pyrolysis zone. Removing oxidation product and/or oxidation fluids may allow a reducing environment to be maintained in the pyrolysis zone.

In an in situ conversion process embodiment, natural disfributed combustors may be used to heat a formation. FIG. 53 depicts an embodiment of a natural disfributed combustor. A flow of oxidizing fluid 517 may be confrolled along a length of opening 514 or reaction zone 524. Opening 514 may be referred to as an "elongated opening," such that reaction zone 524 and opening 514 may have a common boundary along a determined length of the opening. The flow of oxidizing fluid may be confrolled using one or more orifices 515 (the orifices may be critical flow orifices). The flow of oxidizing fluid may be confrolled by a diameter of orifices 515, a number of orifices 515, and or by a pressure within inner conduit 513 (a pressure behind orifices 515). Controlling the flow of oxidizing fluid may confrol a temperature at a face of reaction zone 524 in opening 514. For example, an increased flow of oxidizing fluid 517 will tend to increase a temperature at the face of reaction zone 524. Increasing the flow of oxidizing fluid into the opening tends to increase a rate of oxidation of hydrocarbons in the reaction zone. Since the oxidation of hydrocarbons is an exothermic reaction, increasing the rate of oxidation tends to increase the temperature in the reaction zone.

In certain natural disfributed combustor embodiments, the flow of oxidizing fluid 517 may be varied along the length of inner conduit 513 (e.g., using critical flow orifices 515) such that the temperature at the face of reaction zone 524 is variable. The temperature at the face of reaction zone 524, or within opening 514, may be varied to confrol a rate of heat transfer within reaction zone 524 and/or a heating rate within selected section 526. Increasing the temperature at the face of reaction zone 524 may increase the heating rate within selected section 526. A property of oxidation product 519 may be monitored (e.g., oxygen content, nifrogen content, temperature, etc.). The property of oxidation product 519 may be monitored and used to confrol input properties (e.g., oxidizing fluid input) into the natural disfributed combustor. A rate of diffusion of oxidizing fluid 517 through reaction zone 524 may vary with a temperature of and adjacent to the reaction zone. In general, the higher the temperature, the faster a gas will diffuse because of the increased energy in the gas. A temperature within the opening may be assessed (e.g., measured by a thermocouple) and related to a temperature of the reaction zone. The temperature within the opening may be confrolled by controlling the flow of oxidizing fluid into the opening from inner conduit 513. For example, increasing a flow of oxidizing fluid into the opening may increase the temperature within the opening. Decreasing the flow of oxidizing fluid into the opening may decrease the temperature within the opening. In an embodiment, a flow of oxidizing fluid may be increased until a selected temperature below the metallurgical temperature limits of the equipment being used is reached. For example, the flow of oxidizing fluid can be increased until a working temperature limit of a metal used in a conduit placed in the opening is reached. The temperature of the metal may be directly measured using a thermocouple or other temperature measurement device.

In a natural disfributed combustor embodiment, production of carbon dioxide within reaction zone 524 may be inhibited. An increase in a concenfration of hydrogen in the reaction zone may inhibit production of carbon dioxide within the reaction zone. The concenfration of hydrogen may be increased by transferring hydrogen into the reaction zone. In an embodiment, hydrogen may be transfened into the reaction zone from selected section 526.

Hydrogen may be produced during the pyrolysis of hydrocarbons in the selected section. Hydrogen may fransfer by diffusion and/or convection into the reaction zone from the selected section. In addition, additional hydrogen may be provided into opening 514 or another opening in the formation through a conduit placed in the opening. The additional hydrogen may fransfer into the reaction zone from opening 514. In some natural disfributed combustor embodiments, heat may be supplied to the formation from a second heat source in the wellbore of the natural disfributed combustor. For example, an electric heater (e.g., an insulated conductor heater or a conductor-in-conduit heater) used to preheat a portion of the formation may also be used to provide heat to the formation along with heat from the natural distributed combustor. In addition, an additional electric heater may be placed in an opening in the formation to provide additional heat to the formation. The electric heater may be used to provide heat to the formation so that heat provided from the combination of the electric heater and the natural distributed combustor is maintained at a constant heat input rate. Heat input into the formation from the electric heater may be varied as heat input from the natural disfributed combustor varies, or vice versa. Providing heat from more than one type of heat source may allow for substantially uniform heating of the formation. In certain in situ conversion process embodiments, up to 10%, 25%, or 50% of the total heat input into the formation may be provided from electric heaters. A percentage of heat input into the formation from electric heaters may be varied depending on, for example, electricity cost, natural disfributed combustor heat input, etc. Heat from electric heaters can be used to compensate for low heat output from natural disfributed combustors to maintain a substantially constant heating rate in the formation. If electrical costs rise, more heat may be generated from natural distributed combustors to reduce the amount of heat supplied by electric heaters. In some embodiments, heat from electric heaters may vary due to the source of electricity (e.g., solar or wind power). In such an embodiments, more or less heat may be provided by natural disfributed combustors to compensate for changes in electrical heat input.

In a heat source embodiment, an electric heater may be used to inhibit a natural disfributed combustor from "burning out." A natural disfributed combustor may "bum out" if a portion of the formation cools below a temperature sufficient to support combustion. Additional heat from the electric heater may be needed to provide heat to the portion and/or another portion of the formation to heat a portion to a temperature sufficient to support oxidation of hydrocarbons and maintain the natural disfributed combustor heating process.

In some natural disfributed combustor embodiments, electric heaters may be used to provide more heat to a formation proximate an upper portion and/or a lower portion of the formation. Using the additional heat from the electric heaters may compensate for heat losses in the upper and/or lower portions of the formation. Providing additional heat with the electric heaters proximate the upper and/or lower portions may produce more uniform heating of the formation. In some embodiments, electric heaters may be used for similar puφoses (e.g., provide heat at upper and/or lower portions, provide supplemental heat, provide heat to maintain a minimum combustion temperature, etc.) in combination with other types of fueled heater, such as flameless disfributed combustors or downhole combustors.

In some in situ conversion process embodiments, exhaust fluids from a fueled heater (e.g., a natural disfributed combustor, or downhole combustor) may be used in an air compressor located at a surface of the formation proximate an opening used for the fueled heater. The exhaust fluids may be used to drive the air compressor and reduce a cost associated with compressing air for use in the fueled heater. Electricity may also be generated using the exhaust fluids in a turbine or similar device. In some embodiments, fluids (e.g., oxidizing fluid and/or fuel) used for one or more fueled heaters may be provided using a compressor or a series of compressors. A compressor may provide oxidizing fluid and/or fuel for one heater or more than one heater. In addition, oxidizing fluid and/or fuel may be provided from a centralized facility for use in a single heater or more than one heater. Pyrolysis of hydrocarbons, or other heat-controlled processes, may take place in heated selected section 526. Selected section 526 may be at a temperature between about 270 °C and about 400 °C for pyrolysis. The temperature of selected section 526 may be increased by heat transfer from reaction zone 524.

A temperature within opening 514 may be monitored with a thermocouple disposed in opening 514. Alternatively, a thermocouple may be coupled to conduit 512 and or disposed on a face of reaction zone 524. Power input or oxidant introduced into the formation may be confrolled based upon the monitored temperature to maintain the temperature in a selected range. The selected range may vary or be varied depending on location of the thermocouple, a desired heating rate of hydrocarbon layer 516, and other factors. If a temperature within opening 514 falls below a minimum temperature of the selected temperature range, the flow rate of oxidizing fluid 517 may be increased to increase combustion and thereby increase the temperature within opening 514.

In certain embodiments, one or more natural disfributed combustors may be placed along strike of a hydrocarbon layer and/or horizontally. Placing natural disfributed combustors along strike or horizontally may reduce pressure differentials along the heated length of the heat source. Reduced pressure differentials may make the temperature generated along a length of the heater more uniform and easier to control.

In some embodiments, presence of air or oxygen (0₂) in oxidation product 519 may be monitored. Alternatively, an amount of nifrogen, carbon monoxide, carbon dioxide, oxides of nifrogen, oxides of sulfur, etc. may be monitored in oxidation product 519. Monitoring the composition and or quantity of exhaust products (e.g., oxidation product 519) may be useful for heat balances, for process diagnostics, process confrol, etc.

FIG. 55 illustrates a cross-sectional representation of an embodiment of a natural distributed combustor having a second conduit 6200 disposed in opening 514 in hydrocarbon layer 516. Second conduit 6200 may be used to remove oxidation products from opening 514. Second conduit 6200 may have orifices 515 disposed along its length. In certain embodiments, oxidation products are removed from an upper region of opening 514 through orifices 515 disposed on second conduit 6200. Orifices 515 may be disposed along the length of conduit 6200 such that more oxidation products are removed from the upper region of opening 514.

In certain natural distributed combustor embodiments, orifices 515 on second conduit 6200 may face away from orifices 515 on conduit 513. The orientation may inhibit oxidizing fluid provided through conduit 513 from passing directly into second conduit 6200.

In some embodiments, conduit 6200 may have a higher density of orifices 515 (and/or relatively larger diameter orifices 515) towards the upper region of opening 514. The preferential removal of oxidation products from the upper region of opening 514 may produce a substantially uniform concenfration of oxidizing fluid along the length of opening 514. Oxidation products produced from reaction zone 524 tend to be more concentrated proximate the upper region of opening 514. The large concenfration of oxidation products 519 in the upper region of opening 514 tends to dilute a concenfration of oxidizing fluid 517 in the upper region. Removing a significant portion of the more concentrated oxidation products from the upper region of opening 514 may produce a more uniform concenfration of oxidizing fluid 517 throughout opening 514. Having a more uniform concenfration of oxidizing fluid throughout the opening may produce a more unifoπn driving force for oxidizing fluid to flow into reaction zone 524. The more uniform driving force may produce a more unifoπn oxidation rate within reaction zone 524, and thus produce a more uniform heating rate in selected section 526 and/or a more uniform temperature within opening 514.

In a natural disfributed combustor embodiment, the concentration of air and/or oxygen in the reaction zone may be confrolled. A more even disfribution of oxygen (or oxygen concenfration) in the reaction zone may be desirable. The rate of reaction may be confrolled as a function of the rate in which oxygen diffuses in the reaction zone. The rate of oxygen diffusion correlates to the oxygen concentration. Thus, controlling the oxygen concenfration in the reaction zone (e.g., by controlling oxidizing fluid flow rates, the removal of oxidation products along some or all of the length of the reaction zone, and/or the disfribution of the oxidizing fluid along some or all of the length of the reaction zone) may control oxygen diffusion in the reaction zone and thereby control the reaction rates in the reaction zone.

In the embodiment shown in FIG. 56, conductor 580 is placed in opening 514. Conductor 580 may extend from first end 6170 of opening 514 to second end 6172 of opening 514. In certain embodiments, conductor 580 may be placed in opening 514 within hydrocarbon layer 516. One or more low resistance sections 584 may be coupled to conductor 580 and used in overburden 540. In some embodiments, conductor 580 and/or low resistance sections 584 may extend above the surface of the formation.

In some heat source embodiments, an electric current may be applied to conductor 580 to increase a temperature of the conductor. Heat may transfer from conductor 580 to heated portion 518 of hydrocarbon layer 516. Heat may transfer from conductor 580 to heated portion 518 substantially by radiation. Some heat may also transfer by convection or conduction. Current may be provided to the conductor until a temperature within heated portion 518 is sufficient to support the oxidation of hydrocarbons within the heated portion. As shown in FIG. 56, oxidizing fluid may be provided into conductor 580 from oxidizing fluid source 508 at one or both ends 6170, 6172 of opening 514. A flow of the oxidizing fluid from conductor 580 into opening 514 may be controlled by orifices 515. The orifices may be critical flow orifices. The flow of oxidizing fluid from orifices 515 may be controlled by a diameter of the orifices, a number of orifices, and/or by a pressure within conductor 580 (i.e., a pressure behind the orifices). Reaction of oxidizing fluids with hydrocarbons in reaction zone 524 may generate heat. The rate of heat generated in reaction zone 524 may be confrolled by a flow rate of the oxidizing fluid into the fonnation, the rate of diffusion of oxidizing fluid through the reaction zone, and/or a removal rate of oxidation products from the formation. In an embodiment, oxidation products from the reaction of oxidizing fluid with hydrocarbons in the formation are removed through one or both ends of opening 514. In some embodhnents, a conduit may be placed in opening 514 to remove oxidation products. All or portions of the oxidation products may be recycled and/or reused in other oxidation type heaters (e.g., natural distributed combustors, surface burners, downhole combustors, etc.). Heat generated in reaction zone 524 may fransfer to a surrounding portion (e.g., selected section) of the formation. The fransfer of heat between reaction zone 524 and selected section may be substantially by conduction. In certain embodiments, the transferred heat may increase a temperature of the selected section above a minimum mobilization temperature of the hydrocarbons and/or a minimum pyrolysis temperature of the hydrocarbons.

In some heat source embodiments, a conduit may be placed in the opening. The opening may extend through the foπnation contacting a surface of the earth at a first location and a second location. Oxidizing fluid may be provided to the conduit from the oxidizing fluid source at the first location and/or the second location after a portion of the foπnation that has been heated to a temperature sufficient to support oxidation of hydrocarbons by the oxidizing fluid.

FIG. 57 illustrates an embodiment of a section of overburden with a natural disfributed combustor as described in FIG. 53. Overburden casing 541 may be disposed in overburden 540 of hydrocarbon layer 516. Overburden casing 541 may be suπounded by materials (e.g., an insulating material such as cement) that inhibit heating of overburden 540. Overburden casing 541 may be made of a metal material such as, but not limited to, carbon steel or 304 stainless steel.

Overburden casing 541 may be placed in reinforcing material 544 in overburden 540. Reinforcing material 544 may be, but is not limited to, cement, gravel, sand, and or concrete. Packing material 542 may be disposed between overburden casing 541 and opening 514 in the formation. Packing material 542 may be any substantially non-porous material (e.g., cement, concrete, grout, etc.). Packing material 542 may inhibit flow of fluid outside of conduit 512 and between opening 514 and surface 550. Inner conduit 513 may introduce fluid into opening 514 in hydrocarbon layer 516. Conduit 512 may remove combustion product (or excess oxidation fluid) from opening 514 in hydrocarbon layer 516. Diameter of conduit 512 may~be determined by an amount of the combustion product produced by oxidation in the natural distributed combustor. For example, a larger diameter may be required for a greater amount of exhaust product produced by the natural distributed combustor heater.

In some heat source embodiments, a portion of the foπnation adjacent to a wellbore may be heated to a temperature and at a heating rate that converts hydrocarbons to coke or char adjacent to the wellbore by a first heat source. Coke and or char may be formed at temperatures above about 400 °C. In the presence of an oxidizing fluid, the coke or char will oxidize. The wellbore may be used as a natural disfributed combustor subsequent to the formation of coke and/or char. Heat may be generated from the oxidation of coke or char.

FIG. 58 illustrates an embodiment of a natural disfributed combustor heater. Insulated conductor 562 may be coupled to conduit 532 and placed in opening 514 in hydrocarbon layer 516. Insulated conductor 562 may be disposed internal to conduit 532 (thereby allowing retrieval of insulated conductor 562), or, alternately, coupled to an external surface of conduit 532. Insulating material for the conductor may include, but is not limited to, mineral coating and/or ceramic coating. Conduit 532 may have critical flow orifices 515 disposed along its length within opening 514. Electrical cunent may be applied to insulated conductor 562 to generate radiant heat in opening 514. Conduit 532 may serve as a return for cunent. Insulated conductor 562 may heat portion 518 of hydrocarbon layer 516 to a temperature sufficient to support oxidation of hydrocarbons.

Oxidizing fluid source 508 may provide oxidizing fluid into conduit 532. Oxidizing fluid may be provided into opening 514 through critical flow orifices 515 in conduit 532. Oxidizing fluid may oxidize at least a portion of the hydrocarbon layer in reaction zone 524. A portion of heat generated at reaction zone 524 may transfer to selected section 526 by convection, radiation, and/or conduction. Oxidation product may be removed through a separate conduit placed in opening 514 or through opening 543 in overburden casing 541.

FIG. 59 illustrates an embodiment of a natural distributed combustor heater with an added fuel conduit. Fuel conduit 536 may be placed in opening 514. Fuel conduit may be placed adjacent to conduit 533 in certain embodiments. Fuel conduit 536 may have critical flow orifices 535 along a portion of the length within opening 514. Conduit 533 may have critical flow orifices 515 along a portion of the length within opening 514. The critical flow orifices 535, 515 may be positioned so that a fuel fluid provided through fuel conduit 536 and an oxidizing fluid provided through conduit 533 do not react to heat the fuel conduit and the conduit. Heat from reaction of the fuel fluid with oxidizing fluid may heat fuel conduit 536 and/or conduit 533 to a temperature sufficient to begin melting metallurgical materials in fuel conduit 536 and/or conduit 533 if the reaction takes place proximate fuel conduit 536 and or conduit 533. Critical flow orifices 535 on fuel conduit 536 and critical flow orifices 515 on conduit 533 may be positioned so that the fuel fluid and the oxidizing fluid do not react proximate the conduits. For example, conduits 536 and 533 may be positioned such that orifices that spiral around the conduits are oriented in opposite directions.

Reaction of the fuel fluid and the oxidizing fluid may produce heat. In some embodiments, the fuel fluid may be methane, ethane, hydrogen, or synthesis gas that is generated by in situ conversion in another part of the formation. The produced heat may heat portion 518 to a temperature sufficient to support oxidation of hydrocarbons. Upon heating of portion 518 to a temperature sufficient to support oxidation, a flow of fuel fluid into opening 514 may be turned down or may be turned off. In some embodiments, the supply of fuel may be continued throughout the heating of the formation.

The oxidizing fluid may oxidize at least a portion of the hydrocarbons at reaction zone 524. Generated heat may fransfer heat to selected section 526 by radiation, convection, and/or conduction. An oxidation product may be removed through a separate conduit placed in opening 514 or through opening 543 in overburden casing 541.

FIG. 54 illustrates an embodiment of a system that may heat a relatively low permeability formation containing heavy hydrocarbons. Electric heater 510 may be disposed within opening 514 in hydrocarbon layer 516. Opening 514 may be formed through overburden 540 into hydrocarbon layer 516. Opening 514 may be at least about 5 cm in diameter. Opening 514 may, as an example, have a diameter of about 13 cm. Electric heater 510 may heat at least portion 518 of hydrocarbon layer 516 to a temperature sufficient to support oxidation (e.g., about

260 °C). Portion 518 may have a width of about 1 m. An oxidizing fluid may be provided into the opening through conduit'512 or any other appropriate fluid transfer mechanism. Conduit 512 may have critical flow orifices 515 disposed along a length of the conduit.

Conduit 512 may be a pipe or tube that provides the oxidizing fluid into opening 514 from oxidizing fluid source 508. In an embodiment, a portion of conduit 512 that may be exposed to high temperatures is a stainless steel tube and a portion of the conduit that will not be exposed to high temperatures (i.e., a portion of the tube that extends through the overburden) is carbon steel. The oxidizing fluid may include air or any other oxygen containing fluid (e.g., hydrogen peroxide, oxides of nifrogen, ozone). Mixtures of oxidizing fluids may be used. An oxidizing fluid mixture may be a fluid including fifty percent oxygen and fifty percent nifrogen. In some embodiments, the oxidizing fluid may include compounds that release oxygen when heated, such as hydrogen peroxide. The oxidizing fluid may oxidize at least a portion of the hydrocarbons in the formation.

FIG. 60 illustrates an embodiment of a system that heats a relatively low permeability formation containing heavy hydrocarbons. Heat exchanger 520 may be disposed external to opening 514 in hydrocarbon layer 516. Opening 514 may be formed through overburden 540 into hydrocarbon layer 516. Heat exchanger 520 may provide heat from another surface process, or it may include a heater (e.g., an electric or combustion heater). Oxidizing fluid source 508 may provide an oxidizing fluid to heat exchanger 520. Heat exchanger 520 may heat an oxidizing fluid (e.g., above 200 °C or to a temperature sufficient to support oxidation of hydrocarbons). The heated oxidizing fluid may be provided into opening 514 through conduit 521. Conduit 521 may have critical flow orifices 515 disposed along a length of the conduit. The heated oxidizing fluid may heat, or at least contribute to the heating of, at least portion 518 of the formation to a temperature sufficient to support oxidation of hydrocarbons. The oxidizing fluid may oxidize at least a portion of the hydrocarbons in the formation. After temperature in the formation is sufficient to support oxidation, use of heat exchanger 520 may be reduced or phased out.

An embodiment of a natural distributed combustor may include a surface combustor (e.g., a flame-ignited heater). A fuel fluid may be oxidized in the combustor. The oxidized fuel fluid may be provided into an opening in the formation from the heater through a conduit. Oxidation products and unreacted fuel may return to the surface through another conduit. In some embodiments, one of the conduits may be placed within the other conduit. The oxidized fuel fluid may heat, or conttibute to the heating of, a portion of the formation to a temperature sufficient to support oxidation of hydrocarbons. Upon reaching the temperature sufficient to support oxidation, the oxidized fuel fluid may be replaced with an oxidizing fluid. The oxidizing fluid may oxidize at least a portion of the hydrocarbons at a reaction zone within the formation. An electric heater may heat a portion of the relatively low permeability formation containing heavy hydrocarbons to a temperature sufficient to support oxidation of hydrocarbons. The portion may be proximate or substantially adjacent to the opening in the formation. The portion may radially extend a width of less than approximately 1 m from the opening. An oxidizing fluid may be provided to the opening for oxidation of hydrocarbons. Oxidation of the hydrocarbons may heat the relatively low permeability formation containing heavy hydrocarbons in a process of natural disfributed combustion. Electrical cunent applied to the electric heater may subsequently be reduced or may be turned off. Natural disfributed combustion may be used in conjunction with an electric heater to provide a reduced input energy cost method to heat the relatively low permeability formation containing heavy hydrocarbons compared to using only an electric heater.

An insulated conductor heater may be a heater element of a heat source. In an embodiment of an insulated conductor heater, the insulated conductor heater is a mineral insulated cable or rod. An insulated conductor heater may be placed in an opening in a relatively low permeability formation containing heavy hydrocarbons. The insulated conductor heater may be placed in an uncased opening in the relatively low peπneability formation containing heavy hydrocarbons. Placing the heater in an uncased opening in the relatively low permeability formation containing heavy hydrocarbons may allow heat fransfer from the heater to the formation by radiation as well as conduction. Using an uncased opening may facilitate retrieval of the heater from the well, if necessary.

Using an uncased opening may significantly reduce heat source capital cost by eliminating a need for a portion of casing able to withstand high temperature conditions. In some heat source embodiments, an insulated conductor heater may be placed within a casing in the formation; may be cemented within the formation; or may be packed in an opening with sand, gravel, or other fill material. The insulated conductor heater may be supported on a support member positioned within the opening. The support member may be a cable, rod, or a conduit (e.g., a pipe). The support member may be made of a metal, ceramic, inorganic material, or combinations thereof. Portions of a support member may be exposed to formation fluids and heat during use, so the support member may be chemically resistant and thermally resistant.

Ties, spot welds, and/or other types of connectors may be used to couple the insulated conductor heater to the support member at various locations along a length of the insulated conductor heater. The support member may be attached to a wellhead at an upper surface of the formation. In an embodiment of an insulated conductor heater, the insulated conductor heater is designed to have sufficient structural sfrength so that a support member is not needed. The insulated conductor heater will in many instances have some flexibility to inhibit thermal expansion damage when heated or cooled.

In certain embodiments, insulated conductor heaters may be placed in wellbores without support members and or cenfralizers. An insulated conductor heater without support members and/or cenfralizers may have a suitable combination of temperature and conosion resistance, creep sfrength, length, thickness (diameter), and metallurgy that will inhibit failure of the insulated conductor during use. In some in situ conversion embodiments, insulated conductors that are heated to a working temperature of about 700 °C, are less than about 150 m in length, are made of 310 stainless steel may be used without support members. FIG. 61 depicts a perspective view of an end portion of an embodiment of insulated conductor heater 562.

An insulated conductor heater may have any desired cross-sectional shape, such as, but not limited to round (as shown in FIG. 61), friangular, ellipsoidal, rectangular, hexagonal, or irregular shape. An insulated conductor heater may include conductor 575, electrical insulation 576, and sheath 577. Conductor 575 may resistively heat when an electrical cunent passes through the conductor. An alternating or direct cunent may be used to heat conductor 575. In an embodiment, a 60-cycle AC cunent is used.

In some embodiments, electrical insulation 576 may inhibit cunent leakage and arcing to sheath 577. Electrical insulation 576 may also thermally conduct heat generated in conductor 575 to sheath 577. Sheath 577 may radiate or conduct heat to the formation. Insulated conductor heater 562 may be 1000 m or more in length. In an embodiment of an insulated conductor heater, insulated conductor heater 562 may have a length from about 15 m to about 950 m. Longer or shorter insulated conductors may also be used to meet specific application needs. In embodiments of insulated conductor heaters, purchased insulated conductor heaters have lengths of about 100 m to 500 m (e.g., 230 m). In certain embodiments, dimensions of sheaths and/or conductors of an insulated conductor may be selected so that the insulated conductor has enough sfrength to be self supporting even at upper working temperature limits. Such insulated cables may be suspended from wellheads or supports positioned near an interface between an overburden and a relatively low permeability formation containing heavy hydrocarbons without the need for support members extending into the hydrocarbon formation along with the insulated conductors.

In an embodiment, a higher frequency cunent may be used to take advantage of the skin effect in certain metals. In some embodiments, a 60 cycle AC cunent may be used in combination with conductors made of metals that exhibit pronounced skin effects. For example, fenomagnetic metals like iron alloys and nickel may exhibit a skin effect. The skin effect confines the cunent to a region close to the outer surface of the conductor, thereby effectively increasing the resistance of the conductor. A high resistance may be desired to decrease the operating cunent, minimize ohmic losses in surface cables, and minimize the cost of surface facilities.

Insulated conductor 562 may be designed to operate at power levels of up to about 1650 watts/meter. Insulated conductor heater 562 may typically operate at a power level between about 500 watts/meter and about 1150 watts/meter when heating a formation. Insulated conductor heater 562 may be designed so that a maximum voltage level at a typical operating temperature does not cause substantial thermal and/or electrical breakdown of electrical insulation 576. The insulated conductor heater 562 may be designed so that sheath 577 does not exceed a temperature that will result in a significant reduction in conosion resistance properties of the sheath material. In an embodiment of insulated conductor heater 562, conductor 575 may be designed to reach temperatures within a range between about 650 °C and about 870 °C. The sheath 577 may be designed to reach temperatures within a range between about 535 °C and about 760 °C. Insulated conductors having other operating ranges may be formed to meet specific operational requirements. In an embodiment of insulated conductor heater 562, conductor 575 is designed to operate at about 760 °C, sheath 577 is designed to operate at about 650 °C, and the insulated conductor heater is designed to dissipate about 820 watts/meter. Insulated conductor heater 562 may have one or more conductors 575. For example, a single insulated conductor heater may have three conductors within electrical insulation that are sunounded by a sheath. FIG. 61 depicts insulated conductor heater 562 having a single conductor 575. The conductor may be made of metal. The material used to form a conductor may be, but is not limited to, nichrome, nickel, and a number of alloys made from copper and nickel in increasing nickel concentrations from pure copper to Alloy 30, Alloy 60, Alloy 180, and Monel. Alloys of copper and nickel may advantageously have better electrical resistance properties than substantially pure nickel or copper.

In an embodiment, the conductor may be chosen to have a diameter and a resistivity at operating temperatures such that its resistance, as derived from Ohm's law, makes it electrically and structurally stable for the chosen power dissipation per meter, the length of the heater, and/or the maximum voltage allowed to pass through the conductor. In some embodiments, the conductor may be designed using Maxwell's equations to make use of skin effect.

The conductor may be made of different materials along a length of the insulated conductor heater. For example, a first section of the conductor may be made of a material that has a significantly lower resistance than a second section of the conductor. The first section may be placed adjacent to a formation layer that does not need to be heated to as high a temperature as a second formation layer that is adjacent to the second section. The resistivity of various sections of conductor may be adjusted by having a variable diameter and/or by having conductor sections made of different materials.

A diameter of conductor 575 may typically be between about 1.3 mm to about 10.2 mm. Smaller or larger diameters may also be used to have conductors with desired resistivity characteristics. In an embodiment of an insulated conductor heater, the conductor is made of Alloy 60 that has a diameter of about 5.8 mm.

Electrical insulator 576 of insulated conductor heater 562 may be made of a variety of materials. Pressure may be used to place electrical insulator powder between conductor 575 and sheath 577. Low flow characteristics and other properties of the powder and/or the sheaths and conductors may inhibit the powder from flowing out of the sheaths. Commonly used powders may include, but are not limited to, MgO, A1₂0₃, Zirconia, BeO, different chemical variations of Spinels, and combinations thereof. MgO may provide good thermal conductivity and electrical insulation properties. The desired electrical insulation properties include low leakage cunent and high dielectric sfrength. A low leakage cunent decreases the possibility of thermal breakdown and the high dielectric strength decreases the possibility of arcing across the insulator. Thermal breakdown can occur if the leakage cunent causes a progressive rise in the temperature of the insulator leading also to arcing across the insulator. An amount of impurities 578 in the electrical insulator powder may be tailored to provide required dielectric sfrength and a low level of leakage cunent. Impurities 578 added may be, but are not limited to, CaO, Fe₂0₃, A1₂0₃, and other metal oxides. Low porosity of the electrical insulation tends to reduce leakage cunent and increase dielectric strength. Low porosity may be achieved by increased packing of the MgO powder during fabrication or by filling of the pore space in the MgO powder with other granular materials, for example, A1₂0₃.

Impurities 578 added to the electrical insulator powder may have particle sizes that are smaller than the particle sizes of the powdered electrical insulator. The small particles may occupy pore space between the larger particles of the electrical insulator so that the porosity of the electrical insulator is reduced. Examples of powdered electrical insulators that may be used to form electrical insulation 576 are "H" mix manufactured by Idaho Laboratories Coφoration (Idaho Falls, Idaho) or Standard MgO used by Pyrotenax Cable Company (Trenton, Ontario) for high temperature applications. In addition, other powdered electrical insulators may be used. Sheath 577 of insulated conductor heater 562 may be an outer metallic layer. Sheath 577 may be in

, contact with hot formation fluids. Sheath 577 may need to be made of a material having a high resistance to conosion at elevated temperatures. Alloys that may be used in a desired operating temperature range of the sheath include, but are not limited to, 304 stainless steel, 310 stainless steel, Incoloy 800, and Inconel 600. The thickness of the sheath has to be sufficient to last for three to ten years in a hot and conosive environment. A thickness of the sheath may generally vary between about 1 mm and about 2.5 mm. For example, a 1.3 mm thick, 310 stainless steel outer layer may be used as sheath 577 to provide good chemical resistance to sulfidation conosion in a heated zone of a formation for a period of over 3 years. Larger or smaller sheath thicknesses may be used to meet specific application requirements.

An insulated conductor heater may be tested after fabrication. The insulated conductor heater may be required to withstand 2-3 times an operating voltage at a selected operating temperature. Also, selected samples of produced insulated conductor heaters may be required to withstand 1000 VAC at 760 °C for one month.

As illustrated in FIG. 62, short flexible transition conductor 571 may be connected to lead-in conductor 572 using connection 569 made during heater installation in the field. Transition conductor 571 may be a flexible, low resistivity, stranded copper cable that is sunounded by rubber or polymer insulation. Transition conductor 571 may typically be between about 1.5 m and about 3 m, although longer or shorter transition conductors may be used to accommodate particular needs. Temperature resistant cable may be used as transition conductor 571. Transition conductor 571 may also be connected to a short length of an insulated conductor heater that is less resistive than a primary heating section of the insulated conductor heater. The less resistive portion of the insulated conductor heater may be refened to as "cold pin" 568. Cold pin 568 may be designed to dissipate about one-tenth to about one-fifth of the power per unit length as is dissipated in a unit length of the primary heating section. Cold pins may typically be between about 1.5 m and about 15 m, although shorter or longer lengths may be used to accommodate specific application needs. In an embodiment, the conductor of a cold pin section is copper with a diameter of about 6.9 mm and a length of 9.1 m. The electrical insulation is the same type of insulation used in the primary heating section. A sheath of the cold pin may be made of Inconel 600. Chloride conosion cracking in the cold pin region may occur, so a chloride conosion resistant metal such as Inconel 600 may be used as the sheath. As illustrated in FIG. 62, small, epoxy filled canister 573 may be used to create a connection between fransition conductor 571 and cold pin 568. Cold pins 568 may be connected to the primary heating sections of insulated conductor 562 heaters by "splices" 567. The length of cold pin 568 may be sufficient to significantly reduce a temperature of insulated conductor heater 562. The heater section of the insulated conductor heater 562 may operate from about 530 °C to about 760 °C, splice 567 may be at a temperature from about 260 °C to about

370 °C, and the temperature at the lead-in cable connection to the cold pin may be from about 40 °C to about 90 °C. In addition to a cold pin at a top end of the insulated conductor heater, a cold pin may also be placed at a bottom end of the insulated conductor heater. The cold pin at the bottom end may in many instances make a bottom termination easier to manufacture. Splice material may have to withstand a temperature equal to half of a target zone operating temperature.

Density of electrical insulation in the splice should in many instances be high enough to withstand the required temperature and the operating voltage.

Splice 567 may be required to withstand 1000 VAC at 480 °C. Splice material may be high temperature splices made by Idaho Laboratories Coφoration or by Pyrotenax Cable Company. A splice may be an internal type of splice or an external splice. An internal splice is typically made without welds on the sheath of the insulated conductor heater. The lack of weld on the sheath may avoid potential weak spots (mechanical and/or electrical) on the insulated cable heater. An external splice is a weld made to couple sheaths of two insulated conductor heaters together. An external splice may need to be leak tested prior to insertion of the insulated cable heater into a formation. Laser welds or orbital TIG (tungsten inert gas) welds may be used to form external splices. An additional strain relief assembly may be placed around an external splice to improve the splice's resistance to bending and to protect the external splice against partial or total parting.

In certain embodiments, an insulated conductor assembly, such as the assembly depicted in FIG. 63 and FIG. 62, may have to withstand a higher operating voltage than normally would be used. For example, for heaters greater than about 700 m in length, voltages greater than about 2000 V may be needed for generating heat with the insulated conductor, as compared to voltages of about 480 V that may be used with heaters having lengths of less than about 225 m. In such cases, it may be advantageous to form insulated conductor 562, cold pin 568, fransition conductor 571, and lead-in conductor 572 into a single insulated conductor assembly. In some embodiments, cold pin 568 and canister 573 may not be required as shown in FIG. 62. In such an embodiment, splice 567 can be used to directly couple insulated conductor 562 to fransition conductor 571. In a heat source embodiment, insulated conductor 562, fransition conductor 571, and lead-in conductor 572 each include insulated conductors of varying resistance. Resistance of the conductors may be varied, for example, by altering a type of conductor, a diameter of a conductor, arid/or a length of a conductor. In an embodiment, diameters of insulated conductor 562, transition conductor 571, and lead-in conductor 572 are different. Insulated conductor 562 may have a diameter of 6 mm, transition conductor 571 may have a diameter of 7 mm, and lead-in conductor 572 may have a diameter of 8 mm. Smaller or larger diameters may be used to accommodate site conditions (e.g., heating requirements or voltage requirements). Insulated conductor 562 may have a higher resistance than either fransition conductor 571 or lead-in conductor 572, such that more heat is generated in the insulated conductor. Also, fransition conductor 571 may have a resistance between a resistance of insulated conductor 562 and lead-in conductor 572. Insulated conductor 562, fransition conductor 571, and lead-in conductor 572 may be coupled using splice 567 and/or connection 569. Splice 567 and/or connection 569 may be required to withstand relatively large operating voltages depending on a length of insulated conductor 562 and/or lead-in conductor 572. Splice 567 and/or connection 569 may inhibit arcing and/or voltage breakdowns within the insulated conductor assembly. Using insulated conductors for each cable within an insulated conductor assembly may allow for higher operating voltages within the assembly.

An insulated conductor assembly may include heating sections, cold pins, splices, termination canisters and flexible fransition conductors. The insulated conductor assembly may need to be examined and electrically tested before installation of the assembly into an opening in a formation. The assembly may need to be examined for competent welds and to make sure that there are no holes in the sheath anywhere along the whole heater (including the heated section, the cold-pins, the splices, and the termination cans). Periodic X-ray spot checking of the commercial product may need to be made. The whole cable may be immersed in water prior to electrical testing. Electrical testing of the assembly may need to show more than 2000 megaohms at 500 VAC at room temperature after water immersion. In addition, the assembly may need to be connected to 1000 VAC and show less than about 10 microamps per meter of resistive leakage cunent at room temperature. In addition, a check on leakage cunent at about 760 °C may need to show less than about 0.4 milliamps per meter.

A number of companies manufacture insulated conductor heaters. Such manufacturers include, but are not limited to, MI Cable Technologies (Calgary, Alberta), Pyrotenax Cable Company (Trenton, Ontario), Idaho

Laboratories Coφoration (Idaho Falls, Idaho), and Watlow (St. Louis, MO). As an example, an insulated conductor heater may be ordered from Idaho Laboratories as cable model 355-A90-310-"H" 307750730' with Inconel 600 sheath for the cold-pins, three phase Y configuration and bottom jointed conductors. The specification for the heater may also include 1000 VAC, 1400 °F quality cable. The designator 355 specifies the cable OD (0.355"); A90 specifies the conductor material; 310 specifies the heated zone sheath alloy (SS 310); "H" specifies the MgO mix; and 307750730' specifies about a 230 m heated zone with cold-pins top and bottom having about 9 m lengths. A similar part number with the same specification using high temperature Standard purity MgO cable may be ordered from Pyrotenax Cable Company.

One or more insulated conductor heaters may be placed within an opening in a formation to form a heat source or heat sources. Electrical cunent may be passed through each insulated conductor heater in the opening to heat the formation. Alternately, electrical cunent may be passed through selected insulated conductor heaters in an opening. The unused conductors may be backup heaters. Insulated conductor heaters may be electrically coupled to a power source in any convenient manner. Each end of an insulated conductor heater may be coupled to lead-in cables that pass through a wellhead. Such a configuration typically has a 180° bend (a "hafrpin" bend) or turn located near a bottom of the heat source. An insulated conductor heater that includes a 180° bend or turn may not require a bottom termination, but the 180° bend or turn may be an electrical and or structural weakness in the heater. Insulated conductor heaters may be electrically coupled together in series, in parallel, or in series and parallel combinations. In some embodiments of heat sources, electrical cunent may pass into the conductor of an insulated conductor heater and may be returned through the sheath of the insulated conductor heater by connecting conductor 575 to sheath 577 at the bottom of the heat source.

In the embodiment of a heat source depicted in FIG. 63, three insulated conductor heaters 562 are electrically coupled in a 3 -phase Y configuration to a power supply. The power supply may provide 60 cycle AC cunent to the electrical conductors. No bottom connection may be required for the insulated conductor heaters. Alternately, all three conductors of the three phase circuit may be connected together near the bottom of a heat source opening. The connection may be made directly at ends of heating sections of the insulated conductor heaters or at ends of cold pins coupled to the heating sections at the bottom of the insulated conductor heaters. The bottom connections may be made with insulator filled and sealed canisters or with epoxy filled canisters. The insulator may be the same composition as the insulator used as the electrical insulation.

The three insulated conductor heaters depicted in FIG. 63 may be coupled to support member 564 using cenfralizers 566. Alternatively, the three insulated conductor heaters may be strapped directly to the support tube using metal straps. Cenfralizers 566 may maintain a location or inhibit movement of insulated conductor heaters

562 on support member 564. Cenfralizers 566 may be made of metal, ceramic, or combinations thereof. The metal may be stainless steel or any other type of metal able to withstand a conosive and hot environment. In some embodhnents, cenfralizers 566 may be bowed metal strips welded to the support member at distances less than about 6 m. A ceramic used in centralizer 566 may be, but is not limited to, A1₂0₃, MgO, or other insulator. Cenfralizers 566 may maintain a location of insulated conductor heaters 562 on support member 564 such that movement of insulated conductor heaters is inhibited at operating temperatures of the insulated conductor heaters. Insulated conductor heaters 562 may also be somewhat flexible to withstand expansion of support member 564 during heating.

Support member 564, insulated conductor heater 562, and cenfralizers 566 may be placed in opening 514 in hydrocarbon layer 516. Insulated conductor heaters 562 may be coupled to bottom conductor junction 570 using cold pin fransition conductor 568. Bottom conductor junction 570 may electrically couple each insulated conductor heater 562 to each other. Bottom conductor junction 570 may include materials that are electrically conducting and do not melt at temperatures found in opening 514. Cold pin fransition conductor 568 may be an insulated conductor heater having lower electrical resistance than insulated conductor heater 562. As illusfrated in FIG. 62, cold pin 568 may be coupled to fransition conductor 571 and insulated conductor heater 562. Cold pin fransition conductor 568 may provide a temperature fransition between fransition conductor 571 and insulated conductor heater 562.

Lead-in conductor 572 may be coupled to wellhead 590 to provide electrical power to insulated conductor heater 562. Lead-in conductor 572 may be made of a relatively low electrical resistance conductor such that relatively little heat is generated from electrical cunent passing through lead-in conductor 572. In some embodiments, the lead-in conductor is a rubber or polymer insulated stranded copper wire. In some embodhnents, the lead-in conductor is a mineral-insulated conductor with a copper core. Lead-in conductor 572 may couple to wellhead 590 at surface 550 through a sealing flange located between overburden 540 and surface 550. The sealing flange may inhibit fluid from escaping from opening 514 to surface 550.

Packing material 542 may be placed between overburden casing 541 and opening 514. In some embodiments, cement 544 may secure overburden casing 541 to overburden 540. In an embodiment of a heat source, overburden casing is a 7.6 cm (3 inch) diameter carbon steel, schedule 40 pipe. Packing material 542 may inhibit fluid from flowing from opening 514 to surface 550. Cement 544 may include, for example, Class G or Class H Portland cement mixed with silica flour for improved high temperature performance, slag or silica flour, and/or a mixture thereof (e.g., about 1.58 grams per cubic centimeter slag/silica flour). In some heat source embodiments, cement 544 extends radially a width of from about 5 cm to about 25 cm. In some embodiments, cement 544 may extend radially a width of about 10 cm to about 15 cm. Cement 544 may inhibit heat transfer from conductor 564 into overburden 540.

In certain embodiments, one or more conduits may be provided to supply additional components (e.g., nifrogen, carbon dioxide, reducing agents such as gas containing hydrogen, etc.) to formation openings, to bleed off fluids, and/or to confrol pressure. Foπnation pressures tend to be highest near heating sources. Providing pressure control equipment in heat sources may be beneficial. In some embodiments, adding a reducing agent proximate the heating source assists in providing a more favorable pyrolysis environment (e.g., a higher hydrogen partial pressure). Since permeability and porosity tend to increase more quickly proximate the heating source, it is often optimal to add a reducing agent proximate the heating source so that the reducing agent can more easily move into the formation. Conduit 5000, depicted in FIG. 63, may be provided to add gas from gas source 5003, through valve 5001, and into opening 514. Opening 5004 is provided in packing material 542 to allow gas to pass into opening 514. Conduit 5000 and valve 5002 may be used at different times to bleed off pressure and/or confrol pressure proximate opening 514. Conduit 5010, depicted in FIG. 65, may be provided to add gas from gas source 5013, through valve 5011, and into opening 514. An opening is provided in cement 544 to allow gas to pass into opening 514. Conduit 5010 and valve 5012 may be used at different times to bleed off pressure and/or confrol pressure proximate opening

514. It is to be understood that any of the heating sources described herein may also be equipped with conduits to supply additional components, bleed off fluids, and/or to control pressure.

As shown in FIG. 63, support member 564 and lead-in conductor 572 may be coupled to wellhead 590 at surface 550 of the foπnation. Surface conductor 545 may enclose cement 544 and couple to wellhead 590. Embodiments of surface conductor 545 may have an outer diameter of about 10.16 cm to about 30.48 cm or, for example, an outer diameter of about 22 cm. Embodiments of surface conductors may extend to depths of approximately 3m to approximately 515 m into an opening in the formation. Alternatively, the surface conductor may extend to a depth of approximately 9 m into the opening. Electrical current may be supplied from a power source to insulated conductor heater 562 to generate heat due to the electrical resistance of conductor 575 as illustrated in FIG. 61. As an example, a voltage of about 330 volts and a current of about 266 amps are supplied to insulated conductor 562 to generate a heat of about 1150 watts/meter in insulated conductor heater 562. Heat generated from the three insulated conductor heaters 562 may fransfer (e.g., by radiation) within opening 514 to heat at least a portion of the hydrocarbon layer 516.

An appropriate configuration of an insulated conductor heater may be deteπnined by optimizing a material cost of the heater based on a length of heater, a power required per meter of conductor, and a desired operating voltage. In addition, an operating cunent and voltage may be chosen to optimize the cost of input electrical energy in conjunction with a material cost of the insulated conductor heaters. For example, as input electrical energy increases, the cost of materials needed to withstand the higher voltage may also increase. The insulated conductor heaters may generate radiant heat of approximately 650 watts/meter of conductor to approximately 1650 watts/meter of conductor. The insulated conductor heater may operate at a temperature between approximately 530

°C and approximately 760 °C within a formation.

Heat generated by an insulated conductor heater may heat at least a portion of a relatively low permeability formation containing heavy hydrocarbons. In some embodiments, heat may be transfened to the foπnation substantially by radiation of the generated heat to the formation. Some heat may be transfened by conduction or convection of heat due to gases present in the opening. The opening may be an uncased opening. An uncased opening eliminates cost associated with thermally cementing the heater to the formation, costs associated with a casing, and/or costs of packing a heater within an opening. In addition, heat fransfer by radiation is typically more efficient than by conduction, so the heaters may be operated at lower temperatures in an open wellbore. Conductive heat fransfer during initial operation of a heat source may be enhanced by the addition of a gas in the opening. The gas may be maintained at a pressure up to about 27 bars absolute. The gas may include, but is not limited to, carbon dioxide and/or helium. An insulated conductor heater in an open wellbore may advantageously be free to expand or contract to accommodate thermal expansion and confraction. An insulated conductor heater may advantageously be removable from an open wellbore.

In an embodiment, an insulated conductor heater may be installed or removed using a spooling assembly. More than one spooling assembly may be used to install both the insulated conductor and a support member simultaneously. U.S. Patent No. 4,572,299 issued to Van Egmond et al., which is incoφorated by reference as if fully set forth herein, describes spooling an electric heater into a well. Alternatively, the support member may be installed using a coiled tubing unit. The heaters may be un-spooled and connected to the support as the support is inserted into the well. The electric heater and the support member may be un-spooled from the spooling assemblies. Spacers may be coupled to the support member and the heater along a length of the support member.

Additional spooling assemblies may be used for additional electric heater elements.

In an in situ conversion process embodiment, a heater may be installed in a substantially horizontal wellbore. Installing a heater in a wellbore (whether vertical or horizontal) may include placing one or more heaters (e.g., three mineral insulated conductor heaters) within a conduit. FIG. 66 depicts an embodiment of a portion of three insulated conductor heaters 6232 placed within conduit 6234. Insulated conductor heaters 6232 may be spaced within conduit 6234 using spacers 6236 to locate the insulated conductor heater within the conduit.

The conduit may be reeled onto a spool. The spool may be placed on a transporting platform such as a track bed or other platform that can be transported to a site of a wellbore. The conduit may be unreeled from the spool at the wellbore and inserted into the wellbore to install the heater within the wellbore. A welded cap may be placed at an end of the coiled conduit. The welded cap may be placed at an end of the conduit that enters the wellbore first. The conduit may allow easy installation of the heater into the wellbore. The conduit may also provide support for the heater.

In some heat source embodhnents, coiled tubing installation may be used to install one or more wellbore elements placed in openings in a formation for an in situ conversion process. For example, a coiled conduit may be used to install other types of wells in a formation. The other types of wells may be, but are not limited to, monitor wells, freeze wells or portions of freeze wells, dewatering wells or portions of dewatering wells, outer casings, injection wells or portions of injection wells, production wells or portions of production wells, and heat sources or portions of heat sources. Installing one or more wellbore elements using a coiled conduit installation process may be less expensive and faster than using other installation processes. Coiled tubing installation may reduce a number of welded and or threaded connections in a length of casing. Welds and/or threaded connections in coiled tubing may be pre-tested for integrity (e.g., by hydraulic pressure testing). Coiled tubing is available from Quality Tubing, Inc. (Houston, Texas), Precision Tubing (Houston, Texas), and other manufacturers. Coiled tubing may be available in many sizes and different materials. Sizes of coiled tubing may range from about 2.5 cm (1 inch) to about 15 cm (6 inches). Coiled tubing may be available in a variety of different metals, including carbon steel. Coiled tubing may be spooled on a large diameter reel. The reel may be caπied on a coiled tubing unit. Suitable coiled tubing units are available from Halliburton (Duncan, Oklahoma), Fleet Cementers, Inc. (Cisco, Texas), and Coiled Tubing Solutions, Inc. (Eastland, Texas). Coiled tubing may be unwound from the reel, passed through a straightener, and inserted into a wellbore. A wellcap may be attached (e.g., welded) to an end of the coiled tubing before inserting the coiling tubing into a well. After insertion, the coiled tubing may be cut from the coiled tubing on the reel. In some embodiments, coiled tubing may be inserted into a previously cased opening, e.g., if a well is to be used later as a heater well, production well, or monitoring well. Alternately, coiled tubing installed within a wellbore can later be perforated (e.g., with a perforation gun) and used as a production conduit.

Embodiments of heat sources, production wells, and/or freeze wells may be installed in a formation using coiled tubing installation. Some embodiments of heat sources, production wells, and freeze wells include an element placed within an outer casing. For example, a conductor-in-conduit heater may include an outer conduit with an inner conduit placed in the outer conduit. A production well may include a heater element or heater elements placed within a casing to inhibit condensation and refluxing of vapor phase production fluids. A freeze well may include a refrigerant input line placed within a casing, or a refrigeration inlet and outlet line. Spacers may be spaced along a length of an element, or elements, positioned within a casing to inhibit the element, or elements, from contacting walls of the casing.

In some embodiments of heat sources, production wells, and freeze wells, casings may be installed using coiled tube installation. Elements may be placed within the casing after the casing is placed in the formation for heat sources or wells that include elements within the casings. In some embodiments, sections of casings may be threaded and/or welded and inserted into a wellbore using a drilling rig or workover rig. In some embodiments of heat sources, production wells, and freeze wells, elements may be placed within the casing before the casing is wound onto a reel.

Some wells may have sealed casings that inhibit fluid flow from the formation into the casing. Sealed casings also inhibit fluid flow from the casing into the formation. Some casings may be perforated, screened or have other types of openings that allow fluid to pass into the casing from the formation, or fluid from the casing to pass into the formation. In some embodiments, portions of wells are open wellbores that do not include casings. In an embodiment, the support member may be installed using standard oil field operations and welding different sections of support. Welding may be done by using orbital welding. For example, a first section of the support member may be disposed into the well. A second section (e.g., of substantially similar length) may be coupled to the first section in the well. The second section may be coupled by welding the second section to the first section. An orbital welder disposed at the wellhead may weld the second section to the first section. This process may be repeated with subsequent sections coupled to previous sections until a support of desired length is within the well.

FIG. 64 illustrates a cross-sectional view of one embodiment of a wellhead coupled to overburden casing 541. Flange 590c may be coupled to, or may be a part of, wellhead 590. Flange 590c may be formed of carbon steel, stainless steel, or any other material. Flange 590c may be sealed with o-ring 590f, or any other sealing mechanism. Support member 564 may be coupled to flange 590c. Support member 564 may support one or more insulated conductor heaters. In an embodiment, support member 564 is sealed in flange 590c by welds 590h. Power conductor 590a may be coupled to a lead-in cable and/or an insulated conductor heater. Power conductor 590a may provide electrical energy to the insulated conductor heater. Power conductor 590a may be sealed in sealing flange 590d. Sealing flange 590d may be sealed by compression seals or o-rings 590e. Power conductor 590a may be coupled to support member 564 with band 590i. Band 590i may include a rigid and conosion resistant material such as stainless steel. Wellhead 590 may be sealed with weld 590h such that fluids are inhibited from escaping the formation through wellhead 590. Lift bolt 590j may lift wellhead 590 and support member 564. Thermocouple 590g may be provided through flange 590c. Thermocouple 590g may measure a temperature on or proximate support member 564 within the heated portion of the well. Compression fittings 590k may serve to seal power cable 590a. Compression fittings 5901 may serve to seal thermocouple 590g. The compression fittings may inhibit fluids from escaping the formation. Wellhead 590 may also include a pressure confrol valve. The pressure confrol valve may confrol pressure within an opening in which support member 564 is disposed.

In a heat source embodiment, a confrol system may confrol electrical power supplied to an insulated conductor heater. Power supplied to the insulated conductor heater may be controlled with any appropriate type of confroller. For alternating cunent, the confroller may be, but is not limited to, a tapped transformer or a zero crossover electric heater firing SCR (silicon confrolled rectifier) confroller. Zero crossover electric heater firing confrol may be achieved by allowing full supply voltage to the insulated conductor heater to pass through the insulated conductor heater for a specific number of cycles, starting at the "crossover," where an instantaneous voltage may be zero, continuing for a specific number of complete cycles, and discontinuing when the instantaneous voltage again crosses zero. A specific number of cycles may be blocked, allowing control of the heat output by the insulated conductor heater. For example, the confrol system may be ananged to block fifteen and/or twenty cycles out of each sixty cycles that are supplied by a standard 60 Hz alternating cunent power supply. Zero crossover firing confrol may be advantageously used with materials having low temperature coefficient materials. Zero crossover firing confrol may inhibit cunent spikes from occuning in an insulated conductor heater.

FIG. 65 illustrates an embodiment of a conductor-in-conduit heater that may heat a relatively low permeability formation containing heavy hydrocarbons. Conductor 580 may be disposed in conduit 582.

Conductor 580 may be a rod or conduit of electrically conductive material. Low resistance sections 584 may be present at both ends of conductor 580 to generate less heating in these sections. Low resistance section 584 may be formed by having a greater cross-sectional area of conductor 580 in that section, or the sections may be made of material having less resistance. In certain embodiments, low resistance section 584 includes a low resistance conductor coupled to conductor 580. In some heat source embodiments, conductors 580 may be 316, 304, or 310 stainless steel rods with diameters of approximately 2.8 cm. In some heat source embodiments, conductors are 316, 304, or 310 stainless steel pipes with diameters of approximately 2.5 cm. Larger or smaller diameters of rods or pipes may be used to achieve desired heating of a formation. The diameter and/or wall thickness of conductor 580 may be varied along a length of the conductor to establish different heating rates at various portions of the conductor.

Conduit 582 may be made of an electrically conductive material. For example, conduit 582 may be a 7.6 cm, schedule 40 pipe made of 316, 304, or 310 stainless steel. Conduit 582 may be disposed in opening 514 in hydrocarbon layer 516. Opening 514 has a diameter able to accommodate conduit 582. A diameter of the opening may be from about 10 cm to about 13 cm. Larger or smaller diameter openings may be used to accommodate particular conduits or designs.

Conductor 580 may be centered in conduit 582 by centralizer 581. Centralizer 581 may electrically isolate conductor 580 from conduit 582. Centralizer 581 may inhibit movement and properly locate conductor 580 within conduit 582. Centralizer 581 may be made of a ceramic material or a combination of ceramic and metallic materials. Cenfralizers 581 may inhibit deformation of conductor 580 in conduit 582. Centralizer 581 may be spaced at intervals between approximately 0.5 m and approximately 3 m along conductor 580. FIGS. 67, 68, and 69 depict embodiments of cenfralizers 581.

A second low resistance section 584 of conductor 580 may couple conductor 580 to wellhead 690, as depicted in FIG. 65. Electrical cunent may be applied to conductor 580 from power cable 585 through low resistance section 584 of conductor 580. Electrical cunent may pass from conductor 580 through sliding connector

583 to conduit 582. Conduit 582 may be electrically insulated from overburden casing 541 and from wellhead 690 to return electrical cunent to power cable 585. Heat may be generated in conductor 580 and conduit 582. The generated heat may radiate within conduit 582 and opening 514 to heat at least a portion of hydrocarbon layer 516. As an example, a voltage of about 330 volts and a cunent of about 795 amps may be supplied to conductor 580 and conduit 582 in a 229 m (750 ft) heated section to generate about 1150 watts/meter of conductor 580 and conduit

582.

Overburden conduit 541 may be disposed in overburden 540. Overburden conduit 541 may, in some embodiments, be sunounded by materials that inhibit heating of overburden 540. Low resistance section 584 of conductor 580 may be placed in overburden conduit 541. Low resistance section 584 of conductor 580 may be made of, for example, carbon steel. Low resistance section 584 may have a diameter between about 2 cm to about 5 cm or, for example, a diameter of about 4 cm. Low resistance section 584 of conductor 580 may be centralized within overburden conduit 541 using cenfralizers 581. Cenfralizers 581 may be spaced at intervals of approximately 6 m to approximately 12 m or, for example, approximately 9 m along low resistance section 584 of conductor 580. In a heat source embodiment, low resistance section 584 of conductor 580 is coupled to conductor 580 by a weld or welds. In other heat source embodiments, low resistance sections may be threaded, threaded and welded, or otherwise coupled to the conductor. Low resistance section 584 may generate little and/or no heat in overburden conduit 541. Packing material 542 may be placed between overburden casing 541 and opening 514. Packing material 542 may inhibit fluid from flowing from opening 514 to surface 550. fri a heat source embodiment, overburden conduit is a 7.6 cm schedule 40 carbon steel pipe. In some embodiments, the overburden conduit may be cemented in the overburden. Cement 544 may be slag or silica flour or a mixture thereof (e.g., about 1.58 grams per cubic centimeter slag/silica flour). Cement 544 may extend radially a width of about 5 cm to about 25 cm. Cement 544 may also be made of material designed to inhibit flow of heat into overburden 540. In other heat source embodiments, overburden may not be cemented into the formation. Having an uncemented overburden casing may facilitate removal of conduit 582 if the need for removal should arise.

Surface conductor 545 may couple to wellhead 690. Surface conductor 545 may have a diameter of about 10 cm to about 30 cm or, in certain embodiments, a diameter of about 22 cm. Electrically insulating sealing flanges may mechanically couple low resistance section 584 of conductor 580 to wellhead 690 and to electrically couple low resistance section 584 to power cable 585. The electrically insulating sealing flanges may couple power cable 585 to wellhead 690. For example, lead-in conductor 585 may include a copper cable, wire, or other elongated member. Lead-in conductor 585 may include any material having a substantially low resistance. The lead-in conductor may be clamped to the bottom of the low resistance conductor to make electrical contact.

In an embodiment, heat may be generated in or by conduit 582. About 10% to about 30%, or, for example, about 20%, of the total heat generated by the heater may be generated in or by conduit 582. Both conductor 580 and conduit 582 may be made of stainless steel. Dimensions of conductor 580 and conduit 582 may be chosen such that the conductor will dissipate heat in a range from approximately 650 watts per meter to 1650 watts per meter. A temperature in conduit 582 may be approximately 480 °C to approximately 815 °C, and a temperature in conductor 580 may be approximately 500 °C to 840 °C. Substantially uniform heating of a relatively low permeability formation containing heavy hydrocarbons may be provided along a length of conduit 582 greater than about 300 m or, even greater than about 600 m.

FIG. 70 depicts a cross-sectional representation of an embodiment of a removable conductor-in-conduit heat source. Conduit 582 may be placed in opening 514 through overburden 540 such that a gap remains between the conduit and overburden casing 541. Fluids may be removed from opening 514 through the gap between conduit 582 and overburden casing 541. Fluids may be removed from the gap through conduit 5010. Conduit 582 and components of the heat source included within the conduit that are coupled to wellhead 690 may be removed from opening 514 as a single unit. The heat source may be removed as a single unit to be repaired, replaced, and/or used in another portion of the formation.

In certain embodiments, portions of a conductor-in-conduit heat source may be moved or removed to adjust a portion of the formation that is heated by the heat source. For example, in a horizontal well the conductor- in-conduit heat source may be initially almost as long as the opening in the foπnation. As products are produced from the formation, the conductor-in-conduit heat source may be moved so that it is placed at location further from the end of the opening in the foπnation. Heat may be applied to a different portion of the formation by adjusting the location of the heat source. In certain embodiments, an end of the heater may be coupled to a sealing mechanism (e.g., a packing mechanism, or a plugging mechanism) to seal off perforations in a liner or casing. The sealing mechanism may inhibit undesired fluid production from portions of the heat source wellbore from which the conductor-in-conduit heat source has been removed.

As depicted in FIG. 71, sliding connector 583 may be coupled near an end of conductor 580. Sliding connector 583 may be positioned near a bottom end of conduit 582. Sliding connector 583 may electrically couple conductor 580 to conduit 582. Sliding connector 583 may move during use to accommodate thermal expansion and/or confraction of conductor 580 and conduit 582 relative to each other. In some embodiments, sliding connector 583 may be attached to low resistance section 584 of conductor 580. The lower resistance of section 584 may allow the sliding connector to be at a temperature that does not exceed about 90 °C. Maintaining sliding connector 583 at a relatively low temperature may inhibit conosion of the sliding connector and promote good contact between the sliding connector and conduit 582. Sliding connector 583 may include scraper 593. Scraper 593 may abut an inner surface of conduit 582 at point 595. Scraper 593 may include any metal or electrically conducting material (e.g., steel or stainless steel). Centralizer 591 may couple to conductor 580. In some embodiments, sliding connector 583 may be positioned on low resistance section 584 of conductor 580. Centralizer 591 may include any electrically conducting material (e.g., a metal or metal alloy). Spring bow 592 may couple scraper 593 to centralizer 591. Spring bow 592 may include any metal or electrically conducting material (e.g., copper-beryllium alloy). In some embodiments, centralizer 591, spring bow 592, and/or scraper 593 are welded together.

More than one sliding connector 583 may be used for redundancy and to reduce the cunent through each scraper 593. In addition, a thickness of conduit 582 may be increased for a length adjacent to sliding connector 583 to reduce heat generated in that portion of conduit. The length of conduit 582 with increased thickness may be, for example, approximately 6 m. FIG. 72 illustrates an embodiment of a wellhead. Wellhead 690 may be coupled to electrical junction box 690a by flange 690n or any other suitable mechanical device. Electrical junction box 690a may control power (cunent and voltage) supplied to an electric heater. Power source 690t may be included in electrical junction box 690a. In a heat source embodiment, the electric heater is a conductor-in-conduit heater. Flange 690n may include stainless steel or any other suitable sealing material. Conductor 690b may electrically couple conduit 582 to power source 690t. In some embodiments, power source 690t may be located outside wellhead 690 and the power source is coupled to the wellhead with power cable 585, as shown in FIG. 65. Low resistance section 584 may be coupled to power source 690t. Compression seal 690c may seal conductor 690b at an inner surface of electrical junction box 690a. Flange 690n may be sealed with metal o-ring 690d. Conduit 690f may couple flange 690n to flange 690m.

Flange 690m may couple to an overburden casing. Flange 690m may be sealed with o-ring 690g (e.g., metal o-ring or steel o-ring). Low resistance section 584 of the conductor may couple to electrical junction box 690a. Low resistance section 584 may be passed through flange 690n. Low resistance section 584 may be sealed in flange 690n with o-ring assembly 690p. Assemblies 690p are designed to insulate low resistance section 584 from flange 690n and flange 690m. Compression seal 690c may be designed to elecfrically insulate conductor 690b from flange

690n and junction box 690a. Centralizer 581 may couple to low resistance section 584. Thermocouples 690i may be coupled to thermocouple flange 690q with connectors 690h and wire 690j. Thermocouples 690i may be enclosed in an elecfrically insulated sheath (e.g., a metal sheath). Thermocouples 690i may be sealed in thermocouple flange 690q with compression seals 690k. Thermocouples 690i may be used to monitor temperatures in the heated portion downhole. In some embodiments, fluids (e.g., vapors) may be removed through wellhead 690.

For example, fluids from outside conduit 582 may be removed through flange 690r or fluids within the conduit may be removed through flange 690s.

FIG. 73 illustrates an embodiment of a conductor-in-conduit heater placed substantially horizontally within hydrocarbon layer 516. Heated section 6011 may be placed substantially horizontally within hydrocarbon layer 516. Heater casing 6014 may be placed within hydrocarbon layer 516. Heater casing 6014 may be formed of a conosion resistant, relatively rigid material (e.g., 304 stainless steel). Heater casing 6014 may be coupled to overburden casing 541. Overburden casing 541 may include materials such as carbon steel. In an embodiment, overburden casing 541 and heater casing 6014 have a diameter of about 15 cm. Expansion mechanism 6012 may be placed at an end of heater casing 6014 to accommodate thermal expansion of the conduit during heating and/or cooling.

To install heater casing 6014 substantially horizontally within hydrocarbon layer 516, overburden casing 541 may bend from a vertical direction in overburden 540 into a horizontal direction within hydrocarbon layer 516. A curved wellbore may be formed during drilling of the wellbore in the formation. Heater casing 6014 and overburden casing 541 may be installed in the curved wellbore. A radius of curvature of the curved wellbore may be determined by properties of drilling in the overburden and the formation. For example, the radius of curvature may be about 200 m from point 6015 to point 6016.

Conduit 582 may be placed within heater casing 6014. In some embodiments, conduit 582 may be made of a conosion resistant metal (e.g., 304 stainless steel). Conduit may be heated to a high temperature. Conduit 582 may also be exposed to hot formation fluids. Conduit 582 may be freated to have a high emissivity. Conduit 582 may have upper section 6002. In some embodiments, upper section 6002 may be made of a less conosion resistant metal than other portions of conduit 582 (e.g., carbon steel). A large portion of upper section 6002 may be positioned in overburden 540 of the formation. Upper section 6002 may not be exposed to temperatures as high as the temperatures of conduit 582. In an embodiment, conduit 582 and upper section 6002 have a diameter of about 7.6 cm.

Conductor 580 may be placed in conduit 582. A portion of the conduit placed adjacent to conduit may be made of a metal that has desired electrical properties, emissivity, creep resistance and conosion resistance at high temperatures. Conductor may include, but is not limited to, 310 stainless steel, 304 stainless steel, 316 stainless steel, 347 stainless steel, and/or other steel or non-steel alloys. Conductor 580 may have a diameter of about 3 cm, however, a diameter of conductor 580 may vary depending on, but not limited to, heating requirements and power requirements. Conductor 580 may be located in conduit 582 using one or more cenfralizers 581. Cenfralizers 581 may be ceramic or a combination of metal and ceramic. Cenfralizers 581 may inhibit conductor from contacting conduit 582. In some embodiments, cenfralizers 581 may be coupled to conductor 580. In other embodiments, cenfralizers 581 may be coupled to conduit 582. Conductor 580 may be elecfrically coupled to conduit 582 using sliding connector 583.

Conductor 580 may be coupled to fransition conductor 6010. Transition conductor 6010 may be used as an electrical fransition between lead-in conductor 6004 and conductor 580. In an embodiment, transition conductor

6010 may be carbon steel. Transition conductor 6010 may be coupled to lead-in conductor 6004 with elecfrical connector 6008. FIG. 74 illustrates an enlarged view of an embodiment of a junction of transition conductor 6010, elecfrical connector 6008, insulator 6006, and lead-in conductor 6004. Lead-in conductor 6004 may include one or more conductors (e.g., three conductors). In certain embodiments, the one or more conductors may be insulated copper conductors (e.g., rabber-insulated copper cable). In some embodiments, the one or more conductors may be insulated or un-insulated stranded copper cable. As shown in FIG. 74, insulator 6006 may be placed inside lead-in conductor 6004. Insulator 6006 may include elecfrically insulating materials such as fiberglass. Insulator 6006 may couple elecfrical connector 6008 to heater support 6000. In an embodiment, electrical cunent may flow from a power supply through lead-in conductor 6004, through fransition conductor 6010, into conductor 580, and return through conduit 582 and upper section 6002.

Refening to FIG. 73, heater support 6000 may include a support that is used to install heated section 6011 in hydrocarbon layer 516. For example, heater support 6000 may be a sucker rod that is inserted through overburden 540 from a ground surface. The sucker rod may include one or more portions that can be coupled to each other at the surface as the rod is inserted into the formation. In some embodiments, heater support 6000 is a single piece assembled in an assembly facility. Inserting heater support 6000 into the formation may push heated section 6011 into the formation.

Overburden casing 541 may be supported within overburden 540 using reinforcing material 544. Reinforcing material may include cement (e.g., Portland cement). Surface conductor 545 may enclose reinforcing material 544 and overburden casing 541 in a portion of overburden 540 proximate the ground surface. Surface conductor 545 may include a surface casing.

FIG. 75 illustrates a schematic of an alternate embodiment of a conductor-in-conduit heater placed substantially horizontally within a formation. In an embodiment, heater support 6000 may be a low resistance conductor (e.g., low resistance section 584 as shown in FIG. 65). Heater support 6000 may include carbon steel or other electrically-conducting materials. Heater support 6000 may be elecfrically coupled to fransition conductor 6010 and conductor 580. In some embodiments, a heat source may be placed within an uncased wellbore in a relatively low peπneability formation containing heavy hydrocarbons. FIG. 77 illustrates a schematic of an embodiment of a conductor-in-conduit heater placed substantially horizontally within an uncased wellbore in a formation. Heated section 6011 may be placed within opening 514 in hydrocarbon layer 516. In certain embodiments, heater support 6000 may be a low resistance conductor (e.g., low resistance section 584 as shown in FIG. 65). Heater support

6000 may be elecfrically coupled to fransition conductor 6010 and conductor 580. FIG. 76 depicts an alternate embodiment of the conductor-in-conduit heater shown in FIG. 77. In certain embodiments, perforated casing 9636 may be placed in opening 514 as shown in FIG. 76. In some embodiments, cenfralizers 581 may be used to support perforated casing 9636 within opening 514. In certain heat source embodiments, a cladding section may be coupled to heater support 6000 and/or upper section 6002. FIG. 78 depicts an embodiment of cladding section 9200 coupled to heater support 6000. Cladding may also be coupled to an upper section of conduit 582. Cladding section 9200 may reduce the electrical resistance of heater support 6000 and or the upper section of conduit 582. In an embodiment, cladding section 9200 is copper tubing coupled to the heater support and the conduit. In other heat source embodiments, heated section 6011, as shown in FIGS. 73, 75, and 77, may be placed in a wellbore with an orientation other than substantially horizontally in hydrocarbon layer 516. For example, heated section 6011 may be placed in hydrocarbon layer 516 at an angle of about 45° or substantially vertically in the formation. In addition, elements of the heat source placed in overburden 540 (e.g., heater support 6000, overburden casing 541, upper section 6002, etc.) may have an orientation other than substantially vertical within the overburden.

In certain heat source embodhnents, the heat source may be removably installed in a formation. Heater support 6000 may be used to install and or remove the heat source, including heated section 6011, from the formation. The heat source may be removed to repair, replace, and/or use the heat source in a different wellbore. The heat source may be reused in the same formation or in a different formation. In some embodiments, a heat source or a portion of a heat source may be spooled on coiled tubing rig and moved to another well location.

In some embodiments for heating a relatively low permeability formation containing heavy hydrocarbons, more than one heater may be installed in a wellbore or heater well. Having more than one heater in a wellbore or heat source may provide the ability to heat a selected portion or portions of a formation at a different rate than other portions of the formation. Having more than one heater in a wellbore or heat source may provide a backup heat source in the wellbore or heat source should one or more of the heaters fail. Having more than one heater may allow a uniform temperature profile to be established along a desired portion of the wellbore. Having more than one heater may allow for rapid heating of a hydrocarbon layer or layers to a pyrolysis temperature from ambient temperature. The more than one heater may include similar types of heaters or may include different types of heaters. For example, the more than one heater may be a natural disfributed combustor heater, an insulated conductor heater, a conductor-in-conduit heater, an elongated member heater, a downhole combustor (e.g., a downhole flameless combustor or a downhole combustor), etc.

In an in situ conversion process embodiment, a first heater in a wellbore may be used to selectively heat a first portion of a formation and a second heater may be used to selectively heat a second portion of the formation. The first heater and the second heater may be independently confrolled. For example, heat provided by a first heater can be controlled separately from heat provided by a second heater. As another example, elecfrical power supplied to a first electric heater may be controlled independently of elecfrical power supplied to a second electric heater. The first portion and the second portion may be located at different heights or levels within a wellbore, either vertically or along a face of the wellbore. The first portion and the second portion may be separated by a third, or separate, portion of a formation. The third portion may contain hydrocarbons or may be a non- hydrocarbon containing portion of the formation. For example, the third portion may include rock or similar non- hydrocarbon containing materials. The third portion may be heated or unheated. In some embodiments, heat used to heat the first and second portions may be used to heat the third portion. Heat provided to the first and second portions may substantially uniformly heat the first, second, and third portions.

FIG. 67 illustrates a perspective view of an embodiment of a cenfralizer in conduit 582. Electrical insulator 581a may be disposed on conductor 580. Insulator 581a may be made of aluminum oxide or other elecfrically insulating material that has a high working temperature limit. Neck portion 581 j may be a bushing which has an inside diameter that allows conductor 580 to pass through the bushing. Neck portion 58 lj may include electtically-insulative materials such as metal oxides and ceramics (e.g., aluminum oxide). Insulator 581a and neck portion 58 lj may be obtainable from manufacturers such as CoorsTek (Golden, Colorado) or Norton Ceramics (United Kingdom). In an embodiment, insulator 581a and/or neck portion 581j are made from 99 % or greater purity machinable aluminum oxide. In certain embodiments, ceramic portions of a heat source may be surface glazed. Surface glazing ceramic may seal the ceramic from contamination from dirt and/or moisture. High temperature surface glazing of ceramics may be done by companies such as NGK-Locke Inc. (Baltimore, Maryland) or Johannes Gebhart (Germany).

A location of insulator 581a on conductor 580 may be maintained by disc 581d. Disc 581d may be welded to conductor 580. Spring bow 581c may be coupled to insulator 581a by disc 581b. Spring bow 581c and disc

581b may be made of metals such as 310 stainless steel and/or any other thermally conducting material that may be used at relatively high temperatures. Spring bow 581c may reduce the sfress on ceramic portions of the centralizer during installation or removal of the heater, and/or during use of the heater. Reducing the stress on ceramic portions of the cenfralizer during installation or removal may increase an operational lifetime of the heater. In some heat source embodiments, cenfralizer 581 may have an opening that fits over an end of conductor. In other embodiments, cenfralizer 581 may be assembled from two or more pieces around a portion of conductor 580. The pieces may be coupled to conductor 580 by fastening device 58 le. Fastening device 58 le may be made of any material that can be used at relatively high temperatures (e.g., steel).

FIG. 68 depicts a representation of an embodiment of centralizer 581 disposed on conductor 580. Discs 581d may maintain positions of centralizer 581 relative to conductor 580. Discs 581d may be metal discs welded to conductor 580. Discs 581d may be tack-welded to conductor 580. FIG. 69 depicts a top view representation of a centralizer embodiment. Cenfralizer 581 may be made of any suitable elecfrically insulating material able to withstand high voltage at high temperatures. Examples of such materials include, but are not limited to, aluminum oxide and/or Macor. Centralizer 581 may electrically insulate conductor 580 from conduit 582. FIG. 79 illustrates a cross-sectional representation of an embodiment of a centralizer placed on a conductor. FIG. 80 depicts a portion of an embodiment of a conductor-in-conduit heat source with a cutout view showing a cenfralizer on the conductor. Centralizer 581 may be used in a conductor-in-conduit heat source. Centralizer 581 may be used to maintain a location of conductor 580 within conduit 582. Cenfralizer 581 may include electrically-insulating materials such as ceramics (e.g., alumina and zirconia). As shown in FIG. 79, centralizer 581 may have at least one recess 58 li. Recess 581i may be, for example, an indentation or notch in cenfralizer 581 or a recess left by a portion removed from the cenfralizer. A cross-sectional shape of recess 581i may be a rectangular shape or any other geometrical shape. In certain embodiments, recess 58 li has a shape that allows protrusion 581g to reside within the recess. Recess 581i may be formed such that the recess will be placed at a junction of cenfralizer 581 and conductor 580. In one embodiment, recess 581i is formed at a bottom of cenfralizer 581.

At least one protrusion 581g may be formed on conductor 580. Protrusion 581g may be welded to conductor 580. In some embodiments, protrusion 581g is a weld bead formed on conductor 580. Protrusion 581g may include electrically-conductive materials such as steel (e.g., stainless steel). In certain embodiments, protrusion 58 lg may include one or more protrusions formed around the circumference of conductor 580. Protrasion 581g may be used to maintain a location of centralizer 581 on conductor 580. For example, protrasion

58 lg may inhibit downward movement of cenfralizer 581 along conductor 580. In some embodiments, at least one additional recess 58 li and at least one additional protrasion 58 lg may be placed at atop of cenfralizer 581 to inhibit upward movement of the centralizer along conduit 580.

In an embodiment, electrically-insulating material 581h is placed over protrasion 581g and recess 581i. Electrically-insulating material 58 lh may cover recess 581 i such that protrasion 581 g is enclosed within the recess and the electrically-insulating material. In some embodiments, electrically-insulating material 58 lh may partially cover recess 58 li. Protrasion 58 lg may be enclosed so that carbon deposition (i.e., coking) on protrasion 58 lg during use is inhibited. Carbon may form electrically-conducting paths during use of conductor 580 and conduit 582 to heat a formation. Electrically-insulating material 581h may include materials such as, but not limited to, metal oxides and/or ceramics (e.g., alumina or zirconia). In some embodiments, electrically-insulating material

58 lh is a thermally conducting material. A thermal plasma spray process may be used to place electrically- insulating material 581h over protrasion 581g and recess 5811. The thermal plasma process may spray coat electrically-insulating material 581h on protrasion 581g and/or cenfralizer 581.

In an embodiment, centralizer 581 with recess 58 li, protrasion 58 lg, and electrically-insulating material 581h are placed on conductor 580 within conduit 582 during installation of the conductor-in-conduit heat source in an opening in a formation. In another embodiment, centralizer 581 with recess 58 li, protrusion 58 lg, and electrically-insulating material 581h are placed on conductor 580 within conduit 582 during assembling of the conductor-in-conduit heat source. For example, an assembling process may include forming protrusion 58 lg on conductor 580, placing centralizer 581 with recess 58 li on conductor 580, covering the protrasion and the recess with electrically-insulating material 58 lh, and placing the conductor within conduit 582.

FIG. 81 depicts an alternate embodiment of cenfralizer 581. Neck portion 58 lj may be coupled to centralizer 581. In certain embodiments, neck portion 58 lj is an extended portion of cenfralizer 581. Protrusion 58 lg may be placed on conductor 580 to maintain a location of centralizer 581 and neck portion 58 lj on the conductor. Neck portion 581j may be a bushing which has an inside diameter that allows conductor 580 to pass through the bushing. Neck portion 58 lj may include electrically-insulative materials such as metal oxides and ceramics (e.g., aluminum oxide). For example, neck portion 581j may be a commercially available bushing from manufacturers such as Borges Technical Ceramics (Pennsburg, PA). In one embodiment, as shown in FIG. 81, a first neck portion 58 lj is coupled to an upper portion of centralizer 581 and a second neck portion 58 lj is coupled to a lower portion of cenfralizer 581. Neck portion 581j may extend between about 1 cm and about 5 cm from cenfralizer 581. In an embodiment, neck portion 581j extends about 2-3 cm from cenfralizer 581. Neck portion 581j may extend a selected distance from cenfralizer 581 such that arcing (e.g., surface arcing) is inhibited. Neck portion 581j may increase a path length for arcing between conductor 580 and conduit 582. A path for arcing between conductor 580 and conduit 582 may be foπned by carbon deposition on centralizer 581 and/or neck portion 581j. Increasing the path length for arcing between conductor 580 and conduit 582 may reduce the likelihood of arcing between the conductor and the conduit. Another advantage of increasing the path length for arcing between conductor 580 and conduit 582 may be an increase in a maximum operating voltage of the conductor.

In an embodiment, neck portion 58 lj also includes one or more grooves 581k. One or more grooves 581k may further increase the path length for arcing between conductor 580 and conduit 582. In certain embodiments, conductor 580 and conduit 582 may be oriented substantially vertically within a formation. In such an embodiment, one or more grooves 581k may also inhibit deposition of conducting particles (e.g., carbon particles or conosion scale) along the length of neck portion 581j. Conducting particles may fall by gravity along a length of conductor 580. One or more grooves 581k may be oriented such that falling particles do not deposit into the one or more grooves. Inhibiting the deposition of conducting particles on neck portion 58 lj may inhibit formation of an arcing path between conductor 580 and conduit 582. In some embodiments, diameters of each of one or more grooves 581k may be varied. Varying the diameters of the grooves may further inhibit the likelihood of arcing between conductor 580 and conduit 582.

FIG. 82 depicts an embodiment of centralizer 581. Cenfralizer 581 may include two or more portions held together by fastening device 58 le. Fastening device 58 le may be a clamp, bolt, snap-lock, or screw. FIGS. 83 and 84 depict top views of embodiments of cenfralizer 581 placed on conduit 580. Centralizer 581 may include two portions. The two portions may be coupled together to form a cenfralizer in a "clam shell" configuration. The two portions may have notches and recesses that are shaped to fit together as shown in either of FIGS. 83 and 84. In some embodiments, the two portions may have notches and recesses that are tapered so that the two portions tightly couple together. The two portions may be slid together lengthwise along the notches and recesses.

In a heat source embodiment, an insulation layer may be placed between a conductor and a conduit. The insulation layer may be used to elecfrically insulate the conductor from the conduit. The insulation layer may also maintain a location of the conductor within the conduit. In some embodiments, the insulation layer may include a layer that remains placed on and/or in the heat source after installation. In certain embodhnents, the insulation layer may be removed by heating the heat source to a selected temperature. The insulation layer may include electrically- insulating materials such as, but not limited to, metal oxides and or ceramics. For example, the insulation layer may be Nextel™ insulation obtainable from 3M Company (St. Paul, MN). An insulation layer may also be used for installation of any other heat source (e.g., insulated conductor heat source, natural disfributed combustor, etc.). In an embodiment, the insulation layer is fastened to the conductor. The insulation layer may be fastened to the conductor with a high temperature adhesive (e.g., a ceramic adhesive such as Cofronics 920 alumina-based adhesive available from Cofronics Coφoration (Brooklyn, N.Y.)). FIG. 85 depicts a cross-sectional representation of an embodiment of a section of a conductor-in-conduit heat source with insulation layer 9180. Insulation layer 9180 may be placed on conductor 580. Insulation layer 9180 may be spiraled around conductor 580 as shown in FIG. 85. In one embodiment, insulation layer 9180 is a single insulation layer wound around the length of conductor 580. In some embodiments, insulation layer 9180 may include one or more individual sections of insulation layers wrapped around conductor 580. Conductor 580 may be placed in conduit 582 after insulation layer 9180 has been placed on the conductor. Insulation layer 9180 may elecfrically insulate conductor 580 from conduit 582. In an embodiment of a conductor-in-conduit heat source, a conduit may be pressurized with a fluid to inhibit a large pressure difference between pressure in the conduit and pressure in the formation. Balanced pressure or a small pressure difference may inhibit deformation of the conduit during use. The fluid may increase conductive heat fransfer from the conductor to the conduit. The fluid may include, but is not limited to, a gas such as helium, nifrogen, air, or mixtures thereof. The fluid may inhibit arcing between the conductor and the conduit. If air and/or air mixtures are used to pressurize the conduit, the air and/or air mixtures may react with materials of the conductor and the conduit to form an oxide layer on a surface of the conductor and/or an oxide layer on an inner surface of the conduit. The oxide layer may inhibit arcing. The oxide layer may make the conductor and/or the conduit more resistant to conosion. Reducing the amount of heat losses to an overburden of a formation may increase an efficiency of a heat source. The efficiency of the heat source may be determined by the energy transfened into the formation through the heat source as a fraction of the energy input into the heat source. In other words, the efficiency of the heat source may be a function of energy that actually heats a desired portion of the formation divided by the elecfrical power (or other input power) provided to the heat source. To increase the amount of energy actually transfened to the formation, heating losses to the overburden may be reduced. Heating losses in the overburden may be reduced for electrical heat sources by the use of relatively low resistance conductors in the overburden that couple a power supply to the heat source. Alternating elecfrical cunent flowing through certain conductors (e.g., carbon steel conductors) tends to flow along the skin of the conductors. This skin depth effect may increase the resistance heating at the outer surface of the conductor (i.e., the cunent flows through only a small portion of the available metal) and, thus increase heating of the overburden. Elecfrically conductive casings, coatings, wiring, and/or claddings may be used to reduce the electrical resistance of a conductor used in the overburden. Reducing the elecfrical resistance of the conductor in the overburden may reduce electricity losses to heating the conduit in the overburden portion and thereby increase the available electricity for resistive heating in portions of the conductor below the overburden. As shown in FIG. 65, low resistance section 584 may be coupled to conductor 580. Low resistance section 584 may be placed in overburden 540. Low resistance section 584 may be, for example, a carbon steel conductor. Carbon steel may be used to provide mechanical sfrength for the heat source in overburden 540. In an embodiment, an electrically conductive coating may be coated on low resistance section 584 to further reduce an elecfrical resistance of the low resistance conductor. In some embodiments, the elecfrically conductive coating may be coated on low resistance section 584 during assembly of the heat source. In other embodiments, the elecfrically conductive coating may be coated on low resistance section 584 after installation of the heat source in opening 514.

In some embodiments, the electrically conductive coating may be sprayed on low resistance section 584. For example, the elecfrically conductive coating may be a sprayed on thermal plasma coating. The elecfrically conductive coating may include conductive materials such as, but not limited to, aluminum or copper. The electrically conductive coating may include other conductive materials that can be thermal plasma sprayed. In certain embodiments, the elecfrically conductive coating may be coated on low resistance section 584 such that the resistance of the low resistance conductor is reduced by a factor of greater than about 2. In some embodiments, the resistance is lowered by a factor of greater than about 4 or about 5. The elecfrically conductive coating may have a thickness of between 0.1 mm and 0.8 mm. In an embodiment, the electrically conductive coating may have a thickness of about 0.25 mm. The electrically conductive coating may be coated on low resistance conductors used with other types of heat sources such as, for example, insulated conductor heat sources, elongated member heat sources, etc.

In another embodiment, a cladding may be coupled to low resistance section 584 to reduce the elecfrical resistance in overburden 540. FIG. 86 depicts a cross-sectional view of a portion of cladding section 9200 of conductor-in-conduit heater. Cladding section 9200 may be coupled to the outer surface of low resistance section

584. Cladding sections 9200 may also be coupled to an inner surface of conduit 582. In certain embodiments, cladding sections may be coupled to inner surface of low resistance section 584 and or outer surface of conduit 582. In some embodiments, low resistance section 584 may include one or more sections of individual low resistance sections 584 coupled together. Conduit 582 may include one or more sections of individual conduits 582 coupled together.

Individual cladding sections 9200 may be coupled to each individual low resistance section 584 and/or conduit 582, as shown in FIG. 86. A gap may remain between each cladding section 9200. The gap may be at a location of a coupling between low resistance sections 584 and or conduits 582. For example, the gap may be at a thread or weld junction between low resistance sections 584 and/or conduits 582. The gap may be less than about 4 cm in length. In certain embodiments, the gap may be less than about 5 cm in length or less than 6 cm in length.

Cladding section 9200 may be a conduit (or tubing) of relatively elecfrically conductive material. Cladding section 9200 may be a conduit that tightly fits against a surface of low resistance section 584 and/or conduit 582. Cladding section 9200 may include non-fenomagnetic metals that have a relatively high elecfrical conductivity. For example, cladding section 9200 may include copper, aluminum, brass, bronze, or combinations thereof. Cladding section 9200 may have a thickness between about 0.2 cm and about 1 cm.^' In some embodiments, low resistance section 584 has an outside diameter of about 2.5 cm and conduit 582 has an inside diameter of about 7.3 cm. In an embodiment, cladding section 9200 coupled to low resistance section 584 is copper tubing with a thickness of about 0.32 cm (about 1/8 inch) and an inside diameter of about 2.5 cm. In an embodiment, cladding section 9200 coupled to conduit 582 is copper tubing with a thickness of about 0.32 cm (about 1/8 inch) and an outside diameter of about 7.3 cm. In certain embodiments, cladding section 9200 has a thickness between about 0.20 cm and about 1.2 cm.

In certain embodiments, cladding section 9200 is brazed to low resistance section 584 and/or conduit 582. In other embodiments, cladding section 9200 may be welded to low resistance section 584 and/or conduit 582. In one embodiment, cladding section 9200 is Everdur® (silicon bronze) welded to low resistance section 584 and/or conduit 582. Cladding section 9200 may be brazed or welded to low resistance section 584 and/or conduit 582 depending on the types of materials used in the cladding section, the low resistance conductor, and the conduit. For example, cladding section 9200 may include copper that is Everdur® welded to low resistance section 584, which includes carbon steel. In some embodiments, cladding section 9200 may be pre-oxidized to inhibit conosion of the cladding section during use. Using cladding section 9200 coupled to low resistance section 584 and/or conduit 582 may inhibit a significant temperature rise in the overburden of a foπnation during use of the heat source (i.e., reduce heat losses to the overburden). For example, using a copper cladding section of about 0.3 cm thickness may decrease the elecfrical resistance of a carbon steel low resistance conductor by a factor of about 20. The lowered resistance in the overburden section of the heat source may provide a relatively small temperature increase adjacent to the wellbore in the overburden of the formation. For example, supplying a cunent of about 500 A into an approximately 1.9 cm diameter low resistance conductor (schedule 40 carbon steel pipe) with a copper cladding of about 0.3 cm thickness produces a maximum temperature of about 93 °C at the low resistance conductor. This relatively low temperature in the low resistance conductor may transfer relatively little heat to the formation. For a fixed voltage at the power source, lowering the resistance of the low resistance conductor may increase the transfer of power into the heated section of the heat source (e.g., conductor 580). For example, a 600 volt power supply may be used to supply power to a heat source through about a 300 m overburden and into about a 260 m heated section. This configuration may supply about 980 watts per meter to the heated section. Using a copper cladding section of about 0.3 cm thickness with a carbon steel low resistance conductor may increase the transfer of power into the heated section by up to about 15 % compared to using the carbon steel low resistance conductor only.

In some embodiments, cladding section 9200 may be coupled to conductor 580 and/or conduit 582 by a "tight fit tubing" (TFT) method. TFT is commercially available from vendors such as Kuroki (Japan) or Karasaki

Steel (Japan). The TFT method includes cryogenically cooling an inner pipe or conduit, which is a tight fit to an outer pipe. The cooled inner pipe is inserted into the heated outer pipe or conduit. The assembly is then allowed to return to an ambient temperature. In some cases, the inner pipe can be hydraulically expanded to bond tightly with the outer pipe. Another method for coupling a cladding section to a conductor or a conduit may include an explosive cladding method. In explosive cladding, an inner pipe is slid into an outer pipe. Primer cord or other type of explosive charge may be set off inside the inner pipe. The explosive blast may bond the inner pipe to the outer pipe.

Elecfromagnetically formed cladding may also be used for cladding section 9200. An inner pipe and an outer pipe may be placed in a water bath. Electrodes attached to the inner pipe and the outer pipe may be used to create a high potential between the inner pipe and the outer pipe. The potential may cause sudden formation of bubbles in the bath that bond the inner pipe to the outer pipe.

In another embodiment, cladding section 9200 may be arc welded to a conductor or conduit. For example, copper may be arc deposited and/or welded to a stainless steel pipe or tube. In some embodiments, cladding section 9200 may be formed with plasma powder welding (PPW). PPW formed material may be obtained from Daido Steel Co. (Japan). In PPW, copper powder is heated to form a plasma. The hot plasma may be moved along the length of a tube (e.g., a stainless steel tube) to deposit the copper and form the copper cladding.

Cladding section 9200 may also be formed by billet co-extrusion. A large piece of cladding material may be extruded along a pipe to form a desired length of cladding along the pipe.

In certain embodiments, forge welding (e.g., shielded active gas welding) may be used to form claddings section 9200 on a conductor and or conduit. Forge welding may be used to form a uniform weld through the cladding section and the conductor or conduit.

Another method is to start with strips of copper and carbon steel that are bonded to together by tack welding or another suitable method. The composite strip is drawn through a shaping unit to form a cylindrically shaped tube. The cylindrically shaped tube is seam welded longitudinally. The resulting tube may be coiled onto a spool.

Another possible embodiment for reducing the elecfrical resistance of the conductor in the overburden is to form low resistance section 584 from low resistance metals (e.g., metals that are used in cladding section 9200). A polymer coating may be placed on some of these metals to inhibit conosion of the metals (e.g., to inhibit conosion of copper or aluminum by hydrogen sulfide). Increasing the emissivity of a conductive heat source may increase the efficiency at which heat is transfened to a foπnation. An emissivity of a surface affects the amount of radiative heat emitted from the surface and the amount of radiative heat absorbed by the surface. In general, the higher the emissivity a surface has, the greater the radiation from the surface or the absoφtion of heat by the surface. Thus, increasing the emissivity of a surface increases the efficiency of heat fransfer because of the increased radiation of energy from the surface into the sunoundings. For example, increasing the emissivity of a conductor in a conductor-in-conduit heat source may increase the efficiency at which heat is transfened to the conduit, as shown by the following equation:

■ 2πr. σ( ⁴ - T₂ ^A ) (38) Q = ^{l λ 2 ■} XX)

where, Q is the rate of heat fransfer between a cylindrical conductor and a conduit, r_t is the radius of the conductor, r₂ is the radius of the conduit, Ti is the temperature at the conductor, T₂ is the temperature at the conduit, σ is the Stefan-Boltzmann constant (5.670 X 10^"s J-K^-m^-s^'1), εj is the emissivity of the conductor, and ε₂ is the emissivity of the conduit. According to EQN. 38, increasing the emissivity of the conductor increases the heat transfer between the conductor and the conduit. Accordingly, for a constant heat fransfer rate, increasing the emissivity of the conductor decreases the temperature difference between the conductor and the conduit (i.e., increases the temperature of the conduit for a given conductor temperature). Increasing the temperature of the conduit increases the amount of heat fransfer to the foπnation.

In an embodiment, a conductor and/or conduit may be treated to increase the emissivity of the conductor and or conduit materials. Treating the conductor and/or conduit may include roughening a surface of the conductor or conduit and/or oxidizing the conductor or conduit. In some embodiments, a conductor and/or conduit may be roughened and/or oxidized prior to assembly of a heat source. In some embodiments, a conductor and or conduit may be roughened and/or oxidized after assembly and/or installation into a formation (e.g., an oxidizing fluid may be introduced into an annular space between the conductor and the conduit when heating a portion of the formation to pyrolysis temperature so that the heat generated in the conductor oxidizes the conductor and the conduit). The treatment method may be used to treat inner surfaces and/or outer surfaces, or portions thereof, of conductors or conduits. In certain embodiments, the outer surface of a conductor and the inner surface of a conduit are freated to increase the emissivities of the conductor and the conduit.

In an embodiment, surfaces of a conductor, or a portion of the surface, may be roughened. The roughened surface of the conductor may be the outer surface of the conductor. The surface of the conductor may be roughened by, but is not limited to being roughened by, sandblasting or beadblasting the surface, peening the surface, emery grinding the surface, or using an electrostatic discharge method on the surface. For example, the surface of the conductor may be sand blasted with fine particles to roughen the surface. The conductor may also be freated by pre-oxidizing the surface of the conductor (i.e., heating the conductor to an oxidation temperature before use of the conductor). Pre-oxidizing the surface of the conductor may include heating the conductor to a temperature between about 850 °C and about 950 °C. The conductor may be heated in an oven or furnace. The conductor may be heated in an oxidizing atmosphere (e.g., an oven with a charge of an oxidizing fluid such as air). In an embodiment, a 304H stainless steel conductor is heated in a furnace at a temperature of about 870 °C for about 2 hours. If the surface of the 304H stainless steel conductor is roughened prior to heating the conductor in the furnace, the emissivity of the 304H stainless steel conductor may be increased from about 0.5 to about 0.85. Increasing the emissivity of the conductor may reduce an operating temperature of the conductor. Operating the conductor at lower temperatures may increase an operational lifetime of the conductor. For example, operating the conductor at lower temperatures may reduce creep and/or conosion.

In some embodiments, applying a coating to a conductor or conduit may increase the emissivity of a conductor or a conduit and increase the efficiency of heat transfer to the formation. An elecfrically insulating and thermally conductive coating may be placed on a conductor and/or conduit. The elecfrically insulating coating may inhibit arcing between the conductor and the conduit. Arcing between the conductor and the conduit may cause shorting between the conductor and the conduit. Arcing may also produce hot spots and/or cold spOts on either the conductor or the conduit. In some embodiments, a coating or coatings on portions of a conduit and/or a conductor may increase emissivity, elecfrically insulate, and promote thermal conduction.

As shown in FIG. 65, conductor 580 and conduit 582 may be placed in opening 514 in hydrocarbon layer 516. In an embodiment, an elecfrically insulative, thermally conductive coating is placed on conductor 580 and conduit 582 (e.g., on an outside surface of the conductor and an inside surface of the conduit). In some embodiments, the electrically insulative, thermally conductive coating is placed on conductor 580. In other embodiments, the elecfrically insulative, thermally conductive coating is placed on conduit 582. The electrically insulative, thermally conductive coating may elecfrically insulate conductor 580 from conduit 582. The elecfrically insulative, thermally conductive coating may inhibit arcing between conductor 580 and conduit 582. In certain embodiments, the electrically insulative, thermally conductive coating maintains an emissivity of conductor 580 or conduit 582 (i.e., inhibits the emissivity of the conductor or conduit from decreasing). In other embodiments, the elecfrically insulative, theπnally conductive coating increases an emissivity of conductor 580 and/or conduit 582. The elecfrically insulative, thermally conductive coating may include, but is not limited to, oxides of silicon, aluminum, and zirconium, or combinations thereof. For example, silicon oxide may be used to increase an emissivity of a conductor or conduit while aluminum oxide may be used to provide better electrical insulation and thermal conductivity. Thus, a combination of silicon oxide and aluminum oxide may be used to increase emissivity while providing improved electrical insulation and thermal conductivity. In an embodiment, aluminum oxide is coated on conductor 580 to elecfrically insulate the conductor followed by a coating of silicon oxide to increase the emissivity of the conductor. In an embodiment, the elecfrically insulative, thermally conductive coating is sprayed on conductor 580 or conduit 582. The coating may be sprayed on during assembly of the conductor-in-conduit heat source. In some embodiments, the coating is sprayed on before assembling the conductor-in-conduit heat source. For example, the coating may be sprayed on conductor 580 or conduit 582 by a manufacturer of the conductor or conduit. In certain embodiments, the coating is sprayed on conductor 580 or conduit 582 before the conductor or conduit is coiled onto a spool for installation. In other embodiments, the coating is sprayed on after installation of the conductor-in- conduit heat source.

In a heat source embodiment, a perforated conduit may be placed in the openmg formed in the relatively low permeability formation containing heavy hydrocarbons proximate and external to the conduit of a conductor-in- conduit heater. The perforated conduit may remove fluids formed in an opening in the formation to reduce pressure adjacent to the heat source. A pressure may be maintained in the opening such that deformation of the first conduit is inhibited. In some embodiments, the perforated conduit may be used to introduce a fluid into the formation adjacent to the heat source. For example, in some embodiments, hydrogen gas may be injected into the formation adjacent to selected heat sources to increase a partial pressure of hydrogen during in situ conversion.

FIG. 87 illustrates an embodiment of a conductor-in-conduit heater that may heat a relatively low permeability formation containing heavy hydrocarbons. Second conductor 586 may be disposed in conduit 582 in addition to conductor 580. Second conductor 586 may be coupled to conductor 580 using connector 587 located near a lowermost surface of conduit 582. Second conductor 586 may be a return path for the elecfrical cunent supplied to conductor 580. For example, second conductor 586 may return elecfrical cunent to wellhead 690 through low resistance second conductor 588 in overburden casing 541. Second conductor 586 and conductor 580 may be formed of elongated conductive material. Second condμctor 586 and conductor 580 may be a stainless steel rod having a diameter of approximately 2.4 cm. Connector 587 may be flexible. Conduit 582 may be elecfrically isolated from conductor 580 and second conductor 586 using cenfralizers 581. The use of a second conductor may eliminate the need for a sliding connector. The absence of a sliding connector may extend the life of the heater. The absence of a sliding connector may allow for isolation of applied power from hydrocarbon layer 516.

In a heat source embodiment that utilizes second conductor 586, conductor 580 and the second conductor may be coupled by a flexible connecting cable. The bottom of the first and second conductor may have increased thicknesses to create low resistance sections. The flexible connector may be made of stranded copper covered with rubber insulation.

In a heat source embodiment, a first conductor and a second conductor may be coupled to a sliding connector within a conduit. The sliding connector may include insulating material that inhibits elecfrical coupling between the conductors and the conduit. The sliding connector may accommodate thermal expansion and contraction of the conductors and conduit relative to each other. The sliding connector may be coupled to low resistance sections of the conductors and/or to a low temperature portion of the conduit.

In a heat source embodiment, the conductor may be formed of sections of various metals that are welded or otherwise joined together. The cross-sectional area of the various metals may be selected to allow the resulting conductor to be long, to be creep resistant at high operating temperatures, and/or to dissipate desired amounts of heat per unit length along the entire length of the conductor. For example, a first section may be made of a creep resistant metal (such as, but not limited to, Inconel 617 or HR120), and a second section of the conductor may be made of 304 stainless steel. The creep resistant first section may help to support the second section. The cross- sectional area of the first section may be larger than the cross-sectional area of the second section. The larger cross- sectional area of the first section may allow for greater strength of the first section. Higher resistivity properties of the first section may allow the first section to dissipate the same amount of heat per unit length as the smaller cross- sectional area second section.

In some embodiments, the cross-sectional area and/or the metal used for a particular conduit section may be chosen so that a particular section provides greater (or lesser) heat dissipation per unit length than an adj cent section. More heat may be provided near an interface between a hydrocarbon layer and a non-hydrocarbon layer

(e.g., the overburden and the hydrocarbon layer and/or an underburden and the hydrocarbon layer) to counteract end effects and allow for more unifoπn heat dissipation into the relatively low permeability formation containing heavy hydrocarbons.

In a heat source embodiment, a conduit may have a variable wall thickness. Wall thickness may be thickest adjacent to portions of the foπnation that do not need to be fully heated. Portions of formation that do not need to be fully heated may include layers of formation that have low grade, little, or no hydrocarbon material. In an embodiment of heat sources placed in a formation, a first conductor, a second conductor and a third conductor may be electrically coupled in a 3 -phase Y elecfrical configuration. Each of the conductors may be a part of a conductor-in-conduit heater. The conductor-in-conduit heaters may be located in separate wellbores within the foπnation. The outer conduits may be elecfrically coupled together or conduits may be connected to ground. The 3 -phase Y electrical configuration may provide a safer and more efficient method to heat a relatively low permeability foπnation containing heavy hydrocarbons than using a single conductor. The first, second, and third conduits may be electrically isolated from the first, second, and third conductors. Each conductor-in-conduit heater in a 3 -phase Y elecfrical configuration may be dimensioned to generate approximately 650 watts per meter of conductor to approximately 1650 watts per meter of conductor. Heat may be generated by the conductor-in-conduit heater within an open wellbore. Generated heat may radiatively heat a portion of a relatively low permeability formation containing heavy hydrocarbons adjacent to the conductor-in-conduit heater. To a lesser extent, gas conduction adjacent to the conductor-in-conduit heater heats the portion of the formation. Using an open wellbore completion may reduce casing and packing costs associated with filling the opening with a material to provide conductive heat fransfer between the insulated conductor and the formation. In addition, heat fransfer by radiation may be more efficient than heat fransfer by conduction in a fonnation, so the heaters may be operated at lower temperatures using radiative heat transfer. Operating at a lower temperature may extend the life of the heat source and/or reduce the cost of material needed to form the heat source.

The conductor-in-conduit heater may be installed in opening 514. In an embodiment, the conductor-in- conduit heater may be installed into a well by sections. For example, a first section of the conductor-in-conduit heater may be suspended in a wellbore by a rig. The section may be about 12 m in length. A second section (e.g., of substantially similar length) may be coupled to the first section in the well. The second section may be coupled by welding the second section to the first section and/or with threads disposed on the first and second section. An orbital welder disposed at the wellhead may weld the second section to the first section. The first section may be lowered into the wellbore by the rig. This process may be repeated with subsequent sections coupled to previous sections until a heater of desired length is placed in the wellbore. In some embodiments, three sections may be welded together prior to being placed in the wellbore. The welds may be formed and tested before the rig is used to attach the three sections to a string already placed in the ground. The three sections may be lifted by a crane to the rig. Having three sections already welded together may reduce installation time of the heat source.

Assembling a heat source at a location proximate a formation (e.g., at the site of a formation) may be more economical than shipping a pre-formed heat source and/or conduits to the hydrocarbon formation. For example, assembling the heat source at the site of the formation may reduce costs for transporting assembled heat sources over long distances. In addition, heat sources may be more easily assembled in varying lengths and/or of varying materials to meet specific formation requfrements at the formation site. For example, a portion of a heat source that is to be heated may be made of a material (e.g., 304 stainless steel or other high temperature alloy) while a portion of the heat source in the overburden may be made of carbon steel. Forming the heat source at the site may allow the heat source to be specifically made for an opening in the formation so that the portion of the heat source in the overburden is carbon steel and not a more expensive, heat resistant alloy. Heat source lengths may vary due to varying foπnation layer depths and formation properties. For example, a formation may have a varying thickness and/or may be located underneath rolling tenain, uneven surfaces, and/or an overburden with a varying thickness. Heat sources of varying length and of varying materials may be assembled on site in lengths determined by the depth of each opening in the formation. FIG. 88 depicts an embodiment for assembling a conductor-in-conduit heat source and installing the heat source in a foπnation. The conductor-in-conduit heat source may be assembled in assembly facility 8650. In some embodiments, the heat source is assembled from conduits shipped to the formation site. In other embodiments, heat sources may be made from plate stock that is formed into conduits at the assembly facility. An advantage of forming a conduit at the assembly facility may be that a surface of plate stock may be freated with a desired coating

(e.g., a coating that allows the emissivity to approach one) or cladding (e.g., copper cladding) before forming the conduit so that the treated surface is an inside surface of the conduit. In some embodiments, portions of heat sources may be formed from plate stock at the assembly facility, while other portions of the heat source may be formed from conduits shipped to the formation site. Individual conductor-in-conduit heat source 8652 may include conductor 580 and conduit 582 as shown in

FIG. 89. In an embodiment, conductor 580 and conduit 582 heat sources may be made of a number of joined together sections. In an embodiment, each section is a standard 40 ft (12.2 m) section of pipe. Other section lengths may also be formed and/or utilized. In addition, sections of conductor 580 and/or conduit 582 may be treated in assembly facility 8650 before, during, or after assembly. The sections may be freated, for example, to increase an emissivity of the sections by roughening and/or oxidation of the sections.

Each conductor-in-conduit heat source 8652 may be assembled in an assembly facility. Components of conductor-in-conduit heat source 8652 may be placed on or within individual conductor-in-conduit heat source 8652 in the assembly facility. Components may include, but are not limited to, one or more cenfralizers, low resistance sections, sliding connectors, insulation layers, and coatings, claddings, or coupling materials. As shown in FIG. 88, each individual conductor-in-conduit heat source 8652 may be coupled to at least one individual conductor-in-conduit heat source 8652 at coupling station 8656 to form conductor-in-conduit heat source of desired length 8654. The desired length may be, for example, a length of a conductor-in-conduit heat source specified for a selected opening in a formation. In certain embodiments, coupling individual conductor-in- conduit heat source 8652 to at least one additional individual conductor-in-conduit heat source 8652 includes welding the individual conductor-in-conduit heat source to at least one additional individual conductor-in-conduit heat source. In one embodiment, welding each individual conductor-in-conduit heat source 8652 to an additional individual conductor-in-conduit heat source is accomplished by forge welding two adjacent sections together.

In some embodiments, sections of welded together conductor-in-conduit heat source of desired length 8654 are placed on a bench, holding fray or in an opening in the ground until the entire length of the heat source is completed. Weld integrity may be tested as each weld is formed. For example, weld integrity may be tested by a non-destructive testing method such as x-ray testing, acoustic testing, and/or electromagnetic testing. After an entire length of conductor-in-conduit heat source of desired length 8654 is completed, the conductor-in-conduit heat source of desired length may be coiled onto spool 8660 in a direction of anow 8662. Coiling conductor-in-conduit heat source of desired length 8654 may make the heat source easier to transport to an opening in a formation. For example, conductor-in-conduit heat source of desired length 8654 may be more easily transported by track or train to an opening in the formation.

In some embodiments, a set length of welded together conductor-in-conduit may be coiled onto spool 8660 while other sections are being formed at coupling station 8656. In some embodiments, the assembly facility may be a mobile facility (e.g., placed on one or more train cars or semi-trailers) that can be moved to an opening in a formation. After forming a welded together length of conductor-in-conduit with components (e.g., cenfralizers, coatings, claddings, sliding connectors), the conductor-in-conduit length may be lowered into the opening in the formation.

In certain embodiments, conductor-in-conduit heat source of desired length 8654 may be tested at testing station 8658 before coiling the heat source. Testing station 8658 may be used to test a completed conductor-in- conduit heat source of desfred length 8654 or sections of the conductor-in-conduit heat source of desired length.

Testing station 8658 may be used to test selected properties of conductor-in-conduit heat source of desired length 8654. For example, testing station 8658 may be used to test properties such as, but not limited to, elecfrical conductivity, weld integrity, thermal conductivity, emissivity, and mechanical sfrength. In one embodiment, testing station 8658 is used to test weld integrity with an Electro-Magnetic Acoustic Transmission (EMAT) weld inspection technique.

Conductor-in-conduit heat source of desired length 8654 may be coiled onto spool 8660 for transporting from assembly facility 8650 to an opening in a formation and installation into the opening. In an embodiment, assembly facility 8650 is located at a site of the formation. For example, assembly facility 8650 may be part of a surface facility used to treat fluids from the formation or located a proximate to the formation (e.g., less than about 10 km from the formation or, in some embodiments, less than about 20 km or less than about 30 km). Other types of heat sources (e.g., insulated conductor heat sources, natural disfributed combustor heat sources, etc.) may also be assembled in assembly facility 8650. These other heat sources may also be spooled onto spool 8660, transported to an opening in a formation, and installed into the opening as is described for conductor-in-conduit heat source of desired length 8654. Transportation of conductor-in-conduit heat source of desired length 8654 to an opening in a formation is represented by anow 8664 in FIG. 88. Transporting conductor-in-conduit heat source of desired length 8654 may include transporting the heat source on a bed, frailer, a cart of a truck or train, or a coiled tubing unit. In some embodiments, more than one heat source may be placed on the bed. Each heat source may be installed in a separate opening in the formation. In one embodiment, a train system (e.g., rail system) may be set up to transport heat sources from assembly facility 8650 to each of the openings in the foπnation. In some instances, a lift and move track system may be used in which train tracks are lifted and moved to another location after use in one location. After spool 8660 with conductor-in-conduit heat source of desired length 8654 has been transported to opening 514, the heat source may be uncoiled and installed into the opening in a direction of anow 8666. Conductor-in-conduit heat source of desired length 8654 may be uncoiled from spool 8660 while the spool remains on the bed of a truck or train. In some embodiments, more than one conductor-in-conduit heat source of desired length 8654 may be installed at one time. In one embodiment, more than one heat source may be installed into one opening 514. Spool 8660 may be re-used for additional heat sources after installation of conductor-in-conduit heat source of desired length 8654. In some embodiments, spool 8660 may be used to removed conductor-in-conduit heat source of desired length 8654 from the opening. Conductor-in-conduit heat source of desired length 8654 may be re-coiled onto spool 8660 as the heat source is removed from opening 514. Subsequently, conductor-in-conduit heat source of desired length 8654 may be re-installed from spool 8660 into opening 514 or transported to an alternate opening in the formation and installed the alternate opening.

In certain embodiments, conductor-in-conduit heat source of desired length 8654, or any heat source (e.g., an insulated conductor heat source), may be installed such that the heat source is removable from opening 514. The heat source may be removable so that the heat source can be repaired or replaced if the heat source fails or breaks.

In other instances, the heat source may be removed from the opening and transported and reused in another opening in the formation (or in a different formation) at a later time. Being able to remove, replace, and/or reuse a heat source may be economically favorable for reducing equipment and/or operating costs. In addition, being able to remove and replace an ineffective heater may eliminate the need to form wellbores in close proximity to existing wellbores that have failed heaters in a heated or heating formation. In some embodiments, a conduit of a desired length may be placed into opening 514 before a conductor of the desired length. The conductor and the conduit of the desired length may be assembled in assembly facility 8650. The conduit of the desired length may be installed into opening 514. After installation of the conduit of the desired length, the conductor of the desired length may be installed into opening 514. In an embodiment, the conduit and the conductor of the desired length are coiled onto a spool in assembly facility 8650 and uncoiled from the spool for installation into opening 514. Components (e.g., cenfralizers 581, sliding connectors 583, etc.) may be placed on the conductor or conduit as the conductor is installed into the conduit and opening 514.

In certain embodiments, cenfralizer 581 may include at least two portions coupled together to form the cenfralizer (e.g., "clam shell" cenfralizers). In one embodiment, the portions are placed on a conductor and coupled together as the conductor is installed into a conduit or opening. The portions may be coupled with fastening devices such as, but not limited to, clamps, bolts, screws, snap-locks, and/or adhesive. The portions may be shaped such that a first portion fits into a second portion. For example, an end of the first portion may have a slightly smaller width than an end of the second portion so that the ends overlap when the two portions are coupled.

In some embodiments, low resistance section 584 is coupled to conductor-in-conduit heat source of desired length 8654 in assembly facility 8650. In other embodiments, low resistance section 584 is coupled to conductor- in-conduit heat source of desired length 8654 after the heat source is installed into opening 514. Low resistance section 584 of a desired length may be assembled in assembly facility 8650. An assembled low resistance conductor may be coiled onto a spool. The assembled low resistance conductor may be uncoiled from the spool and coupled to conductor-in-conduit heat source of desired length 8654 after the heat source is installed in opening 514. In another embodiment, low resistance section 584 is assembled as the low resistance conductor is coupled to conductor-in-conduit heat source of desired length 8654 and installed into opening 514. Conductor-in-conduit heat source of desired length 8654 may be coupled to a support after installation so that low resistance section 584 is coupled to the installed heat source.

Assembling a desired length of a low resistance conductor may include coupling individual low resistance conductors together. The individual low resistance conductors may be plate stock conductors obtained from a manufacturer. The individual low resistance conductors may be coupled to an elecfrically conductive material to lower the electrical resistance of the low resistance conductor. The electrically conductive material may be coupled to the individual low resistance conductor before assembly of the desired length of low resistance conductor. In one embodiment, the individual low resistance conductors may have threaded ends that are coupled together. In another embodiment, the individual low resistance conductors may have ends that are welded together. Ends of the individual low resistance conductors may be shaped such that an end of a first individual low resistance conductor fits into an end of a second individual low resistance conductor. For example, an end of a first individual low resistance conductor may be a female-shaped end while an end of a second individual low resistance conductor is a male-shaped end.

In another embodiment, a conductor-in-conduit heat source of a desired length may be assembled at a wellbore (or opening) in a formation and installed into the wellbore as the conductor-in-conduit heat source is assembled. Individual conductors may be coupled to form a first section of a conductor of desired length. Similarly, conduits may be coupled to form a first section of a conduit of desired length. The first formed sections of the conductor and the conduit may be installed into the wellbore. The first formed sections of the conductor and the conduit may be electrically coupled at a first end that is installed into the wellbore. The first sections of the conductor and conduit may, in some embodiments, be coupled substantially simultaneously. Additional sections of the conductor and/or conduit may be formed during or after installation of the first formed sections. The additional sections of the conductor and/or conduit may be coupled to the first formed sections of the conductor and/or conduit and installed into the wellbore. Cenfralizers and/or other components may be coupled to sections of the conductor and/or conduit and installed with the conductor and the conduit into the wellbore.

A method for coupling conductors or conduits may include a forge welding method (e.g., shielded active gas (SAG) welding). In an embodiment, forge welding includes ananging ends of the conductors and/or conduits that are to be interconnected at a selected distance. Seals may be formed against walls of the conduit and/or conductor to define a chamber. A flushing, reducing fluid may be introduced into the chamber. Each end within the chamber may be heated and moved towards another end until the heated ends contact each other. Contacting the heated ends may form a forge weld between the heated ends. The flushing, reducing fluid mixture may include less than 25% by volume of a reducing agent and more than 75% by volume of a substantially inert gas. The flushing, reducing fluid may inhibit oxidation reactions that can adversely affect weld integrity.

A flushing fluid mixture with less than 25% by volume of a reducing fluid (e.g., hydrogen and/or carbon monoxide) and more than 75% by volume of a substantially inert gas (e.g., nifrogen, argon, and/or carbon dioxide) may be non-explosive when the flushing fluid mixture comes into contact with air at elevated temperatures needed to form the forge weld. In some embodiments, the reducing agent may be or include borax powder and/or beryllium or alkaline hydrites. The flushing fluid mixture may contain a sufficient amount of a reducing gas to flush off oxidized skin from the hot ends that are to be interconnected. In some embodiments, the non-explosive flushing fluid mixture includes between 2% by volume and 10% by volume of the reducing fluid and between 90% by volume and 98% by volume of the substantially inert gas. In certain embodiments, the mixture includes about 5% by volume of the reducing fluid and about 95% by volume of the substantially inert gas. In one embodiment, a non-explosive flushing fluid mixture includes about 95% by volume of nifrogen and about 5% by volume of hydrogen. The non-explosive flushing fluid mixture may also include less than 100 ppm H2O and/or O2 or, in some cases, less than 15 ppm H2O and/or O2.

A substantially inert gas used during a forge welding procedure is a gas that does not significantly react with the metals to be forged welded at the pressures and temperatures used during forge welding. Substantially inert gas may be, but is not limited to, noble gases (e.g., helium and argon), nifrogen or combinations thereof. A non-explosive flushing fluid mixture may be formed in-situ within the chamber. A coating on the conduits and/or conductors may be present and/or a solid may be placed in the chamber. When the conduits and/or conductors are heated, the coating and or solid may be react or physically transform to the flushing fluid mixture. In an embodiment, ends of conductors or conduits are heated by means of high frequency elecfrical heating. The ends may be maintained at a predetermined spacing of between 1 mm and 4 mm from each other by a gripping assembly while being heated. Electrical contacts may be pressed at circumferentially spaced intervals against the wall of each conduit and or conductor adjacent to the end such that the elecfrical contacts fransmit a high frequency elecfrical cunent in a substantially circumferential direction in the segment between the electrical contacts. To equalize the level of heating in a circumferential direction, each end may be heated by at least two pairs of elecfrodesl The elecfrodes of each pair may be pressed at substantially diametrically opposite positions against walls of the conduits and/or conductors. The different pairs of elecfrodes at each end may be activated in an alternating manner. In one embodiment, two pairs of diametrically opposite elecfrodes are pressed at angular intervals of substantially 90° against walls of the conductors and conduits. In another embodiment, three pahs of diametrically opposite elecfrodes are pressed at angular intervals of substantially 60° against the walls of the conductors and conduits. In other embodiments, four, five, six or more pairs of diametrically opposite elecfrodes may be used and activated in an alternating manner to equalize the level of heating of the ends in the circumferential direction. The use of two or more pairs of elecfrodes may reduce unequal heating of the pipe ends because of over heating of the walls in the direct vicinity of the electrode. In addition, using two or more pairs of electrodes may reduce heating of the pipe wall halfway between the elecfrodes.

In another embodiment, the ends may be heated by a direct resistance heating method. The direct resistance heating method may include transmitting a large cunent in an axial direction across the conduits and/or conductors while the conduits and/or conductors are pressed together. In another embodiment, the ends may be heated by induction heating. Induction heating may include using external and/or internal heating coils to create an electromagnetic field that induces electrical cunents in the conduits and/or conductors. The electrical cunents may resistively heat the conduits.

The heating assembly may be used to give the forge welded ends a post weld heat freatment. The post weld heat freatment may include providing at least some heating to the ends such that the ends are cooled down at a predetermined temperature decrease rate (i.e., cool down rate). In some embodiments, the assembly may be equipped with water and/or forced air injectors to increase and/or confrol the cool down rate of the forge welded ends.

In certain embodiments, the quality of the forge weld formed between the interconnected conduits and/or conductors is inspected by means of an Electro-Magnetic Acoustic Transmission weld inspection technique

(EMAT). EMAT may include placing at least one electromagnetic coil adjacent to both sides of the forge welded joint. The coil may be held at a predetermined distance from the conduits and/or conductors during the inspection process. The absence of physical contact between the wall of the hot conduits and or conductors and the coils of the EMAT inspection tool may enable weld inspection immediately after the forge weld joint has been made. FIG. 90 shows an end of tubular 9150 around which two pairs of diametrically opposite electrodes 9152,

9153 and 9154, 9155 are ananged. Tubular 9150 may be a conduit or conductor. Tubular 9150 may be made of elecfrically conductive material (e.g., stainless steel). The first pair of elecfrodes 9152, 9153 may be pressed against the outer surface of tubular 9150 and fransmit high frequency cunent 9156 through the wall of the tubular as illusfrated by anows 9157. An assembly of fenite bars 9158 may serve to enhance the cunent density in the immediate vicinity of the ends of the tubular 9150 and of the adjacent tubular to which tubular 9150 is to be welded.

FIG. 91 depicts an embodiment with ends 9162, 9162A of two adjacent tubulars 9150 and 9150A. Tubulars 9150 and 9150A may be heated by two sets of diametrically opposite elecfrodes 9152, 9153, 9154, 9155 and 9152A, 9153A, 9154A and 9155A, respectively. Tubular ends 9162 and 9162A may be located at a few millimeters distant from each other during a heating phase. The larger spacing of cunent density anows 9157 midway between electrodes 9152, 9153 illustrates that the cunent density midway between these electrodes may be lower than the cunent density adjacent to each of the elecfrodes. The lower cunent density midway between the elecfrodes may create a variation in the heating rate of the tubular ends 9162 and 9162 A. To reduce a possible frregular heating rate, elecfrodes 9152, 9153 and 9152A, 9153 A may be regularly lifted from the outer surface of tubulars 9150, 9150A while the other elecfrodes 9154, 9154A and 9155, 155A are pressed against the outer surface of the tubulars 9150, 9150A and activated to fransmit a high frequency cunent through the ends of the tubulars. By sequentially activating the two sets of diametrically opposite elecfrodes at each tubular end, frregular heating of the tubular ends may be inhibited (i.e., heating of the tubular ends may be more unifoπn).

All elecfrodes 9152-9155 and 9152A-9155A shown in FIG. 91 may be pressed simultaneously against tubular ends 9150 and 9150A if alternating cunent supplied to the electrodes is controlled such that during a first part of a cunent cycle the diametrically opposite electrode pairs 9152A, 9153A and 9154, 9155 transmit a positive elecfrical cunent as indicated by the "+" sign in FIG. 91, whereas elecfrodes 9152, 9153, and 9154A, 9155A fransmit a negative elecfrical cunent as indicated by the "-" sign. During a second part of the alternating cunent cycle, elecfrodes 9152A, 9153A, and 9154, 9155 transmit a negative electrical cunent, whereas elecfrodes 9152, 9153, and 9154A, 9155A fransmit a positive cunent into tubulars 9150 and 9150A. Controlling the alternating cunent in this manner may heat tubular ends 9162 and 9162A in a substantially unifoπn manner. The temperature of heated tubular ends 9162, 9162A may be monitored by an infrared temperature sensor.

When the monitored temperature has reached a temperature sufficient to make a forge weld, tubular ends 9162, 9162A may be pressed onto each other such that a forge weld is made. Tubular ends 9162, 9162A may be profiled and have a smaller wall thickness than other parts of tubulars 9150, 9150A to compensate for the deformation of the tubular ends when the ends are abutted. Profiling the tubular ends may allow tubulars 9150, 9150A to have a substantially uniform wall thickness at forge welded ends.

During the heating phase and while the ends of tubulars 9150, 9150A are moved towards each other, the tubular ends may be encased, both internally and externally, in a chamber 9168. Chamber 9168 may be filled with a non-explosive flushing fluid mixture. The non-explosive flushing fluid mixture may include more than 75% by volume of nifrogen and less than 25% by volume of hydrogen. In one embodiment, the non-explosive flushing fluid mixture for interconnecting steel tubulars 9150, 9150A includes about 5% by volume of hydrogen and about

95% by volume of nitrogen. The flushing fluid pressure in a part of chamber 9168 outside the tubulars 9150 and 9150A may be higher than the flushing fluid pressure in a part of the chamber 9168 within the interior of the tubulars such that throughout the heating process the flushing fluid flows along the ends of the tubulars as illusfrated by anows 9169 until the ends of the tubulars are forged together. In some embodiments, flushing fluid may flow through the chamber.

Hydrogen in the flushing fluid may react with oxidized metal on the ends 9162, 9162A of the tubulars 9150, 9150A so that formation of an oxidized skin is inhibited. Inhibition of an oxidized skin may allow formation of a forge weld with minimal amounts of conoded metal inclusions.

Laboratory experiments reveal that a good metallurgical bond between stainless steel tubulars may be obtained by forge welding with a flushing fluid containing about 5% by volume of hydrogen and about 95% by volume of nifrogen. Experiments also show that such a flushing fluid mixture may be non-explosive during and after forge welding. Two forge welded stainless steel tubulars failed during at a location away from the forge weld when the tubulars were subjected to testing.

In an embodiment, the tubular ends are clamped throughout the forge welding process to a gripping assembly. Clamping the tubular ends may maintain the tubular ends at a predetermined spacing of between 1 mm and 4 mm from each other during the heating phase. The gripping assembly may include a mechanical stop that interrupts axial movement of the heated tubular ends during the forge welding process after the heated tubular ends have moved a predetermined distance towards each other. The heated tubular ends may be pressed into each other such that a high quality forge weld is created without significant deformation of the heated ends.

In certain embodiments, electrodes 9152-9155 and 9152A-9155A may also be activated to give the forged tubular ends a post weld heat freatment. Elecfrical power 9156 supplied to the elecfrodes during the post weld heat treatment may be lower than during the heat up phase before the forge welding operation. Electrical power 9156 supplied during the post weld heat freatment may be confrolled in conjunction with temperature measured by an infrared temperature sensor(s) such that the temperature of the forge welded tubular ends is decreased in accordance with a predeteπnined temperature decrease or cooling cycle. The quality of the forge weld may be inspected by a hybrid electromagnetic acoustic transmission technique which is known as EMAT. EMAT is described in U.S. Patent Nos. 5,652,389 to Schaps et al., 5,760,307 to Latimer et al., 5,777,229 to Geier et al., and 6,155,117 to Stevens et al., each of which is incoφorated by reference as if fully set forth herein. The EMAT technique makes use of an induction coil placed at one side of the welded joint. The induction coil may induce magnetic fields that generate electromagnetic forces in the surface of the welded joint. These forces may produce a mechanical disturbance by coupling to the atomic lattice through a scattering process. In electromagnetic acoustic generation, the conversion may take place within a skin depth of material (i.e., the metal surface acts as a transducer). The reception may take place in a reciprocal way in a receiving coil. When the elastic wave strikes the surface of the conductor in the presence of a magnetic field, induced cunents may be generated in the receiving coil, similar to the operation of an electric generator. An advantage of the EMAT weld inspection technology is that the inductive transmission and receiving coils do not have to contact the welded tubular. Thus, the inspection may be done soon after the forge weld is made (e.g., when the forge welded tubulars are still too hot to allow physical contact with an inspection probe).

Using the SAG method to weld tubular ends of heat sources may inhibit changes in the metallurgy of the tubular materials. For example, the elemental composition of the weld joint may be substantially similar to the elemental composition of the tubulars. Inhibiting changes in metallurgy may reduce the need for heat-treatment of the tubulars before use of the tubulars. The SAG method also appears not to change the grain structure of the near- weld section of the tubulars. Maintaining the grain structure of the tubulars may inhibit conosion and/or creep in the tubulars during use.

FIG. 92 illustrates an end view of an embodiment of a conductor-in-conduit heat source heated by diamefrically opposite electrodes. Conductor 580 may be placed within conduit 582. Conductor 580 may be heated by two sets of diamefrically opposite electrodes 9152, 9153, 9154, 9155. Conduit 582 may be heated by two sets of diametrically opposite elecfrodes 9172, 9173, 9174, 9175. Conductor 580 and conduits 582 may be heated and forge welded together as described in the embodiments of FIGS. 90-91. In some embodiments, two ends of conductors 580 are forged welded together and then two ends of conduits 582 are forged together in a second procedure.

FIG. 93 illustrates a cross-sectional representation of an embodiment of two sections of a conductor-in- conduit heat source before being forge welded. During heating of conductors 580, 580A and conduits 582, 582A and while the ends of the conductors and the conduits are moved towards each other, ends of the conductors and conduits may be encased in a chamber 9176. Chamber 9176 may be filled with the non-explosive flushing fluid mixture. Plugs 9178, 9178A may be placed in the annular space between conductors 580, 580A and conduits 582,

582A. In an embodiment, the plugs may be inflated to seal the annular space. Plugs 9178, 9178A may inhibit the flow of the flushing fluid mixture through the annular space between conductors 580, 580A and conduits 582, 582A. The flushing fluid pressure in a part of chamber 9176 outside the conduits 582, 582A may be higher than the flushing fluid pressure inside the conduits and outside conductors 580, 580A. Similarly, the flushing fluid pressure outside conductors 580, 580A may be higher than the flushing fluid pressure inside the conductors. Due to the pressure differentials throughout the heating process, the flushing fluid tends to flow along the ends of the tubulars as illusfrated by anows 9179 until the ends of the conductors and conduits are forged together.

FIG. 94 depicts an embodiment of three horizontal heat sources placed in a foπnation. Wellbore 9632 may be formed through overburden 540 and into hydrocarbon layer 516. Wellbore 9632 may be formed by any standard drilling method. In certain •embodiments, wellbore 9632 is formed substantially horizontally in hydrocarbon layer 516. In some embodiments, wellbore 9632 may be formed at other angles within hydrocarbon layer 516.

One or more conduits 9634 may be placed within wellbore 9632. A portion of wellbore 9632 and/or second wellbores may include casings. Conduit 9634 may have a smaller diameter than wellbore 9632. In an embodiment, wellbore 9632 has a diameter of about 30.5 cm and conduit 9634 has a diameter of about 14 cm. In an embodiment, an inside diameter of a casing in conduit 9634 may be about 12 cm. Conduits 9634 may have extended sections 9635 that extend beyond the end of wellbore 9632 in hydrocarbon layer 516. Extended sections

9635 may be formed in hydrocarbon layer 516 by drilling or other wellbore forming methods. In an embodiment, extended sections 9635 extend substantially horizontally into hydrocarbon layer 516. In certain embodiments, extended sections 9635 may somewhat diverge as represented in FIG. 94.

Perforated casings 9636 may be placed in extended sections 9635 of conduits 9634. Perforated casings 9636 may provide support for the extended sections so that collapse of wellbores is inhibited during heating of the foπnation. Perforated casings 9636 may be steel (e.g., carbon steel or stainless steel). Perforated casings 9636 may be perforated liners that expand within the wellbores (expandable tubulars). Expandable tubulars are described in U.S. Patent Nos. 5,366,012 to Lohbeck, and 6,354,373 to Vercaemer et al., each of which is incoφorated by reference as if fully set forth herein. In an embodiment, perforated casings 9636 are formed by inserting a perforated casing into each of extended sections 9635 and expanding the perforated casing within each extended section. The perforated casing may be expanded by pulling an expander tool shaped to push the perforated casing towards the wall of the wellbore (e.g., a pig) along the length of each extended section 9635. The expander tool may push each perforated casing beyond the yield point of the perforated casing.

After installation of perforated casings 9636, heat sources 9638 may be installed into extended sections 9635. Heat sources 9638 may be used to provide heat to hydrocarbon layer 516 along the length of extended sections 9635. Heat sources 9638 may include heat sources such as conductor-in-conduit heaters, insulated conductor heaters, etc. In some embodiments, heat sources 9638 have a diameter of about 7.3 cm. Perforated casings 9636 may allow for production of formation fluid from the heat source wellbores. Installation of heat sources 9638 in perforated casings 9636 may also allow the heat sources to be removed at a later time. Heat sources 9638 may, for example, be removed for repair, replacement, and/or used in another portion of a formation.

In an embodiment, an elongated member may be disposed within an opening (e.g., an open wellbore) in a relatively low permeability formation containing heavy hydrocarbons. The opening may be an uncased openmg in the relatively low permeability formation containing heavy hydrocarbons. The elongated member may be a length

(e.g., a strip) of metal or any other elongated piece of metal (e.g., a rod). The elongated member may include stainless steel. The elongated member may be made of a material able to withstand conosion at high temperatures within the opening. An elongated member may be a bare metal heater. "Bare metal" refers to a metal that does not include a layer of elecfrical insulation, such as mineral insulation, that is designed to provide elecfrical insulation for the metal throughout an operating temperature range of the elongated member. Bare metal may encompass a metal that includes a conosion inhibiter such as a naturally occuning oxidation layer, an applied oxidation layer, and/or a film. Bare metal includes metal with polymeric or other types of elecfrical insulation that cannot retain electrical insulating properties at typical operating temperature of the elongated member. Such material may be placed on the metal and may be thermally degraded during use of the heater.

An elongated member may have a length of about 650 m. Longer lengths may be achieved using sections of high sfrength alloys, but such elongated members may be expensive. In some embodiments, an elongated member may be supported by a plate in a wellhead. The elongated member may include sections of different conductive materials that are welded together end-to-end. A large amount of elecfrically conductive weld material may be used to couple the separate sections together to increase sfrength of the resulting member and to provide a path for elecfricity to flow that will not result in arcing and/or conosion at the welded connections. In some embodiments, different sections may be forge welded together. The different conductive materials may include alloys with a high creep resistance. The sections of different conductive materials may have varying diameters to ensure uniform heating along the elongated member. A first metal that has a higher creep resistance than a second metal typically has a higher resistivity than the second metal. The difference in resistivities may allow a section of larger cross-sectional area, more creep resistant first metal to dissipate the same amount of heat as a section of smaller cross-sectional area second metal. The cross-sectional areas of the two different metals may be tailored to result in substantially the same amount of heat dissipation in two welded together sections of the metals. The conductive materials may mclude, but are not limited to, 617 Inconel, HR-I20, 316 stainless steel, and 304 stainless steel. For example, an elongated member may have a 60 meter section of 617 Inconel, 60 meter section of HR-120, and 150 meter section of 304 stainless steel. In addition, the elongated member may have a low resistance section that may run from the wellhead through the overburden. This low resistance section may decrease the heating within the formation from the wellhead through the overburden. The low resistance section may be the result of, for example, choosing a elecfrically conductive material and/or increasing the cross-sectional area available for elecfrical conduction.

In a heat source embodiment, a support member may extend through the overburden, and the bare metal elongated member or members may be coupled to the support member. A plate, a cenfralizer, or other type of support member may be located near an interface between the overburden and the hydrocarbon layer. A low resistivity cable, such as a stranded copper cable, may extend along the support member and may be coupled to the elongated member or members. The low resistivity cable may be coupled to a power source that supplies elecfricity to the elongated member or members.

FIG. 95 illustrates an embodiment of a plurality of elongated members that may heat a relatively low permeability formation containing heavy hydrocarbons. Two or more (e.g., four) elongated members 600 may be supported by support member 604. Elongated members 600 may be coupled to support member 604 using insulated cenfralizers 602. Support member 604 may be a tube or conduit. Support member 604 may also be a perforated tube. Support member 604 may provide a flow of an oxidizing fluid into opening 514. Support member 604 may have a diameter between about 1.2 cm to about 4 cm and, in some embodiments, about 2.5 cm. Support member 604, elongated members 600, and insulated cenfralizers 602 may be disposed in opening 514 in hydrocarbon layer 516. Insulated cenfralizers 602 may maintain a location of elongated members 600 on support member 604 such that lateral movement of elongated members 600 is inhibited at temperatures high enough to deform support member 604 or elongated members 600. Elongated members 600, in some embodiments, may be metal strips of about 2.5 cm wide and about 0.3 cm thick stainless steel. Elongated members 600, however, may also include a pipe or a rod formed of a conductive material. Elecfrical cunent may be applied to elongated members 600 such that elongated members 600 may generate heat due to elecfrical resistance.

Elongated members 600 may generate heat of approximately 650 watts per meter of elongated members 600 to approximately 1650 watts per meter of elongated members 600. Elongated members 600 may be at temperatures of approximately 480 °C to approximately 815 °C. Substantially uniform heating of a relatively low peπneability formation containing heavy hydrocarbons may be provided along a length of elongated members 600 or greater than about 305 m or, maybe even greater than about 610 m.

Elongated members 600 may be electrically coupled in series. Elecfrical cunent may be supplied to elongated members 600 using lead-in conductor 572. Lead-in conductor 572 may be coupled to wellhead 690. Elecfrical cunent may be returned to wellhead 690 using lead-out conductor 606 coupled to elongated members 600. Lead-in conductor 572 and lead-out conductor 606 may be coupled to wellhead 690 at surface 550 through a sealing flange located between wellhead 690 and overburden 540. The sealing flange may inhibit fluid from escaping from opening 514 to the surface 550 and/or atmosphere. Lead-in conductor 572 and lead-out conductor 606 may be coupled to elongated members using a cold pin fransition conductor. The cold pin transition conductor may include an insulated conductor of low resistance. Little or no heat may be generated in the cold pin fransition conductor. The cold pin fransition conductor may be coupled to lead-in conductor 572, lead-out conductor 606, and/or elongated members 600 by splices, mechanical connections and/or welds. The cold pin fransition conductor may provide a temperature transition between lead-in conductor 572, lead-out conductor 606, and/or elongated members 600. Lead-in conductor 572 and lead-out conductor 606 may be made of low resistance conductors so that substantially no heat is generated from elecfrical cunent passing through lead-in conductor 572 and lead-out conductor 606. Weld beads may be placed beneath the cenfralizers 602 on support member 604 to fix the position of the cenfralizers. Weld beads may be placed on elongated members 600 above the uppermost centralizer to fix the position of the elongated members relative to the support member (other types of connecting mechanisms may also be used). When heated, the elongated member may thermally expand downwards. The elongated member may be formed of different metals at different locations along a length of the elongated member to allow relatively long lengths to be formed. For example, a "U" shaped elongated member may include a first length formed of 310 stainless steel, a second length formed of 304 stainless steel welded to the first length, and a third length formed of 310 stainless steel welded to the second length. 310 stainless steel is more resistive than 304 stainless steel and may dissipate approximately 25% more energy per unit length than 304 stainless steel of the same dimensions. 310 stainless steel may be more creep resistant than 304 stainless steel. The first length and the third length may be formed with cross-sectional areas that allow the first length and third lengths to dissipate as much heat as a smaller cross-sectional area of 304 stainless steel. The first and third lengths may be positioned close to wellhead 690. The use of different types of metal may allow the formation of long elongated members. The different metals may be, but are not limited to, 617 Inconel, HR120, 316 stainless steel, 310 stainless steel, and 304 stainless steel.

Packing material 542 may be placed between overburden casing 541 and opening 514. Packing material 542 may inhibit fluid flowing from opening 514 to surface 550 and to inhibit conesponding heat losses towards the surface. In some embodiments, overburden casing 541 may be placed in cement 544 in overburden 540. In other embodiments, overburden casing may not be cemented to the formation. Surface conductor 545 may be disposed in cement 544. Support member 604 may be coupled to wellhead 690 at surface 550. Cenfralizer 581 may maintain a location of support member 604 within overburden casing 541. Elecfrical cunent may be supplied to elongated members 600 to generate heat. Heat generated from elongated members 600 may radiate within opening 514 to heat at least a portion of hydrocarbon layer 516.

The oxidizing fluid may be provided along a length of the elongated members 600 from oxidizing fluid source 508. The oxidizing fluid may inhibit carbon deposition on or proximate the elongated members. For example, the oxidizing fluid may react with hydrocarbons to form carbon dioxide. The carbon dioxide may be removed from the opening. Openings 605 in support member 604 may provide a flow of the oxidizing fluid along the length of elongated members 600. Openings 605 may be critical flow orifices. In some embodiments, a conduit may be disposed proximate elongated members 600 to confrol the pressure in the formation and/or to introduce an oxidizing fluid into opening 514. Without a flow of oxidizing fluid, carbon deposition may occur on or proxhnate elongated members 600 or on insulated cenfralizers 602. Carbon deposition may cause shorting between elongated members 600 and insulated cenfralizers 602 or hot spots along elongated members 600. The oxidizing fluid may be used to react with the carbon in the formation. The heat generated by reaction with the carbon may complement or supplement elecfrically generated heat.

In a heat source embodiment, a bare metal elongated member may be formed in a "U" shape (or hafrpin) and the member may be suspended from a wellhead or from a positioner placed at or near an interface between the overburden and the formation to be heated. In certain embodiments, the bare metal heaters are formed of rod stock. Cylindrical, high alumina ceramic elecfrical insulators may be placed over legs of the elongated members. Tack welds along lengths of the legs may fix the position of the insulators. The insulators may inhibit the elongated member from contacting the formation or a well casing (if the elongated member is placed within a well casing). The insulators may also inhibit legs of the "U" shaped members from contacting each other. High alumina ceramic electrical insulators may be purchased from Cooper Industries (Houston, Texas). In an embodiment, the "U" shaped member may be formed of different metals having different cross-sectional areas so that the elongated members may be relatively long and may dissipate a desired amount of heat per unit length along the entire length of the elongated member.

Use of welded together sections may result in an elongated member that has large diameter sections near a top of the elongated member and a smaller diameter section or sections lower down a length of the elongated member. For example, an embodiment of an elongated member has two 7/8 inch (2.2 cm) diameter first sections, two 1/2 inch (1.3 cm) middle sections, and a 3/8 inch (0.95 cm) diameter bottom section that is bent into a "U" shape. The elongated member may be made of materials with other cross-sectional shapes such as ovals, squares, rectangles, triangles, etc. The sections may be formed of alloys that will result in substantially the same heat dissipation per unit length for each section. In some embodiments, the cross-sectional area and or the metal used for a particular section may be chosen so that a particular section provides greater (or lesser) heat dissipation per unit length than an adjacent section. More heat dissipation per unit length may be provided near an interface between a hydrocarbon layer and a non- hydrocarbon layer (e.g., the overburden and the hydrocarbon layer) to counteract end effects and allow for more uniform heat dissipation into the relatively low permeability formation containing heavy hydrocarbons. A higher heat dissipation may also be located at a lower end of an elongated member to counteract end effects and allow for more uniform heat dissipation. In certain embodiments, the wall thickness of portions of a conductor, or any electrically-conducting portion of a heater, may be adjusted to provide more or less heat to certain zones of a formation. In an embodiment, the wall thickness of a portion of the conductor adjacent to a lean zone (i.e., zone containing relatively little or no hydrocarbons) may be thicker than a portion of the conductor adjacent to a rich zone (i.e., hydrocarbon layer in which hydrocarbons are pyrolyzed and/or produced). Adjusting the wall thickness of a conductor to provide less heat to the lean zone and more heat to the rich zone may more efficiently use elecfricity to heat the formation.

FIG. 96 illustrates a cross-sectional representation of an embodiment of a heater using two oxidizers. One or more oxidizers may be used to heat a hydrocarbon layer or hydrocarbon layers of a formation having a relatively shallow depth (e.g., less than about 250 m). Conduit 6110 may be placed in opening 514 in a formation. Conduit 6110 may have upper portion 6112. Upper portion 6112 of conduit 6110 may be placed primarily in overburden

540 of the fonnation. A portion of conduit 6110 may include high temperature resistant, non-conosive materials (e.g., 316 stainless steel and/or 304 stainless steel). Upper portion 6112 of conduit 6110 may include a less temperature resistant material (e.g., carbon steel). A diameter of opening 514 and conduit 6110 may be chosen such that a cross-sectional area of opening 514 outside of conduit 6110 is approximately equal to a cross-sectional area inside conduit 6110. This may equalize pressures outside and inside conduit 6110. In an embodiment, conduit

6110 has a diameter of about 0.11 m and opening 514 has a diameter of about 0.15 m.

Oxidizing fluid source 508 may provide oxidizing fluid 517 into conduit 6110. Oxidizing fluid 517 may include hydrogen peroxide, air, oxygen, or oxygen enriched air. In an embodiment, oxidizing fluid source 508 may include a membrane system that enriches air by preferentially passing oxygen, instead of nifrogen, through a membrane or membranes. First fuel source 6119 may provide fuel 6118 into first fuel conduit 6116. First fuel conduit 6116 may be placed in upper portion 6112 of conduit 6110. hi some embodiments, first fuel conduit 6116 may be placed outside conduit 6110. In other embodiments, conduit 6110 may be placed within first fuel conduit 6116. Fuel 6118 may include combustible material, including but not limited to, hydrogen, methane, ethane, other hydrocarbon fluids, and/or combinations thereof. Fuel 6118 may include steam to inhibit coking within the fuel conduit or proximate an oxidizer. First oxidizer 6120 may be placed in conduit 6110 at a lower end of upper portion 6112. First oxidizer 6120 may oxidize at least a portion of fuel 6118 from first fuel conduit 6116 with at least a portion of oxidizing fluid 517. First oxidizer may be a burner such as an inline burner. Burners may be obtained from John Zink Company (Tulsa, Oklahoma) or Callidus Technologies (Tulsa, Oklahoma). First oxidizer 6120 may include an ignition source such as a flame. First oxidizer 6120 may also include a flameless ignition source such as, for example, an electric igniter.

In some embodhnents, fuel 6118 and oxidizing fluid 517 may be combined at the surface and provided to opening 514 through conduit 6110. Fuel 6118 and oxidizing fluid 517 may be combined in a mixer, aerator, nozzle, or similar mixing device located at the surface. In such an embodiment, conduit 6110 provides both fuel 6118 and oxidizing fluid 517 into opening 514. Locating first oxidizer 6120 at or proximate the upper portion of the section of the formation to be heated may tend to inhibit or decrease coking in one or more of the fuel conduits (e.g., in first fuel conduit 6116).

Oxidation of fuel 6118 at first oxidizer 6120 will generate heat. The generated heat may heat fluids in a region proximate first oxidizer 6120. The heated fluids may include fuel, oxidizing fluid, and oxidation products. The heated fluids may be allowed to fransfer heat to hydrocarbon layer 6100 along a length of conduit 6110. The amount of heat transfened from the heated fluids to the formation may vary depending on, for example, a temperature of the heated fluids. In general, the greater the temperature of the heated fluids, the more heat that will be fransfened to the formation. In addition, as heat is transfened from the heated fluids, the temperature of the heated fluids decreases. For example, temperatures of fluids in the oxidizer flame may be about 1300 °C or above, and as the fluids reach a distance of about 150 m from the oxidizer, temperatures of fluids may be, for example, about 750 °C. Thus, the temperature of the heated fluids, and hence the heat fransfened to the formation, decreases as the heated fluids flow away from the oxidizer.

First insulation 6122 may be placed on lengths of conduit 6110 proximate a region of first oxidizer 6120. First insulation 6122 may have a length of about 10 m to about 200 m (e.g., about 50 m). In alternative embodiments, first insulation 6122 may have a length that is about 10-40% of the length of conduit 6110 between any two oxidizers (e.g., between first oxidizer 6120 and second oxidizer 6130 in FIG. 96). A length of first insulation 6122 may vary depending on, for example, desired heat fransfer rate to the formation, desired temperature proximate the first oxidizer, and/or desired temperature profile along the length of conduit 6110. First insulation 6122 may have a thickness that varies (either continually or in step fashion) along its length. In certain embodiments, first insulation 6122 may have a greater thickness proximate first oxidizer 6120 and a reduced thickness at a desired distance from the first oxidizer. The greater thickness of first insulation 6122 may preferentially reduce heat fransfer proximate ffrst oxidizer 6120 as compared to a reduced thickness portion of the insulation. Variable thickness insulation may allow for uniform or relatively uniform heating of the formation adjacent to a heated portion of the heat source. In an embodiment, first insulation 6122 may have a thickness of about 0.03 m proximate first oxidizer 6120 and a thickness of about 0.015 m at a distance of about 10 m from the first oxidizer. In the embodiment, the heated portion of the conduit is about 300 m in length, with insulation (first insulation 6122) being placed proximate the upper 100 m portion of this length, and insulation (second insulation

6132) being placed proximate the lower 100 m portion of this length.

A thickness of first insulation 6122 may vary depending on, for example, a desfred heating rate or a desired temperature within opening 514 of hydrocarbon layer 6100. The first insulation may inhibit the fransfer of heat from the heated fluids to the formation in a region proximate the insulating conduit. First insulation 6122 may also inhibit chaning and/or coking of hydrocarbons proximate first oxidizer 6120. First insulation 6122 may inhibit chaning and/or coking by reducing an amount of heat fransfened to the formation proximate the first oxidizer. First insulation 6122 may inhibit or decrease coking in conduit 6128 when a carbon containing fuel is in conduit 6128. First insulation 6122 may be made of a non-conosive, thermally insulating material such as rock wool, Nextel®, calcium silicate, Fiberfrax®, insulating refractory cements such as those manufactured by Harbizon Walker, A.P. Green, or National Refractories, etc. The relatively high temperatures generated at the flame of first oxidizer 6120, which may be about 1300 °C or greater, may generate sufficient heat to convert hydrocarbons proximate the first oxidizer into coke and/or char if no insulation is provided.

Heated fluids from conduit 6110 may exit a lower end of the conduit into opening 514. A temperature of the heated fluids may be lower proximate the lower end of conduit 110 than a temperature of the heated fluids proximate first oxidizer 6120. The heated fluids may return to a surface of the formation through the annulus of opening 514 (exhaust annulus 6124) and/or through exhaust conduit 6126. The heated fluids exiting the formation through exhaust conduit 6126 may be refened to as exhaust fluids. The exhaust fluids may be allowed to thermally contact conduit 6110 so as to exchange heat between exhaust fluids and either oxidizing fluid or fuel within conduit 6110. This exchange of heat may preheat fluids within conduit 6110. Thus, the thermal efficiency of the downhole combustor may be enhanced to as much as 90% or more (i.e., 90% or more of the heat from the heat of combustion is being transfened to a selected section of the foπnation). In certain embodiments, extra oxidizers may be used in addition to oxidizer 6120 and oxidizer 6130 shown in FIG. 96. For example, in some embodiments, one or more extra oxidizers may be placed between oxidizer 6120 and oxidizer 6130. Such extra oxidizers may be, for example, placed at intervals of about 20-50 m. In certain embodiments, one oxidizer (e.g., oxidizer 6120) may provide at least about 50% of the heat to the selected section of the formation, and the other oxidizers may be used to adjust the heat flux along the length of the oxidizer.

In some embodiments, fins may be placed on an outside surface of conduit 6110 to increase exchange of heat between exhaust fluids and fluids within the conduit. Exhaust conduit 6126 may extend into opening 514. A position of lower end of exhaust conduit 6126 may vary depending on, for example, a desired removal rate of exhaust fluids from the opening. In certain embodiments, it may be advantageous to remove fluids through exhaust conduit 6126 from a lower portion of opening 514 rather than allowing exhaust fluids to return to the surface through the annulus of the opening. All or part of the exhaust fluids may be vented, freated in a surface facility, and/or recycled. In some circumstances, the exhaust fluids may be recycled as a portion of fuel 6118 or oxidizing fluid 517 or recycled into an additional heater in another portion of the formation.

Two or more heater wells with oxidizers may be coupled in series with exhaust fluids from a first heater well being used as a portion of fuel for a second heater well. Exhaust fluids from the second heater well may be used as a portion of fuel for a third heater well, and so on as needed. In some embodiments, a separator may separate unused fuel and/or oxidizer from combustion products to increase the energy content of the fuel for the next oxidizer. Using the heated exhaust fluids as a portion of the feed for a heater well may decrease costs associated with pressurizing fluids for use in the heater well. In an embodiment, a portion (e.g., about one-third or about one-half) of the oxygen in the oxidizing fluid stream provided to a first heater well may be utilized in the first heater well. This would leave the remaining oxygen available for use as oxidizing fluid for subsequent heater wells. The heated exhaust fluids tend to have a pressure associated with the previous heater well and may be maintained at that pressure for providing to the next heater well. Thus, connection of two or more heater wells in series can significantly reduce compression costs associated with pressurizing fluids. Casing 541 and reinforcing material 544 may be placed in overburden 540. Overburden 540 may be above hydrocarbon layer 6100. In certain embodiments, casing 541 may extend downward into part or the entire zone being heated. Casing 541 may include steel (e.g., carbon steel or stainless steel). Reinforcing material 544 may include, for example, foamed cement or a cement with glass and or ceramic beads filled with air.

As depicted in the embodiment of FIG. 96, a heater may have second fuel conduit 6128. Second fuel conduit 6128 may be coupled to conduit 6110. Second fuel source 6121 may provide fuel 6118 to second fuel conduit 6128. Second fuel source 6121 may provide fuel that is similar to fuel from first fuel source 6119. In some embodiments, fuel from second fuel source 6121 may be different than fuel from first fuel source 6119. Fuel 6118 may exit second fuel conduit 6128 at a location proximate second oxidizer 6130. Second oxidizer 6130 may be located proximate a bottom of conduit 6110 and/or opening 514. Second oxidizer 6130 may be coupled to a lower end of second fuel conduit 6128. Second oxidizer 6130 may be used to oxidize at least a portion of fuel 6118

(exiting second fuel conduit 6128) with heated fluids exiting conduit 6110. Un-oxidized portions of heated fluids from conduit 6110 may also be oxidized at second oxidizer 6130. Second oxidizer 6130 may be a burner (e.g., a ring burner). Second oxidizer 6130 may be made of stainless steel. Second oxidizer 6130 may include one or more orifices that allow a flow of fuel 6118 into opening 514. The one or more orifices may be critical flow orifices. Oxidized portions of fuel 6118, along with un-oxidized portions of fuel, may combine with heated fluids from conduit 6110 and exit the formation with the heated fluids. Heat generated by oxidation of fuel 6118 from second fuel conduit 6128 proximate a lower end of opening 514, in combination with heat generated from heated fluids in conduit 6110, may provide more uniform heating of hydrocarbon layer 6100 than using a single oxidizer. In an embodiment, second oxidizer 6130 may be located about 200 m from first oxidizer 6120. However, in some embodiments, second oxidizer 6130 may be located up to about 250 m from first oxidizer 6120. Heat generated by oxidation of fuel at the first and second oxidizers may be allowed to transfer to the formation. The generated heat may fransfer to a pyrolysis zone in the formation. Heat transfened to the pyrolysis zone may pyrolyze at least some hydrocarbons within the pyrolysis zone.

In some embodiments, ignition source 6134 may be disposed proximate a lower end of second fuel conduit 6128 and/or second oxidizer 6130. Ignition source 6134 may be an elecfrically confrolled ignition source. Ignition source 6134 may be coupled to ignition source lead-in wire 6136. Ignition source lead-in wire 6136 may be further coupled to a power source for ignition source 6134. Ignition source 6134 may be used to initiate oxidation of fuel 6118 exiting second fuel conduit 6128. After oxidation of fuel 6118 from second fuel conduit 6128 has begun, ignition source 6134 may be turned down and/or off. In other embodiments, an ignition source may also be disposed proximate first oxidizer 6120. In some embodiments, ignition source 6134 may not be used if, for example, the conditions in the wellbore are sufficient to auto-ignite fuel 6118 being used. For example, if hydrogen is used as the fuel, the hydrogen will auto-ignite in the wellbore if the temperature and pressure in the wellbore are sufficient for autoignition of the fuel. As shown in FIG. 96, second insulation 6132 may be disposed in a region proximate second oxidizer 6130. Second insulation 6132 may be disposed on a face of hydrocarbon layer 6100 along an inner surface of opening 514. Second insulation 6132 may have a length of about 10 m to about 200 m (e.g., about 50 m). A length of second insulation 6132 may vary, however, depending on, for example, a desired heat fransfer rate to the formation, a desired temperature proximate the lower oxidizer, or a desired temperature profile along a length of conduit 6110 and/or hydrocarbon layer 6100. In an embodiment, the length of second insulation 6132 is about 10-40% of the length of conduit 6110 between any two oxidizers. Second insulation 6132 may have a thickness that varies (either continually or in step fashion) along its length. In certain embodhnents, second insulation 6132 may have a larger thickness proximate second oxidizer 6130 and a reduced thickness at a desired distance from the second oxidizer. The larger thickness of second insulation 6132 may preferentially reduce heat transfer proximate second oxidizer 6130 as compared to the reduced thickness portion of the insulation. For example, second insulation 6132 may have a thickness of about 0.03 m proximate second oxidizer 6130 and a thickness of about 0.015 m at a distance of about 10 m from the second oxidizer.

A thickness of second insulation 6132 may vary depending on, for example, a desired heating rate or a desired temperature at a surface of hydrocarbon layer 6100. The second insulation may inhibit the transfer of heat from the heated fluids to the formation in a region proximate the insulation. Second insulation 6132 may also inhibit chaning and/or coking of hydrocarbons proximate second oxidizer 6130. Second insulation 6132 may inhibit chaning and/or coking by reducing an amount of heat fransfened to the formation proximate the second oxidizer. Second insulation 6132 may be made of a non-conosive, thermally insulating material such as rock wool, Nextel™, calcium silicate, Fiberfrax®, or thermally insulating concretes such as those manufactured by Harbizon Walker, A.P. Green, or National Refractories. Hydrogen and/or steam may also be added to fuel used in the second oxidizer to further inhibit coking and or chaning of the formation proximate the second oxidizer and/or fuel within the fuel conduit. In other embodiments, one or more additional oxidizers may be placed in opening 514. The one or more additional oxidizers may be used to increase a heat output and/or provide more unifoπn heating of the formation. Additional fuel conduits and/or additional insulating conduits may be used with the one or more additional oxidizers as needed. In an example using two downhole combustors to heat a portion of a formation, the formation has a depth for freatment of about 228 m, with an overburden having a depth of about 91.5 m. Two oxidizers are used, as shown in the embodiment of FIG. 96, to provide heat to the formation in an opening with a diameter of about 0.15 m. To equalize the pressure inside the conduit and outside the conduit, a cross-sectional area inside the conduit should approximately equal a cross-sectional area outside the conduit. Thus, the conduit has a diameter of about 0.11 m.

To heat the formation at a heat input of about 655 watts/meter (W/m), a total heat input of about 150,000 W is needed. About 16,000 W of heat is generated for every 28 standard liters per minute (shn) of methane (CH₄) provided to the burners. Thus, a flow rate of about 270 s n is needed to generate the 150,000 W of heat. A temperature midway between the two oxidizers is about 555 °C less than the temperature at a flame of either oxidizer (about 1315 °C). The temperature midway between the two oxidizers on the wall of the formation (where there is no insulation) is about 690 °C. About 3,800 W can be canied by 2,830 slm of air for every 55 °C of temperature change in the conduit. Thus, for the afr to carry half the heat required (about 75,000 W) from the first oxidizer to the halfway point, 5,660 shn of air is needed. The other half of the heat required may be supplied by air passing the second oxidizer and carrying heat from the second oxidizer. Using air (21% oxygen) as the oxidizing fluid, a flow rate of about 5,660 slm of air can be used to provide excess oxygen to each oxidizer. About half of the oxygen, or about 11% of the air, is used in the two oxidizers in a first heater well. Thus, the exhaust fluid is essentially air with an oxygen content of about 10%. This exhaust fluid can be used in a second heater well. Pressure of the incoming air of the first heater well is about 6.2 bars absolute. Pressure of the outgoing air of the first heater well is about 4.4 bars absolute. This pressure is also the incoming air pressure of a second heater well. The outlet pressure of the second heater well is about 1J bars absolute. Thus, the air does not need to be recompressed between the first heater well and the second heater well.

FIG. 97 illustrates a cross-sectional representation of an embodiment of a downhole combustor heater for heating a formation. As depicted in FIG. 97, electric heater 6140 may be used instead of second oxidizer 6130 (as shown in FIG. 96) to provide additional heat to a portion of hydrocarbon layer 6100. In a heat source embodiment, electric heater 6140 may be an insulated conductor heater. In some embodiments, electric heater 6140 may be a conductor-in-conduit heater or an elongated member heater. In general, electric heaters tend to provide a more controllable and/or predictable heating profile than combustion heaters. The heat profile of electric heater 6140 may be selected to achieve a selected heating profile of the formation (e.g., unifoπn). For example, the heating profile of electric heater 6140 may be selected to "minor" the heating profile of oxidizer 6120 such that, when the heat from electric heater 6140 and oxidizer 6120 are supeφositioned, substantially uniform heating is applied along the length of the conduit.

In other heat source embodiments, any other type of heater, such as a natural distributed combustor or flameless distributed combustor, may be used instead of electric heater 6140. In certain embodiments, electric heater 6140 may be used instead of first oxidizer 6120 to heat a portion of hydrocarbon layer 6100. FIG. 98 depicts an embodiment using a downhole combustor with a flameless disfributed combustor. Second fuel conduit 6128 may have orifices 515 (e.g. , critical flow orifices) disfributed along the length of the conduit. Orifices 515 may be disfributed such that a heating profile along the length of hydrocarbon layer 6100 is substantially uniform. For example, more orifices 515 may be placed on second fuel conduit 6128 in a lower portion of the conduit than in an upper portion of the conduit. This will provide more heating to a portion of hydrocarbon layer 6100 that is farther from first oxidizer 6120. As depicted in FIG. 97, electric heater 6140 may be placed in opening 514 proximate conduit 6110.

Elecfric heater 6140 may be used to provide heat to hydrocarbon layer 6100 in a portion of opening 514 proximate a lower end of conduit 6110. Electric heater 6140 may be coupled to lead-in conductor 6142. Using electric heater 6140 as well as heated fluids from conduit 6110 to heat hydrocarbon layer 6100 may provide substantially uniform heating of hydrocarbon layer 6100. FIG. 99 illustrates a cross-sectional representation of an embodiment of a multilateral downhole combustor heater. Hydrocarbon layer 6100 may be a relatively thin layer (e.g., with a thickness of less than about 10 m, about 30 m, or about 60 m) selected for freatment. Opening 514 may extend below overburden 540 and then diverge in more than one direction within hydrocarbon layer 6100. Opening 514 may have walls that are substantially parallel to upper and lower surfaces of hydrocarbon layer 6100. Conduit 6110 may extend substantially vertically into opening 514 as depicted in FIG. 99. First oxidizer

6120 may be placed in or proximate conduit 6110. Oxidizing fluid 517 may be provided to first oxidizer 6120 through conduit 6110. First fuel conduit 6116 may be used to provide fuel 6118 to first oxidizer 6120. Second conduit 6150 may be coupled to conduit 6110. Second conduit 6150 may be oriented substantially peφendicular to conduit 6110. Third conduit 6148 may also be coupled to conduit 6110. Third conduit 6148 may be oriented substantially peφendicular to conduit 6110. Second oxidizer 6130 may be placed at an end of second conduit 6150.

Second oxidizer 6130 may be a ring burner. Third oxidizer 6144 may be placed at an end of third conduit 6148. In an embodiment, third oxidizer 6144 is a ring burner. Second oxidizer 6130 and third oxidizer 6144 may be placed at or near opposite ends of opening 514.

Second fuel conduit 6128 may be used to provide fuel to second oxidizer 6130. Third fuel conduit 6138 may be used to provide fuel to third oxidizer 6144. Oxidizing fluid 517 may be provided to second oxidizer 6130 through conduit 6110 and second conduit 6150. Oxidizing fluid 517 may be provided to third oxidizer 6144 through conduit 6110 and third conduit 6148. First insulation 6122 may be placed proximate first oxidizer 6120. Second insulation 6132 and third msulation 6146 may be placed proximate second oxidizer 6130 and third oxidizer 6144, respectively. Second oxidizer 6130 and third oxidizer 6144 may be located up to about 175 m from first conduit 6110. In some embodiments, a distance between second oxidizer 6130 or third oxidizer 6144 and first conduit 6110 may be less, depending on heating requirements of hydrocarbon layer 6100. Heat provided by oxidation of fuel at first oxidizer 6120, second oxidizer 6130, and third oxidizer 6144 may allow for substantially unifonn heating of hydrocarbon layer 6100.

Exhaust fluids may be removed through opening 514. The exhaust fluids may exchange heat with fluids entering opening 514 through conduit 6110. Exhaust fluids may also be used in additional heater wells and/or freated in surface facilities.

In a heat source embodiment, one or more elecfric heaters may be used instead of, or in combination with, first oxidizer 6120, second oxidizer 6130, and/or third oxidizer 6144 to provide heat to hydrocarbon layer 6100. Using elecfric heaters in combination with oxidizers may provide for substantially uniform heating of hydrocarbon layer 6100. FIG. 100 depicts a heat source embodiment in which one or more oxidizers are placed in first conduit 6160 and second conduit 6162 to provide heat to hydrocarbon layer 6100. The embodiment may be used to heat a relatively thin formation. First oxidizer 6120 may be placed in first conduit 6160. A second oxidizer 6130 may be placed proximate an end of first conduit 6160. First fuel conduit 6116 may provide fuel to first oxidizer 6120. Second fuel conduit 6128 may provide fuel to second oxidizer 6130. First insulation 6122 may be placed proximate first oxidizer 6120. Oxidizing fluid 517 may be provided into first conduit 6160. A portion of oxidizing fluid 517 may be used to oxidize fuel at first oxidizer 6120. Second insulation may be placed proximate second oxidizer 6130.

Second conduit 6162 may diverge in an opposite direction from first conduit 6160 in opening 514 and substantially minor first conduit 6160. Second conduit 6162 may include elements similar to the elements of first conduit 6160, such as first oxidizer 6120, first fuel conduit 6116, first insulation 6122, second oxidizer 6130, second fuel conduit 6128, and/or second insulation 6132. These elements may be used to substantially uniformly heat hydrocarbon layer 6100 below overburden 540 along lengths of conduits 6160 and 6162.

FIG. 101 illustrates a cross-sectional representation of an embodiment of a downhole combustor for heating a formation. Opening 514 is a single opening within hydrocarbon layer 6100 that may have first end 6170 and second end 6172. Oxidizers 6120 may be placed in opening 514 proximate ajunction of overburden 540 and hydrocarbon layer 6100 at first end 6170 and second end 6172. Insulation 6132 may be placed proximate each oxidizer 6120. Fuel conduit 6116 may be used to provide fuel 6118 from fuel source 6119 to oxidizer 6120. Oxidizing fluid 517 may be provided into opening 514 from oxidizing fluid source 508 through conduit 6110. Casing 6152 may be placed in opening 514. Casing 6152 may be made of carbon steel. Portions of casing 6152 that may be subjected to much higher temperatures (e.g., proximate oxidizers 6120) may include stainless steel or other high temperature, conosion resistant metal. In some embodiments, casing 6152 may extend into portions of opening 514 within overburden 540.

In a heat source embodiment, oxidizing fluid 517 and fuel 6118 are provided to oxidizer 6120 in first end 6170. Heated fluids from oxidizer 6120 in first end 6170 tend to flow through opening 514 towards second end

6172. Heat may fransfer from the heated fluids to hydrocarbon layer 6100 along a length of opening 514. The heated fluids may be removed from the formation through second end 6172. During this time, oxidizer 6120 at second end 6172 may be turned off. The removed fluids may be provided to a second opening in the formation and used as oxidizing fluid and/or fuel in the second opening. After a selected time (e.g., about a week), oxidizer 6120 at first end 6170 may be turned off. At this time, oxidizing fluid 517 and fuel 6118 may be provided to oxidizer

6120 at second end 6172 and the oxidizer turned on. Heated fluids may be removed during this time through first end 6170. Oxidizers 6120 at first end 6170 and at second end 6172 may be used alternately for selected times (e.g., about a week) to heat hydrocarbon layer 6100. This may provide a more substantially uniform heating profile of hydrocarbon layer 6100. Removing the heated fluids from the opening through an end distant from an oxidizer may reduce a possibility of coking within opening 514 as heated fluids are removed from the opening separately from incoming fluids. The use of the heat content of an oxidizing fluid may also be more efficient as the heated fluids can be used in a second opening or second downhole combustor.

FIG. 102 depicts an embodiment of a heat source for a relatively low permeability formation containing heavy hydrocarbons. Fuel conduit 6116 may be placed within opening 514. In some embodiments, opening 514 may include casing 6152. Opening 514 is a single opening within the formation that may have first end 6170 at a first location on the surface of the earth and second end 6172 at a second location on the surface of the earth. Oxidizers 6120 may be positioned proxunate the fuel conduit in hydrocarbon layer 516. Oxidizers 6120 may be separated by a distance ranging from about 3 m to about 50 m (e.g., about 30 m). Fuel 6118 may be provided to fuel conduit 6116. In addition, steam 9674 may be provided to fuel conduit 6116 to reduce coking proximate oxidizers 6120 and/or in fuel conduit 6116. Oxidizing fluid 6110 (e.g., air and/or oxygen) may be provided to oxidizers 6120 through opening 514. Oxidation of fuel 6118 may generate heat. The heat may transfer to a portion of the formation. Oxidation products 9676 may exit opening 514 proximate second location 6172.

FIG. 103 depicts a schematic, from an elevated view, of an embodiment for using downhole combustors depicted in the embodiment of FIG. 101. Openings 6180, 6182, 6184, 6186, 6188, and 6190 may have downhole combustors (as shown in the embodiment of FIG. 101) placed in each opening. More or fewer openings (i.e., openings with a downhole combustor) may be used as needed. A number of openings may depend on, for example, a size of an area for treatment, a desfred heating rate, or a selected well spacing. Conduit 6196 may be used to transport fluids from a downhole combustor in opening 6180 to downhole combustors in openings 6182, 6184, 6186, 6188, and 6190. The openings may be coupled in series using conduit 6196. Compressor 6192 may be used between openings, as needed, to increase a pressure of fluid between the openings. Additional oxidizing fluid may be provided to each compressor 6192 from conduit 6194. A selected flow of fuel from a fuel source may be provided into each of the openings.

For a selected time, a flow of fluids may be from first opening 6180 towards opening 6190. Flow of fluid within first opening 6180 may be substantially opposite flow within second opening 6182. Subsequently, flow within second opening 6182 may be substantially opposite flow within third opening 6184, etc. This may provide substantially more uniform heating of the foπnation using the downhole combustors within each opening. After the selected time, the flow of fluids may be reversed to flow from opening 6190 towards first opening 6180. This process may be repeated as needed during a time needed for treatment of the formation. Alternating the flow of fluids may enhance the uniformity of a heating profile of the formation.

FIG. 104 depicts a schematic representation of an embodiment of a heater well positioned within a relatively low peπneability formation containing heavy hydrocarbons. Heater well 6230 may be placed within opening 514. In certain embodiments, opening 514 is a single opening within the formation that may have first end 6170 and second end 6172 contacting the surface of the earth. Opening 514 may include elongated portions 9630, 9632, 9634. Elongated portions 9630, 9634 may be placed substantially in a non-hydrocarbon containing layer (e.g., overburden). Elongated portion 9632 may be placed substantially within hydrocarbon layer 6100 and/or a freatment zone.

In some heat source embodiments, casing 6152 may be placed in opening 514. In some embodiments, casing 6152 may be made of carbon steel. Portions of casing 6152 that may be subjected to high temperatures may be made of more temperature resistant material (e.g., stainless steel). In some embodiments, casing 6152 may extend into elongated portions 9630, 9634 within overburden 540. Oxidizers 6120, 6130 may be placed proximate ajunction of overburden 540 and hydrocarbon layer 6100 at first end 6170 and second end 6172 of opening 514.

Oxidizers 6120, 6130 may include burners (e.g., inline burners and/or ring burners). Insulation 6132 may be placed proximate each oxidizer 6120, 6130.

Conduit 9620 may be placed within opening 514 forming annulus 9621 between an outer surface of conduit 9620 and an inner surface of the casing 6152. Annulus 9621 may have a regular and/or irregular shape within the opening. In some embodiments, oxidizers may be positioned within the annulus and/or the conduit to provide heat to a portion of the formation. Oxidizer 6120 is positioned within annulus 9621 and may include a ring burner. Heated fluids from oxidizer 6120 may flow within annulus 9621 to end 6172. Heated fluids from oxidizer 6130 may be directed by conduit 9620 through opening 514. Heated fluids may include, but are not limited to oxidation products, oxidizing fluid, and/or fuel. Flow of the heated fluids through annulus 9621 may be in the opposite direction of the flow of heated fluids in conduit 9620. In alternate embodiments, oxidizers 6120, 6130 may be positioned proximate the same end of opening 514 to allow the heated fluids to flow through opening 514 in the same direction.

Fuel conduits 6116 may be used to provide fuel 6118 from fuel source 6119 to oxidizers 6120, 6130. Oxidizing fluid 517 may be provided to oxidizers 6120, 6130 from oxidizing fluid source 508 through conduits 6110. Flow of fuel 6118 and oxidizing fluid 517 may generate oxidation products at oxidizers 6120, 6130. In some embodhnents, a flow of oxidizing fluid 517 may be confrolled to control oxidation at oxidizers 6120, 6130.

Alternatively, a flow of fuel may be confrolled to control oxidation at oxidizers 6120, 6130.

In a heat source embodiment, oxidizing fluid 517 and fuel 6118 are provided to oxidizer 6120. Heated fluids from oxidizer 6120 in first end 6170 tend to flow through opening 514 towards second end 6172. Heat may fransfer from the heated fluids to hydrocarbon layer 6100 along a segment of opening 514. The heated fluids may be removed from the formation through second end 6172. In some embodiments, a portion of the heated fluids removed from the formation may be provided to fuel conduit 6116 at end 6172 to be utilized as fuel in oxidizer 6130. Fluids heated by oxidizer 6130 may be directed through the opening in conduit 9620 to first end 6170. In some embodiments, a portion of the heated fluids is provided to fuel conduit 6116 at first end 6170. Alternatively, heated fluids produced from either end of the opening may be directed to a second opening in the formation for use as either oxidizing fluid and/or fuel. In some embodiments, heated fluids may be directed toward one end of the opening for use in a single oxidizer.

Oxidizers 6120, 6130 may be utilized concunently. In some embodiments, use of the oxidizers may alternate. Oxidizer 6120 may be turned off after a selected time period (e.g., about a week). At this time, oxidizing fluid 517 and fuel 6118 may be provided to oxidizer 6130. Heated fluids may be removed during this time through first end 6170. Use of oxidizer 6120 and oxidizer 6130 may be alternated for selected times to heat hydrocarbon layer 6100. Flowing oxidizing fluids in opposite directions may produce a more uniform heating profile in hydrocarbon layer 6100. Removing the heated fluids from the opening through an end distant from the oxidizer at which the heated fluids were produced may reduce the possibility for coking within the opening. Heated fluids may be removed from the formation in exhaust conduits in some embodiments. In addition, the potential for coking may be further reduced by removing heated fluids from the opening separately from incoming fluids (e.g., fuel and/or oxidizing fluid). In certain instances, some heat within the heated fluids may transfer to the incoming fluids to increase the efficiency of the oxidizers.

FIG. 105 depicts an embodiment of a heat source positioned within a relatively low peπneability foπnation containing heavy hydrocarbons. Surface units 9672 (e.g., burners and/or furnaces) provide heat to an opening in the formation. Surface unit 9672 may provide heat to conduit 9620 positioned in conduit 9622. Surface unit 9672 positioned proximate first end 6170 of opening 514 may heat fluids 9670 (e.g., air, oxygen, steam, fuel, and/or flue gas) provided to surface unit 9672. Conduit 9620 may extend into surface unit 9672 to allow fluids heated in surface unit 9672 proximate first end 6170 to flow into conduit 9620. Conduit 9620 may direct fluid flow to second end 6172. At second end 6172 conduit 9620 may provide fluids to surface unit 9672. Surface unit 9672 may heat the fluids. The heated fluids may flow into conduit 9622. Heated fluids may then flow through conduit 9622 towards end 6170. In some embodiments, conduit 9620 and conduit 9622 may be concentric. In alternate embodhnents, fluids may be compressed prior to entering the surface unit. Compression of the fluids may maintain a fluid flow through the opening. Flow of fluids through the conduits may affect the fransfer of heat from the conduits to the formation.

In alternate embodiments, a single surface unit may be utilized for heating proximate first end 6170. Conduits may be positioned such that fluid within an inner conduit flows into the annulus between the inner conduit and an outer conduit. Thus the fluid flow in the inner conduit and the annulus may be counter cunent.

A heat source embodiment is illusfrated in FIG. 106. Conduits 9620, 9622 may be placed within opening 514. Opening 514 may be an open wellbore. In alternate embodiments, a casing may be included in a portion of the opening (e.g., in the portion in the overburden). In addition, some embodiments may include insulation sunounding a portion of conduits 9620, 9622. For example, the portions of the conduits within overburden 540 may be insulated to inhibit heat fransfer from the heated fluids to the overburden and/or a portion of the formation proximate the oxidizers.

FIG. 107 illustrates an embodiment of a surface combustor that may heat a section of a relatively low permeability formation containing heavy hydrocarbons. Fuel fluid 611 may be provided into burner 610 through conduit 617. An oxidizing fluid may be provided into burner 610 from oxidizing fluid source 508. Fuel fluid 611 may be oxidized with the oxidizing fluid in burner 610 to form oxidation products 613. Fuel fluid 611 may include, but is not limited to, hydrogen, methane, ethane, and/or other hydrocarbons. Burner 610 may be located external to the formation or within opening 614 in hydrocarbon layer 516. Source 618 may heat fuel fluid 611 to a temperature sufficient to support oxidation in burner 610. Source 618 may heat fuel fluid 611 to a temperature of about 1425 °C. Source 618 may be coupled to an end of conduit 617. In a heat source embodiment, source 618 is a pilot flame.

The pilot flame may bum with a small flow of fuel fluid 611. In other embodiments, source 618 may be an elecfrical ignition source.

Oxidation products 613 may be provided into opening 614 within inner conduit 612 coupled to burner 610. Heat may be fransfened from oxidation products 613 through outer conduit 615 into opening 614 and to hydrocarbon layer 516 along a length of inner conduit 612. Oxidation products 613 may cool along the length of inner conduit 612. For example, oxidation products 613 may have a temperature of about 870 °C proximate top of inner conduit 612 and a temperature of about 650°C proximate bottom of inner conduit 612. A section of inner conduit 612 proximate burner 610 may have ceramic insulator 612b disposed on an inner surface of inner conduit 612. Ceramic insulator 612b may inhibit melting of inner conduit 612 and/or insulation 612a proximate burner 610. Opening 614 may extend into the formation a length up to about 550 m below surface 550.

Inner conduit 612 may provide oxidation products 613 into outer conduit 615 proximate a bottom of opening 614. Inner conduit 612 may have insulation 612a. FIG. 108 illustrates an embodiment of inner conduit 612 with insulation 612a and ceramic insulator 612b disposed on an inner surface of inner conduit 612. Insulation 612a may inhibit heat fransfer between fluids in inner conduit 612 and fluids in outer conduit 615. A thickness of insulation 612a may be varied along a length of inner conduit 612 such that heat transfer to hydrocarbon layer 516 may vary along the length of inner conduit 612. For example, a thickness of insulation 612a may be tapered from a larger thickness to a lesser thickness from a top portion to a bottom portion, respectively, of inner conduit 612 in opening 614. Such a tapered thickness may provide more uniform heating of hydrocarbon layer 516 along the length of inner conduit 612 in opening 614. Insulation 612a may include ceramic and metal materials. Oxidation products 613 may return to surface 550 through outer conduit 615. Outer conduit may have insulation 615a, as depicted in FIG. 107. Insulation 615a may inhibit heat fransfer from outer conduit 615 to overburden 540. Oxidation products 613 may be provided to an additional burner through conduit 619 at surface 550.

Oxidation products 613 may be used as a portion of a fuel fluid in the additional burner. Doing so may increase an efficiency of energy output versus energy input for heating hydrocarbon layer 516. The additional burner may provide heat through an additional opening in hydrocarbon layer 516.

In some embodiments, an electric heater may provide heat in addition to heat provided from a surface combustor. The electric heater may be, for example, an insulated conductor heater or a conductor-in-conduit heater as described in any of the above embodiments. The elecfric heater may provide the additional heat to a relatively low permeability formation containing heavy hydrocarbons so that the relatively low permeability formation containing heavy hydrocarbons is heated substantially uniformly along a depth of an opening in the formation. Flameless combustors such as those described in U.S. Patent No. 5,404,952 to Vinegar et al., which is incoφorated by reference as if fully set forth herein, may heat a relatively low permeability formation containing heavy hydrocarbons. FIG. 109 illustrates an embodiment of a flameless combustor that may heat a section of the relatively low permeability formation containing heavy hydrocarbons. The flameless combustor may include center tube 637 disposed within inner conduit 638. Center tube 637 and inner conduit 638 may be placed within outer conduit 636.

Outer conduit 636 may be disposed within opening 514 in hydrocarbon layer 516. Fuel fluid 621 may be provided into the flameless combustor through center tube 637. If a hydrocarbon fuel such as methane is utilized, the fuel may be mixed with steam to inhibit coking in center tube 637. If hydrogen is used as the fuel, no steam may be required.

Center tube 637 may include flow mechanisms 635 (e.g., flow orifices) disposed within an oxidation region to allow a flow of fuel fluid 621 into inner conduit 638. Flow mechanisms 635 may confrol a flow of fuel fluid 621 into inner conduit 638 such that the flow of fuel fluid 621 is not dependent on a pressure in inner conduit 638. Oxidizing fluid 623 may be provided into the combustor through inner conduit 638. Oxidizing fluid 623 may be provided from oxidizing fluid source 508. Flow mechanisms 635 on center tube 637 may inhibit flow of oxidizing fluid 623 into center tube 637.

Oxidizing fluid 623 may mix with fuel fluid 621 in the oxidation region of inner conduit 638. Either oxidizing fluid 623 or fuel fluid 621, or a combination of both, may be preheated external to the combustor to a temperature sufficient to support oxidation of fuel fluid 621. Oxidation of fuel fluid 621 may provide heat generation within outer conduit 636. The generated heat may provide heat to a portion of a relatively low permeability formation containing heavy hydrocarbons proximate the oxidation region of inner conduit 638.

Products 625 from oxidation of fuel fluid 621 may be removed through outer conduit 636 outside inner conduit 638.

Heat exchange between the downgoing oxidizing fluid and the upgoing combustion products in the overburden results in enhanced thermal efficiency. A flow of removed combustion products 625 may be balanced with a flow of fuel fluid 621 and oxidizing fluid 623 to maintain a temperature above auto-ignition temperature but below a temperature sufficient to produce oxides of nifrogen. In addition, a constant flow of fluids may provide a substantially uniform temperature disfribution within the oxidation region of inner conduit 638. Outer conduit 636 may be a stainless steel tube. Heating in the portion of the relatively low permeability formation containing heavy hydrocarbons may be substantially uniform. Maintaining a temperature below temperatures sufficient to produce oxides of nifrogen may allow for relatively inexpensive metallurgical cost. Care may be taken during design and installation of a well (e.g., freeze wells, production wells, monitoring wells, and heat sources) into a formation to allow for thermal effects within the formation. Heating and/or cooling of the formation may expand and/or contract elements of a well, such as the well casing. Elements of a well may expand or contract at different rates (e.g., due to different thermal expansion coefficients). Theπnal expansion or confraction may cause failures (such as leaks, fractures, short-circuiting, etc.) to occur in a well. An operational lifetime of one or more elements in the wellbore may be shortened by such failures.

In some well embodhnents, a portion of the well is an open wellbore completion. Portions of the well may be suspended from a wellbore or a casing that is cemented in the foπnation (e.g., a portion of a well in the overburden). Expansion of the well due to heat may be accommodated in the open wellbore portion of the well. In a well embodiment, an expansion mechanism may be coupled to a heat source or other element of a well placed in an opening in a formation. The expansion mechanism may allow for thermal expansion of the heat source or element during use. The expansion mechanism may be used to absorb changes in length of the well as the well expands or contracts with temperature. The expansion mechanism may inhibit the heat source or element from being pushed out of the opening during thermal expansion. Using the expansion mechanism in the opening may increase an operational lifetime of the well.

FIG. 110 illustrates a representation of an embodiment of expansion mechanism 6012 coupled to heat source 8682 in opening 514 in hydrocarbon layer 516. Expansion mechanism 6012 may allow for thermal expansion of heat source 8682. Heat source 8682 may be any heat source (e.g., conductor-in-conduit heat source, insulated conductor heat source, natural disfributed combustor heat source, etc.). In some embodiments, more than one expansion mechanism 6012 may be coupled to individual components of a heat source. For example, if the heat source includes more than one element (e.g., conductors, conduits, supports, cables, elongated, members, etc.), an expansion mechanism may be coupled to each element. Expansion mechanism 6012 may include spring loading. In one embodiment, expansion mechanism 6012 is an accordion mechanism. In another embodiment, expansion mechanism 6012 is a bellows or an expansion joint. Expansion mechanism 6012 may be coupled to heat source 8682 at a bottom of the heat source in opening

514. In some embodiments, expansion mechanism 6012 may be coupled to heat source 8682 at a top of the heat source. In other embodiments, expansion mechanism 6012 may be placed at any point along the length of heat source 8682 (e.g., in a middle of the heat source). Expansion mechanism 6012 may be used to reduce the hanging weight of heat source 8682 (i.e., the weight supported by a wellhead coupled to the heat source). Reducing the hanging weight of heat source 8682 may reduce creeping of the heat source during heating.

Certain heat source embodiments may include an operating system coupled to a heat source or heat sources by insulated conductors or other types of wiring. The operating system may interface with the heat source. The operating system may receive a signal (e.g., an electromagnetic signal) from a heater that is representative of a temperature distribution of the heat source. Additionally, the operating system may confrol the heat source, either locally or remotely. For example, the operating system may alter a temperature of the heat source by altering a parameter of equipment coupled to the heat source. The operating system may monitor, alter, and/or confrol the heating of at least a portion of the formation.

For some heat source embodiments, a heat source or heat sources may operate without a confrol and/or operating system. A heat source may only require a power supply from a power source such as an elecfric transformer. A conductor-in-conduit heater and or an elongated member heater may include a heater element formed of a self-regulating material, such as 304 stainless steel or 316 stainless steel. Power dissipation and amperage through a heater element made of a self-regulating material decrease as temperature increases, and increase as temperature decreases due in part to the resistivity properties of the material and Ohm's Law. For a substantially constant voltage supply to a heater element, if the temperature of the heater element increases, the resistance of the element will increase, the amperage through the heater element will decrease, and the power dissipation will decrease; thus forcing the heater element temperature to decrease. On the other hand, if the temperature of the heater element decreases, the resistance of the element will decrease, the amperage through the heater element will increase, and the power dissipation will increase; thus forcing the heater element temperature to increase. Some metals, such as certain types of nichrome, have resistivity curves that decrease with increasing temperature for certain temperature ranges. Such materials may not be capable of being self-regulating heaters. In some heat source embodiments, leakage cunent of elecfric heaters may be monitored. For insulated heaters, an increase in leakage cunent may show deterioration in an insulated conductor heater. Voltage breakdown in the insulated conductor heater may cause failure of the heat source. In some heat source embodiments, a cunent and voltage applied to electric heaters may be monitored. The cunent and voltage may be monitored to assess/indicate resistance in a heater element of the heat source. The resistance in the heat source may represent a temperature in the heat source since the resistance of the heat source may be known as a function of temperature. In some embodiments, a temperature of a heat source may be monitored with one or more thermocouples placed in or proximate the heat source. In some embodiments, a control system may monitor a parameter of the heat source. The confrol system may alter parameters of the heat source to establish a desired output such as heating rate and/or temperature increase. In some embodiments, a thennowell may be disposed into an opening in a relatively low peπneability formation containing heavy hydrocarbons that includes a heat source. The thennowell may be disposed in an opening that may or may not have a casing. In the opening without a casing, the thennowell may include appropriate metallurgy and thickness such that conosion of the thennowell is inhibited. A thennowell and temperature logging process, such as that described in U.S. Patent No. 4,616,705 issued to Stegemeier et al., which is incoφorated by reference as if fully set forth herein, may be used to monitor temperature. Only selected wells may be equipped with thermowells to avoid expenses associated with installing and operating temperature monitors at each heat source. Some thermowells may be placed midway between two heat sources. Some thermowells may be placed at or close to a center of a well pattern. Some thermowells may be placed in or adjacent to production wells. In an embodiment for freating a relatively low permeability formation containing heavy hydrocarbons in situ, an average temperature within a majority of a selected section of the foπnation may be assessed by measuring temperature within a wellbore or wellbores. The wellbore may be a production well, heater well, or monitoring well. The temperature within a wellbore may be measured to monitor and/or determine operating conditions within the selected section of the formation. The measured temperature may be used as a property for input into a program for controlling production within the formation. In certain embodiments, a measured temperature may be used as input for a software executable on a computational system. In some embodiments, a temperature within a wellbore may be measured using a moveable thermocouple. The moveable thermocouple may be disposed in a conduit of a heater or heater well. An example of a moveable thermocouple and its use is described in U.S. Patent No. 4,616,705 to Stegemeier et al. In an alternate embodiment, more than one thermocouple may be placed in a wellbore to measure the temperature within the wellbore. The thermocouples may be part of a multiple thermocouple anay. The thermocouples may be located at various depths and/or locations. The multiple thermocouple anay may include a magnesium oxide insulated sheath or sheaths placed around portions of the thermocouples. The insulated sheaths may include conosion resistant materials. A conosion resistant material may include, but is not limited to, stainless steels 304, 310, 316 or Inconel. Multiple thermocouple anays may be obtained from Pyrotenax Cables Ltd. (Ontario, Canada) or Idaho Labs (Idaho Falls, Idaho). The multiple thermocouple anay may be moveable within the wellbore.

In certain thermocouple embodiments, voltage isolation may be used with a moveable thermocouple placed in a wellbore. FIG. Ill illustrates a schematic of thermocouple 9202 placed inside conductor 580. Conductor 580 may be placed within conduit 582 of a conductor-in-conduit heat source. Conductor 580 may be coupled to low resistance section 584. Low resistance section 584 may be placed in overburden 540. Conduit 582 may be placed in wellbore 9206. Thermocouple 9202 may be used to measure a temperature within conductor 580 along a length of the conductor in hydrocarbon layer 516. Thermocouple 9202 may include thermocouple wires that are coupled at the surface to spool 9208 so that the thermocouple is moveable along the length of conductor 580 to obtain a temperature profile in the heated section. Thermocouple isolation 9204 may be coupled to thermocouple 9202. Thermocouple isolation 9204 may be, for example, a fransfoπner coupled thermocouple isolation block available from Watlow Elecfric Manufacturing Company (St. Louis, Missouri). Alternately, an optically isolated thermocouple isolation block may be used. Thermocouple isolation 9204 may reduce voltages above the thermocouple isolation and at wellhead 690. High voltages may exist within wellbore 9206 due to use of the elecfric heat source within the wellbore. The high voltages can be dangerous for operators or personnel working around wellhead 690. With thermocouple isolation 9204, voltages at wellhead 690 (e.g., at spool 9208) may be lowered to safer levels (e.g., about zero or ground potential). Thus, using thermocouple isolation 9204 may increase safety at wellhead 690.

In some embodiments, thermocouple isolation 9204 may be used along the length of low resistance section 584. Temperatures within low resistance section 584 may not be above a maximum operating temperature of thermocouple isolation 9204. Thermocouple isolation 9204 may be moved along the length of low resistance section 584 as thermocouple 9202 is moved along the length of conductor 580 by spool 9208. In other embodiments, thermocouple isolation 9204 may be placed at wellhead 690.

In a temperature monitor embodiment, a temperature within a wellbore in a formation is measured using a fiber assembly. The fiber assembly may include optical fibers made from quartz or glass. The fiber assembly may have fibers sunounded by an outer shell. The fibers may include fibers that fransmit temperature measurement signals. A fiber that may be used for temperature measurements can be obtained from Sensa Highway (Houston, Texas). The fiber assembly may be placed within a wellbore in the formation. The wellbore may be a heater well, a monitoring well, or a production well. Use of the fibers may be limited by a maximum temperature resistance of the outer shell, which may be about 800 °C in some embodiments. A signal may be sent down a fiber disposed within a wellbore. The signal may be a signal generated by a laser or other optical device. Thermal noise may be developed in the fiber from conditions within the wellbore. The amount of noise may be related to a temperature within the wellbore. hi general, the more noise on the fiber, the higher the temperature within the wellbore. This may be due to changes in the index of refraction of the fiber as the temperature of the fiber changes. The relationship between noise and temperature may be characterized for a certain fiber. This relationship may be used to determine a temperature of the fiber along the length of the fiber. The temperature of the fiber may represent a temperature within the wellbore. In some in situ conversion process embodiments, a temperature within a wellbore in a formation may be measured using pressure waves. A pressure wave may include a sound wave. Examples of using sound waves to measure temperature are shown in U.S. Patent Nos. 5,624,188 to West, 5,437,506 to Gray, 5,349,859 to Kleppe, 4,848,924 to Nuspl et al., 4,762,425 to Shakkottai et al., and 3,595,082 to Miller, Jr., which are incoφorated by reference as if fully set forth herein. Pressure waves may be provided into the wellbore. The wellbore may be a heater well, a production well, a monitoring well, or a test well. A test well may be a well placed in a formation that is used primarily for measurement of properties of the formation. A plurality of discontinuities may be placed within the wellbore. A predetermined spacing may exist between each discontinuity. The plurality of discontinuities may be placed inside a conduit placed within a wellbore. For example, the plurality of discontinuities may be placed within a conduit used as a portion of a conductor-in-conduit heater or a conduit used to provide fluid into a wellbore. The plurality of discontinuities may also be placed on an external surface of a conduit in a wellbore. A discontinuity may include, but may not be limited to, an alumina cenfralizer, a stub, a node, a notch, a weld, a collar, or any such point that may reflect a pressure wave.

FIG. 112 depicts a schematic view of an embodiment for using pressure waves to measure temperature within a wellbore. Conduit 6350 may be placed within wellbore 6352. Plurality of discontinuities 6354 may be placed within conduit 6350. The discontinuities may be separated by substantially constant separation distance 6356. Distance 6356 may be, in some embodiments, about 1 m, about 5 m, or about 15 m. A pressure wave may be provided into conduit 6350 from pressure wave source 6358. Pressure wave source 6358 may include, but is not limited to, an air gun, an explosive, device (e.g., blank shotgun), a piezoelectric crystal, a magnetosfrictive transducer, an electrical sparker, or a compressed air source. A compressed air source may be operated or controlled by a solenoid valve. The pressure wave may propagate through conduit 6350. In some embodiments, an acoustic wave may be propagated through the wall of the conduit.

A reflection (or signal) of the pressure wave within conduit 6350 may be measured using wave measuring device 6363. Wave measuring device 6363 may be, for example, a piezoelectric crystal, a magnetosfrictive transducer, or any device that measures a time-domain pressure of the wave within the conduit. Wave measuring device 6363 may determine time-domain pressure wave 6360 that represents travel of the pressure wave within conduit 6350. Each slight increase in pressure, or pressure spike 6362, represents a reflection of the pressure wave at a discontinuity 6354. The pressure wave may be repeatedly provided into the wellbore at a selected frequency. The reflected signal may be continuously measured to increase a signal-to-noise ratio for pressure spike 6362 in the reflected signal. This may include using a repetitive stacking of signals to reduce noise. A repeatable pressure wave source may be used. For example, repeatable signals may be producible from a piezoelectric crystal. A trigger signal may be used to start wave measuring device 6363 and pressure wave source 6358. The time, as measured using pressure wave 6360, may be used with the distance between each discontinuity 6356 to determine an average temperature between the discontinuities for a known gas within conduit 6350. Since the velocity of the pressure wave varies with temperature within conduit 6350, the time for travel of the pressure wave between discontinuities will vary with an average temperature between the discontinuities. For dry air within a conduit or wellbore, the temperature may be approximated using the equation:

(39) c = 33,145 x (1 + 7 273.16) •Λ . in which c is the velocity of the wave in cm/sec and Tis the temperature in degrees Celsius. If the gas includes other gases or a mixture of gases, EQN. 39 can be modified to incoφorate properties of the alternate gas or the gas mixture. EQN. 39 can be derived from the more general equation for the velocity of a wave in a gas:

(40) c = [(RT/M)(l+ R/C_v)γ ;

in which R is the ideal gas constant, T is the temperature in Kelvin, and C_v is the heat capacity of the gas.

Alternatively, a reference time-domain pressure wave can be determined at a known ambient temperature. Thus, a time-domain pressure wave determined at an increased temperature within the wellbore may be compared to the reference pressure wave to determine an average temperature within the wellbore after heating the formation.

The change in velocity between the reference pressure wave and the increased temperature pressure wave, as measured by the change in distance between pressure spikes 6362, can be used to determine the increased temperature within the conduit. Use of pressure waves to measure an average temperature may require relatively low maintenance. Using the velocity of pressure waves to measure temperature may be less expensive than other temperature measurement methods.

In some embodiments, a heat source may be turned down and/or off after an average temperature in a formation reaches a selected temperature. Turning down and/or off the heat source may reduce input energy costs, inhibit overheating of the formation, and allow heat to fransfer into colder regions of the formation.

In some in situ conversion process embodiments, elecfrical power used in heating a relatively low permeability formation containing heavy hydrocarbons may be supplied from alternate energy sources. Alternate energy sources include, but are not limited to, solar power, wind power, hydroelectric power, geothermal power, biomass sources (i.e., agricultural and forestry by-products and energy crops), and tidal power. Elecfric heaters used to heat a formation may use any available cunent, voltage (AC or DC), or frequency that will not result in damage to the heater element. Because the heaters can be operated at a wide variety of voltages or frequencies, transformers or other conversion equipment may not be needed to allow for the use of electricity from alternate energy sources to power the elecfric heaters. This may significantly reduce equipment costs associated with using alternate energy sources, such as wind power in which a significant cost is associated with equipment that establishes a relatively nanow cunent and/or voltage range.

Power generated from alternate energy sources may be generated at or proximate an area for freating a relatively low permeability formation containing heavy hydrocarbons. For example, one or more solar panels and equipment for converting solar energy to elecfricity may be placed at a location proximate a foπnation. A wind farm, which includes a plurality of wind turbines, may be placed near a formation that is to be, or is being, subjected to an in situ conversion process. A power station that combusts or otherwise uses local or imported biomass for electrical generation may be placed near a foπnation that is to be, or is being, subjected to an in situ conversion process. If suitable geothermal or hydroelectric sites are located sufficiently nearby, these resources may be used for power generation. Power for elecfric heaters may be generated at or proximate the location of a formation, thus reducing costs associated with obtaining and/or transporting elecfrical power. In certain embodiments, steam and/or other exhaust fluids from freating a formation may be used to power a generator that is also primarily powered by wind turbines. In an embodiment in which an alternate energy source such as wind or solar power is used to power electric heaters, supplemental power may be needed to complement the alternate energy source when the alternate energy source does not provide sufficient power to supply the heaters. For example, with a wind power source, during times when there is insufficient wind to power a wind turbine to provide power to an elecfric heater, the additional power required may be obtained from line power sources such as a fossil fuel plant or nuclear power plant. In other embodiments, power from alternate energy sources may be used for supplemental power in addition to power from line power sources to reduce costs associated with heating a formation.

Alternate energy sources such as wind or solar power may be used to supplement or replace elecfrical grid power during peak energy cost times. If excess elecfricity that is compatible with the electricity grid is generated using alternate energy sources, the excess elecfricity may be sold to the grid. If excess elecfricity is generated, and if the excess energy is not easily compatible with an existing elecfricity grid, the excess electricity may be used to create stored energy that can be recaptured at a later time. Methods of energy storage may include, but are not limited to, converting water to oxygen and hydrogen, powering a flywheel for later recovery of the mechanical energy, pumping water into a higher reservoir for later use as a hydroelectric power source, and/or compression of air (as in underground caverns or spent areas of the reservoir).

Use of wind, solar, hydroelectric, biomass, or other such energy sources in an in situ conversion process essentially converts the alternate energy into liquid transportation fuels and other energy containing hydrocarbons with a very high efficiency. Alternate energy source usage may allow reduced life cycle greenhouse gas emissions, as in many cases the alternate energy sources (other than biomass) would replace an equivalent amount of power generated by fossil fuel. Even in the case of biomass, the carbon dioxide emitted would not come from fossil fuel, but would instead be recycled from the existing global carbon portfolio through photosynthesis. Unlike with fossil fuel combustion, there would therefore be no net addition of carbon dioxide to the atmosphere. If carbon dioxide from the biomass was captured and sequestered underground or elsewhere, there may be a net removal of carbon from the environment.

Use of alternate energy sources may allow for formation heating in areas where a power grid is lacking or where there otherwise is insufficient coal, oil, or natural gas available for power generation. In embodiments of in situ conversion processes that use combustion (e.g., natural distributed combustors) for heating a portion of a formation, the use of alternate energy sources may allow start up without the need for construction of expensive power plants or grid connections.

The use of alternate energy sources is not limited to supplying elecfricity for electric heaters. Alternate energy sources may also be used to supply power to surface facilities for processing fluids produced from a formation. Alternate energy sources may supply fuel for surface burners or other gas combustors. For example, biomass may produce methane and/or other combustible hydrocarbons for reservoir heating.

FIG. 113 illustrates a schematic of an embodiment using wind to generate electricity to heat a formation. Wind farm 6214 may include one or more windmills. The windmills may be of any type of mechanism that converts wind to a usable mechanical form of motion. For example, windmill 6216 can be a design as shown in the embodiment of FIG. 113 or have a design shown as an example in FIG. 114. fri some embodiments, the wind farm may include advanced windmills as suggested by the National Renewable Energy Laboratory (Golden, CO). Wind farm 6214 may provide power to generator 6212. Generator 6212 may convert power from wind farm 6214 into electrical power. In some embodiments, each windmill may include a generator. Elecfrical power from generator 6212 may be supplied to formation 6210. The elecfrical power may be used in formation 6210 to power heaters, pumps, or any elecfrical equipment that may be used in freating formation 6210. FIG. 115 illustrates a schematic of an embodiment for using solar power to heat a formation. A heating fluid may be provided from storage tank 6220 to solar anay 6224. The heating fluid may include any fluid that has a relatively low viscosity with relatively good heat fransfer properties (e.g., water, superheated steam, or molten ionic salts such as molten carbonate). In certain embodiments, a low melting point ionic salt may be used. Pump 6222 may be used to draw heating fluid from storage tank 6220 and provide the heating fluid to solar anay 6224.

Solar anay 6224 may include any anay designed to heat the heating fluid to a relatively high temperature (e.g., above about 650 °C) using solar energy. For example, solar anay 6224 may include a reflective trough with the heating fluid flowing through tubes within the reflective trough. The heating fluid may be provided to heater wells 6230 through hot fluid conduit 6226. Each heater well 6230 may be coupled to a branch of hot fluid conduit 6226. A portion of the heating fluid may be provided into each heater well 6230.

Each heater well 6230 may include two concentric conduits. Heating fluid may be provided into a heater well through an inner conduit. Heating fluid may then be removed from the heater well through an outer conduit. Heat may be fransfened from the heating fluid to at least a portion of the formation within each heater well 6230 to provide heat to the formation. A portion of each heater well 6230 in an overburden of the formation may be insulated such that no heat is fransfened from the heating fluid to the overburden. Heating fluid from each heater well 6230 may flow into cold fluid conduit 6228, which may return the heating fluid to storage tank 6220. Heating fluid may have cooled within the heater well to a temperature of about 480 °C. Heating fluid may be recfrculated in a closed loop process as needed. An advantage of using the heating fluid to provide heat to the formation may be that solar power is used directly to heat the formation without converting the solar power to electricity. Certain in situ conversion embodiments may include providing heat to a first portion of a relatively low permeability formation containing heavy hydrocarbons from one or more heat sources. Formation fluids may be produced from the first portion. A second portion of the formation may remain unpyrolyzed by maintaining temperature in the second portion below a pyrolysis temperature of hydrocarbons in the formation. In some embodiments, the second portion or significant sections of the second portion may remain unheated. A second portion that remains unpyrolyzed may be adjacent to a first portion of the formation that is subjected to pyrolysis. The second portion may provide structural sfrength to the formation. The second portion may be between the first portion and the third portion. Formation fluids may be produced from the third portion of the formation. A processed formation may have a pattern that resembles a striped or checkerboard pattern with alternating pyrolyzed portions and unpyrolyzed portions. In some in situ conversion embodiments, columns of unpyrolyzed portions of fonnation may remain in a formation that has undergone in situ conversion.

Unpyrolyzed portions of formation among pyrolyzed portions of formation may provide structural strength to the formation. The structural sfrength may inhibit subsidence of the formation. Inhibiting subsidence may reduce or eliminate subsidence problems such as changing surface levels and/or decreasing peπneability and flow of fluids in the formation due to compaction of the formation. Temperature (and average temperatures) within a heated relatively low permeability formation containing heavy hydrocarbons may vary depending on a number of factors. The factors may include, but are not limited to proximity to a heat source, thermal conductivity and thermal diffusivity of the formation, type of reaction occuning, type of relatively low permeability formation containing heavy hydrocarbons, and the presence of water within the relatively low peπneability formation containing heavy hydrocarbons. A temperature within the relatively low permeability formation containing heavy hydrocarbons may be assessed using a numerical simulation model. The numerical simulation model may calculate a subsurface temperature distribution. In addition, the numerical simulation model may assess various properties of a subsurface foπnation using the calculated temperature disfribution.

Assessed properties of the subsurface formation may include, but are not limited to, thermal conductivity of the subsurface portion of the formation and penneability of the subsurface portion of the formation. The numerical simulation model may also assess various properties of fluid foπned within a subsurface formation using the calculated temperature disfribution. Assessed properties of formed fluid may include, but are not limited to, a cumulative volume of a fluid foπned in the formation, fluid viscosity, fluid density, and a composition of the fluid in the formation. The numerical simulation model may be used to assess the performance of commercial-scale operation of a small-scale field experiment. For example, a performance of a commercial-scale development may be assessed based on, but is not limited to, a total volume of product producible from a commercial-scale operation, amount of producible undesired products, and/or a time frame needed before production becomes economical.

In some in situ conversion process embodiments, the in situ conversion process increases a temperature or average temperature within a selected portion of a relatively low penneability formation containing heavy hydrocarbons. A temperature or average temperature increase (AT) in a specified volume (V) of the relatively low permeability formation containing heavy hydrocarbons may be assessed for a given heat input rate (q) over time (t) by EQN. 41:

In EQN. 41, an average heat capacity of the formation (C_v) and an average bulk density of the formation (p_B) may be estimated or determined using one or more samples taken from the relatively low permeability formation containing heavy hydrocarbons.

An in situ conversion process may include heating a specified volume of relatively low permeability formation containing heavy hydrocarbons to a pyrolysis temperature or average pyrolysis temperature. Heat input rate (q) dining a time (t) required to heat the specified volume (V) to a desired temperature increase (AT) may be determined or assessed using EQN. 42:

(42) ∑ q * t = tAT * c_v * p Υ

In EQN. 42, an average heat capacity of the formation (C„) and an average bulk density of the formation (p_B) may be estimated or determined using one or more samples taken from the relatively low permeability formation containing heavy hydrocarbons.

EQNS. 41 and 42 may be used to assess or estimate temperatures, average temperatures (e.g., over selected sections of the formation), heat input, etc. Such equations do not take into account other factors (such as heat losses), which would also have some effect on heating and temperature assessments. However such factors can ordinarily be addressed with conection factors.

In some in situ conversion process embodiments, a portion of a relatively low permeability formation containing heavy hydrocarbons may be heated at a heating rate in a range from about 0.1 °C/day to about 50 °C/day.

Alternatively, a portion of a relatively low permeability formation containing heavy hydrocarbons may be heated at a heating rate in a range of about 0.1 °C/day to about 10 °C/day . For example, a maj ority of hydrocarbons may be produced from a formation at a heating rate within a range of about 0.1 °C/day to about 10 °C/day. In addition, a relatively low permeability foπnation containing heavy hydrocarbons may be heated at a rate of less than about 0J °C/day through a significant portion of a pyrolysis temperature range. The pyrolysis temperature range may include a range of temperatures as described in above embodhnents. For example, the heated portion may be heated at such a rate for a time greater than 50% of the time needed to span the temperature range, more than 75% of the time needed to span the temperature range, or more than 90% of the time needed to span the temperature range.

A rate at which a relatively low permeability formation containing heavy hydrocarbons is heated may affect the quantity and quality of the formation fluids produced from the relatively low permeability formation containing heavy hydrocarbons. For example, heating at high heating rates may allow for production of a large quantity of condensable hydrocarbons from a relatively low permeability foπnation containing heavy hydrocarbons. The products of such a process may be of a significantly lower quality than would be produced using heating rates less than about 10 °C/day. Heating at a rate of temperature increase less than approximately 10 °C/day may allow pyrolysis to occur within a pyrolysis temperature range in which production of undesirable products and heavy hydrocarbons may be reduced. In addition, a rate of temperature increase of less than about 3 °C/day may further increase the quality of the produced condensable hydrocarbons by further reducing the production of undesirable products and further reducing production of heavy hydrocarbons from a relatively low permeability formation containing heavy hydrocarbons.

It is believed that decreasing the heating rate of the formation may decrease production of olefins. The heating rate of the foπnation may be determined, in part, by the spacings of heat sources within the formation and/or by the amount of heat that is transfened from the heat sources to the formation.

In some in situ conversion process embodiments, controlling temperature within a relatively low permeability formation containing heavy hydrocarbons may involve controlling a heating rate within the formation. For example, controlling the heating rate such that the heating rate is less than approximately 3 °C/day may provide better control of temperature within the relatively low permeability formation containing heavy hydrocarbons.

An in situ process for hydrocarbons may include monitoring a rate of temperature increase at a production well. A temperature within a portion of a relatively low permeability formation containing heavy hydrocarbons, however, may be measured at various locations within the portion of the formation. An in situ process may include monitoring a temperature of the portion at a midpoint between two adjacent heat sources. The temperature may be monitored over time to allow for calculation of rate of temperature increase. A rate of temperature increase may affect a composition of formation fluids produced from the formation. Energy input into a formation may be adjusted to change a heating rate of the formation based on calculated rate of temperature increase in the formation to promote production of desired products.

In some embodiments, a power (Pwr) required to generate a heating rate (h) in a selected volume (V) of a relatively low permeability formation containing heavy hydrocarbons may be determined by EQN. 43:

(43) Pwr=h*V*C_v*p_B

In EQN. 43, an average heat capacity of the relatively low permeability formation containing heavy hydrocarbons is described as Cy. The average heat capacity of the relatively low permeability formation containing heavy hydrocarbons may be a relatively constant value. Average heat capacity may be estimated or determined using one or more samples taken from a relatively low permeability formation containing heavy hydrocarbons, or the average heat capacity may be measured in situ using a thermal pulse test. Methods of determining average heat capacity based on a thermal pulse test are described by I. Berchenko, E. Detournay, N. Chandler, J. Martino, and E. Kozak, "In-situ measurement of some thermoporoelastic parameters of a granite" in Poromechanics, A Tribute to Maurice A. Biot, pages 545-550, Rotterdam, 1998 (Balkema), which is incoφorated by reference as if fully set forth herein.

An average bulk density of the relatively low permeability formation containing heavy hydrocarbons is described as p_B. The average bulk density of the relatively low permeability formation containing heavy hydrocarbons may be a relatively constant value. Average bulk density may be estimated or determined using one or more samples taken from a relatively low permeability formation containing heavy hydrocarbons. In certain embodiments, the product of average heat capacity and average bulk density of the relatively low permeability formation containing heavy hydrocarbons may be a relatively constant value (such product can be assessed in situ using a thermal pulse test).

A determined power may be used to determine heat provided from a heat source into the selected volume such that the selected volume may be heated at a heating rate, h. For example, a heating rate may be less than about 3 °C/day, and even less than about 2 °C/day. A heating rate within a range of heating rates may be maintained within the selected volume. It is to be understood that in this context "power" is used to describe energy input per time. The form of such energy input may vary (e.g., energy may be provided from electrical resistance heaters, combustion heaters, etc.).

The heating rate may be selected based on a number of factors including, but not limited to, the maximum temperature possible at the well, a predetermined quality of formation fluids that may be produced from the formation, and/or spacing between heat sources. . A quality of hydrocarbon fluids may be defined by an API gravity of condensable hydrocarbons, by olefin content, by the nifrogen, sulfur and/or oxygen content, etc. In an in situ conversion process embodiment, heat may be provided to at least a portion of a relatively low permeability formation containing heavy hydrocarbons to produce formation fluids having an API gravity of greater than about 20°. The API gravity may vary, however, depending on a number of factors including the heating rate and a pressure within the portion of the formation and the time relative to initiation of the heat sources when the formation fluid is produced.

Subsurface pressure in a relatively low permeability formation containing heavy hydrocarbons may conespond to the fluid pressure generated within the formation. Heating hydrocarbons within a relatively low permeability formation containing heavy hydrocarbons may generate fluids by pyrolysis. The generated fluids may be vaporized within the formation. Vaporization and pyrolysis reactions may increase the pressure within the formation. Fluids that contribute to the increase in pressure may include, but are not limited to, fluids produced during pyrolysis and water vaporized during heating. As temperatures within a selected section of a heated portion of the formation increase, a pressure within the selected section may increase as a result of increased fluid generation and vaporization of water. Controlling a rate of fluid removal from the formation may allow for confrol of pressure in the formation.

In some embodiments, pressure within a selected section of a heated portion of a relatively low permeability formation containing heavy hydrocarbons may vary depending on factors such as depth, distance from a heat source, a richness of the hydrocarbons within the relatively low permeability formation containing heavy hydrocarbons, and/or a distance from a producer well. Pressure within a formation may be determined at a number of different locations (e.g., near or at production wells, near or at heat sources, or at monitor wells). Heating of a relatively low permeability formation containing heavy hydrocarbons to a pyrolysis temperature range may occur before substantial peπneability has been generated within the relatively low permeability formation containing heavy hydrocarbons. An initial lack of peπneability may inhibit the transport of generated fluids from a pyrolysis zone within the formation to a production well. As heat is initially fransfened from a heat source to a relatively low permeability formation containing heavy hydrocarbons, a fluid pressure within the relatively low penneability formation containing heavy hydrocarbons may increase proximate a heat source. Such an increase in fluid pressure may be caused by generation of fluids during pyrolysis of at least some hydrocarbons in the formation. The increased fluid pressure may be released, monitored, altered, and/or confrolled through the heat source. For example, the heat source may include a valve that allows for removal of some fluid from the foπnation. In some heat source embodiments, the heat source may include an open wellbore configuration that inhibits pressure damage to the heat source.

In some in situ conversion process embodiments, pressure generated by expansion of pyrolysis fluids or other fluids generated in the formation may be allowed to increase although an open path to the production well or any other pressure sink may not yet exist in the formation. The fluid pressure may be allowed to increase towards a lithostatic pressure. Fractures in the relatively low permeability formation containing heavy hydrocarbons may form when the fluid approaches the lithostatic pressure. For example, fractures may form from a heat source to a production well. The generation of fractures within the heated portion may relieve some of the pressure within the portion.

When permeability or flow channels to production wells are established, pressure within the foπnation may be controlled by controlling production rate from the production wells. In some embodiments, a back pressure may be maintained at production wells or at selected production wells to maintain a selected pressure within the heated portion.

A formation may include one or more lean zones. Lean zones may include zones with a relatively low hydrocarbon content. Rich zones may include zones with a relatively high hydrocarbon content. Lean zones may exist at an upper or lower boundary of a rich zone and/or may exist as lean zone layers between layers of rich zone layers. Generally, lean zones may be more permeable and include more brittle material than rich zones. In addition, rich zones typically have a lower thermal conductivity than lean zones. For example, lean zones may include zones through which fluids (e.g., water) can flow or flow through. In some cases, however, lean zones may have lower permeabilities and/or include somewhat less brittle material. In an in situ process for freating a formation, heat may be applied to rich zones with substantial amounts of hydrocarbons to pyrolyze and produce hydrocarbons from the rich zones. Applying heat to lean zones may be inhibited to avoid creating fractures within the lean zones (e.g., when the lean zone is at an outer boundary of the formation).

In certain embodiments, heat may be applied to a lean zone (e.g., a lean zone between two rich zones) to create and propagate fractures within the lean zone. Applying heat to a lean zone and creating fractures within the lean zone may allow for earlier production of hydrocarbons from a formation. In some embodhnents, heating of the lean zone may not be needed as fractures or high permeability is initially present within the lean zone. Formation fluids may flow through a permeable lean zone more rapidly than through other portions of a formation. Formation fluids may be produced through a production well earlier during heating of the foπnation in the presence of a permeable lean zone. The permeable lean zone may provide a pathway for the flow of fluids between the heat front where fluids are pyrolyzed and the production well. Production of formation fluids through the permeable lean zone may increase the production of fluids as liquids, inhibit pressure buildup in the formation, inhibit failure/collapse of wells due to high pressures, and/or allow for convective heat fransfer through the fractures.

FIG. 116 depicts a cross-sectional representation of an embodiment for freating lean zones 8690 and rich zones 8691 of a formation. Lean zones 8690 and rich zones 8691 are below overburden 540. In some embodiments, lean zones 8690 may be relatively penneable sections of the formation. Rich zones 8691 may be sections of the formation that are selected for freatment based on a richness of the section. Rich zones 8691 may have an initial average permeability thickness product of less than about 10 millidarcy feet. Certain rich zones may have an initial average permeability thickness product of less than about I millidarcy feet or less than about 0.5 millidarcy feet. Heat source 8692 may be placed through overburden 540 and into opening 514. Reinforcing material 544

(e.g., cement) may seal a portion of opening 514 to overburden 540. Heat source 8692 may apply heat to lean zones 8690 and/or rich zones 8691. hi some embodiments, heat source 8692 may include a conductor with a thickness that is adjusted to provide more heat to rich zones 8691 than lean zones 8690 (i.e., the thickness of the conductor is larger proximate the lean zones than the thickness of the conductor proximate the rich zones). In certain embodiments, rich zones 8691 may not fracture. For example, the rich zones may have a ductility that is high enough to inhibit the formation of fractures. A formation may have one or more lean zones 8690 and one or more rich zones 8691 that are layered throughout the formation as shown in FIG. 116. Formation fluids formed in rich zones 8691 may be produced through pre-existing fractures in lean zone 8690. In some embodiments, lean zone 8690 may have a permeability sufficiently high to allow production of fluids. This high permeability may be initially present in the lean zone because of, for example, water flow through the lean zone that leached out minerals over geological time prior to initiation of the in situ conversion process. In some embodiments, the application of heat to the formation from heat sources may produce, or increase the size of, fractures 8696 and/or increase the permeability in lean zones 8690. Fractures 8696 may increase the permeability of lean zones 8690 by providing a pathway for fluids to propagate through the lean zones. During early times of heating, permeability may be created near opening 514. Permeability may be created in permeable zone 8695 adjacent opening 514. Permeable zone 8695 will increase in size and move out radially as the heat front produced by heat source 8692 moves outward. As the heat front migrates through the formation, hydrocarbons may be pyrolyzed as temperatures within rich zones 8691 reach pyrolysis temperatures. Pyrolyzation of the hydrocarbons, along with heating of the rich zones, may increase the permeability of rich zones 8691. At later times of heating, hydrocarbons in coking portion 8693 of permeable zone 8695 may coke as temperatures within this portion increase to coking temperatures. At some point permeable zone 8695 will move outward to a distance from opening 514 at which no coking of hydrocarbons occurs (i.e., a distance at which temperatures do not approach coking temperatures). Permeable zone 8695 may continue to expand with the migration of the heat front through the formation. If sufficient water is present, coking may be suppressed near opening 514. In certain embodiments, fluids formed in rich zones 8691 may flow into lean zones 8690 through permeable zone 8695. Coking portion 8693 may inhibit the flow of fluids between rich zones 8691 and lean zones 8690. Fluids may continue to flow into lean zones 8690 through un-coked portions of penneable zone 8695. In some embodiments, fluids may flow to opening 514 (e.g., during early times of heating before permeable zone 8695 has sufficient permeability for fluid flow into the lean zones). Fluids that flow to opening 514 may be produced through the opening or be allowed to flow through lean zones 8690 to production well 8698. In addition, during early times of heating, some coke formation may occur near opening 514. Allowing formation fluids to be produced through lean zones 8690 may allow for earlier production of fluids formed in rich zones 8691. For example, fluids foπned in rich zones 8690 may be produced through lean zones 8690 before sufficient permeability has been created in the rich zones for fluids to flow directly within the rich zones to production well 8698. Producing at least some fluids through lean zone 8690 or through opening 514 may inhibit a buildup of pressure within the formation during heating of the formation.

In certain embodiments, fractures 8696 may propagate in a horizontal direction. However, fractures 8696 may propagate in other directions depending on, for example, a depth of the fracturing layer and structure of the fracturing layer. In certain embodiments, the creation of angled or vertical fractures may be inhibited to inhibit fracturing into an aquifer or other environmentally sensitive area. In some embodiments, applying heat to rich zones 8691 may create fractures within the rich zones.

Fractures within rich zone 8691 may be less likely to initially occur due to the more ductile (less brittle) composition of the rich zone as compared to lean zones 8690. In an embodiment, fractures may develop that connect lean zones 8690 and rich zones 8691. These fractures may provide a path for propagation of fluids from one zone to the other zone. Production well 8698 may be placed at an angle, vertically, or horizontally into lean zones 8690 and rich zones 8691. Production well 8698 may produce formation fluids from lean zones 8690 and/or rich zones 8691.

In some embodiments, more than one production well may be placed in lean zones 8690 and/or rich zones 8691. A number of production wells may be determined by, for example, a desired product quality of the produced fluids, a desired production rate, a desired weight percentage of a component in the produced fluids, etc. In other embodiments, formation fluids may be produced through opening 514, which may be uncased or perforated. Producing formation fluids through opening 514 tends to increase cracking of hydrocarbons (from the heat provided by heat source 8692) as the fluids propagate along the length of the opening. Fluids produced through opening 514 may have lower carbon numbers than fluids produced through production well 8698.

In an in situ conversion process embodiment, pressure may be increased within a selected section of a portion of a relatively low permeability formation containing heavy hydrocarbons to a selected pressure during pyrolysis. A selected pressure may be within a range from about 2 bars absolute to about 72 bars absolute or, in some embodiments, 2 bars absolute to 36 bars absolute. Alternatively, a selected pressure may be within a range from about 2 bars absolute to about 18 bars absolute. In some in situ conversion process embodiments, a majority of hydrocarbon fluids may be produced from a formation having a pressure within a range from about 2 bars absolute to about 18 bars absolute. The pressure during pyrolysis may vary or be varied. The pressure may be varied to alter and/or confrol a composition of a formation fluid produced, to confrol a percentage of condensable fluid as compared to non-condensable fluid, and or to confrol an API gravity of fluid being produced. For example, decreasing pressure may result in production of a larger condensable fluid component. The condensable fluid component may contain a larger percentage of olefins. In some in situ conversion process embodiments, increased pressure due to fluid generation may be maintained within the heated portion of the formation. Maintaining increased pressure within a formation may inhibit formation subsidence during in situ conversion. Increased formation pressure may promote generation of high quality products during pyrolysis. Increased formation pressure may facilitate vapor phase production of fluids from the formation. Vapor phase production may allow for a reduction in size of collection conduits used to transport fluids produced from the formation. Increased formation pressure may reduce or eliminate the need to compress formation fluids at the surface to transport the fluids in collection conduits to surface facilities. Maintaining increased pressure within a formation may also facilitate generation of elecfricity from produced non- condensable fluid. For example, the produced non-condensable fluid may be passed through a turbine to generate elecfricity.

Increased pressure in the formation may also be maintained to produce more and/or improved formation fluids. In certain in situ conversion process embodiments, significant amounts (e.g., a majority) of the hydrocarbon fluids produced from a fonnation may be non-condensable hydrocarbons. Pressure may be selectively increased and/or maintained within the formation to promote formation of smaller chain hydrocarbons in the formation. Producing small chain hydrocarbons in the formation may allow more non-condensable hydrocarbons to be produced from the formation. The condensable hydrocarbons produced from the foπnation at higher pressure may be of a higher quality (e.g., higher API gravity) than condensable hydrocarbons produced from the formation at a lower pressure.

A high pressure may be maintained within a heated portion of a relatively low permeability foπnation containing heavy hydrocarbons to inhibit production of formation fluids having carbon numbers greater than, for example, about 25. Some high carbon number compounds may be entrained in vapor in the formation and may be removed from the formation with the vapor. A high pressure in the foπnation may inhibit entrainment of high carbon number compounds and or multi-ring hydrocarbon compounds in the vapor. Increasing pressure within the relatively low permeability formation containing heavy hydrocarbons may increase a boiling point of a fluid within the portion. High carbon number compounds and or multi-ring hydrocarbon compounds may remain in a liquid phase in the formation for significant time periods. The significant time periods may provide sufficient time for the compounds to pyrolyze to form lower carbon number compounds.

Maintaining increased pressure within a heated portion of the formation may suφrisingly allow for production of large quantities of hydrocarbons of increased quality. Maintaining increased pressure may promote vapor phase transport of pyrolyzation fluids within the formation. Increasing the pressure often permits production of lower molecular weight hydrocarbons since such lower molecular weight hydrocarbons will more readily transport in the vapor phase in the formation.

Generation of lower molecular weight hydrocarbons (and conesponding increased vapor phase transport) is believed to be due, in part, to autogenous generation and reaction of hydrogen within a portion of the relatively low permeability formation containing heavy hydrocarbons. For example, maintaining an increased pressure may force hydrogen generated during pyrolysis into a liquid phase (e.g., by dissolving). Heating the portion to a temperature within a pyrolysis temperature range may pyrolyze hydrocarbons within the formation to generate pyrolyzation fluids in a liquid phase. The generated components may include double bonds and/or radicals. H₂ in the liquid phase may reduce double bonds of the generated pyrolyzation fluids, thereby reducing a potential for polymerization or formation of long chain compounds from the generated pyrolyzation fluids. In addition, hydrogen may also neutralize radicals in the generated pyrolyzation fluids. Therefore, H₂ in the liquid phase may inhibit the generated pyrolyzation fluids from reacting with each other and/or with other compounds in the formation. Shorter chain hydrocarbons may enter the vapor phase and may be produced from the formation.

Increasing the formation pressure may reduce the potential for coking within a selected section of the formation. Coking reactions may occur substantially in a liquid phase at high temperatures. Coking reactions may occur in localized sections of the formation. An in situ conversion process embodiment may slowly raise temperature within a selected section. Pyrolysis reactions that occur in a liquid phase may result in the production of small molecules in the liquid phase. The small molecules may leave the liquid as a vapor due to local - temperature and pressure conditions. The small molecules undergoing phase change from a liquid phase to a vapor phase may absorb a significant amount of heat. The absorbed heat may help to inhibit high temperatures that could result in coking reactions. In addition, increased pressure in the formation may result in a significant amount of hydrogen being forced into the liquid phase present in the formation. The hydrogen may inhibit polymerization reactions that result in the generation of large hydrocarbon molecules. Inhibiting the production of large hydrocarbon molecules may result in less coking within the formation.

Operating an in situ conversion process at increased pressure may allow for vapor phase production of fonnation fluid from the foπnation. Vapor phase production may permit increased recovery of lighter (and relatively high quality) pyrolyzation fluids. Vapor phase production may result in less formation fluid being left in the formation after the fluid is produced by pyrolysis. Vapor phase production may allow for fewer production wells in the formation than is present using liquid phase or liquid/vapor phase production. Fewer production wells may significantly reduce equipment costs associated with an in situ conversion process.

In an embodiment, a portion of a relatively low permeability formation containing heavy hydrocarbons may be heated to increase a partial pressure of H₂. In some embodiments, an increased H₂ partial pressure may include H₂ partial pressures in a range from about 0.5 bars absolute to about 7 bars absolute. Alternatively, an increased H₂ partial pressure range may include H₂ partial pressures in a range from about 5 bars absolute to about 7 bars absolute. For example, a majority of hydrocarbon fluids may be produced wherein a H₂ partial pressure is within a range of about 5 bars absolute to about 7 bars absolute. A range of H₂ partial pressures within the pyrolysis H₂ partial pressure range may vary depending on, for example, temperature and pressure of the heated portion of the formation.

Maintaining a H₂ partial pressure within the formation of greater than atmospheric pressure may increase an API value of produced condensable hydrocarbon fluids. Maintaining an increased H₂ partial pressure may increase an API value of produced condensable hydrocarbon fluids to greater than about 25° or, in some instances, greater than about 30°. Maintaining an increased H₂ partial pressure within a heated portion of a relatively low permeability formation containing heavy hydrocarbons may increase a concenfration of H₂ within the heated portion. The H₂ may be available to react with pyrolyzed components of the hydrocarbons. Reaction of H₂ with the pyrolyzed components of hydrocarbons may reduce polymerization of olefins into tars and other cross-linked, difficult to upgrade, products. Therefore, production of hydrocarbon fluids having low API gravity values may be inhibited. In an embodiment, a method for freating a relatively low permeability formation containing heavy hydrocarbons in situ may include adding hydrogen to a selected section of the formation when the selected section is at or undergoing certain conditions. For example, the hydrogen may be added through a heater well or production well located in or proximate the selected section. Since hydrogen is sometimes in relatively short supply (or relatively expensive to make or procure), hydrogen may be added when conditions in the formation optimize the use of the added hydrogen. For example, hydrogen produced in a section of a formation undergoing synthesis gas generation may be added to a section of the formation undergoing pyrolysis. The added hydrogen in the pyrolysis section of the formation may promote formation of aliphatic compounds and inhibit formation of olefϊnic compounds that reduce the quality of hydrocarbon fluids produced from formation.

In some embodiments, hydrogen may be added to the selected section after an average temperature of the formation is at a pyrolysis temperature (e.g., when the selected section is at least about 270 °C). In some embodiments, hydrogen may be added to the selected section after the average temperature is at least about 290 °C, 320 °C, 375 °C, or 400 °C. Hydrogen may be added to the selected section before an average temperature of the formation is about 400 °C. In some embodiments, hydrogen may be added to the selected section before the average temperature is about 300 °C or about 325 °C.

The average temperature of the formation may be confrolled by selectively adding hydrogen to the selected section of the formation. Hydrogen added to the formation may react in exothermic reactions. The exothermic reactions may heat the formation and reduce the amount of energy that needs to be supplied from heat sources to the formation. In some embodiments, an amount of hydrogen may be added to the selected section of the formation such that an average temperature of the formation does not exceed about 400 °C.

A valve may maintain, alter, and/or control a pressure within a heated portion of a relatively low permeability formation containing heavy hydrocarbons. For example, a heat source disposed within a relatively low permeability formation containing heavy hydrocarbons may be coupled to a valve. The valve may release fluid from the formation through the heat source. In addition, a pressure valve may be coupled to a production well within the relatively low permeability formation containing heavy hydrocarbons. In some embodiments, fluids released by the valves may be collected and transported to a surface unit for further processing and/or freatment. An in situ conversion process for hydrocarbons may include providing heat to a portion of a relatively low peπneability foπnation containing heavy hydrocarbons and controlling a temperature, rate of temperature increase, and/or pressure within the heated portion. A temperature and/or a rate of temperature increase of the heated portion may be controlled by altering the energy supplied to heat sources in the formation.

Controlling pressure and temperature within a relatively low permeability formation containing heavy hydrocarbons may allow properties of the produced formation fluids to be controlled. For example, composition and quality of formation fluids produced from the formation may be altered by altering an average pressure and/or an average temperature in a selected section of a heated portion of the formation. The quality of the produced fluids may be evaluated based on characteristics of the fluid such as, but not limited to, API gravity, percent olefins in the produced formation fluids, ethene to ethane ratio, atomic hydrogen to carbon ratio, percent of hydrocarbons within produced formation fluids having carbon numbers greater than 25, total equivalent production (gas and liquid), total liquids production, and/or liquid yield. Controlling the quality of the produced foπnation fluids may include controlling average pressure and average temperature in the selected section such that the average assessed pressure in the selected section is greater than the pressure (p) as set forth in the form of EQN. 44 for an assessed average temperature (T) in the selected section:

where/? is measured in psia (pounds per square inch absolute), Tis measured in Kelvin, and ,4 and B are parameters dependent on the value of the selected property.

EQN. 44 may be rewritten such that the natural log of pressure is a linear function of the inverse of temperature. This form of EQN. 44 is expressed as: ln(p) = A/T+B. In a plot of the absolute pressure as a function of the reciprocal of the absolute temperature, A is the slope and B is the intercept. The intercept B is defined to be the natural logarithm of the pressure as the reciprocal of the temperature approaches zero. The slope and intercept values (A and B) of the pressure-temperature relationship may be determined from at least two pressure-temperature data points for a given value of a selected property. The pressure-temperature data points may include an average pressure within a foπnation and an average temperature within the formation at which the particular value of the property was, or may be, produced from the formation. The pressure-temperature data points may be obtained from an experiment such as a laboratory experiment or a field experiment.

A relationship between the slope parameter, A, and a value of a property of formation fluids may be determined. For example, values of A may be plotted as a function of values of a formation fluid property. A cubic polynomial may be fitted to these data. For example, a cubic polynomial relationship such as EQN. 45:

(45) A = a ι* (property)³ + a₂*(property)² + a₃* (property) + a₄;

may be fitted to the data, where a a₂, a₃, and a₄ are empirical constants that describe a relationship between the first parameter, A, and a property of a formation fluid. Alternatively, relationships having other functional forms such as another order polynomial, trigonometric function, or a logarithmic function may be fitted to the data. Values for a_t, a₂, ..., may be estimated from the results of the data fitting. Similarly, a relationship between the second parameter, B, and a value of a property of formation fluids may be determined. For example, values of B may be plotted as a function of values of a property of a formation fluid. A cubic polynomial may also be fitted to the data. For example, a cubic polynomial relationship such as EQN. 46:

(46) B = bi* (property)³ + b₂* (property)² + b₃* (property) + b₄;

may be fitted to the data, where b_h b₂, b₃, and b are empirical constants that may describe a relationship between the parameter B and the value of a property of a formation fluid. As such, b_h b₂, b₃, and b₄ may be esthnated from results of fitting the data.

To detennine an average pressure and an average temperature for producing a formation fluid having a selected property, the value of the selected property and the empirical constants may be used to determine values for the first parameter A and the second parameter B, according to EQNS. 47 and 48:

(47) A = aι* (property)³ + a₂* (property)² + a₃* (property) + a₄

(48) B = b i* (property)³ + b₂*(property)² + b₃*(property) + b₄

In some in situ conversion process embodiments, the determined values for the parameter A and the parameter B may be used to determine an average pressure in the selected section of the formation using an assessed average temperature, T, in the selected section. For example, an average pressure of the selected section may be determined by EQN. 49:

(49) p = exp[(A/T) + BJ,

in which ? is expressed in psia, and Tis expressed in Kelvin. Alternatively, an average absolute pressure of the selected section, measured in bars, may be determined using EQN. 50:

(50) _ars= exp[(Λ/7) + 2? -2.6744]. An average pressure within the selected section may be confrolled such that the average pressure within the selected section is about the value calculated from the equation. Formation fluid produced from the selected section may approximately have the chosen value of the selected property, and therefore, the desired quality.

In some in situ conversion process embodhnents, the determined values for the parameter A and the parameter B may be used to determine an average temperature in the selected section of the formation using an assessed average pressure, p, in the selected section. Using the relationships described above, an average temperature within the selected section may be confrolled to approxhnate the calculated average temperature to produce hydrocarbon fluids having a selected property and quality.

It is believed that pyrolyzing at reduced temperature and increased pressure may decrease an olefin to paraffin ratio in produced fluids. Ethene to ethane ratio in non-condensable hydrocarbons may be reflective of olefin content in all produced hydrocarbons. Pyrolyzing hydrocarbons for a longer period of time, which may be accomplished by increasing pressure within the system, tends to result in a lower average molecular weight oil and higher API gravity. In addition, production of gas may increase and a non- olatile coke may be formed.

In addition, it is believed that operating at high pressure and a pyrolysis temperature at the lower end of the pyrolysis zone tends to decrease the fraction of fluids with carbon numbers greater than 25 produced from the heavy oil.

It is believed that lower temperatures and/or increased partial pressure of hydrogen in the heavy oil containing diatomite formation will tend to produce less olefins in the produced hydrocarbon fluids. In addition, lower temperatures and or higher partial pressures of hydrogen also tend to increase the atomic hydrogen to atomic carbon ratio in the produced hydrocarbon fluids.

It is believed that at higher pyrolysis temperatures production of oil liquids tends to be higher than at the lower pyrolysis temperatures. In addition, high pressures tend to decrease the quantity of oil liquids produced from a heavy oil containing diatomite foπnation. Operating an in situ conversion process at low pressures and high temperatures may produce a higher quantity of oil liquids than operating at low temperatures and high pressures. Formation fluid properties may vary depending on a location of a production well in the formation. For example, a location of a production well with respect to a location of a heat source in the formation may affect the composition of fonnation fluid produced from the formation. Distance between a production well and a heat source in the formation may be varied to alter the composition of formation fluid producible from the formation. Having a short distance between a production well and a heat source or heat sources may allow a high temperature to be maintained at and adjacent to the production well. Having a high temperature at and adjacent to the production well may allow a substantial portion of pyrolyzation fluids flowing to and through the production well to crack to non- condensable compounds. In some in situ conversion process embodiments, location of production wells relative to heat sources may be selected to allow for production of formation fluid having a large non-condensable gas fraction. In some in situ conversion process embodiments, location of production wells relative to heat sources may be selected to increase a condensable gas fraction of the produced formation fluids. During operation of in situ conversion process embodiments, energy input into heat sources adjacent to production wells may be confrolled to allow for production of a desired ratio of non-condensable to condensable hydrocarbons.

A carbon number distribution of a produced formation fluid may indicate a quality of the produced foπnation fluid. In general, condensable hydrocarbons with low carbon numbers are considered to be more valuable than condensable hydrocarbons having higher carbon numbers. Low carbon numbers may include, for example, carbon numbers less than about 25. High carbon numbers may include carbon numbers greater than about 25. In an in situ conversion process embodiment, the in situ conversion process may include providing heat to a portion of a formation so that a majority of hydrocarbons produced from the formation have carbon numbers of less than approximately 25.

An in situ conversion process may be operated so that carbon numbers of the largest weight fraction of hydrocarbons produced from the formation are about 12, for a given time period. The time period may be total time of operation, or a selected subset of operation (e.g., a day, week, month, year, etc.). Operating conditions of an in situ conversion process may be adjusted to shift the carbon number of the largest weight fraction of hydrocarbons produced from the formation. For example, increasing pressure in a formation may shift the carbon number of the largest weight fraction of hydrocarbons produced from the formation to a smaller carbon number. Shifting the carbon number of the largest weight fraction of hydrocarbons produced from the formation may also be expressed as shifting the mean carbon number of the carbon number disfribution.

In some in situ conversion process embodiments, hydrocarbons produced from the formation may have a mean carbon number less than about 25. In some in situ conversion process embodiments, less than about 15 weight % of the hydrocarbons in the condensable hydrocarbons have carbon numbers greater than approximately 25. In some embodiments, less than about 5 weight % of hydrocarbons in the condensable hydrocarbons have carbon numbers greater than about 25, and/or less than about 2 weight % of hydrocarbons in the condensable hydrocarbons have carbon numbers greater than about 25.

In an in situ conversion process embodiment, the in situ conversion process may include providing heat to at least a portion of a relatively low permeability formation containing heavy hydrocarbons at a rate sufficient to alter and/or control production of olefins. The in situ conversion process may include heating the portion at a rate to produce formation fluids having an olefin content of less than about 10 weight % of condensable hydrocarbons of the formation fluids. Reducing olefin production may reduce coating of pipe surfaces by the olefins, thereby reducing difficulty associated with transporting hydrocarbons through the piping. Reducing olefin production may inhibit polymerization of hydrocarbons during pyrolysis, thereby increasing permeability in the foπnation and/or enhancing the quality of produced fluids (e.g., by lowering the mean carbon number of the carbon number distribution for fluids produced from the formation, increasing API gravity, etc.).

In some in situ conversion process embodiments, however, the portion may be heated at a rate to allow for production of olefins from formation fluid in sufficient quantities to allow for economic recovery of the olefins. Olefins in produced formation fluid may be separated from other hydrocarbons. Operating conditions (i.e., temperature and pressure) within the formation may be selected to confrol the composition of olefins produced along with other formation fluid. For example, operating conditions of an in situ conversion process may be selected to produce a carbon number distribution with a mean carbon number of about 9. Only a small weight fraction of the olefins produced may have carbon numbers greater than 9. The small weight fraction may not significantly affect the quality (e.g., API gravity) of the produced fluid from the formation. The fluid may remain easy to process even with enough olefins present to make separation of olefins economically viable.

Hydrocarbons in produced fluids may include a mixture of a number of different hydrocarbon components. Hydrocarbons in formation fluid produced from a formation may have a hydrogen to carbon atomic ratio that is at least approximately 1.7 or above. For example, the hydrogen to carbon atomic ratio of a produced fluid may be approximately 1.8, approximately 1.9, or greater. The ratio may be below two because of the presence of aromatic compounds and/or olefins. Some of the hydrocarbon components are condensable and some are not. The fraction of non-condensable hydrocarbons within the produced fluid may be altered and/or confrolled by altering, controlling, and/or maintaining a high temperature and/or high pressure during pyrolysis within the formation. Surface facilities may separate hydrocarbon fluids from non-hydrocarbon fluids. Surface facilities may also separate condensable hydrocarbons from non-condensable hydrocarbons.

In some embodiments, the non-condensable hydrocarbons may include hydrocarbons having carbon numbers less than or equal to 5. Produced formation fluid may also include non-hydrocarbon, non-condensable fluids such as, but not limited to, H₂, C0₂, ammonia, H₂S, N and/or CO. In certain embodiments, non-condensable hydrocarbons of a fluid produced from a portion of a relatively low permeability formation containing heavy hydrocarbons may have a weight ratio of hydrocarbons having carbon numbers from 2 through 4 ("C_2-4 hydrocarbons") to methane of greater than about 0.3, greater than about 0.75, or greater than about 1 in some circumstances. Hydrocarbon resource characteristics may influence the ratio of C₂. hydrocarbons to methane.

Operating conditions (e.g., temperature and pressure) may be adjusted to influence a ratio of C_2- hydrocarbons to methane. For example, producing hydrocarbons from a relatively hot formation at a relatively high formation may produce significant amount of methane, which may result in a significantly lower value for the ratio of C_2-4 hydrocarbons to methane as compared to fluid produced from the same formation at milder temperature and pressure conditions.

An in situ conversion process may be able to produce a high weight ratio of C_2- hydrocarbons to methane as compared to ratios producible using other processes such as fire floods or steam floods. High weight ratios of C_{2- 4} hydrocarbons to methane may indicate the presence of significant amounts of hydrocarbons with 2, 3, and/or 4 carbons (e.g., ethane, ethene, propane, propene, butane, and butene). C_2-4 hydrocarbons may have significant value. The value of C₃ and C hydrocarbons may be many times (e.g., 2, 3, or greater) than the value of methane.

Production of hydrocarbon fluids having high C_2-4 hydrocarbons to methane weight ratios may be due to conditions applied to the formation during pyrolysis (e.g., confrolled heating and/or pressure used in reducing environments or non-oxidizing environments). The conditions may allow for long chain hydrocarbons to be reduced to small (and in many cases more saturated) chain hydrocarbons with only a portion of the long chain hydrocarbons being reduced to methane or carbon dioxide.

Methane and at least a portion of ethane may be separated from non-condensable hydrocarbons in produced fluid. The methane and ethane may be utilized as natural gas. A portion of propane and butane may be separated from non-condensable hydrocarbons of the produced fluid. In addition, the separated propane and butane may be utilized as fuels or as feedstocks for producing other hydrocarbons. Ethane, propane and butane produced from the formation may be used to generate olefins. A portion of the produced fluid having carbon numbers less than 4 may be reformed to produce additional H₂ and/or methane. In some in situ conversion process embodiments, the reformation may be performed in the formation. In addition, ethane, propane, and butane may be separated from the non-condensable hydrocarbons.

Formation fluid produced from a formation during a pyrolysis stage of an in situ conversion process may have a H₂ content of greater than about 5 weight %, greater than about 10 weight %, or even greater than about 15 weight %. The H₂may be used for a variety of pmposes. The puφoses may include, but are not limited to, as a fuel for a fuel cell, to hydrogenate hydrocarbon fluids in situ, and/or to hydrogenate hydrocarbon fluids ex situ. Formation fluid produced from a formation may include some hydrogen sulfide. The hydrogen sulfide may be a non-condensable, non-hydrocarbon component of the formation fluid. The hydrogen sulfide may be separated from other compounds. The separated hydrogen sulfide may be used to produce, for example, sulfuric acid, fertilizer, and/or elemental sulfur. Formation fluid produced from a formation during in situ conversion may include carbon dioxide. Carbon dioxide produced from the formation may be used for a variety of puφoses. The puφoses may include, but are not limited to, drive fluid for enhanced oil recovery, drive fluid for coal bed methane production, as a feedstock for production of urea, and/or a component of a synthesis gas fluid generating fluid. In some embodiments, a portion of carbon dioxide produced during an in situ conversion process may be sequestered in a spent portion of the formation being processed.

Formation fluid produced from a formation during in situ conversion may include carbon monoxide. Carbon monoxide produced from the formation may be used, for example, as a feedstock for a fuel cell, as a feedstock for a Fischer-Tropsch process, as a feedstock for production of methanol, and/or as a feedstock for production of methane.

Condensable hydrocarbons of formation fluids produced from a formation may be separated from the formation fluids. Foπnation fluids may be separated into a non-condensable portion (hydrocarbon and non- hydrocarbon) and a condensable portion (hydrocarbon and non-hydrocarbon). The condensable portion may include condensable hydrocarbons and compounds found in an aqueous phase. The aqueous phase may be separated from the condensable component.

An aqueous phase may include ammonia. The ammonia content of the total produced fluids may be greater than about 0.1 weight % of the fluid, greater than about 0.5 weight % of the fluid, and, in some embodiments, up to about 10 weight % of the produced fluids. The ammonia may be used to produce, for example, urea. In some in situ conversion process embodiments, condensable hydrocarbons of a fluid produced from a relatively low permeability formation containing heavy hydrocarbons may include olefins. For example, an olefin content of the condensable hydrocarbons may be in a range from about 0.1 weight % to about 15 weight %. Alternatively, an olefin content of the condensable hydrocarbons may be within a range from about 0.1 weight % to about 5 weight %. An olefin content of the condensable hydrocarbons may also be within a range from about 0.1 weight % to about 2.5 weight %. An olefin content of the condensable hydrocarbons may be altered and/or controlled by controlling a pressure and/or a temperature within the formation. For example, olefin content of the condensable hydrocarbons may be reduced by selectively increasing pressure within the formation, by selectively decreasing temperature within the foπnation, by selectively reducing heating rates within the formation, and/or by selectively increasing hydrogen partial pressures in the formation. In some in situ conversion process embodiments, a reduced olefin content of the condensable hydrocarbons may be desired. For example, if a portion of the produced fluids is used to produce motor fuels, a reduced olefin content may be desired.

In some in situ conversion process embodiments, a higher olefin content may be desired. For example, if a portion of the condensable hydrocarbons may be sold, a higher olefin content may be selected due to a high economic value of olefin products. In some embodiments, olefins may be separated from the produced fluids and then sold and/or used as a feedstock for the production of other compounds.

Non-condensable hydrocarbons of a produced fluid may include olefins. An ethene/ethane molar ratio may be used as an estimate of olefin content of non-condensable hydrocarbons. In certain in situ conversion process embodhnents, the ethene/ethane molar ratio may range from about 0.001 to about 0.15.

Fluid produced from a relatively low peπneability formation containing heavy hydrocarbons may include aromatic compounds. For example, the condensable hydrocarbons may include an amount of aromatic compounds greater than about 20 weight % or about 25 weight % of the condensable hydrocarbons. Alternatively, the condensable hydrocarbons may include an amount of aromatic compounds greater than about 30 weight % of the condensable hydrocarbons. The condensable hydrocarbons may also include relatively low amounts of compounds with more than two rings in them (e.g., tri-aromatics or above). For example, the condensable hydrocarbons may include less than about 1 weight % or less than about 2 weight % of tri-aromatics or above in the condensable hydrocarbons. Alternatively, the condensable hydrocarbons may include less than about 5 weight % of tri- aromatics or above in the condensable hydrocarbons.

Fluid produced from a relatively low permeability formation containing heavy hydrocarbons may include a small amount of asphaltenes (i.e., large multi-ring aromatics that may be substantially soluble in hydrocarbons) as compared to fluid produced from a formation using other techniques such as fire floods and/or steam floods. Temperature and pressure confrol within a selected portion may inhibit the production of asphaltenes using an in situ conversion process. Some asphaltenes may be entrained in formation fluid produced from the formation. Asphaltenes may make up less than about 0.3 weight % of the condensable hydrocarbons produced using an in situ conversion process. In some in situ conversion process embodiments, asphaltenes may be less than 0.1 weight %, 0.05 weight %, or 0.01 weight %. In some in situ conversion process embodiments, the in situ conversion process may result in no, or substantially no, asphaltene production, especially if initial production from the formation is inhibited or if initial production is ignored until the formation produces hydrocarbons of a minimum quality.

Condensable hydrocarbons of a produced fluid may include relatively large amounts of cycloalkanes. Linear chain molecules may form ring compounds (e.g., hexane may form cyclohexane) in the formation. In addition, some aromatic compounds may be hydrogenated in the formation to produce cycloalkanes (e.g., benzene may be hydrogenated to form cyclohexane). The condensable hydrocarbons may include a cycloalkane component . of from about 0 weight % to about 30 weight %. In some in situ conversion process embodiments, the condensable hydrocarbons may include a cycloalkane component from about 1% to about 20%, or from about 5% to about 20%. In certain in situ conversion process embodiments, the condensable hydrocarbons of a fluid produced from a formation may include compounds containing nifrogen. For example, less than about 1 weight % (when calculated on an elemental basis) of the condensable hydrocarbons may be nitrogen (e.g., typically the nifrogen may be in nitrogen containing compounds such as pyridines, amines, amides, carbazoles, etc.). The amount of nitrogen containing compounds may depend on the amount of nifrogen in the initial hydrocarbon material present in the formation.

Some of the nifrogen in the initial hydrocarbon material present may be produced as ammonia. Produced ammonia may be separated from hydrocarbons. The ammonia may be separated, along with water, from formation fluid produced from the formation. Formation fluid produced from the formation may include about 0.05 weight % or more of ammonia. Certain formations may produce larger amounts of ammonia (e.g., up to about 10 weight % of the total fluid produced may be ammonia).

In some in situ conversion process embodiments, condensable hydrocarbons of the fluid produced from a formation may include compounds containing sulfur. For example, less than about 1 weight % (when calculated on an elemental basis) of the condensable hydrocarbons may be sulfur containing compounds. Typical sulfur containing compounds may include compounds such as thiophenes, mercaptans, etc. The amount of sulfur containing compounds may depend on the amount of sulfur in the initial hydrocarbon material present in the formation. Some of the sulfur in the initial hydrocarbon material present may be produced as hydrogen sulfide. In some in situ conversion process embodiments, formation fluid produced from the formation may include molecular hydrogen (H₂). Hydrogen may be from about 0.1 volume % to about 80 volume % of a non- condensable component of formation fluid produced from the formation. In some in situ conversion process embodiments, H₂ may be about 5 volume % to about 70 volume % of the non-condensable component of formation fluid produced from the formation. The amount of hydrogen in the formation fluid may be strongly dependent on the temperature of the foπnation. A high formation temperature may result in the production of significant amounts of hydrogen. A high temperature may also result in the formation of a significant amount of coke within the foπnation.

In some in situ conversion process embodiments, a large portion of the total organic carbon content of a formation may be converted into hydrocarbon fluids. In some embodiments, up to about 20 weight % of the total organic carbon content of hydrocarbons in the portion may be transformed into hydrocarbon fluids. In some in situ conversion process embodiments, the weight percentage of total organic carbon content of hydrocarbons in the portion removed during the in situ process may be significantly increased if synthesis gas is generated within the portion.

In certain embodiments, heating of the selected section of the formation may be confrolled to pyrolyze at least about 20 weight % (or in some embodiments about 25 weight %) of the hydrocarbons within the selected section of the formation. Conversion of selected portions of hydrocarbon layers within a formation may be avoided to inhibit subsidence of the formation.

Heating at least a portion of a foπnation may cause some of the hydrocarbons within the portion to pyrolyze. Pyrolyzation may generate hydrocarbon fragments. The hydrocarbon fragments may be reactive and may react with other compounds in the formation and/or with other hydrocarbon fragments produced by pyrolysis. Reaction of the hydrocarbon fragments with other compounds and/or with each other, however, may reduce production of a selected product. A reducing agent in, or provided to, the portion of the formation during heating may increase production of the selected product. The reducing agent may be, but is not limited to, H₂, methane, and/or other non-condensable hydrocarbon fluids.

In an in situ conversion process embodiment, molecular hydrogen may be provided to the formation to create a reducing environment. Hydrogenation reactions between the molecular hydrogen and some of the hydrocarbons within a portion of the formation may generate heat. The heat may heat the portion of the formation. Molecular hydrogen may also be generated within the portion of the formation. The generated H₂ may hydrogenate hydrocarbon fluids within a portion of a formation/ The hydrogenation may generate heat that fransfers to the formation to maintain a desired temperature within the formation. H₂ may be produced from a first portion of a relatively low permeability formation containing heavy hydrocarbons. The H₂ may be separated from formation fluid produced from the first portion. The H₂ from the first portion, along with other reducing or substantially inert fluid (e.g., methane, ethane, and or nitrogen), may be provided to a second portion of the formation to create a reducing environment within the second portion. The second portion of the formation may be heated by heat sources. Power input into the heat sources may be reduced after introduction of H₂ due to heating of the formation by hydrogenation reactions within the formation. H₂ may be introduced into the formation continuously or batchwise.

Hydrogen introduced into the second portion of the formation may reduce (e.g., at least partially saturate) some pyrolyzation fluid being produced or present in the second section. Reducing the pyrolyzation fluid may decrease a concenfration of olefins in the pyrolyzation fluids. Reducing the pyrolysis products may improve the product quality of the hydrocarbon fluids. An in situ conversion process may generate significant amounts of H₂ and hydrocarbon fluids within the formation. Generation of hydrogen within the formation, and pressure within the formation sufficient to force hydrogen into a liquid phase within the formation, may produce a reducing environment within the formation without the need to introduce a reducing fluid (e.g., H₂ and/or non-condensable saturated hydrocarbons) into the fonnation. A hydrogen component of formation fluid produced from the formation may be separated and used for desired puφoses. The desfred puφoses may include, but are not limited to, fuel for fuel cells, fuel for combustors, and/or a feed stream for surface hydrogenation units.

In an in situ conversion process embodiment, heating a portion of a relatively low permeability fonnation containing heavy hydrocarbons in situ to a temperature less than an upper pyrolysis temperature may increase permeability of the heated portion. Permeability may increase due to formation of thermal fractures within the heated portion. Theπnal fractures may be generated by thermal expansion of the formation and/or by localized increases in pressure due to vaporization of liquids (e.g., water and/or hydrocarbons) in the formation. As a temperature of the heated portion increases, water in the formation may be vaporized. The vaporized water may escape and/or be removed from the formation. Removal of water may also increase the permeability of the heated portion. In addition, permeability of the heated portion may also increase as a result of mass loss from the formation due to generation of pyrolysis fluids in the formation. Pyrolysis fluid may be removed from the formation through production wells.

Heating the formation from heat sources placed in the foπnation may allow a penneability of the heated portion of a relatively low peπneability formation containing heavy hydrocarbons to be substantially unifoπn. A substantially uniform peπneability may inhibit channeling of formation fluids in the formation and allow production from substantially all portions of the heated formation. An assessed (e.g., calculated or estimated) permeability of any selected portion in the formation having a substantially uniform permeability may not vary by more than a factor of 10 from an assessed average permeability of the selected portion.

Permeability of a selected section within the heated portion of the relatively low permeability formation containing heavy hydrocarbons may rapidly increase when the selected section is heated by conduction. A permeability of an impermeable hydrocarbon containing formation may be less than about 0.1 millidarcy (9.9 x 10^{" 17} m²) before freatment.

In some in situ conversion process embodiments, supeφosition (e.g., overlapping influence) of heat from one or more heat sources may result in substantially uniform heating of a portion of a relatively low permeability formation containing heavy hydrocarbons. Since formations during heating will typically have a temperature gradient that is highest near heat sources and reduces with increasing distance from the heat sources, "substantially uniform" heating means heating such that temperature in a majority of the section does not vary by more than 100 °C from an assessed average temperature in the majority of the selected section (volume) being treated. Physical characteristics of a portion of a relatively low permeability foπnation containing heavy hydrocarbons after pyrolysis may be similar to those of a porous bed. The physical characteristics of a formation subjected to an in situ conversion process may significantly differ from physical characteristics of a relatively low peπneability formation containing heavy hydrocarbons subjected to injection of gases that bum hydrocarbons to heat the hydrocarbons and or to formations subjected to steam flood production. Gases injected into virgin or fractured formations may channel through the fonnation. The gases may not be uniformly disfributed throughout the formation. In confrast, a gas injected into a portion of a relatively low permeability formation containing heavy hydrocarbons subjected to an in situ conversion process may readily and substantially uniformly contact the carbon and/or hydrocarbons remaining in the formation. Gases produced by heating the hydrocarbons may be fransfened a significant distance within the heated portion of the formation with minimal pressure loss.

Transfer of gases in a formation over significant distances may be particularly advantageous to reduce the number of production wells needed to produce formation fluid from the formation. A first portion of a hydrocarbon formation may be subjected to an in situ conversion process. The volume of the formation subjected to in situ conversion may be expanded by heating abutting portions of the relatively low permeability formation containing heavy hydrocarbons. Formation fluid produced in the abutting portions of the formation may be produced from production wells in the first portion. If needed, a few additional production wells may be installed in the abutting portions of formation, but such production wells may have large separation distances. The ability to fransfer fluid in a formation over long distances may be advantageous for freating a steeply dipping relatively low permeability formation containing heavy hydrocarbons. Production wells may be placed in an upper portion of the dipping hydrocarbon production. Heat sources may be inserted into the steeply dipping formation. The heat sources may follow the dip of the formation. The upper portion may be subjected to thermal treatment by activating portions of the heat sources in the upper portion. Abutting portions of the steeply dipping formation may be subjected to thermal treatment after freatment in the upper portion increases the permeability of the formation so that fluids in lower portions may be produced from the upper portions.

Synthesis gas may be produced from a portion of a relatively low permeability formation containing heavy hydrocarbons. Synthesis gas may be produced from heavy hydrocarbons (tar sands, etc.) and other bitumen containing formations. The relatively low permeability formation containing heavy hydrocarbons may be heated prior to synthesis gas generation to produce a substantially uniform, relatively high permeability formation. In an in situ conversion process embodiment, synthesis gas production may be commenced after production of pyrolysis fluids has been exhausted or becomes uneconomical. Alternately, synthesis gas generation may be commenced before substantial exhaustion or uneconomical pyrolysis fluid production has been achieved if production of synthesis gas will be more economically favorable. Formation temperatures will usually be higher than pyrolysis temperatures during synthesis gas generation. Raising the formation temperature from pyrolysis temperatures to synthesis gas generation temperatures allows further utilization of heat applied to the formation to pyrolyze the formation. While raising a temperature of a formation from pyrolysis temperatures to synthesis gas temperatures, methane and or H₂ may be produced from the formation.

Producing synthesis gas from a formation from which pyrolyzation fluids have been previously removed allows a synthesis gas to be produced that includes mostly H₂, CO, water, and/or C0₂. Produced synthesis gas, in certain embodiments, may have substantially no hydrocarbon component unless a separate source hydrocarbon stream is introduced into the formation with or in addition to the synthesis gas producing fluid. Producing synthesis gas from a substantially uniform, relatively high permeability formation that was formed by slowly heating a formation through pyrolysis temperatures may allow for easy introduction of a synthesis gas generating fluid into the formation, and may allow the synthesis gas generating fluid to contact a relatively large portion of the formation. The synthesis gas generating fluid can do so because the permeability of the formation has been increased during pyrolysis and/or because the surface area per volume in the formation has increased during pyrolysis. The relatively large surface area (e.g., "contact area") in the post-pyrolysis formation tends to allow synthesis gas generating reactions to be substantially at equilibrium conditions for C, H₂, CO, water, and C0₂. Reactions in which methane is formed may, however, not be at equilibrium because they are kinetically limited. The relatively high, substantially unifoπn formation permeability may allow production wells to be spaced farther apart than production wells used during pyrolysis of the fonnation.

A temperature of at least a portion of a formation that is used to generate synthesis gas may be raised to a synthesis gas generating temperature (e.g., between about 400 °C and about 1200 °C). In some embodiments, composition of produced synthesis gas may be affected by formation temperature, by the temperature of the fonnation adjacent to synthesis gas production wells, and/or by residence time of the synthesis gas components. A relatively low synthesis gas generation temperature may produce a synthesis gas having a high H₂ to CO ratio, but the produced synthesis gas may also include a large portion of other gases such as water, C0₂, and methane. A relatively high foπnation temperature may produce a synthesis gas having a H₂ to CO ratio that approaches 1, and the stream may include mostly and, in some cases, only H₂ and CO. If the synthesis gas generating fluid is substantially pure steam, then the H₂ to CO ratio may approach 1 at relatively high temperatures. At a formation temperature of about 700 °C, the formation may produce a synthesis gas with a H₂ to CO ratio of about 2 at a certain pressure. The composition of the synthesis gas tends to depend on the nature of the synthesis gas generating fluid. Synthesis gas generation is generally an endothermic process. Heat may be added to a portion of a formation during synthesis gas production to keep formation temperature at a desired synthesis gas generating temperature or above a minimum synthesis gas generating temperature. Heat may be added to the formation from heat sources, from oxidation reactions within the portion, and/or from introducing synthesis gas generating fluid into the foπnation at a higher temperature than the temperature of the formation. An oxidant may be introduced into a portion of the foπnation with synthesis gas generating fluid. The oxidant may exothermically react with carbon within the portion of the formation to heat the formation. Oxidation of carbon within a formation may allow a portion of a foπnation to be economically heated to relatively high synthesis gas generating temperatures. The oxidant may be introduced into the formation without synthesis gas generating fluid to heat the portion. Using an oxidant, or an oxidant and heat sources, to heat the portion of the formation may be significantly more favorable than heating the portion of the formation with only the heat sources.

The oxidant may be, but is not limited to, air, oxygen, or oxygen enriched afr. The oxidant may react with carbon in the formation to produce C0₂ and/or CO. The use of air, or oxygen enriched afr (i.e., air with an oxygen content greater than 21 volume %), to generate heat within the formation may cause a significant portion of N₂ to be present in produced synthesis gas. Temperatures in the formation may be maintained below temperatures needed to generate oxides of nifrogen (NO_x), so that little or no NO_x compounds may be present in produced synthesis gas.

A mixture of steam and oxygen, steam and enriched air, or steam and air, may be continuously injected into a formation. If injection of steam and oxygen or steam and enriched afr is used for synthesis gas production, the oxygen may be produced on site (or near to the site) by electrolysis of water utilizing direct cunent output of a fuel cell. H₂ produced by the electrolysis of water may be used as a fuel stream for the fuel cell. 0₂ produced by the electrolysis of water may also be injected into the hot formation to raise a temperature of the formation.

Heat sources and/or production wells within a formation for pyrolyzing and producing pyrolysis fluids from the formation may be utilized for different puφoses during synthesis gas production. A well that was used as a heat source or a production well during pyrolysis may be used as an injection well to introduce synthesis gas producing fluid into the formation. A well that was used as a heat source or a production well during pyrolysis may be used as a production well during synthesis gas generation. A well that was used as a heat source or a production well during pyrolysis may be used as a heat source to heat the formation during synthesis gas generation. Some production wells used during a pyrolysis phase may be shut in. Synthesis gas production wells may be spaced further apart than pyrolysis production wells because of the relatively high, substantially uniform permeability of the fonnation. Some production wells used during a pyrolysis phase may be shut in or converted to other uses.

Synthesis gas production wells may be heated to relatively high temperatures so that a portion of the formation adjacent to the production well is at a temperature that will produce a desired synthesis gas composition.

Comparatively, pyrolysis fluid production wells may not be heated at all, or may only be heated to a temperature that will inhibit condensation of pyrolysis fluid within the production well.

Synthesis gas may be produced from a dipping formation from wells used during pyrolysis of the formation. As shown in FIG. 8, synthesis gas production wells 206 may be located above and down dip from injection well 202. Hot synthesis gas producing fluid may be introduced into injection well 202. Hot synthesis gas fluid that moves down dip may generate synthesis gas that is produced through synthesis gas production wells 206.

Synthesis gas generating fluid that moves up dip may generate synthesis gas in a portion of the formation that is at synthesis gas generating temperatures. A portion of the synthesis gas generating fluid and generated synthesis gas that moves up dip above the portion of the formation at synthesis gas generating temperatures may heat adjacent portions of the formation. The synthesis gas generating fluid that moves up dip may condense, heat adjacent portions of formation, and flow downwards towards or into a portion of the formation at synthesis gas generating temperature. The synthesis gas generating fluid may then generate additional synthesis gas.

Synthesis gas generating fluid may be any fluid capable of generating H₂ and CO within a heated portion of a formation. Synthesis gas generating fluid may include water, 0₂, afr, C0₂, hydrocarbon fluids, or combinations thereof. Water may be introduced into a formation as a liquid or as steam. Water may react with carbon in a formation to produce H₂, CO, and C0₂. C0₂ may react with hot carbon to form CO. Air and 0₂ may be oxidants that react with carbon in a formation to generate heat and form C0₂, CO, and other compounds. Hydrocarbon fluids may react within a formation to form H₂, CO, C0₂, H₂0, coke, methane, and/or other light hydrocarbons.

Introducing low carbon number hydrocarbons (i.e., compounds with carbon numbers less than 5) may produce additional H₂ within the formation. Adding higher carbon number hydrocarbons to the formation may increase an energy content of generated synthesis gas by having a significant methane and other low carbon number compounds fraction within the synthesis gas.

Water provided as a synthesis gas generating fluid may be derived from numerous different sources.

Water may be produced during a pyrolysis stage of freating a formation. The water may include some entrained hydrocarbon fluids. Such fluid may be used as synthesis gas generating fluid. Water that includes hydrocarbons may advantageously generate additional H₂ when used as a synthesis gas generating fluid. Water produced from water pumps that inhibit water flow into a portion of foπnation being subjected to an in situ conversion process may provide water for synthesis gas generation.

It is believed that as temperature is increased, a greater amount of additional synthesis gas may be produced for a given injected water rate. The reason may be that, at higher temperatures, the reaction rate and conversion of water into synthesis gas may increase.

Reactions involved in the formation of synthesis gas may include, but are not limited to:

(51) C + H₂0 <^> H₂ + CO (52) C + 2H₂0 <^> 2H₂ + C0₂

(53) C + C0₂ <=• 2CO Thermodynamics also allows the following reactions to proceed:

(54) 2C + 2H₂0 <■-= CH₄ + C0₂

(55) C + 2H₂ <*■■> CH₄

However, kinetics of the reactions are slow in certain embodiments, so that relatively low amounts of methane are formed at formation conditions from Reactions 54 and 55.

In the presence of oxygen, the following reaction may take place to generate carbon dioxide and heat:

(56) C + 0₂ → C0₂

Equilibrium gas phase compositions of coal in contact with steam may provide an indication of the compositions of components produced in a formation during synthesis gas generation. Equilibrium composition data for H₂, carbon monoxide, and carbon dioxide may be used to determine appropriate operating conditions (e.g., temperature) that may be used to produce a synthesis gas having a selected composition. Equilibrium conditions may be approached within a formation due to a high, substantially unifoπn peπneability of the foπnation. Composition data obtained from synthesis gas production may in many in situ conversion process embodiments, deviate by less than 10% from equilibrium values.

In one synthesis gas production embodiment, a composition of the produced synthesis gas can be changed by injecting additional components into the formation along with steam. Carbon dioxide may be provided in the synthesis gas generating fluid to inhibit production of carbon dioxide from the formation during synthesis gas generation. The carbon dioxide may shift the equilibrium of Reaction 52 to the left, thus reducing the amount of carbon dioxide generated from formation carbon. The carbon dioxide may also shift the equilibrium of Reaction 53 to the right to generate carbon monoxide. Carbon dioxide may be separated from the synthesis gas and may be re- injected into the formation with the synthesis gas generating fluid. Addition of carbon dioxide in the synthesis gas generating fluid may, however, reduce the production of hydrogen.

FIG. 117 depicts a schematic diagram of use of water recovered from pyrolysis fluid production to generate synthesis gas. Heat source 801 with elecfric heater 803 produces pyrolysis fluid 807 from first section 805 of the formation. Produced pyrolysis fluid 807 may be sent to separator 809. Separator 809 may include a number of individual separation units and processing units that produce aqueous sfream 811, vapor sfream 813, and hydrocarbon condensate sfream 815. Aqueous sfream 811 from separator 809 may be combined with synthesis gas generating fluid 818 to form synthesis gas generating fluid 821. Synthesis gas generating fluid 821 may be . provided to injection well 817 and infroduced to second portion 819 of the formation. Synthesis gas 823 may be produced from synthesis gas production well 825. FIG. 118 depicts a schematic diagram of an embodhnent of a system for synthesis gas production.

Synthesis gas 830 may be produced from formation 832 through production well 834. Gas separation unit 836 may separate a portion of carbon dioxide from synthesis gas 830 to produce C0₂ sfream 838 and remaining synthesis gas stream 840. C0₂ stream 838 may be mixed with synthesis gas producing fluid stream 842 that is introduced into formation 832 through injection well 837. In some synthesis gas process embodiments, C0₂ may be infroduced into the formation separate from synthesis gas producing fluid. Introducing C0₂may inhibit conversion of carbon within the formation to C0₂ and/or may increase an amount of CO generated within the formation.

Synthesis gas generating fluid may be infroduced into a formation in a variety of different ways. Steam may be injected into a heated relatively low permeability formation containing heavy hydrocarbons at a lowermost portion of the heated formation. Alternatively, in a steeply dipping formation, steam may be injected up dip with synthesis gas production down dip. The injected steam may pass through the remaining relatively low permeability formation containing heavy hydrocarbons to a production well. In addition, endotheπnic heat of reaction may be provided to the formation with heat sources disposed along a path of the injected steam. In alternate embodiments, steam may be injected at a plurality of locations along the relatively low permeability foπnation containing heavy hydrocarbons to increase penetration of the steam throughout the formation. A line drive pattern of locations may also be utilized. The line drive pattern may include alternating rows of steam injection wells and synthesis gas production wells.

Synthesis gas reactions may be slow at relatively low pressures and at temperatures below about 400 °C. At relatively low pressures, and temperatures between about 400 °C and about 700 °C, Reaction 52 may predominate so that synthesis gas composition is primarily hydrogen and carbon dioxide. At relatively low pressures and temperatures greater than about 700 °C, Reaction 51 may predominate so that synthesis gas composition is primarily hydrogen and carbon monoxide.

Advantages of a lower temperature synthesis gas reaction may include lower heat requirements, cheaper metallurgy, and less endothermic reactions (especially when methane formation takes place). An advantage of a higher temperature synthesis gas reaction is that hydrogen and carbon monoxide may be used as feedstock for other processes (e.g., Fischer-Tropsch processes).

A pressure of the relatively low permeability formation containing heavy hydrocarbons may be maintained at relatively high pressures during synthesis gas production. The pressure may range from atmospheric pressure to a pressure that approaches a lithostatic pressure of the formation. Higher formation pressures may allow generation of elecfricity by passing produced synthesis gas through a turbine. Higher formation pressures may allow for smaller collection conduits to transport produced synthesis gas and reduced downstream compression requirements on the surface.

In some synthesis gas process embodiments, synthesis gas may be produced from a portion of a formation in a substantially continuous manner. The portion may be heated to a desfred synthesis gas generating temperature. A synthesis gas generating fluid may be introduced into the portion. Heat may be added to, or generated within, the portion of the formation during introduction of the synthesis gas generating fluid to the portion. The added heat may compensate for the loss of heat due to the endothermic synthesis gas reactions as well as heat losses to a top layer (overburden), bottom layer (underburden), and unreactive material in the portion.

FIG. 119 illustrates a schematic representation of an embodiment of a continuous synthesis gas production system. FIG. 119 includes a formation with heat injection wellbore 850 and heat injection wellbore 852. The wellbores may be members of a larger pattern of wellbores placed throughout a portion of the formation. The portion of the foπnation may be heated to synthesis gas generating temperatures by heating the formation with heat sources, by injecting an oxidizing fluid, or by a combination thereof. Oxidizing fluid 854 (e.g., air, enriched afr, or oxygen) and synthesis gas generating fluid 856 (e.g., water, or steam) may be injected into wellbore 850. In a synthesis gas process embodiment that uses oxygen and steam, the ratio of oxygen to steam may range from approximately 1:2 to approximately 1:10, or approximately 1:3 to approximately 1:7 (e.g., about 1:4). In situ combustion of hydrocarbons may heat region 858 of the formation between wellbores 850 and 852. Injection of the oxidizing fluid may heat region 858 to a particular temperature range, for example, between about 600 °C and about 700 °C. The temperature may vary, however, depending on a desired composition of the synthesis gas. An advantage of the continuous production method may be that a temperature gradient established across region 858 may be substantially unifoπn and substantially constant with time once the formation approaches thermal equilibrium. Continuous production may also eliminate a need for use of valves to reverse injection dfrections on a frequent basis. Further, continuous production may reduce temperatures near the injection wells due to endothermic cooling from the synthesis gas reaction that occur in the same region as oxidative heating. The substantially constant temperature gradient may allow for confrol of synthesis gas composition. Produced synthesis gas 860 may exit continuously from wellbore 852.

In a synthesis gas process embodiment, oxygen may be used instead of afr as oxidizing fluid 854 in continuous production. If air is used, nifrogen may need to be separated from the produced synthesis gas. The use of oxygen as oxidizing fluid 854 may increase a cost of production due to the cost of obtaining substantially pure oxygen. The cryogenic nifrogen by-product obtained from an air separation plant used to produce the required oxygen may, however, be used in a heat exchanger to condense hydrocarbons from a hot vapor sfream produced during pyrolysis of hydrocarbons. The pure nifrogen may also be used for ammonia production.

In some synthesis gas process embodiments, synthesis gas may be produced in a batch manner from a portion of the formation. The portion of the formation may be heated, or heat may be generated within the portion, to raise a temperature of the portion to a high synthesis gas generating temperature. Synthesis gas generating fluid may then be added to the portion until generation of synthesis gas reduces the temperature of the formation below a temperature that produces a desired synthesis gas composition. Introduction of the synthesis gas generating fluid may then be stopped. The cycle may be repeated by reheating the portion of the formation to the high synthesis gas generating temperature and adding synthesis gas generating fluid after obtaining the high synthesis gas generating temperature. Composition of generated synthesis gas may be monitored to determine when addition of synthesis gas generating fluid to the formation should be stopped.

FIG. 120 illustrates a schematic representation of an embodiment of a batch production of synthesis gas in a relatively low permeability formation containing heavy hydrocarbons. Wellbore 870 and wellbore 872 may be located within a portion of the formation. The wellbores may be members of a larger pattern of wellbores throughout the portion of the formation. Oxidizing fluid 874, such as air or oxygen, may be injected into wellbore 870. Oxidation of hydrocarbons may heat region 876 of a formation between wellbores 870 and 872. Injection of air or oxygen may continue until an average temperature of region 876 is at a desired temperature (e.g., between about 900 °C and about 1000 °C). Higher or lower temperatures may also be developed. A temperature gradient may be formed in region 876 between wellbore 870 and wellbore 872. The highest temperature of the gradient may be located proximate injection wellbore 870. When a desired temperature has been reached, or when oxidizing fluid has been injected for a desired period of time, oxidizing fluid injection may be lessened and/or ceased. Synthesis gas generating fluid 877, such as steam or water, may be injected into injection wellbore 872 to produce synthesis gas. A back pressure of the injected steam or water in the injection wellbore may force the synthesis gas produced and un-reacted steam across region 876. A decrease in average temperature of region 876 caused by the endothermic synthesis gas reaction may be partially offset by the temperature gradient in region 876 in a direction indicated by anow 878. Product stream 880 may be produced through heat source wellbore 870. If the composition of the product deviates from a desired composition, then steam injection may cease, and air or oxygen injection may be reinitiated.

Synthesis gas of a selected composition may be produced by blending synthesis gas produced from different portions of the formation. A first portion of a formation may be heated by one or more heat sources to a first temperature sufficient to allow generation of synthesis gas having a H₂ to carbon monoxide ratio of less than the selected H₂ to carbon monoxide ratio (e.g., about 1 : 1 or 2: 1). A first synthesis gas generating fluid may be provided to the first portion to generate a first synthesis gas. The first synthesis gas may be produced from the foπnation. A second portion of the formation may be heated by one or more heat sources to a second temperature sufficient to allow generation of synthesis gas having a H₂ to carbon monoxide ratio of greater than the selected H₂ to carbon monoxide ratio (e.g., a ratio of 3 : 1 or more). A second synthesis gas generating fluid may be provided to the second portion to generate a second synthesis gas. The second synthesis gas may be produced from the formation. The first synthesis gas may be blended with the second synthesis gas to produce a blend synthesis gas having a desired H₂ to carbon monoxide ratio.

The first temperature may be different than the second temperature. Alternatively, the first and second temperatures may be approximately the same temperature. For example, a temperature sufficient to allow generation of synthesis gas having different compositions may vary depending on compositions of the first and second portions and/or prior pyrolysis of hydrocarbons within the first and second portions. The first synthesis gas generating fluid may have substantially the same composition as the second synthesis gas generating fluid. Alternatively, the first synthesis gas generating fluid may have a different composition than the second synthesis gas generating fluid. Appropriate first and second synthesis gas generating fluids may vary depending upon, for example, temperatures of the first and second portions, compositions of the first and second portions, and prior pyrolysis of hydrocarbons within the ffrst and second portions.

In addition, synthesis gas having a selected ratio of H₂ to carbon monoxide may be obtained by controlling the temperature of the formation. In one embodiment, the temperature of an entire portion or section of the formation may be confrolled to yield synthesis gas with a selected ratio. Alternatively, the temperature in or proximate a synthesis gas production well may be confrolled to yield synthesis gas with the selected ratio. Controlling temperature near a production well may be sufficient because synthesis gas reactions may be fast enough to allow reactants and products to approach equilibrium concentrations.

In a synthesis gas process, synthesis gas having a selected ratio of H₂ to carbon monoxide may be obtained by treating produced synthesis gas at the surface. First, the temperature of the formation may be controlled to yield synthesis gas with a ratio different than a selected ratio. For example, the formation may be maintained at a relatively high temperature to generate a synthesis gas with a relatively low H₂ to carbon monoxide ratio (e.g., the ratio may approach 1 under certain conditions). Some or all of the produced synthesis gas may then be provided to a shift reactor (shift process) at the surface. Carbon monoxide reacts with water in the shift process to produce H₂ and carbon dioxide. Therefore, the shift process increases the H₂ to carbon monoxide ratio. The carbon dioxide may then be separated to obtain a synthesis gas having a selected H₂ to carbon monoxide ratio.

Produced synthesis gas 918 may be used for production of energy. In FIG. 121, treated gases 920 may be routed from freatment section 900 to energy generation unit 902 for extraction of useful energy. In some embodiments, energy may be extracted from the combustible gases in the synthesis gas by oxidizing the gases to produce heat and converting a portion of the heat into mechanical and or electrical energy. Alternatively, energy generation unit 902 may include a fuel cell that produces electrical energy. In addition, energy generation unit 902 may include, for example, a molten carbonate fuel cell or another type of fuel cell, a turbine, a boiler firebox, or a downhole gas heater. Produced elecfrical energy 904 may be supplied to power grid 906. A portion of produced elecfricity 908 may be used to supply energy to elecfrical heating elements 910 that heat formation 912.

In one embodiment, energy generation unit 902 may be a boiler firebox. A firebox may include a small refractory-lined chamber, built wholly or partly in the wall of a kiln, for combustion of fuel. Air or oxygen 914 may be supplied to energy generation unit 902 to oxidize the produced synthesis gas. Water 916 produced by oxidation of the synthesis gas may be recycled to the formation to produce additional synthesis gas.

A portion of synthesis gas produced from a foπnation may, in some embodiments, be used for fuel in downhole gas heaters. Downhole gas heaters (e.g., flameless combustors, downhole combustors, etc.) may be used to provide heat to a relatively low permeability formation containing heavy hydrocarbons. In some embodiments, downhole gas heaters may heat portions of a formation substantially by conduction of heat through the formation. Providing heat from gas heaters may be primarily self-reliant and may reduce or eliminate a need for elecfric heaters. Because downhole gas heaters may have thennal efficiencies approaching 90 %, the amount of carbon dioxide released to the environment by downhole gas heaters may be less than the amount of carbon dioxide released to the environment from a process using fossil-fuel generated elecfricity to heat the relatively low permeability formation containing heavy hydrocarbons.

Carbon dioxide may be produced during pyrolysis and/or during synthesis gas generation. Carbon dioxide may also be produced by energy generation processes and/or combustion processes. Net release of carbon dioxide to the atmosphere from an in situ conversion process for hydrocarbons may be reduced by utilizing the produced carbon dioxide and/or by storing carbon dioxide within the foπnation or within another formation. For example, a portion of carbon dioxide produced from the formation may be utilized as a flooding agent or as a feedstock for producing chemicals.

In an in situ conversion process embodiment, an energy generation process may produce a reduced amount of emissions by sequestering carbon dioxide produced during extraction of useful energy. For example, emissions from an energy generation process may be reduced by storing carbon dioxide within a hydrocarbon containing formation. In an in situ conversion process embodiment, the amount of stored carbon dioxide may be approximately equivalent to that in an exit stream from the formation.

FIG. 121 illustrates a reduced emission energy process. Carbon dioxide 928 produced by energy generation unit 902 may be separated from fluids exiting the energy generation unit. Carbon dioxide may be separated from H₂ at high temperatures by using a hot palladium film supported on porous stainless steel or a ceramic substrate, or by using high temperature and pressure swing adsoφtion. The carbon dioxide may be sequestered in spent hydrocarbon containing formation 922, injected into oil producing fields 924 for enhanced oil recovery by improving mobility and production of oil in such fields, sequestered into a deep hydrocarbon containing formation 926 containing methane by adsoφtion and subsequent desoφtion of methane, or re-injected 928 into a section of the formation tiirough a synthesis gas production well to enhance production of carbon monoxide. Carbon dioxide leaving the energy generation unit may be sequestered in a dewatered coal bed methane reservoir. The water for synthesis gas generation may come from dewatering a coal bed methane reservoir. Additional methane may be produced by alternating carbon dioxide and nifrogen. An example of a method for sequestering carbon dioxide is illusfrated in U.S. Pat. No. 5,566,756 to Chaback et al., which is incoφorated by reference as if fully set forth herein. Additional energy may be utilized by removing heat from the carbon dioxide stream leaving the energy generation unit. In an in situ conversion process embodiment, a hot spent foπnation may be cooled before being used to sequester carbon dioxide. A larger quantity of carbon dioxide may be adsorbed in a coal foπnation if the coal formation is at ambient or near ambient temperature. In addition, cooling a formation may strengthen the formation. The spent foπnation may be cooled by introducing water into the formation. The steam produced may be removed from the formation through production wells. The generated steam may be used for any desired process. For example, the steam may be provided to an adjacent portion of a formation to heat the adjacent portion or to generate synthesis gas.

FIG. 122 illustrates an in situ conversion process embodiment in which fluid produced from pyrolysis may be separated into a fuel cell feed stream and fed into a fuel cell to produce electricity. The embodiment may include relatively low permeability formation containing heavy hydrocarbons 940 with production well 942 that produces pyrolysis fluid. Heater well 944 with elecfric heater 946 may be a heat source that heats, or contributes to heating, the formation. Heater well 944 may also be a production well used to produce pyrolysis fluid 948. Pyrolysis fluid from heater well 944 may include H₂ and hydrocarbons with carbon numbers less than 5. Larger chain hydrocarbons may be reduced to hydrocarbons with carbon numbers less than 5 due to the heat adjacent to heater well 944. Pyrolysis fluid 948 produced from heater well 944 may be fed to gas membrane separation system

950 to separate H₂ and hydrocarbons with carbon numbers less than 5. Fuel cell feed stream 952, which may be substantially composed of H₂, may be fed into fuel cell 954. Air feed sfream 956 may be fed into fuel cell 954. Nitrogen sfream 958 may be vented from fuel cell 954. Elecfricity 960 produced from the fuel cell may be routed to a power grid. Elecfricity 962 may also be used to power electric heaters 946 in heater wells 944. Carbon dioxide 965 produced in fuel cell 954 may be injected into formation 940.

Hydrocarbons having carbon numbers of 4, 3, and 1 typically have fairly high market values. Separation and selling of these hydrocarbons may be desirable. Ethane (carbon number 2) may not be sufficiently valuable to separate and sell in some markets. Ethane may be sent as part of a fuel sfream to a fuel cell or ethane may be used as a hydrocarbon fluid component of a synthesis gas generating fluid. Ethane may also be used as a feedstock to produce ethene. In some markets, there may be no market for any hydrocarbons having carbon numbers less than 5.

In such a situation, all of the hydrocarbon gases produced during pyrolysis may be sent to fuel cells, used as fuels, and/or be used as hydrocarbon fluid components of a synthesis gas generating fluid.

Pyrolysis fluid 964, which may be substantially composed of hydrocarbons with carbon numbers less than 5, may be injected into a hot foπnation 940. When the hydrocarbons contact the formation, hydrocarbons may crack within the formation to produce methane, H₂, coke, and olefins such as ethene and propylene. In one embodiment, the production of olefins may be increased by heating the temperature of the formation to the upper end of the pyrolysis temperature range and by injecting hydrocarbon fluid at a relatively high rate. Residence time of the hydrocarbons in the formation may be reduced and dehydrogenated hydrocarbons may form olefins rather than cracking to form H₂ and coke. Olefin production may also be increased by reducing formation pressure. In some in situ conversion process embodiments, a hot formation that was subjected to pyrolysis and/or synthesis gas generation may be used to produce olefins. Hot formation 940 may be significantly less efficient at producing olefins than a reactor designed to produce olefins. However, a hot formation may have a several orders of magnitude more surface area and volume than a reactor designed to produce olefins. The reduction in efficiency of a hot formation may be more than offset by the increased size of the hot formation. A feed sfream for olefin production in a hot formation may be produced adjacent to the hot formation from a portion of a foπnation undergoing pyrolysis. The availability of a feed stream may also offset efficiency of a hot formation for producing olefins as compared to generating olefins in a reactor designed to produced olefins.

In some in situ conversion process embodiments, H₂ and/or non-condensable hydrocarbons may be used as a fuel, or as a fuel component, for surface burners or combustors. The combustors may be heat sources used to heat a relatively low permeability formation containing heavy hydrocarbons. In some heat source embodiments, the combustors may be flameless disfributed combustors. In some heat source embodiments, the combustors may be natural disfributed combustors and the fuel may be provided to the natural distributed combustor to supplement the fuel available from hydrocarbon material in the foπnation.

Heater well 944 may heat a portion of a formation to a synthesis gas generating temperature range. Pyrolysis fluid 964, or a portion of the pyrolysis fluid, may be injected into formation 940. In some process embodiments, pyrolysis fluid 964 infroduced into formation 940 may include no, or substantially no, hydrocarbons having carbon numbers greater than about 4. In other process embodiments, pyrolysis fluid 964 infroduced into formation 940 may include a significant portion of hydrocarbons having carbon numbers greater than 4. In some process embodiments, pyrolysis fluid 964 introduced into formation 940 may include no, or substantially no, hydrocarbons having carbon numbers less than 5. When hydrocarbons in pyrolysis fluid 964 are introduced into formation 940, the hydrocarbons may crack within the formation to produce methane, H₂, and coke.

FIG. 123 depicts an embodiment of a synthesis gas generating process from relatively low permeability formation containing heavy hydrocarbons 976 with flameless distributed combustor 996. Synthesis gas 980 produced from production well 978 may be fed into gas separation plant 984. Gas separation plant 984 may separate carbon dioxide 986 from other components of synthesis gas 980. First portion 990 of carbon dioxide may be routed to a formation for sequesfration. Second portion 992 of carbon dioxide may be injected into the formation with synthesis gas generating fluid. Portion 993 of synthesis gas 988 from separation plant 984 may be infroduced into heater well 994 as a portion of fuel for combustion in flameless disfributed combustor 996. Flameless disfributed combustor 996 may provide heat to the formation. Portion 998 of synthesis gas 988 may be fed to fuel cell 1000 for the production of elecfricity. Electricity 1002 may be routed to a power grid. Steam 1004 produced in the fuel cell and steam 1006 produced from combustion in the distributed burner may be introduced into the formation as a portion of a synthesis gas generation fluid.

In an in situ conversion process embodiment, carbon dioxide generated with pyrolysis fluids may be sequestered in a hydrocarbon containing formation. FIG. 124 illustrates in situ pyrolysis in relatively low permeability formation containing heavy hydrocarbons 1020. Heat source 1022 with electric heater 1024 may be placed in formation 1020. Pyrolysis fluids 1026 may be produced from formation 1020 and fed into gas separation unit 1028. Gas separation unit 1028 may separate pyrolysis fluid 1026 into carbon dioxide 1030, vapor component 1032, and liquid component 1031. Portion 1034 of carbon dioxide 1030 may be stored in formation 1036. Formation 1036 may be a coal bed with entrained methane. The carbon dioxide may displace some of the methane and allow for production of methane. The carbon dioxide may be sequestered in spent hydrocarbon containing formation 1038, injected into oil producing fields 1040 for enhanced oil recovery, or sequestered into coal bed 1042. In some embodiments, portion 1044 of carbon dioxide 1030 may be re-injected into a section of formation 1020 through a synthesis gas production well to promote production of carbon monoxide.

Vapor component 1032 and/or carbon dioxide 1030 may pass through turbine 1033 or turbines to generate electricity. A portion of electricity 1035 generated by the vapor component and/or carbon dioxide may be used to power elecfric heaters 1024 placed within formation 1020. Initial power and/or make-up power may be provided to electric heaters from a power grid.

As depicted in FIG. 125, heater well 1060 may be located within relatively low permeability formation containing heavy hydrocarbons 1062. Additional heater wells may also be located within formation 1062. Heater well 1060 may include elecfric heater 1064 or another type of heat source. Pyrolysis fluid 1066 produced from the formation may be fed to reformer 1068 to produce synthesis gas 1070. In some process embodiments, reformer

1068 is a steam reformer. Synthesis gas 1070 may be sent to fuel cell 1072. A portion of pyrolysis fluid 1060 and/or produced synthesis gas 1070 may be used as fuel to heat steam reformer 1068. Steam reformer 1068 may include a catalyst material that promotes the reforming reaction and a burner to supply heat for the endothermic reforming reaction. A steam source may be connected to reformer 1068 to provide steam for the reforming reaction. The burner may operate at temperatures well above that required by the reforming reaction and well above the operating temperatures of fuel cells. As such, it may be desirable to operate the burner as a separate unit independent of fuel cell 1072.

In some process embodiments, reformer 1068 may be a tube reformer. Reformer 1068 may include multiple tubes made of refractory metal alloys. Each tube may include a packed granular or pelletized material having a reforming catalyst as a surface coating. A diameter of the tubes may vary from between about 9 cm and about 16 cm. A heated length of each tube may noπnally be between about 6 m and about 12 m. A combustion zone may be provided external to the tubes, and may be formed in the burner. A surface temperature of the tubes may be maintained by the burner at a temperature of about 900 °C to ensure that the hydrocarbon fluid flowing inside the tube is properly catalyzed with steam at a temperature between about 500 °C and about 700 °C. A traditional tube reformer may rely upon conduction and convection heat transfer within the tube to distribute heat for reforming.

Pyrolysis fluids 1066 from formation 1062 may be pre-processed prior to being fed to reformer 1068.

Reformer 1068 may transform pyrolysis fluids 1066 into simpler reactants prior to introduction to a fuel cell. For example, pyrolysis fluids 1066 may be pre-processed in a desulfurization unit. Subsequent to pre-processing, pyrolysis fluids 1066may be provided to a reformer and a shift reactor to produce a suitable fuel stock for a H₂ fueled fuel cell.

Synthesis gas 1070 produced by reformer 1068 may include a number of components including carbon dioxide, carbon monoxide, methane, and/or hydrogen. Produced synthesis gas 1070 may be fed to fuel cell 1072. Portion 1074 of elecfricity produced by fuel cell 1072 may be sent to a power grid. In addition, portion 1076 of elecfricity may be used to power elecfric heater 1064. Carbon dioxide 1078 exiting the fuel cell may be routed to sequesfration area 1080. The sequesfration area may be a spent portion of formation 1062.

In a process embodiment, pyrolysis fluid produced from a formation may be fed to the reformer. The reformer may produce carbon dioxide sfream and a H₂ sfream. For example, the reformer may include a flameless distributed combustor for a core, and a membrane. The membrane may allow only H₂ to pass through the membrane resulting in separation of the H₂ and carbon dioxide. The carbon dioxide may be routed to a sequestration area.

Synthesis gas produced from a formation may be converted to heavier condensable hydrocarbons. For example, a Fischer-Tropsch hydrocarbon synthesis process may be used for conversion of synthesis gas. A Fischer- Tropsch process may include converting synthesis gas to hydrocarbons. The process may use elevated temperatures, normal or elevated pressures, and a catalyst, such as magnetic iron oxide or a cobalt catalyst. Products produced from a Fischer-Tropsch process may include hydrocarbons having a broad molecular weight distribution and may include branched and/or unbranched paraffins. Products from a Fischer-Tropsch process may also include considerable quantities of olefins and oxygen containing organic compounds. An example of a Fischer-Tropsch reaction may be illusfrated by Reaction 57:

(57) (n+2)CO + (2n+5)H₂ «-► CH₃ (-CH₂-)_n CH₃ + (n+2)H₂0

A hydrogen to carbon monoxide ratio for synthesis gas used as a feed gas for a Fischer-Tropsch reaction may be about 2:1. In certain embodhnents, the ratio may range from approximately 1.8:1 to 2.2:1. Higher or lower ratios may be accommodated by certain Fischer-Tropsch systems.

FIG. 126 illustrates a flow chart of a Fischer-Tropsch process that uses synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons as a feed stream. Hot foπnation 1090 may be used to produce synthesis gas having a H₂ to CO ratio of approximately 2:1. The proper ratio may be produced by operating synthesis production wells at approximately 700 °C, or by blending synthesis gas produced from different sections of formation to obtain a synthesis gas having approximately a 2:1 H₂ to CO ratio. Synthesis gas generating fluid 1092 may be fed into hot formation 1090 to generate synthesis gas. H₂ and CO may be separated from the synthesis gas produced from the hot formation 1090 to form feed sfream 1094. Feed sfream 1094 may be sent to Fischer-Tropsch plant 1096. Feed sfream 1094 may supplement or replace synthesis gas 1098 produced from catalytic methane reformer 1100. Fischer-Tropsch plant 1096 may produce wax feed stream 1102. The Fischer-Tropsch synthesis process that produces wax feed sfream 1102 is an exothermic process. Steam 1104 may be generated during the Fischer- Tropsch process. Steam 1104 may be used as a portion of synthesis gas generating fluid 1092.

Wax feed sfream 1102 produced from Fischer-Tropsch plant 1096 may be sent to hydrocracker 1106. Hydrocracker 1106 may produce product sfream 1108. The product sfream may include diesel, jet fuel, and/or naphtha products. Examples of methods for conversion of synthesis gas to hydrocarbons in a Fischer-Tropsch process are illusfrated in U.S. Patent Nos. 4,096,163 to Chang et al., 6,085,512 to Agee et al., and 6,172,124 to Wolflick et al., which are incoφorated by reference as if fully set forth herein.

FIG. 127 depicts an embodiment of in situ synthesis gas production integrated with a Shell Middle Distillates Synthesis (SMDS) Fischer-Tropsch and wax cracking process. An example of a SMDS process is illusfrated in U.S. Pat. No. 4,594,468 to Minderhoud, and is incoφorated by reference as if fully set forth herein. A middle distillates hydrocarbon mixture may be produced from produced synthesis gas using the SMDS process as illusfrated in FIG. 127. Synthesis gas 1120, having a H₂ to carbon monoxide ratio of about 2:l, may exit production well 1128. The synthesis gas may be fed into SMDS plant 1122. In certain embodiments, the ratio may range from approximately 1.8:1 to 2.2:1. Products of the SMDS plant include organic liquid product 1124 and steam 1126. Steam 1126 may be supplied to injection wells 1127. Steam may be used as a feed for synthesis gas production. Hydrocarbon vapors may in some circumstances be added to the steam.

FIG. 128 depicts an embodiment of in situ synthesis gas production integrated with a catalytic methanation process. Synthesis gas 1140 exiting production well 1142 may be supplied to catalytic methanation plant 1144. Synthesis gas supplied to catalytic methanation plant 1144 may have a H₂ to carbon monoxide ratio of about 3:1. Methane 1146 may be produced by catalytic methanation plant 1144. Steam 1148 produced by plant 1144 may be supplied to injection well 1141 for production of synthesis gas. Examples of a catalytic methanation process are illusfrated in U.S. Patent Nos. 3,922,148 to Child; 4,130,575 to Jom et al; and 4,133,825 to Sfroud et al., which are incoφorated by reference as if fully set forth herein.

Synthesis gas produced from a foπnation may be used as a feed for a process for producing methanol. Examples of processes for production of methanol are described in U.S. Patent Nos. 4,407,973 to van Dijk et al.,

4,927,857 to McShea, III et al., and 4,994,093 to Wetzel et al., each of which is incoφorated by reference as if fully set forth herein. The produced synthesis gas may also be used as a feed gas for a process that converts synthesis gas to engine fuel (e.g., gasoline or diesel). Examples of process for producing engine fuels are described in U.S. Patent Nos. 4,076,761 to Chang et al., 4,138,442 to Chang et al., and 4,605,680 to Beuther et al., each of which is incoφorated by reference as if fully set forth herein.

In a process embodiment, produced synthesis gas may be used as a feed gas for production of ammonia and urea. FIGS. 129 and 130 depict embodiments of making ammonia and urea from synthesis gas. Ammonia may be synthesized by the Haber-Bosch process, which involves synthesis directly from N₂ and H₂ according to Reaction 58:

(58) N₂ + 3 H₂* 2NH₃.

The N₂ and H₂ may be combined, compressed to high pressure, (e.g., from about 80 bars to about 220 bars), and then heated to a relatively high temperature. The reaction mixture may be passed over a catalyst composed substantially of iron to produce ammonia. During ammonia synthesis, the reactants (i.e., N₂ and H₂) and the product (i.e., ammonia) may be in equilibrium. The total amount of ammonia produced may be increased by' shifting the equilibrium towards product formation. Equilibrium may be shifted to product fonnation by removing ammonia from the reaction mixture as ammonia is produced.

Removal of the ammonia may be accomplished by cooling the gas mixture to a temperature between about -5 °C to about 25 °C. In this temperature range, a two-phase mixture may be formed with ammonia in the liquid phase and N₂ and H₂ in the gas phase. The ammonia may be separated from other components of the mixture. The nifrogen and hydrogen may be subsequently reheated to the operating temperature for ammonia conversion and passed through the reactor again.

Urea may be prepared by introducing ammonia and carbon dioxide into a reactor at a suitable pressure, (e.g., from about 125 bars absolute to about 350 bars absolute), and at a suitable temperature, (e.g., from about 160

°C to about 250 °C). Ammonium carbamate may be formed according to Reaction 59:

(59) 2 NH₃ + C0₂ → NH₂ (C0₂ ) NH₄.

Urea may be subsequently formed by dehydrating the ammonium carbamate according to equilibrium

Reaction 60:

(60) NH₂ (C0₂ ) NH₄ <→ NH₂ (CO ) NH₂ + H₂ O.

The degree to which the ammonia conversion takes place may depend on the temperature and the amount of excess ammonia. The solution obtained as the reaction product may include urea, water, ammonium carbamate, and unbound ammonia. The ammonium carbamate and the ammonia may need to be removed from the solution and returned to the reactor. The reactor may include separate zones for the formation of ammonium carbamate and urea. However, these zones may also be combined into one piece of equipment.

In a process embodiment, a high pressure urea plant may operate such that the decomposition of ammonium carbamate that has not been converted into urea and the expulsion of the excess ammonia are conducted at a pressure between 15 bars absolute and 100 bars absolute. This pressure may be considerably lower than the pressure in the urea synthesis reactor. The synthesis reactor may be operated at a temperature of about 180 °C to about 210 °C and at a pressure of about 180 bars absolute to about 300 bars absolute. Ammonia and carbon dioxide may be directly fed to the urea reactor. The NH₃/C0₂ molar ratio (N/C molar ratio) in the urea synthesis may generally be between about 3 and about 5. The unconverted reactants may be recycled to the urea synthesis reactor following expansion, dissociation, and/or condensation.

In a process embodiment, an ammonia feed sfream having a selected ratio of H₂ to N₂ may be generated from a fonnation using enriched air. A synthesis gas generating fluid and an enriched air sfream may be provided to the formation. The composition of the enriched afr may be selected to generate synthesis gas having the selected ratio of H₂ to N₂. In one embodiment, the temperature of the formation may be confrolled to generate synthesis gas having the selected ratio.

In a process embodiment, the H₂ to N₂ ratio of the feed sfream provided to the ammonia synthesis process may be approximately 3:1. m other embodiments, the ratio may range from approximately 2.8:1 to 3.2:1. An ammonia synthesis feed sfream having a selected H₂ to N₂ ratio may be obtained by blending feed sfreams produced from different portions of the formation.

In a process embodiment, ammonia from the ammonia synthesis process may be provided to a urea synthesis process to generate urea. Ammonia produced during pyrolysis may be added to the ammonia generated from the ammonia synthesis process. In another process embodiment, ammonia produced during hydrotreating may be added to the ammonia generated from the ammonia synthesis process. Some of the carbon monoxide in the synthesis gas may be converted to carbon dioxide in a shift process. The carbon dioxide from the shift process may be fed to the urea synthesis process. Carbon dioxide generated from treatment of the formation may also be fed, in some embodiments, to the urea synthesis process.

FIG. 129 illustrates an embodiment of a method for production of ammonia and urea from synthesis gas using membrane-enriched air. Enriched afr 1170 and steam, or water, 1172 may be fed into hot carbon containing formation 1174 to produce synthesis gas 1176 in a wet oxidation mode.

In some synthesis gas production embodiments, enriched air 1170 is blended from air and oxygen sfreams such that the nifrogen to hydrogen ratio in the produced synthesis gas is about 1:3. The synthesis gas may be at a conect ratio of nifrogen and hydrogen to form ammonia. For example, it has been calculated that for a formation temperature of 700 °C, a pressure of 3 bars absolute, and with 13 ,231 tons/day of char that will be converted into synthesis gas, one could inject 14.7 kilotons/day of afr, 6.2 kilotons/day of oxygen, and 21.2 kilotons/day of steam.

This would result in production of 2 billion cubic feet/day of synthesis gas including 5689 tons/day of steam, 16,778 tons/day of carbon monoxide, 1406 tons/day of hydrogen, 18,689 tons/day of carbon dioxide, 1258 tons/day of methane, and 11,398 tons/day of nifrogen. After a shift reaction (to shift the carbon monoxide to carbon dioxide and to produce additional hydrogen), the carbon dioxide may be removed, the product stream may be methanated (to remove residual carbon monoxide), and then one can theoretically produce 13,840 tons/day of ammonia and

1258 tons/day of methane. This calculation includes the products produced from Reactions (54) and (55) above. Enriched air may be produced from a membrane separation unit. Membrane separation of air may be primarily a physical process. Based upon specific characteristics of each molecule, such as size and permeation rate, the molecules in air may be separated to form substantially pure fonns of nitrogen, oxygen, or combinations thereof. In a membrane system embodiment, the membrane system may include a hollow tube filled with a plurality of very thin membrane fibers. Each membrane fiber may be another hollow tube in which afr flows. The walls of the membrane fiber may be porous such that oxygen permeates through the wall at a faster rate than nitrogen. A nifrogen rich sfream may be allowed to flow out the other end of the fiber. Afr outside the fiber and in the hollow tube may be oxygen enriched. Such air may be separated for subsequent uses, such as production of synthesis gas from a formation.

In some membrane system embodiments, the purity of nifrogen generated may be confrolled by variation of the flow rate and/or pressure of air through the membrane. Increasing air pressure may increase permeation of oxygen molecules through a fiber wall. Decreasing flow rate may increase the residence time of oxygen in the membrane and, thus, may increase permeation through the fiber wall. Air pressure and flow rate may be adjusted to allow a system operator to vary the amount and purity of the nifrogen generated in a relatively short amount of time.

The amount of N₂ in the enriched air may be adjusted to provide a N:H ratio of about 3:1 for ammonia production. Synthesis gas may be generated at a temperature that favors the production of carbon dioxide over carbon monoxide. The temperature during synthesis gas may be maintained between about 400 °C and about 550 °C, or between about 400 °C and about 450 °C. Synthesis gas produced at such low temperatures may include N_2, H₂, and carbon dioxide with little carbon monoxide.

As illustrated in FIG. 129, a feed stream for ammonia production may be prepared by first feeding synthesis gas stream 1176 into ammonia feed stream gas processing unit 1178. In ammonia feed sfream gas processing unit 1178, the feed sfream may undergo a shift reaction (to shift the carbon monoxide to carbon dioxide and to produce additional hydrogen). Carbon dioxide may be removed from the feed sfream, and the feed sfream can be methanated (to remove residual carbon monoxide). In certain embodiments, carbon dioxide may be separated from the feed sfream (or any gas sfream) by absoφtion in an amine unit. Membranes or other carbon dioxide separation techniques/equipment may also be used to separate carbon dioxide from a feed stream.

Ammonia feed sfream 1180 may be fed to ammonia production facility 1182 to produce ammonia 1184. Carbon dioxide 1186 exiting gas separation unit 1178 (and/or carbon dioxide from other sources) may be fed, with ammonia 1184, into urea production facility 1188 to produce urea 1190.

Ammonia and urea may be produced using a carbon containing foπnation and using an 0₂ rich sfream and a N₂ rich sfream. The 0₂ rich stream and synthesis gas generating fluid may be provided to a formation. The formation may be heated, or partially heated, by oxidation of carbon in the formation with the 0₂ rich sfream. H₂ in the synthesis gas and N₂ from the N₂ rich sfream may be provided to an ammonia synthesis process to generate ammonia.

FIG. 130 illustrates a flow chart of an embodiment for production of ammonia and urea from synthesis gas using cryogenically separated air. Air 2000 may be fed into cryogenic air separation unit 2002. Cryogenic separation involves a distillation process that may occur at temperatures between about -168 °C and -172 °C. In other embodiments, the distillation process may occur at temperatures between about -165 °C and -175 °C. Air may liquefy in these temperature ranges. The distillation process may be operated at a pressure between about 8 bars absolute and about 10 bars absolute. High pressures may be achieved by compressing air and exchanging heat with cold air exiting the column. Nifrogen is more volatile than oxygen and may come off as a distillate product.

N₂2004 exiting separator 2002 may be utilized in heat exchanger 2006 to condense higher molecular weight hydrocarbons from pyrolysis stream 2008 and to remove lower molecular weight hydrocarbons from the gas phase into a liquid oil phase. Upgraded gas sfream 2010 containing a higher composition of lower molecular weight hydrocarbons than sfream 2008 and liquid stream 2012, which includes condensed hydrocarbons, may exit heat exchanger 2006. N₂ 2004 may also exit heat exchanger 2006.

Oxygen 2014 from cryogenic separation unit 2002 and steam 2016, or water, may be fed into hot carbon containing formation 2018 to produce synthesis gas 2020 in a continuous process. Synthesis gas may be generated at a temperature that favors the formation of carbon dioxide over carbon monoxide. Synthesis gas 2020 may include H₂ and carbon dioxide. Carbon dioxide may be removed from synthesis gas 2020 to prepare a feed stream for ammonia production using amine gas separation unit 2022. H₂ stream 2024 from gas separation unit 2022 and N₂ sfream 2004 from the heat exchanger may be fed into ammonia production facility 2028 to produce ammonia ^■ 2030. Carbon dioxide 2032 exiting gas separation unit 2022 and ammonia 2030 may be fed into urea production facility 2034 to produce urea 2036.

FIG. 131 illustrates an embodiment of a method for preparing a nifrogen sfream for an ammonia and urea process. Air 2060 may be injected into hot carbon containing fonnation 2062 to produce carbon dioxide by oxidation of carbon in the formation. In an embodiment, a heater may heat at least a portion of the carbon containing formation to a temperature sufficient to support oxidation of the carbon. The temperature sufficient to support oxidation may be, for example, about 260 °C for coal. Stream 2064 exiting the hot formation may include carbon dioxide and nifrogen. In some embodiments, a flue gas stream may be added to stream 2064, or sfream 2064 may be a flue gas stream instead of a stream from a portion of a formation.

Nifrogen may be separated from carbon dioxide in sfream 2064 by passing the stream through cold spent carbon containing formation 2066. Carbon dioxide may preferentially adsorb versus nitrogen in cold spent formation 2066. For example, at 50 °C and 0.35 bars, the adsoφtion of carbon dioxide on a spent portion of coal may be about 72 m /mefric ton compared to about 15.4 mVinetric ton for nitrogen. Nifrogen 2068 exiting cold spent portion 2066 may be supplied to ammonia production facility 2070 with H₂ sfream 2072 to produce ammonia 2074. In some process embodiments, H₂ sfream 2072 may be obtained from a product sfream produced during synthesis gas generation of a portion of the formation. An in situ process may be used to provide heat to mobilize and/or pyrolyze hydrocarbons within a relatively low permeability formation containing heavy hydrocarbons to produce hydrocarbons from the formation that are not technically or economically producible using cunent production techniques such as surface mining, solution extraction, steam injection, etc. Such hydrocarbons may exist in relatively deep, relatively low peπneability formations containing heavy hydrocarbons. For example, such hydrocarbons may exist in a relatively low permeability formation containing heavy hydrocarbons that is greater than about 500 m below a ground surface but less than about 700 m below the surface. Hydrocarbons within these relatively deep, relatively low permeability formations containing heavy hydrocarbons may still be at a relatively cool temperature such that the hydrocarbons are substantially immobile. Hydrocarbons found in deeper formations (e.g., a depth greater than about 700 m below the surface) may be somewhat more mobile due to increased natural heating of the formations as formation depth increases below the surface. Typically, the temperature in the formation increases about 2 °C to about 4 °C for every 100 meters in depth below the surface. The temperature at a certain depth may vary, however, depending on, for example, the surface temperature which may be anywhere from about -5 °C to about 30 °C. Hydrocarbons may be more readily produced from these deeper formations because of their mobility. However, these hydrocarbons will generally be heavy hydrocarbons with an API gravity below about 20°. In some embodiments, the API gravity may be below about 15° or below about 10°. Heavy hydrocarbons produced from a relatively low permeability formation containing heavy hydrocarbons may be mixed with light hydrocarbons so that the heavy hydrocarbons can be transported to a surface facility (e.g., pumping the hydrocarbons through a pipeline). In some embodhnents, the light hydrocarbons (such as naphtha or gas condensate) are brought in through a second pipeline (or are tracked) from other areas (such as a surface facility or another production site) to be mixed with the heavy hydrocarbons. The cost of purchasing and/or transporting the light hydrocarbons to a formation site can add significant cost to a process for producing hydrocarbons from a formation. In an embodiment, producing the light hydrocarbons at or near a formation site (e.g., less than about 100 km from the foπnation site) that produces heavy hydrocarbons instead of using a second pipeline for supply of the light hydrocarbons may allow for use of the second pipeline for other puφoses. The second pipeline may be used, in addition to a first pipeline already used for pumping produced fluids, to pump produced fluids from the formation site to a surface facility. Use of the second pipeline for this piupose may further increase the economic viability of producing light hydrocarbons (i.e., blending agents) at or near the formation site. Another option is to build a surface facility or refinery at a formation site. However, this can be expensive and, in some cases, not possible.

In an embodiment, light hydrocarbons (e.g., a blending agent) may be produced at or near a formation site that produces heavy hydrocarbons (i.e., near the production site of heavy hydrocarbons). The light hydrocarbons may be mixed with heavy hydrocarbons to produce a transportable mixture. The transportable mixture may be introduced into a first pipeline used to transport fluid to a remote refinery or transportation facility, which may be located more than about 100 km from the production site. The transportable mixture may also be infroduced into a second pipeline that was previously used to transport a blending agent (e.g., naphtha, condensate, etc.) to or near the production site. Producing the blending agent at or near the production site may allow the ability to significantly increase throughput to the remote refinery or transportation facility without installation of additional pipelines. Additionally, the blending agent used may be recovered and sold from the refinery instead of being transported back to the heavy hydrocarbon production site. The transportable mixture may also be used as a raw material feed for a production process at the remote refinery. Throughput of heavy hydrocarbons to an existing remote surface facility may be a limiting factor in embodiments that use a two pipeline system with one of the pipelines dedicated to transporting a blending agent to the heavy hydrocarbon production site. Using a blending agent produced at or near the heavy hydrocarbon production site may allow for a significant increase in the throughput of heavy hydrocarbons to the remote surface facility. For example, a pair of pipelines with a blending agent to heavy hydrocarbon ratio of 1:2 may fransport twice as much oil if recycling of the blending agent is not necessary. In some embodiments, the blending agent may be used to clean tanks, pipes, wellbores, etc. The blending agent may be used for such puφoses without precipitating out components (e.g., asphaltenes or waxes) cleaned from the tanks, pipes, or wellbores.

In an embodiment, heavy hydrocarbons are produced as a first mixture from a first section of a relatively low permeability formation containing heavy hydrocarbons. Heavy hydrocarbons may include hydrocarbons with an API gravity below about 20°, 15°, or 10°. Heat provided to the first section may mobilize at least some hydrocarbons within the first section. The first mixture may include at least some mobilized hydrocarbons from the first section. Heavy hydrocarbons in the first mixture may include a relatively high asphaltene content compared to saturated hydrocarbon content. For example, heavy hydrocarbons in the first mixture may include an asphaltene content to saturated hydrocarbon content ratio greater than about 1, greater than about 1.5, or greater than about 2. Heat provided to a second section of the formation may pyrolyze at least some hydrocarbons within the second section. A second mixture may be produced from the second section. The second mixture may include at least some pyrolyzed hydrocarbons from the second section. Pyrolyzed hydrocarbons from the second section may include light hydrocarbons produced in the second section. The second mixture may include relatively higher amounts (as compared to heavy hydrocarbons or hydrocarbons found in the formation) of hydrocarbons such as naphtha, methane, ethane, or propane (i.e., saturated hydrocarbons) and/or aromatic hydrocarbons. In some embodhnents, light hydrocarbons may include an asphaltene content to saturated hydrocarbon content ratio less than about 0.5, less than about 0.05, or less than about 0.005.

A condensable fraction of the light hydrocarbons of the second mixture may be used as a blending agent. The presence of compounds in the blending agent in addition to naphtha may allow the blending agent to dissolve a large amount of asphaltenes and/or solid hydrocarbons. The blending agent may be used to clean tanks, pipelines or other vessels that have solid (or semi-solid) hydrocarbon deposits.

The light hydrocarbons of the second mixture may include less nifrogen, oxygen, sulfur, and/or metals (e.g., vanadium or nickel) than heavy hydrocarbons. For example, light hydrocarbons may have a nifrogen, oxygen, and sulfur combined weight percentage of less than about 5 %, less than about 2 %, or less than about 1 %. Heavy hydrocarbons may have a nifrogen, oxygen, and sulfur combined weight percentage greater than about 10 %, greater than about 15 %, or greater than about 18 %. Light hydrocarbons may have an API gravity greater than about 20°, greater than about 30°, or greater than about 40°.

The first mixture and the second mixture may be blended to produce a third mixture. The thfrd mixture may be formed in a surface facility located at or near production facilities for the heavy hydrocarbons. The third mixture may have a selected API gravity. The selected API gravity may be at least about 10° or, in some embodiments, at least about 20° or 30°. The API gravity may be selected to allow the third mixture to be efficiently transported (e.g., through a pipeline).

A ratio of the first mixture to the second mixture in the third mixture may be determined by the API gravities of the first mixture and the second mixture. For example, the lower the API gravity of the first mixture, the more of the second mixture that may be needed to produce a selected API gravity in the third mixture. Likewise, if the API gravity of the second mixture is increased, the ratio of the first mixture to the second mixture may be increased. In some embodiments_> a ratio of the first mixture to the second mixture in the third mixture is at least about 3:1. Other ratios may be used to produce a thfrd mixture with a desired API gravity. In certain embodiments, a ratio of the first mixture to the second mixture is chosen such that a total mass recovery from the formation will be as high as possible. In one embodiment, the ratio of the first mixture to the second mixture may be chosen such that at least about 50 % by weight of the initial mass of hydrocarbons in the formation is produced.

In other embodiments, at least about 60 % by weight or at least about 70 % by weight of the initial mass of hydrocarbons may be produced. In some embodiments, the first mixture and the second mixture are blended in a specific ratio that may increase the total mass recovery from the formation compared to production of only the second mixture from the formation (i.e., in situ processing of the formation to produce light hydrocarbons). The ratio of the first mixture to the second mixture in the thfrd mixture may be selected based on a desfred viscosity, desfred boiling point, desired composition, desired ratio of components (e.g., a desired asphaltene to saturated hydrocarbon ratio or a desired aromatic hydrocarbon to saturated hydrocarbon ratio), and/or desired density of the third mixture. The viscosity and/or density may be selected such that the third mixture is transportable through a pipeline or usable in a surface facility. In some embodiments, the viscosity (at about 4 °C) may be selected to be less than about 7500 centistokes (cs) less than about 2000 cs, less than about 100 cs, or less than about 10 cs. Centistokes is a unit of kinematic viscosity. Kinematic viscosity multiplied by the density yields absolute viscosity. The density (at about 4 °C) may be selected to be less than about 1.0 g/cm³, less than about 0.95 g/cm³, or less than about 0.9 g cm³. The asphaltene to saturated hydrocarbon ratio may be selected to be less than about 1, less than about 0.9, or less than about 0J. The aromatic hydrocarbon to saturated hydrocarbon ratio may be selected to be less than about 4, less than about 3.5, or less than about 2.5. The viscosity of a thfrd mixture may have improved viscosity compared to conventionally produced crade oils. For example, in "The Viscosity of Afr, Natural Gas, Crude Oil and Its Associated Gases at Oil Field Temperatures and Pressures" by Carlton Beal, AIME Transactions, vol. 165, p. 94, 1946, which is incoφorated by reference as if fully set forth herein. Beal found a conelation for 655 samples of crade oil that indicates an average viscosity of about 50 centipoise (cp) at 38 °C for crade oil with an API gravity of 24°. The lowest average viscosity was found to be about 20 cp at 38 °C for 200 California crade oil samples with an API gravity of 24°. A third mixture produce by mixing of a first mixture and a second mixture may have a viscosity of about 11 cp at 38 °C and 24° API. Thus, a mixture produced by mixing heavy hydrocarbons with light hydrocarbons produced by an in situ conversion process may have improved viscosity compared to typical produced crade oils.

In an embodiment, the ratio of the first mixture to the second mixture in the third mixture is selected based on the relative stability of the third mixture. A component or components of the thfrd mixture may precipitate out of the thfrd mixture. For example, asphaltene precipitation may be a problem for some mixtures of heavy hydrocarbons and light hydrocarbons. Asphaltenes may precipitate when fluid is de-pressurized (e.g., removed from a pressurized formation or vessel) and/or there is a change in mixture composition. For the third mixture to be transportable through a pipeline or usable in a surface facility, the third mixture may need a minimum relative stability. The minimum relative stability may include a ratio of the first mixture to the second mixture such that asphaltenes do not precipitate out of the thfrd mixture at ambient and/or elevated temperatures. Tests may be used to determine desired ratios of the first mixture to the second mixture that will produce a relatively stable third mixture. For example, induced precipitation, chromatography, titration, and/or laser techniques may be used to detennine the stability of asphaltenes in the thfrd mixture. In some embodhnents, asphaltenes precipitate out of a mixture but are held suspended in the mixture and, hence, the mixture may be transportable. A blending agent produced by an in situ process may have excellent blending characteristics with heavy hydrocarbons (i.e., low probability for precipitation of heavy hydrocarbons from a mixture with the blending agent).

In certain embodiments, resin content in the second mixture (i.e., light hydrocarbon mixture) may determine the stability of the thfrd mixture. For example, resins such as maltenes or resins containing heteroatoms such as N, S, or O may be present in the second mixture. These resins may enhance the stability of a third mixture produced by mixing a first mixture with the second mixture. In some cases, the resins may suspend asphaltenes in the mixture and inhibit asphaltene precipitation.

In certain embodhnents, market conditions may determine characteristics of a thfrd mixture. Examples of market conditions may include, but are not limited to, demand for a selected octane of gasoline, demand for heating oil in cold weather, demand for a selected cetane rating in a diesel oil, demand for a selected smoke point for jet fuel, demand for a mixture of gaseous products for chemical synthesis, demand for transportation fuels with a certain sulfur or oxygenate content, or demand for material in a selected chemical process.

In an embodiment, a blending agent may be produced from a section of a relatively low permeability formation containing heavy hydrocarbons. "Blending agent" is a material that is mixed with another material to produce a mixture having a desired property (e.g., viscosity, density, API gravity, etc.). The blending agent may include at least some pyrolyzed hydrocarbons. The blending agent may include properties of the second mixture of light hydrocarbons described above. For example, the blending agent may have an API gravity greater than about 20°, greater than about 30°, or greater than about 40°. The blending agent may be blended with heavy hydrocarbons to produce a mixture with a selected API gravity. For example, the blending agent may be blended with heavy hydrocarbons with an API gravity below about 15° to produce a mixture with an API gravity of at least about 20°. In certain embodiments, the blending agent may be blended with heavy hydrocarbons to produce a transportable mixture (e.g., movable through a pipeline). In some embodiments, the heavy hydrocarbons are produced from another section of the relatively low permeability formation containing heavy hydrocarbons. In other embodiments, the heavy hydrocarbons may be produced from another relatively low permeability foπnation containing heavy hydrocarbons or any other formation containing heavy hydrocarbons, at the same site or another site.

In some embodiments, the first section and the second section of the formation may be at different depths within the same formation. For example, the heavy hydrocarbons may be produced from a section having a depth between about 500 m and about 1500 m, a section having a depth between about 500 m and about 1200 m, or a section having a depth between about 500 m and about 800 m. At these depths, the heavy hydrocarbons may be somewhat mobile (and producible) due to a relatively higher natural temperature in the reservoir. The light hydrocarbons may be produced from a section having a depth between about 10 m and about 500 m, a section having a depth between about 10 m and about 400 m, or a section having a depth between about 10 m and about 250 m. At these shallower depths, heavy hydrocarbons may not be readily producible because of the lower natural temperatures at the shallower depths. In addition, the API gravity of heavy hydrocarbons may be lower at shallower depths due to increased water washing, loss of lighter hydrocarbons due to leaks in the seal of the formation, and/or bacterial degradation. In other embodiments, heavy hydrocarbons and light hydrocarbons are produced from first and second sections that are at a similar depth below the surface. In another embodiment, the light hydrocarbons and the heavy hydrocarbons are produced from different formations. The different formations, however, may be located near each other.

In an embodiment, heavy hydrocarbons are cold produced from a formation (e.g., a tar sands formation in the Faja (Venezuela)) at depths between about 760 m and about 1070 m. The produced hydrocarbons may have an API gravity of less than about 9°. Cold production of heavy hydrocarbons is generally defined as the production of heavy hydrocarbons without providing heat (or providing relatively little heat) to the formation or the production well. In other embodiments, the heavy hydrocarbons may be produced by steam injection or a mixture of steam injection and cold production. The heavy hydrocarbons may be mixed with a blending agent to transport the produced heavy hydrocarbons through a pipeline. In one embodhnent, the blending agent is naphtha. Naphtha may be produced in surface facilities that are located remotely from the formation.

In other embodiments, the heavy hydrocarbons may be mixed with a blending agent produced from a shallower section of the formation using an in situ conversion process. The shallower section may be at a depth less than about 400 m (e.g., less than about 150 m). The shallower section of the foπnation may contain heavy hydrocarbons with an API gravity of less than about 7°. The blending agent may include light hydrocarbons produced by pyrolyzing at least some of the heavy hydrocarbons from the shallower section of the formation. The blending agent may have an API gravity above about 35° (e.g., above about 40°).

In certain embodiments, a blending agent may be produced in a first portion of a relatively low permeability formation containing heavy hydrocarbons and injected (e.g., into a production well) into a second portion of the relatively low permeability formation containing heavy hydrocarbons (or, in some embodiments, a second portion in another relatively low permeability formation containing heavy hydrocarbons). Heavy hydrocarbons may be produced from the second portion (e.g., by cold production). Mixing between the blending agent may occur within the production well and/or within the second portion of the formation. The blending agent may be produced through a production well in the first portion and pumped to a production well in the second portion. In some embodiments, non-hydrocarbon fluids (e.g., water or carbon dioxide), vapor-phase hydrocarbons, and/or other undesired fluids may be separated from the blending agent prior to mixing with heavy hydrocarbons.

Injecting the blending agent into a portion of a relatively low permeability formation containing heavy hydrocarbons may provide mixing of the blending agent and heavy hydrocarbons in the portion. The blending agent may be used to assist in the production of heavy hydrocarbons from the formation. The blending agent may reduce a viscosity of heavy hydrocarbons in the formation. Reducing the viscosity of heavy hydrocarbons in the formation may reduce the possibility of clogging or other problems associated with cold producing heavy hydrocarbons. In some embodiments, the blending agent may be at an elevated temperature and be used to provide at least some heat to the foπnation to increase the mobilization (i.e., reduce the viscosity) of heavy hydrocarbons within the formation. The elevated temperature of the blending agent may be a temperature proximate the temperature at which the blending agent is produced minus some heat losses during production and fransport of the blending agent. In certain embodiments, the blending agent may be pumped through an insulated pipeline to reduce heat losses during fransport.

The blending agent may be mixed with the cold produced heavy hydrocarbons in a selected ratio to produce a third mixture with a selected API gravity. For example, the blending agent may be mixed with cold produced heavy hydrocarbons in a 1 to 2 ratio or a 1 to 4 ratio to produce a third mixture with an API gravity greater than about 20°. In some embodiments, other ratios of blending agent to heavy hydrocarbons may be selected as desired to produce a third mixture with one or more selected properties. In certain embodiments, the third mixture may have an overall API gravity greater than about 25° or an API gravity sufficiently high such that the third mixture is transportable through a conduit or pipeline. In some embodiments, the third mixture of hydrocarbons may have an API gravity between about 20° and about 45°. In other embodiments, the blending agent may be mixed with cold produced heavy hydrocarbons to produce a third mixture with a selected viscosity, a selected stability, and/or a selected density.

The thfrd mixture may be transported through a conduit, such as a pipeline, between the formation and a surface facility or refinery. The third mixture may be transported through a pipeline to another location for further transportation (e.g., the mixture can be transported to a facility at a river or a coast through the pipeline where the mixture can be further transported by tanker to a processing plant or refinery). Producing the blending agent at the formation site (i.e., producing the blending agent from the formation) may reduce a total cost for producing hydrocarbons from the formation. In addition, producing the third hydrocarbon mixture at a foπnation site may eliminate a need for a separate supply of light hydrocarbons and/or construction of a surface facility at the site. In an embodiment, a mixture of hydrocarbons may include about 20 weight % light hydrocarbons (or blending agent) or greater (e.g., about 50 weight % or about 80 weight % light hydrocarbons) and about 80 weight % heavy hydrocarbons or less (e.g., about 50 weight % or about 20 weight % heavy hydrocarbons). The weight percentage of light hydrocarbons and heavy hydrocarbons may vary depending on, for example, a weight distribution (or API gravity) of light and heavy hydrocarbons, a relatively stability of the thfrd mixture or a desired

API gravity of the mixture. For example, in some embodiments, the weigh percentage of light hydrocarbons in the mixture may be less than 50 weight % or less than 20 %. In certain embodiments, the weight percentage of light hydrocarbons may be selected to blend the least amount of light hydrocarbons with heavy hydrocarbons that produces a mixture with a desired density or viscosity. Reducing the viscosity of heavy hydrocarbons with a blending agent may make it easier to separate water from the blended hydrocarbons.

FIG. 132 depicts a plan view of an embodiment of a relatively low permeability formation containing heavy hydrocarbons used to produce a first mixture that is blended with a second mixture. Relatively low permeability formation containing heavy hydrocarbons 9300 may include first section 9304 and second section 9302. First section 9304 may be at depths greater than, for example, about 800 m below a surface of the foπnation. Heavy hydrocarbons in first section 9304 may be produced through production well 9306 placed in the first section.

Heavy hydrocarbons in first section 9304 may be produced without heating because of the depth of the first section. Ffrst section 9304 may be below a depth at which natural heating mobilizes heavy hydrocarbons within the first section. In some embodiments, at least some heat may be provided to first section 9304 to mobilize fluids within the first section. Second section 9302 may be heated using heat sources 6700 placed in the second section. Heat sources

6700 are depicted as substantially horizontal heat sources in FIG. 132. Heat provided by heat sources 6700 may pyrolyze at least some hydrocarbons within second section 9302. Pyrolyzed fluids may be produced from second section 9302 through production well 6710. Production well 6710 is depicted as a substantially vertical production well in FIG. 132. fri an embodiment, heavy hydrocarbons from first section 9304 are produced in a first mixture through production well 9306. Light hydrocarbons (i.e., pyrolyzed hydrocarbons) may be produced in a second mixture through production well 6710. The first mixture and the second mixture may be mixed to produce a third mixture in surface facility 9310. The first and the second mixture may be mixed in a selected ratio to produce a desfred thfrd mixture. The thfrd mixture may be transported through pipeline 9312 to a production facility or a transportation facility. The production facility or fransportation facility may be located remotely from surface facility 9310. In some embodiments, the third mixture may be trucked or shipped to a production facility or transportation facility. In certain embodiments, surface facility 9310 may be a simple mixing station to combine the mixtures produced from production well 9306 and production well 6710.

In certain embodiments, the blending agent produced from second section 9302 may be injected through production well 9306 into first section 9304. A mixture of light hydrocarbons and heavy hydrocarbons may be produced through production well 9306 after mixing of the blending agent and heavy hydrocarbons in first section 9304. In some embodiments, the blending agent may be produced by separating non-desirable components (e.g., water) from a mixture produced from second section 9302. The blending agent may be produced in surface facility 9310. The blending agent may be pumped from surface facility 9310 through production well 9306 and into first section 9304. FIGS. 151-138 depict results from an experiment. In the experiment, blending agent 102 produced by pyrolysis was mixed with Athabasca tar (heavy hydrocarbons 110) in three blending mixtures of different ratios. First mixture 9645 included 80 % blending agent 9644 and 20 % heavy hydrocarbons 9648. Second mixture 9646 included 50 % blending agent 9644 and 50 % heavy hydrocarbons 9648. Thfrd mixture 9647 included 20 % blending agent 9644 and 80 % heavy hydrocarbons 9648. Composition, physical properties, and asphaltene stability were measured for the blending agent, heavy hydrocarbons, and each of the mixtures.

TABLE 9 presents results of composition measurements of the mixtures. SARA analysis determined composition on a topped oil basis. SARA analysis includes a combination of induced precipitation (for asphaltenes) and column chromatography. Whole oil basis compositions were also determined.

TABLE 9

Key:

Sat Saturates

Aro Aromatics

NSO Resins (containing heteroatoms such asN, S and O)

Asph Asphaltenes

FIG. 151 depicts asphaltene content (on a whole oil basis) in the blend versus percent blending agent in the mixture for each of the three mixtures (9645, 9646, and 9647), blending agent 9644, and heavy hydrocarbons 9648. As shown in FIG. 151, asphaltene content on a whole oil basis varies linearly with the percentage of blending agent 9644 in the mixture.

FIG. 133 depicts SARA results (saturate/aromatic ratio versus asphaltene/resin ratio) for each of the blends (9644, 9645, 9646, 9647, and 9648). The line in FIG. 133 represents the differentiation between stable mixtures and unstable mixtures based on SARA results. The topping procedure used for SARA removed a greater proportion of the contribution of blending agent 9644 (as compared to whole oil analysis) and resulted in the non-linear disfribution in FIG. 133. First mixture 9645, second mixture 9646, and thfrd mixture 9647 plotted closer to heavy hydrocarbons 9648 than blending agent 9644. In addition, second mixture 9646 and third mixture 9647 plotted relatively closely. All blends (9644, 9645, 9646, 9647, and 9648) plotted in a region of marginal stability.

Blending agent 9644 included very little asphaltene (0.01 % by weight, whole oil basis). Heavy hydrocarbons 9648 included about 13.2 % by weight (whole oil basis) with the amount of asphaltenes in the mixtures (9645, 9646, and 9647) varying between 2.2 % by weight and 10.3 % by weight on a whole oil basis. Other indicators of the gross oil properties is the ratio between saturates and aromatics and the ratio between asphaltenes and resins. The asphaltene/resin ratio was lowest for first mixture 9645, which has the largest percentage of blending agent 9644. Second mixture 9646 and thfrd mixture 9647 had relatively similar asphaltene/resin ratios indicating that the majority of resins in the mixtures are due to contribution from heavy hydrocarbons 9648. The saturate/aromatic ratio was relatively similar for each of the mixtures. Density and viscosity of the mixtures were measured at three temperatures 4.4 °C (40 °F), 21 °C (70 °F), and 32 °C (90 °F). The density and API gravity of the mixtures were also determined at 15 °C (60 °F) and used to calculate API gravities at other temperatures. In addition, a Floe Point Analyzer (FPA) value was determined for each of the three blended mixtures (9645, 9646, and 9647). FPA is detennined by n-heptane titration. The floe point is detected with a near infrared laser. The light source is blocked by asphaltenes precipitating out of solution. The FPA test was calibrated with a set of known problem and non-problem mixtures. Generally, FPA values less than 2.5 are considered unstable, greater than 3.0 are considered stable, and 2.5-3.0 are considered marginal. TABLE 10 presents values for FPA, density, viscosity, and API gravity for the three blended mixtures at four temperatures.

TABLE 10

Key: FPA Flocculation Point Analyzer value

Spec. Grav. Specific Gravity relative to water Density (g/cc) Density in grams per cubic centimeter API API gravity relative to water Vise, (cs) Viscosity in centistokes

FPA tests showed that the mixtures containing lower amounts of heavy hydrocarbons were less stable. The lower stability was likely due to the proportion of aliphatic components already in these mixtures, which reduces asphaltene solubility. First mixture 9645 was the least stable with a FPA value of 1.5, indicating instability with respect to asphaltene precipitation. FIG. 134 illusfrates near infrared fransmittance versus volume (ml) of n- heptane added to first mixture 9645. The peak in the plot for first mixture 9645 illustrates that precipitation of asphaltenes occurs rapidly with the addition of n-heptane.

Second mixture 9646 exhibited different behavior. Second mixture 9646 had a FPA value of 2.2 indicating instability with respect to asphaltene precipitation. FIG. 135 illusfrates near infrared transmittance versus volume (ml) of n-heptane added to second mixture 9646. Two distinct peaks are seen in FIG. 135 indicating that asphaltenes were precipitated, re-dissolved, and then re-precipitated with continuous addition of n-heptane.

FIG. 136 illusfrates near infrared fransmittance versus volume (ml) of n-heptane added to third mixture 9647. Third mixture 9647 showed similar behavior to second mixture 9646 as shown in FIGS. 135 and 136. The first peak in FIG. 136, however, was less pronounced than the first peak in FIG. 135. The FPA value of 2.8 found for third mixture 9647 indicates marginal stability for the third mixture. Slow homogenization, associated with a high viscosity of the sample mixtures, is most likely responsible for the appearance of double peaks in FIGS. 135 and 136. Each of the mixtures (9645, 9646, and 9647) showed relatively similar changes in density with increasing temperature (as shown in FIG. 137). API values increased conespondingly with decreasing density. Viscosity changes, however, varied between each of the mixtures.

First mixture 9645 was the least affected by temperature with viscosity values at 21 °C and 32 °C determined to be about 70 % and about 57 % of that at 4.4 °C, respectively. Second mixture 9646 had viscosity values that decreased to values (of that at 4.4 °C) of about 48 % at 21 °C and about 30 % at 32 °C. Thfrd mixture 9647 was the most affected by temperature with viscosity values of about 21 % and about 9 % at 21 °C and 32 °C, respectively. Viscosity changes are approximately linear on a logarithmic plot of viscosity versus temperature as shown in FIG. 138. An in situ conversion process may be used to produce hydrocarbons from a relatively low penneability formation. Hydrocarbon material in the low permeability formation may be heavy hydrocarbons. Hydrocarbons in a selected section of the foπnation may be pyrolyzed by heat from heat sources. Heat provided by the heat sources may allow for vapor phase transport to production wells in the formation.

In addition to allowing for vapor phase fransport through the selected section of formation, heating the formation may also increase the average permeability of at least a portion of the selected section. The increase in temperature of the foπnation may create thermal fractures in the formation. The thermal fractures may propagate between heat sources, further increasing the permeability in a portion of a selected section of the formation. During heating of the formation to pyrolysis temperatures, water in the selected section may vaporize. Vaporization may generate localized areas of very high pressure that cause fracturing of the selected formation. In some formations, the formation and/or heavy hydrocarbons in the formation may absorb a portion of the energy caused by thermal expansion and/or by vaporization pressure change to limit increasing permeability.

In an in situ conversion process embodiment, the pressure in at least a portion of the relatively low peπneability formation may be controlled to maintain a composition of produced formation fluids within a desired range. The composition of the produced formation fluids may be monitored. The pressure may be controlled by a back pressure valve located proximate where the formation fluids are produced. A desfred operating pressure of a production well to produce a desired composition may be determined from experimental data for the relationship between pressure and the composition of pyrolysis products of the heavy hydrocarbons in the formation.

FIG. 139 is a view of an embodiment of a heat source and production well pattern for heating heavy hydrocarbons in a relatively low permeability foπnation. Heat sources 2502, 2503, and 2504 may be ananged in a triangular pattern with the heat sources at the apices of the friangular grid. Production well 2500 may be located proximate the center of the triangular grid. In other pattern embodhnents, a production well may be placed at any location in the grid pattern. Heat sources may be ananged in patterns other than the triangular pattern shown in FIG. 139. For example, wells may be ananged in square patterns. Heat sources 2502, 2503, and 2504 may heat a portion of the foπnation to a temperature that allows for pyrolysis of heavy hydrocarbons in the formation. Pyrolyzation fluids produced by pyrolysis may flow toward the production well, as indicated by the anows, and formation fluids may be produced through production well 2500.

In some in situ conversion process embodiments for freating low permeability formations, average distances between heat sources effective to pyrolyze heavy hydrocarbons in the formation may be between about 5 m and about 8 m. In some embodiments, a smaller average distance may be needed. In some in situ conversion process embodiments for freating low permeability formations, average distance between heat sources may be between about 2 m and about 5 m. FIG. 140 is a view of an embodiment of a heat source pattern for heating heavy hydrocarbons in a portion of a hydrocarbon containing formation of relatively low permeability and producing fluids from one or more heater wells. Heat sources 2502 may be ananged in a friangular pattern. The heat sources may provide heat to pyrolyze some or all of the fluid in the formation. Fluids may be produced through one or more of the heat sources. An embodiment for freating hydrocarbons in a relatively low permeability formation may include heating the formation to create at least two zones within the formation such that the zones have different average temperatures. Heat sources may heat a first section of the fonnation to create a pyrolysis zone. Heat sources may heat a second section to an average temperature that is less than a pyrolysis temperature to create a low viscosity zone. The decrease in viscosity of the heavy hydrocarbons in the selected second section may be sufficient to produce mobilized fluids within the selected second section. The mobilized fluids may flow into the pyrolysis zone of the first section. For example, increasing the temperature of the heavy hydrocarbons in the formation to between about 200 °C and about 250 °C may decrease the viscosity of the heavy hydrocarbons sufficiently for the heavy hydrocarbons to flow through the foπnation. In another embodiment, increasing the temperature of the fluid to between about 180 °C and about 200 °C may also be sufficient to mobilize the heavy hydrocarbons. For example, the viscosity of heavy hydrocarbons in a formation at 200 °C may be about 50 centipoise to about 200 centipoise. Production wells in the first section may create a low pressure zone that facilitates fluid flow from the second section into the first section.

Heating may create thermal fractures that propagate between heat sources in both the selected first section and the selected second section. The thermal fractures may substantially increase the permeability of the formation and may facilitate the flow of mobilized fluids from the low viscosity zone to the pyrolysis zone. In one embodiment, a vertical hydraulic fracture may be created in the formation to further increase penneability. The presence of a hydraulic fracture may also be desirable since heavy hydrocarbons that collect in the hydraulic fracture may have an increased residence time in the pyrolysis zone. The increased residence time may result in increased pyrolysis of the heavy hydrocarbons in the pyrolysis zone.

In addition, the pressure in the low viscosity zone may increase due to thermal expansion of the formation and evaporation of entrained water in the formation to form steam. For example, pressures in the low viscosity zone may range from about 10 bars absolute to an overburden pressure. In some process embodiments, the pressure may range from about 15 bars absolute to about 50 bars absolute. The value of the pressure may depend upon factors such as, but not limited to, the degree of thermal fracturing, the amount of water in the formation, and material properties of the foπnation. The pressure in the pyrolysis zone may be substantially lower than the pressure in the low viscosity zone because of the higher permeability of the pyrolysis zone. The higher temperature in the pyrolysis zone compared to the low viscosity zone may cause a higher degree of thermal fracturing, and thus a greater permeability. For example, pyrolysis zone pressures may range from about 3.5 bars absolute to about 10 bars absolute. In some embodiments, pyrolysis zone pressures may range from about 10 bars absolute to about 15 bars absolute.

The pressure differential between the pyrolysis zone and the low viscosity zone may force some mobilized fluids to flow from the low viscosity zone into the pyrolysis zone. Heavy hydrocarbons in the pyrolysis zone may be upgraded by pyrolysis into pyrolyzation fluids. Pyrolyzation fluids may be produced from the formation through a production well or production wells. A production well or production wells may be designed to remove liquids, vapor or a combination of liquid and vapor from the formation. In an in situ conversion process embodiment, the concenfration (or density) of heat sources in the pyrolysis zone may be greater than the concentration of heat sources in the low viscosity zone. The increased concenfration of heat sources in the pyrolysis zone may establish and maintain a uniform pyrolysis temperature in the pyrolysis zone. Using a lower concenfration of heat sources in the low viscosity zone may be more efficient and economical due to the lower temperature required in the low viscosity zone. In one process embodiment, an average distance between heat sources for heating the first selected section may be between about 5 m and about 10 m. Alternatively, an average distance may be between about 2 m and about 5 m. In some embodhnents, an average distance between heat sources for heating the second selected section may be between about 5 m and about 20 m. In an in situ conversion process embodiment, the pyrolysis zone and one or more low viscosity zones may be heated sequentially over time. Heat sources may heat the first selected section until an average temperature of the pyrolysis zone reaches a desired pyrolysis temperature. Subsequently, heat sources may heat one or more low viscosity zones of the selected second section that may be nearest the pyrolysis zone until such low viscosity zones reach a desired average temperature. Heating low viscosity zones of the selected second section farther away from the pyrolysis zone may continue in a like manner. In an in situ conversion process embodiment, heat may be provided to a formation to create a first volume of formation at pyrolysis temperature (pyrolysis zone) and an adjacent volume of formation below pyrolysis temperature (low viscosity zone). One or more planar low viscosity zones may be created with symmetry about the pyrolysis zone. In an in situ conversion process embodiment, the pyrolysis zone may be sunounded by an annular low viscosity zone. In some embodiments, portions of the pyrolysis zone that no longer produce formation fluids of a desired quality and/or quantity are allowed to cool while a leading edge or leading edges (or a circumference) of pyrolysis zone is maintained at pyrolysis temperatures. Formation fluids may be produced through a production well or production wells. The production well or production wells may be located in the pyrolysis zone and/or in a produced portion of the formation that is no longer maintained at pyrolysis temperature.

FIG. 141 is a view of an embodiment of a heat source and production well pattern illustrating a pyrolysis zone and a low viscosity zone. Heat sources 2512 along plane 2506B and plane 2506A may heat planar region

2508 to create a pyrolysis zone. Heating may create thermal fractures 2510 in the pyrolysis zone. Heating with heat sources 2514 in planes 2516, 2518, 2520, and 2522 may create a low viscosity zone with an increased permeability due to thermal fractures. Pressure differential between the low viscosity zone and the pyrolysis zone may force mobilized fluid from the low viscosity zone into the pyrolysis zone. The permeability created by theπnal fractures 2510 may be sufficiently high to create a substantially uniform pyrolysis zone. Pyrolyzation fluids may be produced tiirough production well 2500.

In an in situ conversion process embodiment, a pyrolysis zone and/or low viscosity zone may move as time spent processing the formation advances. In an embodiment, the heat sources nearest the pyrolysis zone may be activated first. For example, heat sources 2512 in plane 2506B and plane 2506A of FIG. 141. A substantially uniform temperature may be established in the pyrolysis zone after a period of time. Mobilized fluids that flow through the pyrolysis zone may undergo pyrolysis and vaporize. Once the pyrolysis zone is established, heat sources in the low viscosity zone (e.g., heat sources 2514 in plane 2516 and plane 2520) nearest the pyrolysis zone may be turned on and/or up to establish a low viscosity zone. A larger low viscosity zone may be developed by repeatedly activating heat sources (e.g., heat sources 2514 in plane 2518 and plane 2522) farther away from the pyrolysis zone. FIG. 142 is an expanded view of the pattern shown in FIG. 141. The four planar vertical regions that conespond to region 2508 in FIG. 141 may include heat sources that create pyrolysis zones 2540. Regions 2548, 2550, and 2552 may include heat sources that apply heat to create a low viscosity zone. Production wells 2500 may be disposed in regions where pyrolysis occurs. Production wells 2500 may remove pyrolyzation fluids from the formation. In one embodiment, a length of pyrolysis zones 2540 may be between about 75 m and about 300 m. In another embodiment, a length of the pyrolysis zones may be between about 100 m and about 125 m. In an embodiment, an average distance between production wells in the same plane may be between about 100 m and about 150 m. Shorter or longer production zones may be established to conespond to foπnation conditions. In one embodiment, a distance between plane 2542 and plane 2544 may be between about 40 m and about 80 m. In some embodiments, more than one production well may be disposed in a region where pyrolysis occurs. Plane 2542 and plane 2544 may be substantially parallel. The formation may include additional planar vertical pyrolysis zones that may be substantially parallel to each other. Hot fluids may be provided into vertical planar regions such that in situ pyrolysis of heavy hydrocarbons may occur. Pyrolyzation fluids may be removed by production wells disposed in the vertical planar regions. An embodiment of a planar pyrolysis zone may include a vertical hydraulic fracture created by hydraulically fracturing through a production well in the formation. The formation may include heat sources located substantially parallel to the vertical hydraulic fracture in the formation. Heat sources in a planar region adjacent to the fracture may provide heat sufficient to pyrolyze at least some or all of the heavy hydrocarbons in a pyrolysis zone. Heat sources outside the planar region may heat the formation to a temperature sufficient to decrease the viscosity of the fluids in a low viscosity zone.

FIG. 143 is a view of an embodhnent for freating heavy hydrocarbons in at least a portion of a hydrocarbon containing formation of relatively low permeability. Fracture 2602 may be created from wellbore of production well 2600. In an embodiment, the width of fracture 2602 generated by hydraulic fracturing may be between about 0.3 cm and about 1 cm. In other embodiments, the width of fracture 2602 may be between about 1 cm and about 3 cm. The pyrolysis zone may be foπned in a planar region on either side of the vertical hydraulic fracture by heating the planar region to an average temperature within a pyrolysis temperature range with heat sources 2604 in plane 2605 and plane 2606. Creation of a low viscosity zone on both sides of the pyrolysis zone, above plane 2605 and below plane 2606, may be accomplished by heat sources outside the pyrolysis zone. For example, heat sources 2608 in planes 2610, 2612, 2614, and 2616 may heat the low viscosity zone to a temperature sufficient to lower the viscosity of heavy hydrocarbons in the foπnation. Mobilized fluids in the low viscosity zone may flow to the pyrolysis zone due to the pressure differential between the low viscosity zone and the pyrolysis zone and the increased permeability from thermal fractures.

FIG. 144 is an expanded view of an embodiment shown in FIG. 143. FIG. 144 illustrates a foπnation with two fractures 2645a, 2645b along plane 2645 and two fractures 2646a, 2646b along plane 2646. Each fracture may be produced from wellbores of production wells 2640. Plane 2645 and plane 2646 may be substantially parallel. The length of a fracture created by hydraulic fracturing in relatively low permeability formations may be between about 75 m and about 100 m. In some embodiments, the vertical hydraulic fracture may be between about 100 m and about 125 m. Vertical hydraulic fractures may propagate substantially equal distances along a plane from a production well. The distance between production wells along the same plane may be between about 100 m and about 150 m to inhibit fractures from joining together. As the distance between fractures on different planes increases, for example the distance between plane 2645 and plane 2646, the flow of mobilized fluids farthest from either fracture may decrease. A distance between fractures on different planes that may be economical and effective for the fransport of mobilized fluids to the pyrolysis zone may be about 40 m to about 80 m.

Plane 2648 and plane 2649 may include heat sources that may provide heat sufficient to create a pyrolysis zone between plane 2648 and plane 2649. Plane 2651 and plane 2652 may include heat sources that create a pyrolysis zone between plane 2651 and plane 2652. Heat sources in regions 2650, 2660, 2655, and 2656 may provide heat that may create low viscosity zones. Mobilized fluids in regions 2650, 2660, 2655, and 2656 may tend to flow in a direction toward the closest fracture in the formation. Mobilized fluids entering the pyrolysis zone may be pyrolyzed. Pyrolyzation fluids may be produced from production wells 2640. In one in situ conversion process embodiment, heat may be provided to a relatively low permeability formation to create a pyrolysis zone and a low viscosity zone around a production well. Fluids may be pyrolyzed in the pyrolysis zone. Pyrolyzation fluids may be produced from the production well in the pyrolysis zone. Heat sources may be located around a production well in a pattern. Heat sources closest to a production well may heat portions of the formation adjacent to the production well to a pyrolysis temperature. Additional heaters farther from the production well may heat the formation to create a low viscosity zone. Mobilized fluid in the low viscosity zone may flow to the pyrolysis zone due to the pressure differential between the low viscosity zone and the pyrolysis zone. An increased permeability due to thermal fracturing of the formation may facilitate flow of hydrocarbons to the pyrolysis zone and production well.

Several patterns of heat sources ananged in rings around production wells may be utilized to create a pyrolysis region around a production well and a low viscosity zone in a relatively low permeability formation containing heavy hydrocarbons. Various pattern embodiments are shown in FIGS. 145-158. Although the patterns are discussed in the context of heavy hydrocarbons, it is to be understood that any of the patterns shown in FIGS. 145-158 may be used for other hydrocarbon containing formations.

FIG. 145 illusfrates an embodiment of a pattern of heat sources 2705 that may create a pyrolysis zone and low viscosity zone around production well 2701. Production well 2701 may be sunounded by rings 2702, 2703, and 2704 of heat sources 2705. Heat sources 2705 in ring 2702 may heat the formation to create pyrolysis zone 2710. Heat sources 2705 in rings 2703 and 2704 outside pyrolysis zone 2710 may heat the formation to create a low viscosity zone. The viscosity of a portion of the hydrocarbons in the low viscosity zone may be reduced sufficiently to allow the hydrocarbons to flow inward from the low viscosity zone to pyrolysis zone 2710. Fluids may be produced tiirough production well 2701. In some embodiments, an average distance between heat sources may be between about 2 m and about 10 m. In other embodiments, the average distance between heat sources may be between about 10 m and about 20 m.

Pyrolysis zones and low viscosity zones in a formation may be created sequentially. Heat sources 2705 nearest production well 2701 may be activated first, for example, heat sources 2705 in ring 2702. A substantially uniform temperature pyrolysis zone may be established after a period of time. Fluids that flow through the pyrolysis zone may undergo pyrolysis and/or vaporization. Once the pyrolysis zone is established, heat sources 2705 in the low viscosity zone near the pyrolysis zone (e.g., heat sources 2705 in ring 2703) may be activated to provide heat to a portion of a low viscosity zone. Fluid may flow inward towards production well 2701 due to a pressure differential between the low viscosity zone and the pyrolysis zone, as indicated by the anows. A larger low viscosity zone may be developed by repeatedly activating heat sources farther away from production well 2701

(e.g., heat sources 2705 in ring 2704).

Production wells 2701 and heat sources 2712 may be located at the apices of a triangular grid, as depicted in FIG. 146. The friangular grid may be an equilateral triangular grid with sides of length s. Production wells 2701 may be spaced at a distance of about 1.132(s). Each production well 2701 may be disposed at a center of ring 2713 of heat sources 2712 in a hexagonal pattern. Each heat source 2712 may provide substantially equal amounts of heat to three production wells. Therefore, each ring 2713 of six heat sources 2712 may contribute approximately two equivalent heat sources per production well 2701.

FIG. 147 illusfrates a pattern of production wells 2701 with an inner hexagonal ring 2713 and an outer hexagonal ring 2715 of heat sources 2712. In this pattern, production wells 2701 may be spaced at a distance of about 2(1.732)5'. Heat sources 2712 may be located at all other grid positions. This pattern may result in a ratio of equivalent heat sources to production wells that may approach 11:1 (i.e., 6 equivalent heat sources for ring 2713;

(l/2)(6) or 3 equivalent heat sources for the 6 heat sources of ring 2715 between apices of the hexagonal pattern; and (l/3)(6) or 2 equivalent heat sources for the 6 heat sources of ring 2715 at the apices of the hexagonal pattern). FIG. 148 illusfrates three rings of heat sources 2712 sunounding production well 2701. Production well

2701 may be sunounded by ring 2713 of six heat sources 2712. Second hexagonally shaped ring 2716 of twelve heat sources 2712 may sunound ring 2713. Thfrd ring 2718 of heat sources 2712 may include twelve heat sources that may provide substantially equal amounts of heat to two production wells and six heat sources that may provide substantially equal amounts of heat to three production wells. Therefore, a total of eight equivalent heat sources may be disposed on thfrd ring 2718. Production well 2701 may be provided heat from an equivalent of about twenty-six heat sources. FIG. 149 illusfrates an even larger pattern that may have a greater spacing between production wells 2701.

FIGS. 150, 151, 152, and 153 illustrate embodiments in which both production wells and heat sources are located at the apices of a triangular grid. In FIG. 150, a friangular grid with a spacing of s may have production wells 2701 spaced at a distance of 2s. A hexagonal pattern may include one ring 2730 of six heat sources 2732.

Each heat source 2732 may provide substantially equal amounts of heat to two production wells 2701. Therefore, each ring 2730 of six heat sources 2732 contributes approximately three equivalent heat sources per production well

2701.

FIG. 151 illustrates a pattern of production wells 2701 with inner hexagonal ring 2734 and outer hexagonal ring 2736. Production wells 2701 may be spaced at a distance of 3_J. Heat sources 2732 may be located at apices of hexagonal ring 2734 and hexagonal ring 2736. Hexagonal ring 2734 and hexagonal ring 2736 may include six heat sources each. The pattern in FIG. 151 may result in a ratio of heat sources 2732 to production well

2701 of about eight.

FIG. 152 illusfrates a pattern of production wells 2701 also with two hexagonal rings of heat sources sunounding each production well. Production well 2701 may be sunounded by ring 2738 of six heat sources 2732.

Production wells 2701 may be spaced at a distance of As. Second hexagonal ring 2740 may sunound ring 2738.

Second hexagonal ring 2740 may include twelve heat sources 2732. This pattern may result in a ratio of heat sources 2732 to production wells 2701 that may approach fifteen. FIG. 153 illustrates a pattern of heat sources 2732 with three rings of heat sources 2732 sunounding each production well 2701. Production wells 2701 may be sunounded by ring 2742 of six heat sources 2732. Second ring 2744 of twelve heat sources 2732 may sunound ring 2742. Thfrd ring 2746 of heat sources 2732 may sunound second ring 2744. Third ring 2746 may include 6 equivalent heat sources. This pattern may result in a ratio of heat sources 2732 to production wells 2701 that is about 24:1.

FIGS. 154, 155, 156, and 157 illustrate patterns in which the production well may be disposed at a center of a friangular grid such that the production well may be equidistant from the apices of the friangular grid. In FIG. 154, the friangular grid of heater wells with a spacing of s may include production wells 2760 spaced at a distance of s. Each production well 2760 may be sunounded by ring 2764 of three heat sources 2762. Each heat source 2762 may provide substantially equal amounts of heat to three production wells 2760. Therefore, each ring

2764 of three heat sources 2762 may contribute one equivalent heat source per production well 2760.

FIG. 155 illusfrates a pattern of production wells 2760 with inner friangular ring 2766 and outer hexagonal ring 2768. In this pattern, production wells 2760 may be spaced at a distance of 2s. Heat sources 2762 may be located at apices of inner triangular ring 2766 and outer hexagonal ring 2768. Inner friangular ring 2766 may conttibute three equivalent heat sources per production well 2760. Outer hexagonal ring 2768 containing three heater wells may contribute one equivalent heat source per production well 2760. Thus, a total of four equivalent heat sources may provide heat to production well 2760.

FIG. 156 illusfrates a pattern of production wells with one inner triangular ring of heat sources sunounding each production well and one frregular hexagonal outer ring. Production wells 2760 may be sunounded by ring 2770 of three heat sources 2762. Production wells 2760 may be spaced at a distance of 3s. frregular hexagonal ring 2772 of nine heat sources 2762 may sunound ring 2770. This pattern may result in a ratio of heat sources 2762 to production wells 2760 of about 9:1.

FIG. 157 illusfrates triangular patterns of heat sources with three rings of heat sources sunounding each production well. Production wells 2760 may be sunounded by ring 2774 of three heat sources 2762. frregular hexagon pattern 2776 of nine heat sources 2762 may sunound ring 2774. Third set 2778 of heat sources 2762 may sunound frregular hexagonal pattern 2776. Third set 2778 may contribute four equivalent heat sources to production well 2760. A ratio of equivalent heat sources to production well 2760 may be sixteen.

FIG. 158 depicts an embodiment of a pattern of heat sources 2705 ananged in a triangular pattern. Production well 2701 may be sunounded by triangles 2780, 2782, and 2784 of heat sources 2705. Heat sources 2705 in triangles 2780, 2782, and 2784 may provide heat to the formation. The provided heat may raise an average temperature of the formation to a pyrolysis temperature. Pyrolyzation fluids may flow to production well 2701. Formation fluids may be produced in production well 2701.

FIG. 159 illusfrates an example of a square pattern of heat sources 3000 and production wells 3002. Heat sources 3000 are disposed at vertices of squares 3010. Production well 3002 is placed in a center of every third square in both x- and y-directions. Midlines 3006 are formed equidistant to two production wells 3002, and peφendicular to a line connecting such production wells. Intersections of midlines 3006 at vertices 3008 form unit cell 3012. Heat source 3000a is completely within unit cell 3012. Heat source 3000b and heat source 3000c are only partially within unit cell 3012. Only the one-half fraction of heat source 3000b and the one-quarter fraction of heat source 3000c within unit cell 3012 provide heat within unit cell 3012. The fraction of heat source 3000 outside of unit cell 3012 may provide heat outside of unit cell 3012. The number of heat sources 3000 within one unit cell 3012 is a ratio of heat sources 3000 per production well 3002 within the formation.

The total number of heat sources inside unit cell 3012 may be deteπnined by the following method:

(a) 4 heat sources 3000a inside unit cell 3012 are counted as one heat source each;

(b) 8 heat sources 3000b on midlines 3006 are counted as one-half heat source each; and

(c) 4 heat sources 3000c at vertices 3008 are counted as one-quarter heat source each.

The total number of heat sources is determined from adding the heat sources counted by, (a) 4, (b) 8/2 = 4, and (c) 4/4 - 1, for a total number of 9 heat sources 3000 in unit cell 3012. Therefore, a ratio of heat sources 3000 to production wells 3002 is deteπnined as 9:1 for the pattern illusfrated in FIG. 159.

FIG. 160 illusfrates an example of another pattern of heat sources 3000 and production wells 3002. Midlines 3006 are formed equidistant from two production wells 3002, and peφendicular to a line connecting such production wells. Unit cell 3014 is deteπnined by intersection of midlines 3006 at vertices 3008. Twelve heat sources 3000 are counted in unit cell 3014, of which six are whole sources of heat, and six are one-third sources of heat (with the other two-thirds of heat from such six wells going to other patterns). Thus, a ratio of heat sources 3000 to production wells 3002 is determined as 8: 1 for the pattern illusfrated in FIG. 160.

FIG. 161 illustrates an embodiment oftriangular pattern 3100 of heat sources 3102. FIG. 162 illustrates an embodhnent of square pattern 3101 of heat sources 3103. FIG. 163 illustrates an embodiment of hexagonal pattern 3104 of heat sources 3106. FIG. 164 illustrates an embodiment of 12:1 pattern 3105 of heat sources 3107.

A temperature distribution for all patterns may be deteπnined by an analytical method. The analytical method may be simplified by analyzing only temperature fields within "confined" patterns (e.g., hexagons), i.e., completely sunounded by others. In addition, the temperature field may be estimated to be a supeφosition of analytical solutions conesponding to a single heat source. FIG. 165 illustrates a schematic diagram ofan embodiment ofsurface facilities 2800 that may treat a formation fluid. The formation fluid may be produced though a production well. As shown in FIG. 165, surface facilities 2800 may be coupled to separator 2802. Separator may receive formation fluid produced from a relatively low permeability formation containing heavy hydrocarbons during an in situ conversion process. Separator 2802 may separate the formation fluid into gas sfream 2804, liquid hydrocarbon condensate sfream 2806, and water stream 2808.

Water sfream 2808 may flow from separator 2802 to a portion of a formation, to a containment system, or to a processing unit. For example, water stream 2808 may flow from separator 2802 to an ammonia production unit. Ammonia produced in the ammonia production unit may flow to an ammonium sulfate unit. The ammonium sulfate unit may combine the ammonia with H₂S0₄ or S0₂/S0₃ to produce ammonium sulfate. In addition, ammonia produced in the ammonia production unit may flow to a urea production unit. The urea production unit may combine carbon dioxide with the ammonia to produce urea.

Gas sfream 2804 may flow through a conduit from separator 2802 to gas freatment unit 2810. The gas freatment unit may separate various components of gas sfream 2804. For example, the gas freatment unit may separate gas sfream 2804 into carbon dioxide stream 2812, hydrogen sulfide sfream 2814, hydrogen sfream 2816, and stream 2818 that may include, but is not limited to, methane, ethane, propane, butanes (including n-butane or isobutane), pentane, ethene, propene, butene, pentene, water, or combinations thereof.

The carbon dioxide sfream may flow through a conduit to a formation, to a containment system, to a disposal unit, and/or to another processing unit. In addition, the hydrogen sulfide sfream may also flow through a conduit to a containment system and/or to another processing unit. For example, the hydrogen sulfide sfream may be converted into elemental sulfur in a Claus process unit. The gas freatment unit may separate gas sfream 2804 into stream 2819. Sfream 2819 may include heavier hydrocarbon components from gas stream 2804. Heavier hydrocarbon components may include, for example, hydrocarbons having a carbon number of greater than about 5. Heavier hydrocarbon components in sfream 2819 may be provided to liquid hydrocarbon condensate sfream 2806. Surface facilities 2800 may also include processing unit 2821. Processing unit 2821 may separate sfream

2818 into a number of sfreams. Each of the streams may be rich in a predetermined component or a predetermined number of compounds. For example, processing unit 2821 may separate sfream 2818 into first portion 2820 of sfream 2818, second portion 2823 of sfream 2818, thfrd portion 2825 of sfream 2818, and fourth portion 2831 of sfream 2818. First portion 2820 of sfream 2818 may include lighter hydrocarbon components such as methane and ethane. First portion 2820 of sfream 2818 may flow from gas freatment unit 2810 to power generation unit 2822.

Power generation unit 2822 may extract useable energy from the first portion of stream 2818. For example, sfream 2818 may be produced under pressure. Power generation unit 2822 may include a turbine that generates elecfricity from the first portion of sfream 2818. The power generation unit may also include, for example, a molten carbonate fuel cell, a solid oxide fuel cell, or other type of fuel cell. The extracted useable energy may be provided to user 2824. User 2824 may include, for example, surface facilities 2800, a heat source disposed within a formation, and/or a consumer of useable energy.

Second portion 2823 of sfream 2818 may also include light hydrocarbon components. For example, second portion 2823 of sfream 2818 may include, but is not limited to, methane and ethane. Second portion 2823 of sfream 2818 may be provided to natural gas pipeline 2827. Alternatively, second portion 2823 of sfream 2818 may be provided to a local market. The local market may be a consumer market or a commercial market. Second portion 2823 of sfream 2818 may be used as an end product or an intermediate product depending on, for example, a composition of the light hydrocarbon components.

Third portion 2825 of sfream 2818 may include liquefied petroleum gas ("LPG"). Major constituents of LPG may include hydrocarbons containing three or four carbon atoms such as propane and butane. Butane may include n-butane or isobutane. LPG may also include relatively small concenfrations of other hydrocarbons, such as ethene, propene, butene, and pentene. Some LPG may also include additional components. LPG may be a gas at atmospheric pressure and normal ambient temperatures. LPG may be liquefied, however, when moderate pressure is applied or when the temperature is sufficiently reduced. When such moderate pressure is released, LPG gas may have about 250 times a volume of LPG liquid. Therefore, large amounts of energy may be stored and transported compactly as LPG.

Third portion 2825 of sfream 2818 may be provided to local market 2829. The local market may include a consumer market or a commercial market. Third portion 2825 of stream 2818 may be used as an end product or an inteπnediate product. LPG may be used in applications, such as food processing, aerosol propellants, and automotive fuel. LPG may be provided in for standard heating and cooking puφoses as commercial propane and/or commercial butane. Propane may be more versatile for general use than butane because propane has a lower boiling point than butane. Fourth portion 2831 of stream 2818 may flow from the gas treatment unit to hydrogen manufacturing unit 2828. Hydrogen-rich stream 2830 is shown exiting hydrogen manufacturing unit 2828. Examples of hydrogen manufacturing unit 2828 may include a steam reformer and a catalytic flameless disfributed combustor with a hydrogen separation membrane. FIG. 166 illusfrates an embodhnent of a catalytic flameless disfributed combustor. An example of a catalytic flameless distributed combustor with a hydrogen separation membrane is illustrated in U.S. Patent Application No. 60/273,354, filed on March 5, 2001, which is incoφorated by reference as if fully set forth herein. A catalytic flameless disfributed combustor may include fuel line 2850, oxidant line 2852, catalyst 2854, and membrane 2856. Fourth portion 2831 of sfream 2818 (shown in FIG. 165) may be provided to hydrogen manufacturing unit 2828 as fuel 2858. Fuel 2858 within fuel line 2850 may mix within reaction volume in annular space 2859 between the fuel line and the oxidant line. Reaction of the fuel with the oxidant in the presence of catalyst 2854 may produce reaction products that include H₂. Membrane 2856 may allow a portion of the generated H₂ to pass into annular space 2860 between outer wall 2862 of oxidant line 2852 and membrane 2856. Excess fuel passing out of fuel line 2850 may be circulated back to enfrance of hydrogen manufacturing unit 2828. Combustion products leaving oxidant line 2852 may include carbon dioxide and other reactions products as well as some fuel and oxidant. The fuel and oxidant may be separated and recirculated back to the hydrogen manufacturing unit. Carbon dioxide may be separated from the exit sfream. The carbon dioxide may be sequestered within a portion of a formation or used for an alternate piupose.

Fuel line 2850 may be concentrically positioned within oxidant line 2852. Critical flow orifices 2863 within fuel line 2850 may allow fuel to enter into a reaction volume in annular space 2859 between the fuel line and oxidant line 2852. The fuel line may carry a mixture of water and Vaporized hydrocarbons such as, but not limited to, methane, ethane, propane, butane, methanol, ethanol, or combinations thereof. The oxidant line may carry an oxidant such as, but not limited to, air, oxygen enriched air, oxygen, hydrogen peroxide, or combinations thereof. Catalyst 2854 may be located in the reaction volume to allow reactions that produce H₂ to proceed at relatively low temperatures. Without a catalyst and without membrane separation of H₂, a steam reformation reaction may need to be conducted in a series of reactors with temperatures for a shift reaction occuning in excess of 980 °C. With a catalyst and with separation of H₂ from the reaction sfream, the reaction may occur at temperatures within a range from about 300 °C to about 600 °C, or within a range from about 400 °C to about 500 °C. Catalyst 2854 may be any steam reforming catalyst. In selected embodiments, catalyst 2854 is a group VIII fransition metal, such as nickel. The catalyst may be supported on porous substrate 2864. The substrate may include group III or group IV elements, such as, but not limited to, aluminum, silicon, titanium, or zirconium. In an embodiment, the substrate is alumina (A1₂0₃).

Membrane 2856 may remove H₂ from a reaction stream within a reaction volume of a hydrogen manufacturing unit 2828. When H₂ is removed from the reaction sfream, reactions within the reaction volume may generate additional H₂. A vacuum may draw H₂ from an annular region between membrane 2856 and outer wall

2862 of oxidant line 2852. Alternately, H₂ may be removed from the annular region in a canier gas. Membrane 2856 may separate H₂ from other components within the reaction stream. The other components may include, but are not limited to, reaction products, fuel, water, and hydrogen sulfide. The membrane may be a hydrogen- permeable and hydrogen selective material such as, but not limited to, a ceramic, carbon, metal, or combination thereof. The membrane may include, but is not limited to, metals of group VIII, V, in, or I such as palladium, platinum, nickel, silver, tantalum, vanadium, yttrium, and/or niobium. The membrane may be supported on a porous substrate such as alumina. The support may separate the membrane 2856 from catalyst 2854. The separation distance and insulation properties of the support may help to maintain the membrane within a desfred temperature range.

Hydrogen manufacturing unit 2828 of the surface facilities embodiment depicted in FIG. 165 may produce hydrogen-rich stream 2830 from the second portion sfream 2818. Hydrogen-rich sfream 2830 may flow into hydrogen stream 2816 to form stream 2832. Sfream 2832 may include a larger volume of hydrogen than either hydrogen-rich sfream 2830 or hydrogen sfream 2816.

Hydrocarbon condensate stream 2806 may flow through a conduit from wellhead 2803 to hydrotreating unit 2834. Hydrofreating unit 2834 may hydrogenate hydrocarbon condensate sfream 2806 to form hydrogenated hydrocarbon condensate sfream 2836. The hydrofreater may upgrade and swell the hydrocarbon condensate.

Surface facilities 2800 may provide sfream 2832 (which includes a relatively high concenfration of hydrogen) to hydrofreating unit 2834. H₂ in sfream 2832 may hydrogenate a double bond of the hydrocarbon condensate, thereby reducing a potential for polymerization of the hydrocarbon condensate. In addition, hydrogen may also neutralize radicals in the hydrocarbon condensate. The hydrogenated hydrocarbon condensate may include relatively short chain hydrocarbon fluids. Furthermore, hydrofreating unit 2834 may reduce sulfur, nifrogen, and aromatic hydrocarbons in hydrocarbon condensate sfream 2806. Hydrofreating unit 2834 may be a deep hydrotreating unit or a mild hydrofreating unit. An appropriate hydrotreating unit may vary depending on, for example, a composition of sfream 2832, a composition of the hydrocarbon condensate sfream, and/or a selected composition of the hydrogenated hydrocarbon condensate sfream. Hydrogenated hydrocarbon condensate sfream 2836 may flow from hydrotreating unit 2834 to transportation unit 2838. Transportation unit 2838 may collect a volume of the hydrogenated hydrocarbon condensate and/or to fransport the hydrogenated hydrocarbon condensate to market center 2840. Market center 2840 may include, but is not limited to, a consumer markeφlace or a commercial marketplace. A commercial marketplace may include a refinery. The hydrogenated hydrocarbon condensate may be used as an end product or an intermediate product.

Alternatively, hydrogenated hydrocarbon condensate stream 2836 may flow to a splitter or an ethene production unit. The splitter may separate the hydrogenated hydrocarbon condensate stream into a hydrocarbon sfream including components having carbon numbers of 5 or 6, a naphtha sfream, a kerosene stream, and/or a diesel sfream. Selected sfreams exiting the splitter may be fed to the ethene production unit. In addition, the hydrocarbon condensate stream and the hydrogenated hydrocarbon condensate stream may be fed to the ethene production unit.

Ethene produced by the ethene production unit may be fed to a petrochemical complex to produce base and industrial chemicals and polymers. Alternatively, the sfreams exiting the splitter may be fed to a hydrogen conversion unit. A recycle stream may flow from the hydrogen conversion unit to the splitter. The hydrocarbon sfream exiting the splitter and the naphtha sfream may be fed to a mogas production unit. The kerosene sfream and the diesel sfream may be distributed as product.

FIG. 167 illusfrates an embodiment of an additional processing unit that may be included in surface facilities 2800, such as the facilities depicted in FIG. 165. Afr 2903 may be fed to air separation unit 2900. Air separation unit 2900 may generate nitrogen stream 2902 and oxygen sfream 2905. Oxygen sfream 2905 and steam 2904 may be injected into exhausted coal resource 2906 to generate synthesis gas 2907. Produced synthesis gas 2907 may be provided to Shell Middle Distillates process unit 2910 that produces middle distillates 2912. In addition, produced synthesis gas 2907 may be provided to catalytic methanation process unit 2914 that produces natural gas 2916. Produced synthesis gas 2907 may also be provided to methanol production unit 2918 to produce methanol 2920. Produced synthesis gas 2907 may be provided to process unit 2922 for production of ammonia and or urea 2924. Synthesis gas may be used as a fuel for fuel cell 2926 that produces elecfricity 2928. Synthesis gas 2907 may also be routed to power generation unit 2930, such as a turbine or combustor, to produce elecfricity

2932.

The comparisons of patterns of heat sources were evaluated for the same heater well density and the same heating input regime. For example, a number of heat sources per unit area in a friangular pattern is the same as the number of heat sources per unit area in the 10 m hexagonal pattern if the space between heat sources is increased to about 12.2 m in the triangular pattern. The equivalent spacing for a square pattern would be 11.3 m, while the equivalent spacing for a 12:1 pattern would be 15J m.

FIG. 168 illusfrates temperature proflle 3110 after three years of heating for a triangular pattern with a 12.2 m spacing. FIG. 161 depicts an embodhnent of a triangular pattern. Temperature profile 3110 is a three- dimensional plot of temperature versus a location within a friangular pattern. FIG. 169 illusfrates temperature profile 3108 after three years of heating for a square pattern with 11.3 m spacing. Temperature profile 3108 is a three-dimensional plot of temperature versus a location within a square pattern. FIG. 162 depicts an embodiment of a square pattern. FIG. 170 illustrates temperature profile 3109 after three years of heating for a hexagonal pattern with 10.0 m spacing. Temperature profile 3109 is a three-dimensional plot of temperature versus a location within a hexagonal pattern. FIG. 163 depicts an embodiment of a hexagonal pattern. As shown in a comparison of FIGS. 168, 169, and 170, a temperature proflle of the friangular pattern is more uniform than a temperature profile of the square or hexagonal pattern. For example, a minimum temperature of the square pattern is approximately 280 °C, and a minimum temperature of the hexagonal pattern is approximately 250 °C. In confrast, a minimum temperature of the friangular pattern is approximately 300 °C. Therefore, a temperature variation within the friangular pattern after 3 years of heating is 20 °C less than a temperature variation within the square pattern and 50 °C less than a temperature variation within the hexagonal pattern. For a chemical process, where reaction rate is proportional to an exponent of temperature, a 20 °C difference may have a substantial effect on products being produced in a pyrolysis zone.

FIG. 171 illusfrates a comparison plot between the average pattern temperature (in degrees Celsius) and temperatures at the coldest spots for each pattern as a function of time (in years). The coldest spot for each pattern is located at a pattern center (centroid). As shown in FIG. 161 , the coldest spot of a friangular pattern is point

3118, while point 3117 is the coldest spot of a square pattern, as shown in FIG. 162. As shown in FIG. 163, the coldest spot of a hexagonal pattern is point 3114, while point 3115 is the coldest spot of a 12: 1 pattern, as shown in FIG. 164. The difference between an average pattern temperature and temperature of the coldest spot represents how unifoπn the temperature disfribution for a given pattern is. The more uniform the heating, the better the product quality that may be made in the formation. The larger the volume fraction of resource that is overheated, the greater the amount of undesirable product tends to be made.

As shown in FIG. 171 , the difference between average temperature 3120 of a pattern and temperature of the coldest spot is less for friangular pattern 3118 than for square pattern 3117, hexagonal pattern 3114, or 12:1 pattern 3115. Again, there is a substantial difference between triangular and hexagonal patterns. Another way to assess the uniformity of temperature disfribution is to compare temperatures of the coldest spot of a pattern with a point located at the center of a side of a pattern midway between heaters. As shown in FIG. 163, point 3112 is located at the center of a side of the hexagonal pattern midway between heaters. As shown in FIG. 161, point 3116 is located at the center of a side of a friangular pattern midway between heaters. Point 3119 is located at the center of a side of the square pattern midway between heaters, as shown in FIG. 162.

FIG. 172 illusfrates a comparison plot between average pattern temperature 3120 (in degrees Celsius), temperatures at coldest spot 3118 for friangular patterns, coldest spot 3114 for hexagonal patterns, point 3116 located at the center of a side of friangular pattern midway between heaters, and point 3112 located at the center of a side of hexagonal pattern midway between heaters, as a function of time (in years). FIG. 173 illusfrates a comparison plot between average pattern temperature 3120 (in degrees Celsius), temperatures at coldest spot 3117 and point 3119 located at the center of a side of a pattern midway between heaters, as a function of time (in years), for a square pattern.

As shown in a comparison of FIGS. 172 and 173, for each pattern, a temperature at a center of a side midway between heaters is higher than a temperature at a center of the pattern. A difference between a temperature at a center of a side midway between heaters and a center of the hexagonal pattern increases substantially during the first year of heating, and stays relatively constant afterward. A difference between a temperature at an outer lateral boundary and a center of the friangular pattern, however, is negligible. Therefore, a temperature disfribution in a triangular pattern is more uniform than a temperature disfribution in a hexagonal pattern. A square pattern also provides more uniform temperature distribution than a hexagonal pattern, however, it is still less uniform than a temperature disfribution in a triangular pattern.

A triangular pattern of heat sources may have, for example, a shorter total process time than a square, hexagonal, or 12: 1 pattern of heat sources for the same heater well density. A total process time may include a time required for an average temperature of a heated portion of a formation to reach a target temperature and a time required for a temperature at a coldest spot within the heated portion to reach the target temperature. For example, heat may be provided to the portion of the formation until an average temperature of the heated portion reaches the target temperature. After the average temperature of the heated portion reaches the target temperature, an energy supply to the heat sources may be reduced such that less or minimal heat may be provided to the heated portion. An example of a target temperature may be approximately 340 °C. The target temperature, however, may vary depending on, for example, foπnation composition and/or foπnation conditions such as pressure. FIG. 174 illustrates a comparison plot between the average pattern temperature and temperatures at the coldest spots for each pattern, as a function of time when heaters are turned off after the average temperature reaches a target value. As shown in FIG. 174, average temperature 3120 of the foπnation reaches a target temperature (about 340 °C) in approximately 3 years. As shown in FIG. 174, a temperature at the coldest point within the triangular pattern 3118 reaches the target temperature (about 340 °C) about 0.8 years later. A total process time for such a friangular pattern is about 3.8 years when the heat input is discontinued when the target average temperature is reached. As shown in FIG. 174, a temperature at the coldest point within the triangular pattern reaches the target temperature (about 340 °C) before a temperature at coldest point within the square pattern 3117 or a temperature at the coldest point within the hexagonal pattern 3114 reaches the target temperature. A temperature at the coldest point within the hexagonal pattern, however, reaches the target temperature after an additional time of about 2 years when the heaters are turned off upon reaching the target average temperature. Therefore, a total process time for a hexagonal pattern is about 5.0 years. A total process time for heating a portion of a formation with a triangular pattern is 1.2 years less (approximately 25% less) than a total process time for heating a portion of a formation with a hexagonal pattern. In an embodiment, the power to the heaters may be reduced or turned off when the average temperature of the pattern reaches a target level. This prevents overheating the resource, which wastes energy and produces lower product quality. The triangular pattern has the most unifoπn temperatures and the least overheating. Although a capital cost of such a triangular pattern may be approximately the same as a capital cost of the hexagonal pattern, the friangular pattern may accelerate oil production and requfre a shorter total process time. A friangular pattern may be more economical than a hexagonal pattern. A spacing of heat sources in a triangular pattern that will have about the same process time as a hexagonal pattern having about a 10.0 m space between heat sources may be equal to approximately 14.3 m. The friangular pattern may include about 26% less heat sources than the equivalent hexagonal pattern. Using the friangular pattern may allow for lower capital cost (i.e., there are fewer heat sources and production wells) and lower operating costs (i.e., there are fewer heat sources and production wells to power and operate).

FIG. 58 depicts an embodiment of a natural disfributed combustor. In one experiment, the embodiment schematically shown in FIG. 58 was used to heat high volatile bituminous C coal in situ. A portion of a formation was heated with elecfrical resistance heaters and/or a natural disfributed combustor. Thermocouples were located every 2 feet along the length of the natural disfributed combustor (along conduit 532 schematically shown in FIG. 58). The coal was first heated with electrical resistance heaters until pyrolysis was complete near the well. FIG.

175 depicts square data points measured during electrical resistance heating at various depths in the coal after the temperature proflle had stabilized (the coal seam was about 16 feet thick starting at about 28 feet of depth). At this point heat energy was being supplied at about 300 watts per foot. Air was subsequently injected via conduit 532 at gradually increasing rates, and elecfric power supplied to the elecfrical resistance heaters was decreased. Combustion products were removed from the reaction volume through an annular space between conduit 532 and a well casing. The power supplied to the elecfrical resistance heaters was decreased at a rate that would approximately offset heating provided by the combustion of the coal adjacent to conduit 532. Ah input was increased and power input was decreased over a period of about 2 hours until no elecfric power was being supplied. Diamond data points of FIG. 175 depict temperature as a function of depth for natural disfributed combustion heating (without any elecfrical resistance heating) in the coal after the temperature profile had substantially stabilized. As can be seen in FIG. 175, the natural distributed combustion heating provided a temperature proflle that is comparable to the elecfrical resistance temperature profile (represented by square data points). This experiment demonstrated that natural disfributed combustors may provide formation heating that is comparable to the formation heating provided by electrical resistance heaters. This experiment was repeated at different temperatures and in two other wells, all with similar results.

Numerical calculations have been made for a natural distributed combustor system that configure to heat a relatively low peπneability formation containing heavy hydrocarbons. A commercially available program called PRO-II (Simulation Sciences Inc., Brea, California) was used to make example calculations based on a conduit of diameter 6.03 cm with a wall thickness of 0.39 cm. The conduit was disposed in an opening in the formation with a diameter of 14.4 cm. The conduit had critical flow orifices of 1.27 mm diameter spaced 183 cm apart. The conduit heated a formation of 91.4 m thickness. A flow rate of air was 1.70 standard cubic meters per minute through the critical flow orifices. Pressure of air at the inlet of the conduit was 7 bars absolute. Exhaust gases had a pressure of 3.3 bars absolute. A heating output of 1066 watts per meter was used. A temperature in the opening was set at 760 °C. The calculations determined a minimal pressure drop within the conduit of about 0.023 bars. The pressure drop within the opening was less than 0.0013 bars.

FIG. 176 illustrates extension (in meters) of a reaction zone within a coal formation over time (in years) according to the parameters set in the calculations. The width of the reaction zone increases with time due to oxidation of carbon adjacent to the conduit.

Numerical calculations have been made for heat transfer using a conductor-in-conduit heater. Calculations were made for a conductor having a diameter of about 1 inch (2.54 cm) disposed in a conduit having a diameter of about 3 inches (7.62 cm). The conductor-in-conduit heater was disposed in an opening of a carbon containing formation having a diameter of about 6 inches (15.24 cm). An emissivity of the carbon containing formation was maintained at a value of 0.9, which is expected for geological materials. The conductor and the conduit were given alternate emissivity values of high emissivity (0.86), which is common for oxidized metal surfaces, and low emissivity (0.1), which is for polished and/or un-oxidized metal surfaces. The conduit was filled with either afr or helium. Helium is known to be a more thermally conductive gas than afr. The space between the conduit and the opening was filled with a gas mixture of methane, carbon dioxide, and hydrogen gases. Two different gas mixtures were used. The first gas mixture had mole fractions of 0.5 for methane, 0.3 for carbon dioxide, and 0.2 for hydrogen. The second gas mixture had mole fractions of 0.2 for methane, 0.2 for carbon dioxide, and 0.6 for hydrogen.

FIG. 177 illustrates a calculated ratio of conductive heat fransfer to radiative heat transfer versus a temperature of a face of the relatively low permeability formation containing heavy hydrocarbons in the opening for an air filled conduit. The temperature of the conduit was increased linearly from 93 °C to 871 °C. The ratio of conductive to radiative heat fransfer was calculated based on emissivity values, thermal conductivities, d nensions of the conductor, conduit, and opening, and the temperature of the conduit. Line 3204 is calculated for the low emissivity value (0.1). Line 3206 is calculated for the high emissivity value (0.86). A lower emissivity for the conductor and the conduit provides for a higher ratio of conductive to radiative heat fransfer to the formation. The decrease in the ratio with an increase in temperature may be due to a reduction of conductive heat fransfer with increasing temperature. As the temperature on the face of the formation increases, a temperature difference between the face and the heater is reduced, thus reducing a temperature gradient that drives conductive heat fransfer.

FIG. 178 illustrates a calculated ratio of conductive heat transfer to radiative heat transfer versus a temperature at a face of the carbon containing formation in the opening for a helium filled conduit. The temperature of the conduit was increased linearly from 93 °C to 871 °C. The ratio of conductive to radiative heat fransfer was calculated based on emissivity values; theπnal conductivities; dimensions of the conductor, conduit, and opening; and the temperature of the conduit. Line 3208 is calculated for the low emissivity value (0.1). Line 3210 is calculated for the high emissivity value (0.86). A lower emissivity for the conductor and the conduit again provides for a higher ratio of conductive to radiative heat fransfer to the formation. The use of helium instead of afr in the conduit significantly increases the ratio of conductive heat fransfer to radiative heat transfer. This may be due to a thermal conductivity of helium being about 5.2 to about 5.3 times greater than a theπnal conductivity of air. FIG. 179 illusfrates temperatures of the conductor, the conduit, and the opening versus a temperature at a face of the carbon containing formation for a helium filled conduit and a high emissivity of 0.86. The opening has a gas mixture equivalent to the second mixture described above having a hydrogen mole fraction of 0.6. Opening temperature 3216 was linearly increased from 93 °C to 871 °C. Opening temperature 3216 was assumed to be the same as the temperature at the face of the carbon containing formation. Conductor temperature 3212 and conduit temperature 3214 were calculated from opening temperature 3216 using the dimensions of the conductor, conduit, and opening, values of emissivities for the conductor, conduit, and face, and thermal conductivities for gases (helium, methane, carbon dioxide, and hydrogen). It may be seen from the plots of temperatures of the conductor, conduit, and opening for the conduit filled with helium, that at higher temperatures approaching 871 °C, the temperatures of the conductor, conduit, and opening begin to equilibrate.

FIG. 180 illusfrates temperatures of the conductor, the conduit, and the opening versus a temperature at a face of the carbon containing formation for an air filled conduit and a high emissivity of 0.86. The opening has a gas mixture equivalent to the second mixture described above having a hydrogen mole fraction of 0.6. Opening temperature 3216 was linearly increased from 93 °C to 871 °C. Opening temperature 3216 was assumed to be the same as the temperature at the face of the carbon containing formation. Conductor temperature 3212 and conduit temperature 3214 were calculated from opening temperature 3216 using the dimensions of the conductor, conduit, and opening, values of emissivities for the conductor, conduit, and face, and thermal conductivities for gases (air, methane, carbon dioxide, and hydrogen). It may be seen from the plots of temperatures of the conductor, conduit, and opening for the conduit filled with air, that at higher temperatures approaching 871 °C, the temperatures of the conductor, conduit, and opening begin to equilibrate, as seen for the helium filled conduit with high emissivity.

FIG. 181 illustrates temperatures of the conductor, the conduit, and the opening versus a temperature at a face of the carbon containing formation for a helium filled conduit and a low emissivity of 0.1. The opening has a gas mixture equivalent to the second mixture described above having a hydrogen mole fraction of 0.6. Opening temperature 3216 was linearly increased from 93 °C to 871 °C. Opening temperature 3216 was assumed to be the same as the temperature at the face of the carbon containing formation. Conductor temperature 3212 and conduit temperature 3214 were calculated from opening temperature 3216 using the dimensions of the conductor, conduit, and opening, values of emissivities for the conductor, conduit, and face, and thermal conductivities for gases (helium, methane, carbon dioxide, and hydrogen). It may be seen from the plots of temperatures of the conductor, conduit, and opening for the conduit filled with helium, that at higher temperatures approaching 871 °C, the temperatures of the conductor, conduit, and opening do not begin to equilibrate as seen for the high emissivity example shown in FIG. 179. In addition, higher temperatures in the conductor and the conduit are needed to achieve an opening and face temperature of 871°C. Thus, increasing an emissivity of the conductor and the conduit may be advantageous in reducing operating temperatures needed to produce a desired temperature in a carbon containing formation. Such reduced operating temperatures may allow for the use of less expensive alloys for metallic conduits.

FIG. 182 illustrates temperatures of the conductor, the conduit, and the opening versus a temperature at a face of the carbon containing formation for an afr filled conduit and a low emissivity of 0.1. The opening has a gas mixture equivalent to the second mixture described above having a hydrogen mole fraction of 0.6. Opening temperature 3216 was linearly increased from 93 °C to 871 °C. Opening temperature 3216 was assumed to be the same as the temperature at the face of the carbon containing formation. Conductor temperature 3212 and conduit temperature 3214 were calculated from opening temperature 3216 using the dimensions of the conductor, conduit, and opening, values of emissivities for the conductor, conduit, and face, and thermal conductivities for gases (afr, methane, carbon dioxide, and hydrogen). It may be seen from the plots of temperatures of the conductor, conduit, and opening for the conduit filled with helium, that at higher temperatures approaching 871 °C, the temperatures of the conductor, conduit, and opening do not begin to equilibrate as seen for the high emissivity example shown in

FIG. 180. In addition, higher temperatures in the conductor and the conduit are needed to achieve an opening and face temperature of 871°C. Thus, increasing an emissivity of the conductor and the conduit may be advantageous in reducing operating temperatures needed to produce a desired temperature in a carbon containing formation. Such reduced operating temperatures may provide for a lesser metallurgical cost associated with materials that require less substantial temperature resistance (e.g., a lower melting point).

Calculations were also made using the first mixture of gas having a hydrogen mole fraction of 0.2. The calculations resulted in substantially similar results to those for a hydrogen mole fraction of 0.6.

Formation pressure may also have a significant effect on olefin production. A high formation pressure may result in the production of small quantities of olefins. High pressure within a formation may result in a high H₂ partial pressure within the formation. The high H₂ partial pressure may result in hydrogenation of the fluid within the formation. Hydrogenation may result in a reduction of olefins in a fluid produced from the formation. A high pressure and high H₂ partial pressure may also result in inhibition of aromatization of hydrocarbons within the formation. Aromatization may include formation of aromatic and cyclic compounds from alkanes and/or alkenes within a hydrocarbon mixture. If it is desirable to increase production of olefins from a foπnation, the olefin content of fluid produced from the formation may be increased by reducing pressure within the formation. The pressure may be reduced by drawing off a larger quantity of formation fluid from a portion of the formation that is being produced. In some in situ conversion process embodiments, pressure within a formation adjacent to production wells may be reduced below atmospheric pressure (i.e., a vacuum may be drawn on the formation).

It is believed that increases in the concenfration (and partial pressure) of hydrogen during pyrolysis causes the olefin concenfration to decrease in the fluids produced from pyrolysis.

The amount of useable energy contained in the produced synthesis gas is generally less than that contained in the pyrolysis fluids. Therefore, synthesis gas production is generally less energy efficient than pyrolysis. There are two reasons for this result. First, the two H₂ molecules produced in the synthesis gas reaction have a lower energy content than low carbon number hydrocarbons produced in pyrolysis. Second, endothermic synthesis gas reactions consume energy.

FIG. 183 is a plot of calculated equilibrium gas dry mole fractions for a coal reaction with water. Methane reactions are not included. The fractions are representative of a synthesis gas produced from a relatively low permeability formation containing heavy hydrocarbons and has been passed through a condenser to remove water from the produced gas. Equilibrium gas dry mole fractions are shown in FIG. 183 for H₂4000, carbon monoxide 4002, and carbon dioxide 4004 as a function of temperature at a pressure of 2 bars absolute. Liquid production from a formation substantially stops at temperatures of about 3 0 °C. Gas produced at about 390 °C includes about 67% H₂ and about 33% carbon dioxide. Carbon monoxide is present in negligible quantities below about 410 °C. At temperatures of about 500 °C, however, carbon monoxide is present in the produced gas in measurable quantities. For example, at 500 °C, about 66.5% H₂, about 32% carbon dioxide, and about 2.5% carbon monoxide are present. At 700 °C, the produced gas includes about 57.5% H₂, about 15.5% carbon dioxide, and about 27% carbon monoxide. FIG. 184 is a plot of calculated equilibrium wet mole fractions for a coal reaction with water. Methane reactions are not included. Equilibrium wet mole fractions are shown for water 4006, H₂4008, carbon monoxide 4010, and carbon dioxide 4012 as a function of temperature at a pressure of 2 bars absolute. At 390 °C, the produced gas includes about 89% water, about 7% H₂₎ and about 4% carbon dioxide. At 500 °C, the produced gas includes about 66% water, about 22% H₂, about 11% carbon dioxide, and about 1% carbon monoxide. At 700 °C, the produced gas includes about 18% water, about 47.5% H₂, about 12% carbon dioxide, and about 22.5% carbon monoxide.

FIG. 183 and FIG. 184 illustrate that at the lower end of the temperature range at which synthesis gas may be produced (i.e., about 400 °C), equilibrium gas phase fractions may not favor production of H₂ within and from a formation. As temperature increases, the equilibrium gas phase fractions increasingly favor the production of H₂.

For example, as shown in FIG. 184, the gas phase equilibrium wet mole fraction of H₂ increases from about 9% at 400 °C to about 39% at 610 °C and reaches 50% at about 800 °C. FIG. 183 and FIG. 184 further illustrate that at temperatures greater than about 660 °C, equilibrium gas phase fractions tend to favor production of carbon monoxide over carbon dioxide. FIG. 183 and FIG. 184 illustrate that as the temperature increases from between about 400 °C to about

1000 °C, the H₂ to carbon monoxide ratio of produced synthesis gas may continuously decrease throughout this range. For example, as shown in FIG. 184, the equilibrium gas phase H₂ to carbon monoxide ratio at 500 °C, 660 °C, and 1000 °C is about 22: 1 , about 3:1, and about 1:1, respectively. FIG. 184 also indicates that produced synthesis gas at lower temperatures may have a larger quantity of water and carbon dioxide than at higher temperatures. As the temperature increases, the overall percentage of carbon monoxide and hydrogen within the synthesis gas may increase.

TABLE 11 is an overview of the potential production volume of applications of synthesis gas produced by wet oxidation. The estimates are based on 56.6 million standard cubic meters of synthesis gas produced per day at 700 °C. TABLE 11

Carbon dioxide produced from a formation may be stored in coal that has been pyrolyzed. FIG. 185 is a plot of the cumulative adsorbed methane and carbon dioxide in cubic meters per metric ton versus pressure in bars absolute at 25 °C on coal. The coal sample is sub-bituminous coal from Gillette, Wyoming. Data sets 4402, 4403,

4404, and 4405 are for carbon dioxide adsoφtion on a post freatment coal sample that has been pyrolyzed and has undergone synthesis gas generation. Data set 4406 is for adsoφtion on an unpyrolyzed coal sample from the same formation. Data set 4401 is adsoφtion of methane at 25 °C. Data sets 4402, 4403, 4404, and 4405 are adsoφtion of carbon dioxide at 25 °C, 50 °C, 100 °C, and 150 °C, respectively. Data set 4406 is adsoφtion of carbon dioxide at 25 °C on the unpyrolyzed coal sample. FIG. 185 shows that carbon dioxide at temperatures between 25 °C and 100 °C is more strongly adsorbed than methane at 25 °C in the pyrolyzed coal. FIG. 185 demonsfrates that a carbon dioxide sfream passed through post freatment coal tends to displace methane from the post freatment coal.

Computer simulations have demonstrated that carbon dioxide may be sequestered in both a deep coal formation and a post freatment coal formation. The Comet2™ Simulator (Advanced Resources International, Houston, TX) determined the amount of carbon dioxide that could be sequestered in a San Juan Basin type deep coal foπnation and a post freatment coal formation. The simulator also determined the amount of methane produced from the San Juan Basin type deep coal formation due to carbon dioxide injection. The model employed for both the deep coal foπnation and the post treatment coal fonnation was a 1.3 km² area, with a repeating 5 spot well pattern. The 5 spot well pattern included four injection wells ananged in a square and one production well at the center of the square. The properties of the San Juan Basin and the post freatment coal formations are shown in TABLE 12. Additional details of simulations of carbon dioxide sequesfration in deep coal formations and comparisons with field test results may be found in Pilot Test Demonstrates How Carbon Dioxide Enhances Coal Bed Methane Recovery, Lanny Schoeling and Michael McGovem, Petroleum Technology Digest, Sept. 2000, p. 14- 15.

TABLE 12

The simulation model accounts for the matrix and dual porosity nature of coal and post treatment coal. For example, coal and post treatment coal are composed of matrix blocks. The spaces between the blocks are called

"cleats." Cleat porosity is a measure of available space for flow of fluids in the formation. The relative permeabilities of gases and water within the cleats required for the simulation were derived from field data from the San Juan coal. The same values for relative permeabilities were used in the post freatment coal formation simulations. Carbon dioxide and methane were assumed to have the same relative permeability. The cleat system of the deep coal formation was modeled as initially saturated with water. Relative permeability data for carbon dioxide and water demonsfrate that high water saturation inhibits absoφtion of carbon dioxide within cleats. Therefore, water is removed from the formation before injecting carbon dioxide into the formation.

In addition, the gases within the cleats may adsorb in the coal matrix. The matrix porosity is a measure of the space available for fluids to adsorb in the matrix. The matrix porosity and surface area were taken into account with experimental mass fransfer and isotherm adsoφtion data for coal and post freatment coal. Therefore, it was not necessary to specify a value of the matrix porosity and surface area in the model. The pressure-volume- temperature (PVT) properties and viscosity required for the model were taken from literature data for the pure component gases.

The preferential adsoφtion of carbon dioxide over methane on post freatment coal was incoφorated into the model based on experimental adsoφtion data. For example, FIG. 185 demonsfrates that carbon dioxide has a significantly higher cumulative adsoφtion than methane over an entire range of pressures at a specified temperature. Once the carbon dioxide enters in the cleat system, methane diffuses out of and desorbs off the mafrix. Similarly, carbon dioxide diffuses into and adsorbs onto the mafrix. In addition, FIG. 185 also shows carbon dioxide may have a higher cumulative adsoφtion on a pyrolyzed coal sample than an unpyrolyzed coal sample. The simulation modeled a sequesfration process over a time period of about 3700 days for the deep coal formation model. Removal of the water in the coal formation was simulated by production from five wells. The production rate of water was about 40 m³/day for about the first 370 days. The production rate of water decreased significantly after the ffrst 370 days. It continued to decrease through the remainder of the simulation run to about zero at the end. Carbon dioxide injection was started at approximately 370 days at a flow rate of about 113,000 standard (in this context "standard" means 1 atmosphere pressure and 15.5 °C) m³/day. The injection rate of carbon dioxide was doubled to about 226,000 standard m³/day at approximately 1440 days. The injection rate remained at about 226,000 standard mVday until the end of the simulation run.

FIG. 186 illusfrates the pressure at the wellhead of the injection wells as a function of time during the simulation. The pressure decreased from about 114 bars absolute to about 19 bars absolute over the first 370 days. The decrease in the pressure was due to removal of water from the coal formation. Pressure then started to increase substantially as carbon dioxide injection started at 370 days. The pressure reached a maximum of about 98 bars absolute. The pressure then began to gradually decrease after 480 days. At about 1440 days, the pressure increased again to about 98 bars absolute due to the increase in the carbon dioxide injection rate. The pressure gradually increased until about 3640 days. The pressure jumped at about 3640 days because the production well was closed off. FIG. 187 illustrates the production rate of carbon dioxide 5060 and methane 5070 as a function of time in the simulation. FIG. 187 shows that carbon dioxide was produced at a rate between about 0-10,000 m³/day during approximately the first 2400 days. The production rate of carbon dioxide was significantly below the injection rate. Therefore, the simulation predicts that most of the injected carbon dioxide is being sequestered in the coal foπnation. However, at about 2400 days, the production rate of carbon dioxide started to rise significantly due to onset of saturation of the coal formation.

In addition, FIG. 187 shows that methane was desorbing as carbon dioxide was adsorbing in the coal formation. Between about 370-2400 days, the methane production rate 5070 increased from about 60,000 to about 115,000 standard m³/day. The increase in the methane production rate between about 1440-2400 days was caused by the increase in carbon dioxide injection rate at about 1440 days. The production rate of methane started to decrease after about 2400 days. This was due to the saturation of the coal formation. The shnulation predicted a

50% breakthrough at about 2700 days. "Breakthrough" is defined as the ratio of the flow rate of carbon dioxide to the total flow rate of the total produced gas times 100%. In addition, the simulation predicted about a 90% breakthrough at about 3600 days.

FIG. 188 illustrates cumulative methane produced 5090 and the cumulative net carbon dioxide injected 5080 as a function of time during the simulation. The cumulative net carbon dioxide injected is the total carbon dioxide produced subtracted from the total carbon dioxide injected. FIG. 188 shows that by the end of the simulated injection, about twice as much carbon dioxide was stored as methane produced. In addition, the methane production was about 0.24 billion standard m³ at 50% carbon dioxide breaktlirough. In addition, the carbon dioxide sequesfration was about 0.39 billion standard m³ at 50% carbon dioxide breakthrough. The methane production was about 0.26 billion standard m³ at 90% carbon dioxide breakthrough. In addition, the carbon dioxide sequesfration was about 0.46 billion standard m³ at 90% carbon dioxide breakthrough.

TABLE 12 shows that the permeability and porosity of the simulation in the post freatment coal formation were both significantly higher than in the deep coal formation prior to treatment. In addition, the initial pressure was much lower. The depth of the post freatment coal formation was shallower than the deep coal bed methane fonnation. The same relative permeability data and PVT data used for the deep coal formation were used for the coal formation simulation. The initial water saturation for the post freatment coal formation was set at 70%. Water was present because it is used to cool the hot spent coal formation to 25 °C. The amount of methane initially stored in the post treatment coal is very low.

The simulation modeled a sequesfration process over a time period of about 3800 days for the post treatment coal formation model. The simulation modeled removal of water from the post treatment coal formation with production from five wells. During about the ffrst 200 days, the production rate of water was about 680,000 standard m³/day. From about 200-3300 days, the water production rate was between about 210,000 to about 480,000 standard Vday. Production rate of water was negligible after about 3300 days. Carbon dioxide injection was started at approximately 370 days at a flow rate of about 113,000 standard mVday. The injection rate of carbon dioxide was increased to about 226,000 standard m³/day at approximately 1440 days. The injection rate remained at 226,000 standard m³/day until the end of the simulated injection.

FIG. 189 illustrates the pressure at the wellhead of the injection wells as a function of time during the simulation of the post treatment coal formation model. The pressure was relatively constant up to about 370 days. The pressure increased through most of the rest of the simulation run up to about 36 bars absolute. The pressure rose steeply starting at about 3300 days because the production well was closed off. FIG. 190 illusfrates the production rate of carbon dioxide as a function of time in the simulation of the post treatment coal formation model. FIG. 190 shows that the production rate of carbon dioxide was almost negligible during approximately the first 2200 days. Therefore, the simulation predicts that nearly all of the injected carbon dioxide is being sequestered in the post treatment coal formation. However, at about 2240 days, the produced carbon dioxide began to increase. The production rate of carbon dioxide started to rise significantly due to onset of saturation of the post freatment coal formation.

FIG. 191 illusfrates cumulative net carbon dioxide injected as a function of time during the simulation in the post treatment coal formation model. The cumulative net carbon dioxide injected is the total carbon dioxide produced subtracted from the total carbon dioxide injected. FIG. 191 shows that the simulation predicts a potential net sequesfration of carbon dioxide of 0.56 Bm³. This value is greater than the value of 0.46 Bm³ at 90% carbon dioxide breakthrough in the deep coal formation. However, comparison of FIG. 186 with FIG. 189 shows that sequesfration occurs at much lower pressures in the post freatment coal formation model. Therefore, less compression energy was required for sequestration in the post freatment coal formation.

The simulations show that large amounts of carbon dioxide may be sequestered in both deep coal formations and in post treatment coal formations that have been cooled. Carbon dioxide may be sequestered in the post freatment coal formation, in coal formations that have not been pyrolyzed, and/or in both types of formations. FIG. 192 is a flow chart of an embodiment of in situ synthesis gas production process 4510 integrated with a SMDS Fischer-Tropsch and wax cracking process with heat and mass balances. The synthesis gas generating fluid injected into the formation includes about 24,000 metric tons per day of water 4530, which includes about 5,500 metric tons per day of water 4540 recycled from the SMDS Fischer-Tropsch and wax cracking process 4520. A total of about 1700 MW of energy is supplied to the in situ synthesis gas production process 4510. About 1020

MW of energy 4535 of the approximately 1700 MW of energy is supplied by in situ reaction of an oxidizing fluid with the formation, and approximately 680 MW of energy 4550 is supplied by the SMDS Fischer-Tropsch and wax cracking process 4520 in the form of steam. About 12,700 cubic meters equivalent oil per day of synthesis gas 4560 is used as feed gas to the SMDS Fischer-Tropsch and wax cracking process 4520. The SMDS Fischer- Tropsch and wax cracking process 4520 produces about 4,770 cubic meters per day of products 4570 that may include naphtha, kerosene, diesel, and about 5,880 cubic meters equivalent oil per day of off gas 4580 for a power generation facility.

Controlling a pressure and a temperature within a relatively low permeability formation containing heavy hydrocarbons will, in most instances, affect properties of the produced formation fluids. For example, a composition or a quality of foπnation fluids produced from the formation may be altered by altering an average pressure and or an average temperature in the selected section of the heated portion. The quality of the produced fluids may be defined by a property which may include, but is not limited to, API gravity, percent olefins in the produced formation fluids, ethene to ethane ratio, percent of hydrocarbons within produced formation fluids having carbon numbers greater than 25, total equivalent production (gas and liquid), and/or total liquids production. For example, controlling the quality of the produced formation fluids may include controlling average pressure and average temperature in the selected section such that the average assessed pressure in the selected section may be greater than the pressure (p) as set forth in the form of EQN. 61 for an assessed average temperature (T) in the selected section:

where/; is measured in psia (pounds per square inch absolute), Tis measured in Kelvin, and A and B are parameters dependent on the value of the selected property.

EQN. 61 may be rewritten such that the natural log of pressure may be a linear function of an inverse of temperature. This foπn of EQN. 61 may be written as: ln(p) = AJT +B. In a plot of the absolute pressure as a function of the reciprocal of the absolute temperature, A is the slope and B is the intercept. The intercept B is defined to be the natural logarithm of the pressure as the reciprocal of the temperature approaches zero. Therefore, the slope and intercept values (A and B) of the pressure-temperature relationship may be determined from two pressure-temperature data points for a given value of a selected property. The pressure-temperature data points may include an average pressure within a formation and an average temperature within the formation at which the particular value of the property was, or may be, produced from the formation. For example, the pressure- temperature data points may be obtained from an experiment such as a laboratory experiment or a field experiment.

A relationship between the slope parameter, A, and a value of a property of formation fluids may be deteπnined. For example, values of A may be plotted as a function of values of a formation fluid property. A cubic polynomial may be fitted to these data. For example, a cubic polynomial relationship such as EQN. 62 (62) A = a i* (property)³ + a₂* (property)² + a₃* (property) + a₄

may be fitted to the data, where a,, a₂, a₃, and a₄ are empirical constants that describe a relationship between the first parameter, A, and a property of a fonnation fluid. Alternatively, relationships having other functional forms such as another order polynomial or a logarithmic function may be fitted to the data. Values of a a₂, ..., may be estimated from the results of the data fitting. Similarly, a relationship between the second parameter, B, and a value of a property of formation fluids may be deteπnined. For example, values of B may be plotted as a function of values of a property of a formation fluid. A cubic polynomial may also be fitted to the data. For example, a cubic polynomial relationship such as EQN. 63

(63) B = bi* (property)³ + b₂* (property)² + b₃*(property) + b₄

may be fitted to the data, where b b₂, b₃, and b₄ are empirical constants that describe a relationship between the parameter B and the value of a property of a formation fluid. As such, b_h b₂, b₃, and b₄ may be estimated from results of fitting the data.

To determine an average pressure and an average temperature to produce a formation fluid having a selected property, the value of the selected property and the empirical constants as described above may be used to determine values for the first parameter A and the second parameter B according to EQNS. 64 and 65 :

(64) A - a i* (property)³ + a₂* (property)² + a₃* (property) + a₄

(65) B = bi* (property)³ + b₂* (property)² + b₃* (property) + b₄.

EQNS. 66, 67, and 68 may be used to describe the functional relationship of a given value of a property:

(66) P = exp[(A/T) + BJ,

(61) A = a i* (property)³ + a₂* (property)² + a₃* (property) + a

(68) B = bi* (property)³ + b₂* (property)² + b₃* (property) + b₄.

The generated curves may be used to determine a prefened temperature and a prefened pressure that produce fluids with desired properties.

It is believed that pyrolyzing at reduced temperature and increased pressure may decrease an olefin to paraffin ratio in produced fluids. Ethene to ethane ratio in non-condensable hydrocarbons may be reflective of olefin content in all produced hydrocarbons. Pyrolyzing hydrocarbons for a longer period of time, which may be accomplished by increasing pressure within the system, tends to result in a lower average molecular weight oil and higher API gravity. In addition, production of gas may increase and a non- volatile coke may be formed.

In addition, it is believed that operating at high pressure and a pyrolysis temperature at the lower end of the pyrolysis zone tends to decrease the fraction of fluids with carbon numbers greater than 25 produced from the heavy oil. It is believed that lower temperatures and/or increased partial pressure of hydrogen in the heavy oil containing diatomite formation will tend to produce less olefins in the produced hydrocarbon fluids. In addition, lower temperatures and/or higher partial pressures of hydrogen also tend to increase the atomic hydrogen to atomic carbon ratio in the produced hydrocarbon fluids.

It is believed that at higher pyrolysis temperatures production of oil liquids tends to be higher than at the lower pyrolysis temperatures. In addition, high pressures tend to decrease the quantity of oil liquids produced from a heavy oil containing diatomite formation. Operating an in situ conversion process at low pressures and high temperatures may produce a higher quantity of oil liquids than operating at low temperatures and high pressures.

FURTHER IMPROVEMENTS

Formation fluid produced from a relatively low permeability formation containing heavy hydrocarbons during freatment may include a mixture of different components. To increase the economic value of products generated from the formation, formation fluid may be freated using a variety of treatment processes. Processes utilized to treat formation fluid may include distillation (e.g., atmospheric distillation, fractional distillation, and/or vacuum distillation), condensation (e.g., fractional), cracking (e.g., thermal cracking, catalytic cracking, fluid catalytic cracking, hydrocracking, residual hydrocracking, and/or steam cracking), reforming (e.g., thermal reforming, catalytic reforming, and/or hydrogen steam reforming), hydrogenation, coking, solvent extraction, solvent dewaxing, polymerization (e.g., catalytic polymerization and/or catalytic isomerization), visbreaking, alkylation, isomerization, deasphalting, hydrodesulfurization, catalytic dewaxing, desalting, extraction (e.g., of aromatic compounds, etc.), and/or stripping.

Formation fluids may undergo freatment processes in a ffrst in situ freatment area as the formation fluid is generated and produced, in a second in situ treatment area where a specific freatment process occurs, and/or in surface freatment units. A "surface freatment unit" is a unit used to treat at least a portion of formation fluid at the surface. Surface treatment units may include, but are not limited to, reactors (e.g., hydrotreating units, cracking units, ammonia generating units, fertilizer generating units, and or oxidizing units), separating units (e.g., air separating units, liquid-liquid extraction units, adsoφtion units, absorbers, ammonia recovery and/or generating units, vapor/liquid separating units, distillation columns, reactive distillation columns, and/or condensing units), reboiling units, heat exchangers, pumps, pipes, storage units, and/or energy producing units (e.g., fuel cells and/or gas turbines). Multiple surface freatment units used in series, in parallel, and/or in a combination of series and parallel are refened to as a surface facility configuration. Surface facility configurations may vary dramatically due to a composition of formation fluid as well as the products being generated. Surface freatment configurations may be combined with freatment processes in various surface freatment systems to generate a multitude of products. Products generated at a site may vary with local and/or global market conditions, foπnation characteristics, proximity of formation to a purchaser, and/or available feedstocks. Generated products may be utilized on site, fransfened to another site for use, and/or sold to a purchaser.

Feedstocks for surface freatment units may be generated in freatment areas and/or surface freatment units. A "feedstock" is a sfream containing at least one component required for a treatment process. Feedstocks may include, but are not limited to, fonnation fluid, synthetic condensate, a gas sfream, a water stream, a gas fraction, a light fraction, a middle fraction, a heavy fraction, bottoms, a naphtha fraction, a jet fuel fraction, a diesel fraction, and/or a fraction containing a specific component (e.g., heart fraction, etc.). In some embodiments, feedstocks are hydrofreated prior to entering a surface freatment unit. For example, a hydrofreating unit used to hydrofreat a synthetic condensate may generate hydrogen sulfide to be utilized in the synthesis of a fertilizer such as ammonium sulfate. Alternatively, one or more components (e.g., heavy metals) may have been removed from formation fluids prior to entering the surface freatment unit.

In alternate embodiments, feedstocks for in situ freatment processes may be generated at the surface in surface freatment units. For example, a hydrogen sfream may be separated from formation fluid in a surface treatment unit and then provided to an in situ freatment area to enhance generation of upgraded products. In addition, a feedstock may be injected into a freatment area to be stored for later use. Alternatively, storage of a feedstock may occur in storage units on the surface.

The composition of products generated may be altered by controlling conditions within a freatment area and/or within one or more surface freatment units. Conditions within the freatment area and or one or more surface treatment units which affect product composition include, but are not limited to, average temperature, fluid pressure, partial pressure of H₂, temperature gradients, composition of formation material, heating rates, and composition of fluids entering the freatment area and/or the surface freatment unit. Many different surface facility configurations exist for the synthesis and/or separation of specific components from formation fluid.

Formation fluid may be produced from a foπnation through a wellhead. As shown in FIG. 193, wellhead 7012 may separate formation fluid 7010 into gas sfream 7022, liquid hydrocarbon condensate sfream 7024, and water sfream 7026. Alternatively, formation fluid may be produced from a formation through a wellhead and flow to a separating unit, where the formation fluid is separated into a gas sfream, a liquid hydrocarbon condensate sfream, and a water sfream. A portion of the gas sfream, the liquid hydrocarbon condensate sfream, and/or the water sfream may flow to one or more surface freatment units for use in a freatment process. Alternatively, a portion of the gas sfream, the liquid hydrocarbon condensate stream, and/or the water sfream may be provided to one or more freatment areas.

In some embodiments, formation fluid may flow directly from the formation to a surface freatment unit to be freated. An advantage of freating formation fluid before separation may be a reduction in the number of surface freatment units required. Reducing the number of surface freatment units may result in decreased capital and/or operating expenses for a treatment system for formations.

Fonnation fluid may exit the foπnation at a temperature in excess of about 300 °C. Utilizing thermal energy within the formation fluid may reduce an amount of energy required by the freatment system. In certain embodiments, formation fluid produced at an elevated temperature may be provided to one or more surface freatment units. Formation fluid may enter the surface treatment unit at a temperature greater than about 250 °C, 275 °C, 300 °C, 325 °C, or 350 °C. Alternatively, thermal energy from formation fluid may be transfened to other fluids utilized by the surface facility configuration and/or the in situ freatment process.

As shown in FIG. 194, formation fluid 7010 produced from wellhead 7020 may flow to heat exchange unit 7030. Heat exchange fluid 7034 may flow into heat exchange unit 7030. Thermal energy from formation fluid 7010 may be fransfened to heat exchange fluid 7034 in heat exchange unit 7030 to generate heated fluid 7036 and cooled formation fluid 7032. Heat exchange fluid 7034 may include any fluid sfream produced from a formation

(e.g., formation fluid, pyrolysis fluid, water, and/or synthesis gas), and or any fluid sfream generated and/or separated out within a surface freatment unit (e.g., water stream, light fraction, middle fraction, heavy fraction, hydrofreated liquid hydrocarbon condensate stream, jet fuel stream, etc.).

In some in situ conversion process embodiments, a heat exchange unit may be used to increase a temperature of the formation fluid and decrease a temperature of the heat exchange fluid to generate a cooled fluid and a heated formation fluid. For example, pyrolysis fluids may be produced from a first treatment area at a temperature of about 300 °C. Synthesis gas may be produced from a second freatment area at a temperature of about 600 °C. The pyrolysis fluids and synthesis gas may flow in separate conduits to distant surface freatment units. Heat loss may cause the pyrolysis fluids to condense before reaching a distant surface freatment unit for freatment. Various configurations of conduits, known in the art, may be used to form a heat exchange unit to transfer thermal energy from the synthesis gas to the pyrolysis fluids to decrease, or prevent, condensation of the pyrolysis fluids.

In conventional freatment processes, hydrocarbon fluids produced from a formation may be separated into at least two streams, including a gas stream and a synthetic condensate stream. The gas sfream may contam one or more components and may be further separated into component sfreams using one or more surface freatment units. The liquid hydrocarbon condensate sfream, or synthetic condensate sfream, may contain one or more components that are separated using one or more surface freatment units. In some embodiments, formation fluid may be partially cooled to enhance separation of specific components. For example, formation fluid may flow to a heat exchange unit to reduce a temperature of the formation fluid. Then, the formation fluid may be provided to a separating unit such as a distillation column and/or a condensing unit. Formation fluid may be hydrofreated prior to separation into a gas sfream and a liquid hydrocarbon condensate stream. Alternatively, the gas sfream and/or the liquid hydrocarbon condensate sfream may be hydrofreated in separate hydrotreating units prior to further separation into component sfreams. "Synthetic condensate" is the liquid component of formation fluid that condenses.

In an embodiment, synthetic condensate 7015 flows to surface facilities configuration illusfrated in FIG. 195. Synthetic condensate 7015 may be separated into several fractions in fractionator 7040. In some embodiments, synthetic condensate stream 7015 is separated into four fractions. Light fraction 7042, middle fraction 7044, and heavy fraction 7046 may flow to hydrofreating units 7050, 7052, 7054. Hydrofreating units 7050, 7052, 7054 may upgrade hydrocarbons within fractions 7042, 7044, and 7046 to form light fraction 7053, middle fraction 7055, and/or heavy fraction 7057. In addition, bottoms fraction 7048 may be generated. Bottoms fraction 7048 may flow to an in situ treatment area or a surface facility for further processing. In some embodiments, the use of a synthetic condensate sfream from which sulfur containing compounds have been removed, for example, by hydrofreating or a liquid-liquid extraction process, may increase an effective life of the hydrofreating units.

In an in situ conversion process embodiment, a fractionation unit may separate a feedstock into a light fraction, a heart cut, a middle cut, and/or a heavy fraction. The composition of the heart cut may be confrolled by removing fluid for the heart cut at a point in the fractionator having a given temperature. After the heart cut has been separated, the heart cut may flow to one or more surface treatment units including, but not limited to, a hydrofreater, a reformer, a cracking unit, and/or a component recovery unit. For example, when a naphthalene fraction is desired, a heart cut may be taken from a point in the fractionator resulting in production of a sfream having an atmospheric pressure true boiling point temperature greater than about 210 °C to less than about 230 °C.

This may conespond to the boiling point range for naphthalene. Components that can be separated from a synthetic condensate in a "heart cut" may include, but are not limited to, mono-aromatic hydrocarbons (e.g., benzene, toluene, ethyl benzene, and/or xylene), naphthalene, and/or anthracene.

Temperatures at which components are separated from the foπnation fluid during distillation or condensation may be affected by the concenfration of water (e.g., steam) in the formation fluid. Steam may be present in the formation fluid in varying concenfrations, due to varying water contents of formations and variations in steam generation during freatment. In some embodiments, a steam content of formation fluid may be measured as the formation fluid is produced. The steam content may be used to adjust one or more operating conditions in separating units to enhance separation of fractions.

Formation fluid may flow to one or more distillation columns positioned in series to remove one or more fractions in succession. The one or more fractions from the fluids may be used in one or more surface treatment units. "Serial fractional separation" is the removal of two or more fractions from formation fluid in series. Some of the formation fluid flows to two or more separation units in series, and each separation unit may remove one or more components from the formation fluid. For example, formation fluid may be separated into a gas stream and a synthetic condensate. A "naphtha cut" may be separated from the synthetic condensate. The "naphtha cut" may be further separated into a "phenols cut." Separating successively smaller cuts from the formation fluid may allow the subsequent treatment units to be smaller and less costly, since only a portion of the foπnation fluid needs to be freated to produce a specific product. In addition, molecular hydrogen may be separated for use in one or more of the upstream or downstream processes.

FIG. 196 depicts a serial fractional system. Synthetic condensate 7015 may flow to separating unit 7060, where it is separated into two or more fractions: light fraction 7062 and heavy fraction 7064. Light fraction 7062 may flow to heat exchanger 7065 to generate cooled light fraction 7066, which is separated into light fraction 7072 in separating unit 7070. Heat exchanger 7075 may remove thermal energy from light fraction 7072 to cooled light fraction 7076, which then flows to separating unit 7080. Naphtha fraction 7082 may be separated from cooled light fraction 7076. Naphtha fraction 7082 may be further separated into olefin generating compound fraction 7092 in separating unit 7090 after being cooled in heat exchanger 7085 to form cooled naphtha fraction 7086. Olefin generating compound fraction 7092 may flow to an olefin generating unit to be converted to olefins. Fractions 7064, 7074, 7084, 7094 may flow to one or more surface freatment units and or in situ freatment areas for additional freatment. Extracting thermal energy from fractions 7062, 7072, 7082, and/or 7092 may increase an energy efficiency of the process by utilizing the heat in the fluids. In alternate embodiments, light fractions (e.g., light fraction 7062, light fraction 7072, and/or naphtha fraction 7082) may be heated in heat exchanging units 7065,

7075, 7085 prior to entering the one or more separation units.

As shown in FIG. 197, an embodiment of a surface facility portion utilizes some of heavy fractions 7064, 7074, 7084, 7094 as a recycle stream. Some of heavy fractions 7064, 7074, 7084, 7094 removed from separation units 7060, 7070, 7080, 7090 may flow to reboilers 7067, 7077, 7087, 7097. Recycle sfreams 7069, 7079, 7089, 7099 may flow from reboilers 7067, 7077, 7087, 7097 to separation units 7060, 7070, 7080, 7090 for further upgrading. In some embodiments, steam may be provided to heavy fractions 7064, 7074, 7084, 7094 to form recycle sfreams. In some embodiments, a separating system for freating formation fluid may include a combination of heat exchangers, reboilers, and/or the injection of steam.

In certain surface facility embodiments, catalysts may be used in separating units to upgrade hydrocarbons in formation fluid as the hydrocarbons are being separated into the various fractions. In some embodiments, reactive separating units may contain catalysts that enhance hydrocarbon upgrading through hydrotreating. Molecular hydrogen present in the feedstock may be sufficient to hydrotreat hydrocarbons within the feedstock. In alternate embodiments, molecular hydrogen may be provided to a feedstock entering a reactive separating unit or to the reactive separating unit to enhance hydrogenation. Reactive distillation columns may be used to treat a synthetic condensate such as synthetic condensate and/or hydrofreated synthetic condensate in some embodiments. A reactive distillation column may contain a catalyst to increase hydrofreating of hydrocarbons in fluids passing through the reactive distillation column. In certain embodiments, the catalyst may be a conventional catalyst such as metal on an alumina substrate.

As illusfrated in FIG. 198, multiple distillation columns 7100, 7120, 7130, 7140 may be used to separate synthetic condensate 7015 into fractions. Distillation columns 7100, 7120, 7130, 7140 may contain catalyst 7052, which enables hydrocarbons within synthetic condensate 7015 to be upgraded within distillation columns 7100,

7120, 7130, 7140 through hydrofreating. Molecular hydrogen sfream 7105 may be added to distillation columns 7100, 7120, 7130, 7140 to enhance hydrofreating of hydrocarbons within synthetic condensate stream 7015 in distillation columns 7100, 7120, 7130, 7140. Molecular hydrogen sfream 7105 may come from surface freatment units and/or produced formation fluids. Fractions removed from distillation column 7100 may include light fraction 7102, middle fraction 7104, heavy fraction 7106, and bottoms 7108.

In an embodiment, light fraction 7102 flows to separating unit 7110 that separates light fraction 7102 into gaseous sfream 7112, light fraction 7114, and recycle sfream 7116. Light fraction 7114 may flow to reactive distillation column 7120 to be separated and upgraded. In distillation column 7120, light fraction 7114 may be converted into light fraction 7122. A portion of light fraction 7122 may flow to reboiler 7125 and then flow to distillation column 7120 as recycle sfream 7128. Light sfream 7126 may flow to a surface treatment unit such as a reforming unit, an olefin generating unit, a cracking unit, and/or a separating unit. The reforming unit may alter light stream 7126 to generate aromatics and hydrogen. Alternatively, light sfream 7126 may be used to generate various types of fuel (e.g., gasoline). Light stream 7126 may, in certain embodiments, be blended with other hydrocarbon fluids to increase a value and/or a mobility of the hydrocarbon fluids. In some embodhnents, light stream 7126 may be a naphtha stream.

In some embodiments, middle fraction 7104 flows into reactive distillation column 7130. Middle fraction 7104 may be converted into middle fraction 7132 and recycle sfream 7134 in reactive distillation colmnn 7130. Recycle sfream 7134 may flow into distillation column 7100. A portion of middle fraction 7132 may flow into reboiler unit 7135 to be vaporized and enter distillation column 7130 as recycle sfream 7138. Middle sfream 7136 may be provided to a market and/or flow to a surface freatment unit for further freatment.

Heavy fraction 7106 may flow into distillation column 7140. Heavy fraction 7142 and recycle sfream 7144 may be generated in reactive distillation column 7140. Recycle sfream 7144 may flow into distillation column 7100. A portion of heavy fraction 7142 may flow into reboiler unit 7145 to be vaporized and enters distillation column 7140 as recycle sfream 7148. Heavy sfream 7146 may be provided to a market and/or flow to a surface freatment unit and/or in situ treatment area for further treatment.

Bottoms fraction 7108 may be removed from distillation column 7100. A portion of bottoms fraction 7108 may be vaporized in reboiler unit 7150 and enter distillation column 7100 as recycle sfream 7152. Bottoms sfream 7109 may be cooled in heat exchange units. In certain embodiments, a portion of a bottoms fraction may be used as a feedstock for an olefin plant and/or an in situ treatment area. In some embodiments, a portion of a bottoms fraction may flow to a hydrocracking unit to form a transportation fuel sfream.

In some embodiments, formation fluid produced from the ground may be partially cooled to recover thermal energy from the fluid. In addition, formation fluid may be cooled to a temperature at which a desired component is removed from the formation fluid. Heat exchanging units may remove thermal energy from the formation fluid such that a temperature within the formation fluid is reduced to a temperature at which one or more components are separated from formation fluid. Formation fluid may be provided to a distillation colmnn where the formation fluid is further separated into a liquid sfream and a vapor sfream. The vapor stream may be provided to a heat exchanging unit to remove thermal energy from the vapor sfream. The vapor sfream may be further separated in a distillation column. In some embodiments, multiple distillation columns may be ananged to separate the vapor sfream into one or more fractions.

In some embodiments, formation fluid 7010 flows into condensing unit 7160 as shown in FIG. 199. Condensing unit 7160 may separate formation fluid 7010 into gas fraction 7162, light fraction 7164, heavy fraction

7166, and/or heart cut 7168. Gas fraction 7162, light fraction 7164, heavy fraction 7166, and/or heart cut 7168 may flow to a surface freatment unit for additional freatment.

An example of a surface facility configuration for treating formation fluid is illustrated in FIG. 200. Foπnation fluid 7010 may be produced through wellhead 7020 and cooled in one or more heat exchange units 7170. Cooled formation fluid 7172 may be condensed in condensing unit 7175 to form condensed foπnation fluid 7176.

Condensed foπnation fluid 7176 may be separated in processing unit 7180 into gas sfream 7182 and synthetic condensate 7015. Gas sfream 7182 may be compressed and separated in compressor 7185 into gas stream 7186 and hydrocarbon containing fluids 7187. Hydrocarbon containing fluids 7187 may be heated in heater 7188. Heated hydrocarbon containing fluids 7189 may be separated into gas sfream 7192 and naphtha stream 7126 in processing unit 7190. Gas stream 7186 and gas sfream 7192 may flow into expander 7195. Expander 7195 allows fluids within gas sfream 7186 and gas stream 7192 to expand into light off-gas 7196.

In an embodiment, synthetic condensate sfream 7015 is pumped to hydrofreating unit 7200 to be hydrofreated. Hydrofreated synthetic condensate sfream 7202 may flow through heat exchanging units 7170 to be heated. Heated and hydrofreated synthetic condensate sfream 7205 may be separated into a mixture of non- condensable hydrocarbons 7208 and hydrocarbon containing fluid 7210 in processing unit 7206. Hydrocarbon containing fluid 7210 may be pumped through heat exchange units 7170 to form heated hydrocarbon containing fluid 7212. Heated hydrocarbon containing fluid 7212 may be further heated in heating unit 7214 to form heated hydrocarbon containing fluid 7216. Heated hydrocarbon containing fluid 7216 and non-condensable hydrocarbons 7208 may be distilled in distillation column 7220 to form light fraction 7042, middle fraction 7044, heavy fraction 7046, and bottoms 7228. Light fraction 7042 may be cooled in heat exchange unit 7234. Cooled light fraction

7222 may be separated into heavy off-gas 7224, water sfream 7272, and hydrocarbon condensate stream 7238 in process unit 7236. Hydrocarbon condensate stream 7238 may be split into at least two sfreams, including recycle sfream 7229 and light fraction 7227. Light fraction 7227 may be added to light stream 7126. Olefins may be generated from light stream 7126 in a reforming unit. Alternatively, light sfream 7126 may be used to generate various types of fuel. Light stream 7126, in certain embodhnents, may be blended with other hydrocarbon fluids to increase a value and/or a mobility of the hydrocarbon fluids.

In some embodiments, middle fraction 7044 flows to distillation column 7240. Recycle stream 7244 and middle fraction 7242 may be generated in distillation column 7240. Recycle sfream 7244 may flow to distillation column 7220. Reboiler 7246 may separate middle fraction 7242 into recycle stream 7248 and hot middle fraction 7250. Recycle sfream 7248 flows to distillation column 7240. Hot middle fraction 7250 may be cooled in heat exchange units 7252 to form cooled middle fraction 7254. In addition, cooled middle fraction 7254 may flow into a condensing unit to form a middle sfream. Alternatively, hot middle fraction 7250 may flow directly from reboiler 7246 to a condensing unit to form a middle stream.

In an embodiment, distillation column 7270 separates heavy fraction 7046 into recycle sfream 7256 and heavy fraction 7258. Recycle sfream 7256 may flow to distillation column 7220. Heavy fraction 7258 may flow to reboiler 7260. Reboiler 7260 may separate heavy fraction 7258 into recycle stream 7262 and heated heavy fraction 7264. Heated heavy fraction 7264 may be cooled in heat exchange units 7266 to form cooled heavy fraction 7268. In some embodiments, cooled heavy fraction 7268 may flow into a condensing unit. Alternatively, heavy fraction 7264 may flow from reboiler 7260 to a condensing unit to form a heavy sfream.

In certain embodiments, bottoms fraction 7228 is removed from distillation column 7220 and is cooled in heat exchange units 7230 to form cooled bottoms fraction 7232. In some embodiments, cooled bottoms fraction

7232 may flow into a condensing unit to form a condensate. Alternatively, bottoms fraction 7228 may flow directly from distillation column 7220 to a condensing unit.

In alternate embodiments, distillation columns 7220, 7240, and/or 7270 may contain catalysts to upgrade hydrocarbons. The catalysts may be hydrofreating and/or cracking catalysts. In some embodiments, an additional molecular hydrogen sfream may be added to distillation columns 7220, 7240, and/or 7270 that contain such catalysts.

Formation fluid may contain substances that compromise surface freatment units by altering catalytic surfaces and/or by causing conosion. Many surface freatment units may require the removal of these substances prior to freatment in the surface freatment unit. Components in fonnation fluid that may affect a life span and/or efficiency of the surface freatment unit include heteroatoms (e.g., nifrogen, sulfur, and water). For example, water decreases the catalytic ability of conventional hydrotreating catalysts. In some embodiments, use of a conventional hydrotreating unit may require separation of water from formation fluid prior to treatment. In addition, sulfur containing compounds may cause conosion of a surface freatment unit and decrease the catalytic ability of certain catalysts used in the surface freatment unit. Removal of sulfur containing compounds from formation fluid may increase the value of produced fluid and permit processing of the lower sulfur material in process units not designed for untreated produced fluid.

Components that foul or conode surface freatment units may be removed using a variety of methods including, but not limited to, hydrofreating, solvent extraction, a desalting process, and/or electrostatic precipitation. In some embodhnents, a portion of the water present in formation fluid may be removed from foπnation fluid as the formation fluid is separated into a gas sfream and a liquid hydrocarbon condensate sfream.

In some embodiments, a desalting process may reduce salts in formation fluid and/or any water or fluid separated in a surface freatment unit. The desalting process may include, but is not limited to, chemical separation, electrostatic separation, and/or filtration of water/fluid through a porous structure (e.g., water or fluid may be filtered through diatomaceous earth). Heteroatoms may also be removed from formation fluid using an extraction process. Solvents may include, but are not limited to, acetic acid, sulfuric acid, and/or formic acid. Heteroatoms in acidic form, such as phenols and some sulfur compounds, may be removed by extraction with basic solutions (e.g., caustic or aqueous ammonia). Extraction may vary with a temperature of formation fluid and/or solvent, a solvent to oil ratio, and or an acid sfrength of the acidic solvents. An effective solvent may be characterized by features including, but not limited to, inhibition of emulsion formation, immiscibility with feedstock, rapid phase separation, and/or high capacity. Removal of nitrogen containing components by an extraction process may decrease hydrogen uptake and the hydrofreating severity required in subsequent hydrofreating units, thereby reducing operating and capital costs.

Enactment of more stringent regulatory standards for sulfur in hydrocarbon containing products may require a higher severity to remove sulfur from the products. In some circumstances, sulfur may be removed from foπnation fluid prior to separating the fluid into sfreams to facilitate removal of a maximum amount of sulfur.

Similarly, formation fluid may be hydrofreated prior to separation into sfreams to decrease an overall cost of processing formation fluid. Subsequent sulfur removal and or hydrofreating may further improve the quality of hydrocarbon fluids produced from the formation fluid.

Conventional refiners may not handle high concentrations of heteroatoms in fluid fractions (e.g., naphtha, jet, and diesel). Hydrofreating may produce a product that would be acceptable to a refiner. Another approach, or a complementary approach, may be to optimize the combination of the in situ conversion process conditions and surface hydrofreating processes to obtain the highest product value mix at the lowest total cost. For example, one in situ conversion process change that may improve properties of the liquid foπnation fluid is the use of backpressure on the formation during the heating process. Maintaining a fluid pressure by adjusting the backpressure may produce a much lighter and more hydrogen rich product. Hydrofreating a fluid may alter many properties of the fluid. Hydrofreating may increase the hydrogen content of the hydrocarbons within the fluid and/or the volume of fluid. In addition, hydrofreating may reduce a content of heteroatoms such as oxygen, nitrogen, or sulfur in the fluid. For example, nifrogen removed from the fluid durmg hydrotreating may be converted into ammonia. Removed sulfur may be converted into hydrogen sulfide. Feedstocks for hydrotreating units may include, but are not limited to, fonnation fluid and/or any fluid generated or separated in a surface freatment unit (e.g., synthetic condensate, light fraction, middle fraction, heavy fraction, bottoms, heart cut, pyrolysis gasoline, and/or molecular hydrogen generated at an olefin generating plant). Olefins may be present in formation fluid as a result of in situ freatment processes. In some embodiments, olefin generating compounds may be produced in formation fluid. "Olefin generating compounds" are hydrocarbons having a carbon number equal to and/or greater than 2 and less than 30 (e.g., carbon numbers from 2 to 7). These olefin generating compounds may be converted into olefins, such as ethylene and propylene. Process conditions during freatment within a freatment area of a fonnation may be confrolled to increase, or even to maximize, production of olefins and or olefin generating compounds within the formation fluid.

In an embodiment, olefins and/or olefin generating compounds produced in the formation fluid may be separated from the formation fluid using one or more surface facility configurations. Separation of olefins and/or olefin generating compounds from formation fluid may occur in, but is not limited to, a gas treating unit, a distillation unit, and or a condensing unit. Olefin generating compounds may be separated from formation fluid to form an olefin feedstock used to generate olefins.

Olefin feedstocks may include formation fluid, synthetic condensate, a naphtha stream, a heart cut (e.g., a sfream containing hydrocarbons having carbon number from two to seven), a propane sfream, and/or an ethane stream. For example, formation fluid may be separated into a liquid sfream (e.g., synthetic condensate) and a gas sfream. The gas stream may be further separated into four or more fractions. The fractions may include, but are not limited to, a methane fraction, a molecular hydrogen fraction, a gas fraction, and an olefin generating compound fraction. In some embodiments, olefin feedstocks may have been hydrofreated and/or have had one or more components (e.g., arsenic, lead, mercury, etc.) removed prior to entering the olefin generating unit. Many different surface facility configurations may produce olefins from an olefin feedstock. The particular configuration utilized for synthesis of olefins may depend on a type of formation freated, a composition of foπnation fluid, and/or freatment process conditions used in situ such as a temperature, a pressure, a partial pressure of H₂, and/or a rate of heating.

Conversion of formation fluid and/or olefin generating compounds to olefins occurs when hydrocarbons in formation fluid are heated rapidly to cracking temperatures and then quenched rapidly to inhibit secondary reactions

(e.g., recombination of hydrogen with olefins). Prolonged heating may result in the production of coke and, thus, quenching the reaction is vital to enhancing olefin generation. A temperature required for olefin generation may be greater than about 800 °C. Formation fluid may exit the foπnation at a temperature greater than about 200 °C. In certain embodiments, foπnation fluid may be produced from wells containing a heat source such that a temperature of at least a portion of the formation fluid is about 700 °C. Therefore, additional heating may be required for generation of olefins. Formation fluid may flow to an olefin generating unit where fluid is initially heated and then cooled to quench the reaction to enhance production of olefins.

FIG. 201 depicts an embodiment of surface facility units used to generate olefins from an olefin feedstock that contains olefin generating compounds. The hydrogen content of hydrocarbons within formation fluid may be increased to greater than about 12 weight % by controlling one or more conditions within a freatment area from which formation fluid 7010 is produced. For example, maintaining a pressure greater than about 7 bars (100 psig) and a temperature less than about 375 °C within a freatment area may generate formation fluid having hydrocarbons with a hydrogen content greater than about 12 weight %. A hydrogen content of greater than 12 weight % in the hydrocarbons of formation fluid may decrease the content of heavy hydrocarbons and/or undesirable compounds in the formation fluid produced. In an embodiment, formation fluid 7010 (e.g., fonnation fluid having hydrocarbons with a hydrogen content greater than about 12%) flows directly from wellhead 7020 into olefin generating unit 7280 to be converted to olefin stream 7282. In some embodiments, the olefin generating unit may be a steam cracker. Formation fluid 7010 may flow into olefin generating unit 7280 at a temperature greater than about 300 °C in certain embodiments. Thermal energy within the formation fluid may be utilized in the generation of olefins from the olefin generating compounds. In an embodiment, formation fluid may contain steam. Steam in formation fluid may be utilized in the generation of olefins. A portion of the steam required for the generation of olefins in an olefin generating unit may be provided by steam present in formation fluid.

Alternatively, formation fluid may flow to a component removal unit prior to an olefin generating unit, fn certain embodiments, formation fluid may include components containing small amounts of heavy metals such as arsenic, lead, and or mercury. As depicted in FIG. 202, freatment unit 7290 may separate formation fluid 7010 into two component sfreams (e.g., streams 7292, 7294) and hydrocarbon containing fluids 7296. Component sfreams 7292, 7294 may include a single component or a mixture of multiple components. For example, freatment unit 7290 may remove heavy metals in streams 7292, 7294. Hydrocarbon containing sfream 7296 may flow to olefin generating unit 7280 to be converted to olefin sfream 7282. Olefin sfream 7282 may include, but is not limited to, ethylene, propylene, and/or butylene.

Molecular hydrogen within an olefin feedstock may be removed from the olefin feedstock prior to the feedstock being provided to an olefin generating unit in some embodiments. In alternate embodiments, formation fluid may flow to a hydrofreating unit prior to flowing to an olefin generating unit to convert at least a portion of the olefin generating compounds into olefins. In an olefin generating unit, a portion of the formation fluid may be converted into compounds which may include, but are not limited to, olefins, molecular hydrogen, pyrolysis gasoline that contains BTEX compounds (benzene, toluene, ethylbenzene and or xylene), pyrolysis pitch, and/or butadiene. In some embodiments, the molecular hydrogen generated in the olefin generating unit may flow to a hydrofreating unit to hydrotreat fluids. For example, a portion of the generated molecular hydrogen may be used to hydrotreat pyrolysis gasoline and/or pyrolysis pitch generated in the olefin generating unit. Alternatively, a portion of the generated molecular hydrogen may be provided to an in situ freatment area. In some embodiments, a portion of fluid generated in an olefin generating unit may flow to one or more extraction units to remove components such as butadiene and/or BTEX compounds. In some embodiments, pyrolysis gasoline generated in an olefin generating unit may have a high BTEX content. Pyrolysis gasoline may, in certain embodiments, be provided to a surface freatment unit to remove the BTEX compounds. In some embodiments, pyrolysis pitch may be used as a fuel. Alternatively, pyrolysis pitch may be provided to an in situ treatment area for additional processing.

A steam cracking unit may be utilized as an olefin generating unit as depicted in FIG. 203. Steam cracking unit 7310 may include heating unit 7320 and quenching unit 7330. Olefin feedstock 7300 entering heating unit 7320 may be heated to a temperature greater than about 800 °C. Fluid 7322 may flow to quenching unit 7330 to rapidly quench and compress fluid 7322. Fluid 7332 exiting quenching unit 7330 may include one or more olefin compounds, molecular hydrogen, and/or BTEX compounds. The olefin compounds may include, but are not limited to, ethylene, propylene, and/or butylene. In certain embodiments, fluid 7332 may flow to a separating unit. The components within fluid 7332 may be separated into component sfreams in the separating unit. The component sfreams may be sold, transported to a different facility, stored for later use, and/or utilized on site in freatment areas or in surface freatment units.

Ammonia may be generated during an in situ conversion process. In situ ammonia may be generated during a pyrolysis stage from some of the nifrogen present in hydrocarbon material. Hydrogen sulfide may also be produced within the formation from some of the sulfur present in the hydrocarbon containing material. The ammonia and hydrogen sulfide generated in situ may be dissolved in water condensed from the formation fluids. FIG. 204 depicts a configuration of surface treatment units that may separate ammonia and hydrogen sulfide from water produced in the foπnation. Formation fluid 7010 may be separated at wellhead 7012 into gas stream 7022, synthetic condensate 7015, and water sfream 7026. Gas freating unit 7350 may separate gas sfream 7022 into gas mixture 7352, light hydrocarbon mixture 7354, and/or hydrogen fraction 7356. Gas mixture 7352 may include, but is not limited to, hydrogen sulfide, carbon dioxide, and/or ammonia. Gas mixture 7352 may be blended with water sfream 7026 to form aqueous mixture 7358. Aqueous mixture 7358 may flow to stripping unit

7360, where aqueous mixture 7358 is separated into ammonia stream 7362 and aqueous mixture 7364. Aqueous mixture 7364 may flow to stripping unit 7370 to be separated into hydrogen sulfide sfream 7372 and water sfream 7374. Ammonia sfream 7362 may be stored as an aqueous solution or in anhydrous form. Alternately, ammonia sfream 7362 may be provided to surface treatment units requiring ammonia, such as a urea synthesis unit or an ammonium sulfate synthesis unit.

In some embodiments, ammonia may be formed from nifrogen present in hydrocarbons when fluids are being hydrofreated. The generated ammonia may also be separated from other components, as illusfrated in FIG. 205. Synthetic condensate 7015 may flow to hydrofreating unit 7380 to form ammonia containing sfream 7382 and hydrofreated synthetic condensate 7384. Ammonia containing stream 7382 may be blended with water stream 7026 and gas mixture 7352 prior to entering stripping unit 7360 as aqueous mixture 7386.

Alternatively, fluid containing small amounts or concenfrations of ammonia may flow to Claus freatment unit 7390 for treatment, as depicted in FIG. 206. Wellhead 7012 may separate formation fluid 7010 into gas sfream 7022, synthetic condensate 7015, and water stream 7026. Gas freating unit 7350 may further separate gas stream 7022 into gas mixture 7352, light hydrocarbon mixture 7354, and/or hydrogen fraction 7356. Water sfream 7026 and gas mixture 7352 may be blended to form sfream 7358. Claus freatment unit 7390 may reduce ammonia in sfream 7358 to form fluid sfream 7394. Recovered sulfur may exit Claus treatment unit 7390 as sulfur sfream 7392 and be utilized in any process that requires sulfur, either in surface facilities or treatment areas. In some embodiments, Claus freatment unit 7390 may also generate a carbon dioxide sfream. The carbon dioxide may be utilized in a urea synthesis unit. Alternatively, carbon dioxide may be provided to an in situ freatment area for sequesfration. If a hydrotreating unit is used, then at least a portion of the sulfur in the sfream entering the hydrotreating unit may be converted to hydrogen sulfide. In some embodiments, hydrogen sulfide may be used to make fertilizer, sulfuric acid, and or converted to sulfur in a Claus treatment unit. Similarly, some nifrogen in the sfream entering the hydrofreating unit may be converted to ammonia, which may also be recovered for sale and/or use in processes. In some embodiments, ammonia may be generated on site in surface treatment units using an ammonia synthesis process as shown in FIG. 207. Ah sfream 7400 may flow to air separating unit 7410 to separate nifrogen sfream 7412 and sfream 7414 from air sfream 7400. Nitrogen sfream 7412 may be heated with heat exchanger 7170 to form heated nifrogen feedstock 7416 prior to flowing into ammonia generating unit 7420. Hydrogen feedstock 7418 may flow to ammonia generating unit 7420 to react with nifrogen sfream 7412 to form ammonia sfream 7422. Ammonia generated during in situ or surface freatment processes may be stored in an aqueous solution or as anhydrous ammonia. In some instances, ammonia in either form may be sold commercially. Alternatively, ammonia may be used on site to generate a number of different products that have commercial value (e.g., fertilizers such as ammonium sulfate and/or urea). Production of fertilizer may increase the economic viability of a treatment system used to treat a formation. Precursors for fertilizer production may be produced in situ or while freating formation fluid at surface facilities. Ammonia and carbon dioxide generated during treatment either in situ or at a surface freating unit may be used to generate urea for use as a fertilizer, as illusfrated in FIG. 208. Ammonia stream 7424 and carbon dioxide stream 7426 may react in urea generating unit 7428 to form urea stream 7430.

As illusfrated in FIG. 209, ammonium sulfate may be generated by freating formation fluid in a surface freatment unit. Wellhead 7012 may separate formation fluid 7010 into a mixture of non-condensable hydrocarbon fluids 7432 and synthetic condensate 7015. Separation unit 7434 may be used to separate non-condensable hydrocarbon fluids 7432 into hydrogen stream 7436, hydrogen sulfide sfream 7438, methane sfream 7440, carbon dioxide stream 7442, and non-condensable hydrocarbon fluids 7444.

Hydrogen sulfide stream 7438 may flow to oxidation unit 7446 to be converted to sulfuric acid sfream 7450. Additional hydrogen sulfide may, in certain embodiments, be provided to oxidation unit 7446 from hydrogen sulfide sfream 7448. In some embodiments, hydrogen sulfide sfream 7448 may be provided from a hydrofreating unit. The hydrotreating unit may be a surface facility in a different section of a treatment system or part of a different configuration of a treatment system.

Air separating unit 7410 may be used to separate nifrogen sfream 7412 and sfream 7414 from afr sfream 7400. Heat exchanger 7170 may heat nitrogen sfream 7412 to form heated nifrogen feedstock 7416. Hydrogen stream 7436 and heated nitrogen feedstock 7416 may flow to ammonia generating unit 7420 to form ammonia sfream 7422. In some embodiments, additional hydrogen may be provided to ammonia generating unit 7420. In alternate embodiments, a portion of hydrogen stream 7436 may flow to an in situ treatment area and/or a surface freatment facility. In certain embodiments, process ammonia 7452, produced in formation fluid and/or generated in surface freatment units, is added to ammonia sfream 7422 to form ammonia feedstock 7454. Ammonia feedstock 7454 and sulfuric acid sfream 7450 may flow into fertilizer synthesis unit 7456 to produce ammonium sulfate sfream 7458. Alternatively, a portion of sulfuric acid produced in an oxidation unit may be sold commercially.

In some embodiments, ammonia produced during treatment of a formation may be used to generate ammonium carbonate, ammonium bicarbonate, ammonium carbamate, and/or urea. Separated ammonia may be provided to a stream containing carbon dioxide (e.g., synthesis gas and/or carbon dioxide separated from formation fluid) such that the separated ammonia reacts with carbon dioxide in the sfream to generate ammonium carbonate, ammonium bicarbonate, ammonium carbamate, and/or urea. Utilization of separated ammonia in this manner may reduce carbon dioxide emissions from a freatment process. Ammonium carbonate, ammonium bicarbonate, ammonium carbamate, and/or urea may be commercially marketed to a local market for use (e.g., as a fertilizer or a material to make fertilizer). Ammonium carbonate, ammonium bicarbonate, ammonium carbamate, and/or urea may capture or sequester carbon dioxide in geologic formations.

Formation fluid may include mono-aromatic components such as benzene, toluene, ethyl benzene, and xylene, (i.e., BTEX compounds). In some embodiments, separating BTEX compounds from formation fluid may increase an economic value of the generated products. Separated BTEX compounds may have a higher economic value than the same BTEX compounds in the mixture of component in the fonnation fluid. BTEX compounds may be separated from a synthetic condensate sfream. "Synthetic condensate" may refer to a liquid hydrocarbon condensate stream and/or a hydrofreated liquid condensate sfream.

A process embodiment may include separating synthetic condensate 7015 into BTEX compound sfream 7472 and BTEX compound reduced synthetic condensate 7474 using separating unit 7470, as illusfrated in FIG.

210. Mono-aromatic reduced synthetic condensate 7474 may flow to hydrotreating unit 7476, where BTEX compound reduced synthetic condensate 7474 is hydrofreated to form hydrofreated synthetic condensate 7478. Hydrofreated synthetic condensate 7478 may flow to any surface freatment unit for further treatment. Alternatively, mono-aromatic reduced synthetic condensate 7474 may, in certain embodiments, flow to a surface freatment unit for further treatment.

Mono-aromatic components, specifically BTEX compounds, may also be recovered after a synthetic condensate sfream has been separated into one or more fractions (e.g., a naphtha fraction, a jet fraction, and/or a diesel fraction). The naphtha fraction may be separated from formation fluid using a surface freatment unit. In some embodiments, removal of BTEX compounds prior to hydrofreating the naphtha fraction may reduce capital and operating costs of a hydrofreating unit needed to treat the naphtha fraction. In certain embodiments, a naphtha fraction may be hydrofreated.

In some embodiments, formation fluid may contain BTEX generating compounds such as paraffins and/or naphthalene. BTEX generating compounds may flow to one or more surface freatment units to be converted into BTEX compounds. In some embodiments, a synthetic condensate may be hydrofreated and then separated in separating units to form a naphtha sfream. The naphtha stream may be provided to a reformer unit that converts

BTEX generating compounds to BTEX compounds.

Naphtha stream 7480 may flow to reforming unit 7482, as illusfrated in FIG. 211. Naphtha stream 7480 may be converted into reformate 7484 and hydrogen sfream 7486. In certain embodiments, hydrogen sfream 7486 flows to any surface freatment unit and/or freatment area requiring hydrogen. For example, a hydrofreating unit and/or a reactive distillation column may utilize hydrogen stream 7486. Reformate 7484 may flow to recovery unit

7488. Reformate 7484 may be separated into mono-aromatic sfream 7492 and raffinate 7490 in recovery unit 7488. In some embodiments, raffinate 7490 may flow to a processing unit to be converted to a gasoline stream. The gasoline may be provided to a local market. In alternate embodiments, a mono-aromatic recovery unit may separate reformate 7484 into one or more streams, such as raffinate 7490, a benzene sfream, a toluene sfream, a ethyl benzene sfream, and/or a xylene sfream. In certain embodhnents, naphtha sfream 7480 may be replaced with a "heart cut" (i.e., products distilled in a relatively nanow selected temperature range) conesponding to mono- aromatic compounds.

Conversion of BTEX generating compounds into BTEX compounds in reforming unit 7482 may foπn molecular hydrogen. The molecular hydrogen may be used in one or more surface freatment units and/or in situ freatment areas where molecular hydrogen is needed. An advantage of utilizing a reforming unit may be the generation of molecular hydrogen for use on site. Generating molecular hydrogen on site may lower capital as well as operating costs for a given freatment system.

Formation fluid produced from relatively low peπneability formations containing heavy hydrocarbons during an in situ conversion process may contain one or more components (e.g., naphthalene, anthracene, pyridine, pynoles, and or thiophene and its homologs). Various operating conditions within a treatment area may be confrolled to increase the production of a component. Some of die components may be commercially viable products. Separating some components from formation fluid may increase the total value of generated products. A separated component in relatively concentrated form may have higher economic value than the same component in foπnation fluid. For example, formation fluid containing naphthalene may be sold at a lower price than a naphthalene stream separated from the formation fluid and the remaining fonnation fluid. In an embodiment, separation of naphthalenes may be accomplished using crystallization. In addition, removal of some components may reduce hydrogen consumption in subsequent hydrotreating units.

FIG. 212 depicts an embodiment of recovery unit 7496 used to separate a component from heart cut 7494. Heart cut 7494 may be obtained from a synthetic crude or formation fluid. Heart cut 7494 flows to recovery unit 7496, which may separate heart cut 7494 into component stream 7498 and hydrocarbon mixture 7450. In some embodiments, component sfream 7498 may be sold and/or used on site in an in situ treatment area and/or a surface treatment unit. Hydrocarbon mixture 7450 may flow to one or more treatment units for additional treatment or, in some embodiments, to an in situ freatment area.

In some embodiments, the recovery unit, as shown in FIG. 212, separates the component from a feedstock stream (e.g., formation fluid, synthetic condensate, a gas sfream, a light fraction, a middle fraction, a heavy fraction, bottoms, a naphtha sfream, a jet fuel sfream, a diesel sfream, etc). Recovery units may separate more than one component from the feedstock sfream in certain embodiments. For example, a recovery unit may separate a feedstock sfream into a naphthalene sfream, an anthracene sfream, a naphthalene/anthracene stream, and or a hydrocarbon mixture. Fluids generated during an in situ conversion process (e.g., of a coal formation) may contain naphthalene and/or anthracene. When nitrogen containing components (e.g., pyridines and pynoles) are to be separated from a feedstock, the recovery unit may be a nifrogen exfraction unit. In some embodiments, a nifrogen extraction unit may separate the nifrogen containing components using a sulfuric acid process or a formic acid process. Nifrogen exfraction units may include sulfuric acid exfraction units and/or closed cycle formic acid exfraction units. A sulfuric acid process may separate a portion of the formation fluid into a raffinate and an extract oil. The extract oil may contain pyridines and other nifrogen containing compounds, as well as spent acid. The extract oil may be separated into a nifrogen rich extract and an acid sfream. Oil produced from an in situ thermal conversion process may have major components in the desirable naphtha, jet, and diesel boiling range. The oil, however, may also contain a significant amount of nitrogen compounds. Methods to remove the nitrogen compounds include, but are not limited to, hydrofreating and/or solvent exfraction. Studies of various solvent exfraction configurations were completed to deteπnine the optimal conditions and/or materials for removing nifrogen compounds from oil produced during the in situ conversion process in a formation.

A successful exfraction process exhibits the following properties: inhibition of emulsion formation, immiscibility with the feedstock, rapid phase separation, and high capacity.

FIG. 213 depicts an embodhnent of freatment areas 8000 sunounded by perimeter banier 8002. Each treatment area 8000 may be a volume of formation that is, or is to be, subjected to an in situ conversion process.

Perimeter banier 8002 may include installed portions and naturally occuning portions of the formation. Naturally occuning portions of the foπnation that foπn part of a perimeter banier may include substantially impermeable layers of the formation. Examples of naturally occuning perimeter baniers include overburdens and underburdens. Installed portions of perimeter banier 8002 may be formed as needed to define separate freatment areas 8000. In situ conversion process (ICP) wells 8004 may be placed within freatment areas 8000. ICP wells 8004 may include heat sources, production wells, freatment area dewatering wells, monitor wells, and other types of wells used during in situ conversion.

Different freatment areas 8000 may share common banier sections to minimize the length of perimeter banier 8002 that needs to be formed. Perimeter banier 8002 may inhibit fluid migration into freatment area 8000 undergoing in situ conversion. Advantageously, perimeter banier 8002 may inhibit foπnation water from migrating into freatment area 8000. Formation water typically includes water and dissolved material in the water (e.g., salts). If formation water were allowed to migrate into treatment area 8000 during an in situ conversion process, the formation water might increase operating costs for the process by adding additional energy costs associated with vaporizing the formation water and additional fluid freatment costs associated with removing, separating, and treating additional water in formation fluid produced from the formation. A large amount of foπnation water migrating into a freatment area may inhibit heat sources from raising temperatures within portions of freatment area 8000 to desired temperatures.

Perimeter banier 8002 may inhibit undesired migration of formation fluids out of freatment area 8000 during an in situ conversion process. Perimeter baniers 8002 between adjacent treatment areas 8000 may allow adjacent freatment areas to undergo different in situ conversion processes. For example, a first treatment area may be undergoing pyrolysis, a second freatment area adjacent to the first freatment area may be undergoing synthesis gas generation, and a third treatment area adjacent to the first freatment area and/or the second treatment area may be subjected to an in situ solution mining process. Operating conditions within the different freatment areas may be at different temperatures, pressures, production rates, heat injection rates, etc. Perimeter banier 8002 may define a limited volume of formation that is to be treated by an in situ conversion process. The limited volume of formation is known as treatment area 8000. Defining a limited volume of formation that is to be freated may allow operating conditions within the limited volume to be more readily confrolled. In some formations, a hydrocarbon containing layer that is to be subjected to in situ conversion is located in a portion of the formation that is permeable and/or fractured. Without perimeter banier 8002, formation fluid produced during in situ conversion might migrate out of the volume of formation being freated. Flow of foπnation fluid out of the volume of foπnation being freated may inhibit the ability to maintain a desired pressure within the portion of the formation being freated. Thus, defining a limited volume of foπnation that is to be freated by using perimeter banier 8002 may allow the pressure within the limited volume to be controlled. Controlling the amount of fluid removed from freatment area 8000 through pressure relief wells, production wells and/or heat sources may allow pressure within the freatment area to be confrolled. In some embodiments, pressure relief wells are perforated casings placed within or adjacent to wellbores of heat sources that have sealed casings, such as flameless disfributed combustors. The use of some types of perimeter baniers (e.g., frozen baniers and grout walls) may allow pressure confrol in individual freatment areas 8000.

Uncontrolled flow or migration of formation fluid out of freatment area 8000 may adversely affect the ability to efficiently maintain a desired temperature within freatment area 8000. Perimeter banier 8002 may inhibit migration of hot formation fluid out of freatment area 8000. Inhibiting fluid migration through the perimeter of freatment area 8000 may limit convective heat losses to heat loss in fluid removed from the formation through production wells and/or fluid removed to confrol pressure within the freatment area.

During in situ conversion, heat applied to the fonnation may cause fractures to develop within treatment area 8000. Some of the fractures may propagate towards a perimeter of freatment area 8000. A propagating fracture may intersect an aquifer and allow formation water to enter freatment area 8000. Formation water entering treatment area 8000 may not permit heat sources in a portion of the treatment area to raise the temperature of the formation to temperatures significantly above the vaporization temperature of formation water entering the formation. Fractures may also allow formation fluid produced during in situ conversion to migrate away from freatment area 8000. Perimeter banier 8002 around freatment area 8000 may limit the effect of a propagating fracture on an in situ conversion process. In some embodiments, perimeter baniers 8002 are located far enough away from freatment areas 8000 so that fractures that develop in the formation do not influence perimeter banier integrity. Perimeter baniers 8002 may be located over 10 m, 40 m, or 70 m away from ICP wells 8004. In some embodiments, perimeter banier 8002 may be located adjacent to treatment area 8000. For example, a frozen banier foπned by freeze wells may be located close to heat sources, production wells, or other wells. ICP wells 8004 may be located less than 1 m away from freeze wells, although a larger spacing may advantageously limit influence of the frozen banier on the ICP wells, and limit the influence of formation heating on the frozen banier.

In some perimeter banier embodiments, and especially for natural perimeter baniers, ICP wells 8004 may be placed in perimeter banier 8002 or next to the perimeter banier. For example, ICP wells 8004 may be used to treat hydrocarbon layer 516 that is a thin rich hydrocarbon layer. The ICP wells may be placed in overburden 540 and/or underburden 8010 adjacent to hydrocarbon layer 516, as depicted in FIG. 214. ICP wells 8004 may include heater-production wells that heat the foπnation and remove fluid from the formation. Thin rich layer hydrocarbon layer 516 may have a thickness greater than about 0.2 m and less than about 8 m, and a richness of from about 205 liters of oil per metric ton to about 1670 liters of oil per metric ton. Overburden 540 and underburden 8010 may be portions of perimeter banier 8002 for the in situ conversion system used to treat rich thin layer 516. Heat losses to overburden 540 and/or underburden 8010 may be acceptable to produce rich hydrocarbon layer 516. In other ICP well placement embodiments for treating thin rich hydrocarbon layers 516, ICP wells 8004 may be placed within hydrocarbon layer 516, as depicted in FIG. 215.

In some in situ conversion process embodiments, a perimeter banier may be self-sealing. For example, formation water adjacent to a frozen banier formed by freeze wells may freeze and seal the frozen banier should the frozen banier be ruptured by a shift or fracture hi the formation. In some in situ conversion process embodiments, progress of fractures in the formation may be monitored. If a fracture that is propagating towards the perimeter of the treatment area is detected, a confrollable parameter (e.g., pressure or energy input) may be adjusted to inhibit propagation of the fracture to the sunounding perimeter banier.

Perimeter baniers may be useful to address regulatory issues and/or to insure that areas proximate a freatment area (e.g., water tables or other environmentally sensitive areas) are not substantially affected by an in situ conversion process. The formation within the perimeter banier may be treated using an in situ conversion process. The perhneter banier may inhibit the formation on an outer side of the perimeter banier from being affected by the in situ conversion process used on the formation within the perimeter banier. Perimeter baniers may inhibit fluid migration from a treatment area. Perimeter baniers may inhibit rise in temperature to pyrolysis temperatures on outer sides of the perimeter baniers.

Different types of baniers may be used to fonn a perimeter banier around an in situ conversion process freatment area. The perimeter banier may be, but is not limited to, a frozen banier sunounding the freatment area, dewatering wells, a grout wall formed in the formation, a sulfur cement banier, a banier foπned by a gel produced in the formation, a banier formed by precipitation of salts in the formation, a banier formed by a polymerization reaction in the formation, sheets driven into the formation, or combinations thereof.

FIG. 216 depicts a side representation of a portion of an embodiment of treatment area 8000 having perimeter banier 8002 formed by overburden 540, underburden 8010, and freeze wells 8012 (only one freeze well is shown in FIG. 216). A portion of freeze well 8012 and perimeter banier 8002 formed by the freeze well extend into underburden 8010. In some embodhnents, perimeter banier 8002 may not extend into underburden 8010 (e.g., a perimeter banier may extend into hydrocarbon layer 516 reasonably close to the underburden or some of the hydrocarbon layer may function as part of the perimeter banier). Underburden 8010 may be a rock layer that inhibits fluid flow into or out of freatment area 8000. In some embodiments, a portion of the underburden may be hydrocarbon containing material that is not to be subjected to in situ conversion.

Overburden 540 may extend over freatment area 8000. Overburden 540 may include a portion of hydrocarbon containing material that is not to be subjected to in situ conversion. Overburden 540 may inhibit fluid flow into or out of treatment area 8000.

Some formations may include underburden 8010 that is permeable or includes fractures that would allow fluid flow into or out of freatment area 8000. A portion of perhneter banier 8002 may be formed below freatment area 8000 to inhibit inflow of fluid into the freatment area and/or to inhibit outflow of foπnation fluid during in situ conversion. FIG. 217 depicts freatment area 8000 having a portion of perimeter banier 8002 that is below the freatment area. The perimeter banier may be a frozen banier formed by freeze wells 8012. In some embodiments, a perimeter banier below a freatment area may follow along a geological formation (e.g., along dip of a dipping coal foπnation).

Some formations may include overburden 540 that is permeable or includes fractures that allow fluid flow into or out of freatment area 8000. A portion of perimeter barrier 8002 may be formed above the freatment area to inhibit inflow of fluid into the freatment area and/or to inhibit outflow of formation fluid during in situ conversion. FIG. 217 depicts an embodiment of an in situ conversion process having a portion of perimeter banier 8002 formed above treatment area 8000. In some embodiments, a perimeter banier above a freatment area may follow along a geological fomiation (e.g., along dip of a dipping foπnation). In some embodiments, a perimeter banier above a freatment area may be formed as a ground cover placed at or near the surface of the formation. Such a perhneter banier may allow for freatment of a formation wherein a hydrocarbon layer to be processed is close to the surface. In some formations, water may flow through a fracture system in a relatively low permeability formation containing heavy hydrocarbons. For example, a coal seam may be located between an impermeable overburden and an impeπneable underburden. The coal seam may include a water saturated fracture system. Water may flow through the fracture system of the coal seam. Perimeter baniers may be inserted through the overburden, through the coal seam, and into the underburden to fonn a treatment area. The inserted perimeter banier, the overburden, and the underburden may fonn perimeter baniers that define a treatment area.

As depicted in FIG. 213, several perhneter baniers 8002 may be formed to divide a formation into treatment areas 8000. If a large amount of water is present in the hydrocarbon containing material, dewatering wells may be used to remove water in the freatment area after a perimeter banier is formed. If the hydrocarbon containing material does not contain a large amount of water, heat sources may be activated. The heat sources may vaporize water within the fonnation, and the water vapor may be removed from the freatment area through production wells. '

A perimeter banier may have any desired shape. In some embodiments, portions of perimeter baniers may follow along geological features and/or property lines. In some embodiments, portions of perimeter baniers may have circular, square, rectangular, or polygonal shapes. Portions of perimeter baniers may also have frregular shapes. A perimeter banier having a cfrcular shape may advantageously enclose a larger area than other regular polygonal shapes that have the same perimeter. For example, for equal perimeters, a circular banier will enclose about 27% more area than a square banier. Using a circular perimeter banier may require fewer wells and/or less material to enclose a desired area with a perimeter banier than would other regular perimeter banier shapes. In some embodiments, square, rectangular or other polygonal perimeter baniers are used to conform to property lines and or to accommodate a regular well pattern of heat sources and production wells.

A formation that is to be freated using an in situ conversion process may be separated into several treatment areas by perimeter baniers. FIG. 213 depicts an embodiment of a perimeter banier anangement for a portion of a formation that is to be processed using substantially rectangular treatment areas 8000. A perhneter banier for treatment area 8000 may be formed when needed. The complete pattern of perimeter baniers for all of the formation to be subjected to in situ conversion does not need to be formed prior to treating individual freatment areas.

Perimeter baniers having circular or arced portions may be placed in a formation in a regular pattern. Centers of the circular or arced portions may be positioned at apices of imaginary polygon patterns. For example, FIG. 218 depicts a pattern of perimeter baniers wherein a unit of the pattern is based on an equilateral triangle.

FIG. 219 depicts a pattern of perimeter barriers wherein a unit of the pattern is based on a square. Perimeter banier patterns may also be based on higher order polygons.

FIG. 218 depicts a plan view representation of a perimeter banier embodiment that forms freatment areas 8000 in a formation. Centers of arced portions of perimeter baniers 8002 are positioned at apices of imaginary equilateral triangles. The imaginary equilateral triangles are depicted as dashed lines. First circular banier 8002' may be formed in the formation to define first freatment area 8000'.

Second banier 8002" may be formed. Second banier 8002" and portions of first banier 8002' may define second freatment area 8000". Second banier 8002" may have an arced portion with a radius that is substantially equal to the radius of first circular banier 8002'. The center of second banier 8002" may be located such that if the second banier were formed as a complete circle, the second banier would contact the first banier substantially at a tangent point. Second banier 8002" may include linear sections 8014 that allow for a larger area to be enclosed for the same or a lesser length of perimeter banier than would be needed to complete the second banier as a circle. In some embodiments, second banier 8002" may not include linear sections and the second banier may contact the first banier at a tangent point or at a tangent region. Second freatment area 8000" may be defined by portions of ffrst circular banier 8002' and second banier 8002". The area of second treatment area 8000" may be larger than the area of ffrst freatment area 8000'.

Third banier 8002'" may be foπned adjacent to first banier 8002' and second banier 8002". Third banier 8002'" may be connected to first banier 8002' and second banier 8002" to define third freatment area 8000'". Additional baniers may be formed to form freatment areas for processing desired portions of a foπnation.

FIG. 219 depicts a plan view representation of a perimeter banier embodiment that forms treatment areas 8000 in a formation. Centers of arced portions of perimeter barriers 8002 are positioned at apices of imaginary squares. The imaginary squares are depicted as dashed lines. Ffrst cfrcular banier 8002' may be formed in the formation to define first freatment area 8000' . Second barrier 8002" may be formed around a portion of second treatment area 8000". Second banier 8002" may have an arced portion with a radius that is substantially equal to the radius of first circular barrier 8002'. The center of second banier 8002" may be located such that if the second banier were foπned as a complete circle, the second banier would contact the first banier at a tangent point.

Second banier 8002" may include linear sections 8014 that allow for a larger area to be enclosed for the same or a lesser length of perimeter banier than would be needed to complete the second banier as a circle. Two additional perimeter baniers may be formed to complete a unit of four freatment areas.

In some embodiments, central area 8016 may be isolated by perimeter banier 8002. For perimeter baniers based on a square pattern, such as the perimeter baniers depicted in FIG. 219, central area 8016 may be a square. A length of a side of the square may be up to about 0.586 times a radius of an arc section of a perimeter banier. Surface facilities, or a portion of the surface facilities, used to treat fluid removed from the foπnation may be located in cenfral area 8016. In other embodiments, perimeter banier segments that form a central area may not be installed. FIG. 220 depicts an embodhnent of a banier configuration in which perimeter baniers 8002 are formed radially about a cenfral point. In an embodiment, surface facilities for processing production fluid removed from the formation are located within cenfral area 8016 defined by first banier 8002'. Locating the surface facilities in the center may reduce the total length of piping needed to transport formation fluid to the treatment facilities. In alternate embodiments, ICP wells are installed in the cenfral area and surface facilities are located outside of the pattern of baniers.

A ring of formation between second banier 8002" and first banier 8002' may be treatment area 8000'. Thfrd banier 8002'" may be formed around second banier 8002". The pattern of baniers may be extended as needed. A ring of formation between an inner banier and an outer banier may be a freatment area. If the area of a ring is too large to be freated as a whole, linear sections 8014 extending from the inner banier to the outer banier may be formed to divide the ring into a number of treatment areas. In some embodiments, distances between banier rings may be substantially the same. In other embodiments, a distance between banier rings may be varied to adjust the area enclosed by the baniers.

In some embodiments of in situ conversion processes, formation water may be removed from a freatment area before, during, and/or after formation of a banier around the fonnation. Heat sources, production wells, and other ICP wells may be installed in the formation before, during, or after formation of the banier. Some of the production wells may be coupled to pumps that remove foπnation water from the freatment area. In other embodiments, dewatering wells may be formed within the freatment area to remove formation water from the freatment area. Removing formation water from the treatment area prior to heating to pyrolysis temperatures for in situ conversion may reduce the energy needed to raise portions of the foπnation within the treatment area to pyrolysis temperatures by eliminating the need to vaporize all fonnation water initially within the treatment area. In some embodiments of in situ conversion processes, freeze wells may be used to form a low temperature zone around a portion of a freatment area. "Freeze well" refers to a well or opening in a formation used to cool a portion of the formation. In some embodiments, the cooling may be sufficient to cause freezing of materials (e.g., formation water) that may be present in the formation. In other embodiments, the cooling may not cause freezing to occur; however, the cooling may serve to inhibit the flow of fluid into or out of a treatment area by filling a portion of the pore space with liquid fluid.

In some embodiments, freeze wells may be used to form a side perimeter banier, or a portion of a side perimeter banier, in a formation. In some embodiments, freeze wells may be used to form a bottom perimeter banier, or a portion of a bottom perimeter banier, underneath a fonnation. In some embodiments, freeze wells may be used to form a top perimeter banier, or a portion of a top perimeter banier, above a formation. In some embodiments, freeze wells may be maintained at temperatures significantly colder than a freezing temperature of formation water. Heat may transfer from the formation to the freeze wells so that a low temperature zone is foπned around the freeze wells. A portion of formation water that is in, or flows into, the low temperature zone may freeze to form a banier to fluid flow. Freeze wells may be spaced and operated so that the low temperature zone formed by each freeze well overlaps and connects with a low temperature zone formed by at least one adjacent freeze well.

Sections of freeze wells that are able to form low temperature zones may be only a portion of the overall length of the freeze wells. For example, a portion of each freeze well may be insulated adjacent to an overburden so that heat transfer between the freeze wells and the overburden is inhibited. The freeze wells may form a low temperature zone along sides of a hydrocarbon containing portion of the formation. The low temperature zone may extend above and/or below a portion of the hydrocarbon containing layer to be treated by in situ conversion. The ability to use only portions of freeze wells to form a low temperature zone may allow for economic use of freeze wells when forming baniers for treatment areas that are relatively deep within the fonnation.

A perimeter banier formed by freeze wells may have several advantages over perimeter baniers formed by other methods. A perimeter banier formed by freeze wells may be fonned deep within the ground. A perimeter banier formed by freeze wells may not require an interconnected opening around the perimeter of a freatment area.

An interconnected opening is typically needed for grout walls and some other types of perimeter baniers. A perimeter banier formed by freeze wells develops due to heat fransfer, not by mass transfer. Gel, polymer, and some other types of perimeter baniers depend on mass transfer within the foπnation to form the perimeter banier. Heat fransfer in a formation may vary throughout a formation by a relatively small amount (e.g., typically by less than a factor of 2 within a formation layer). Mass fransfer in a formation may vary by a much greater amount throughout a formation (e.g., by a factor of 10^s or more within a formation layer). A perimeter banier formed by freeze wells may have greater integrity and be easier to form and maintain than a perimeter banier that needs mass fransfer to form.

A perimeter banier formed by freeze wells may provide a theπnal banier between different freatment areas and between sunounding portions of the fonnation that are to remain untreated. The thermal banier may allow adjacent freatment areas to be subjected to different processes. The freatment areas may be operated at different pressures, temperatures, heating rates, and/or formation fluid removal rates. The thermal banier may inhibit hydrocarbon material on an outer side of the banier from being pyrolyzed when the freatment area is heated.

Forming a frozen perimeter banier around a freatment area with freeze wells may be more economical and beneficial over the life of an in situ conversion process than operating dewatering wells around the freatment area. Freeze wells may be less expensive to install, operate, and maintain than dewatering wells. Casings for dewatering wells may need to be fonned of conosion resistant metals to withstand conosion from foπnation water over the life of an in situ conversion process. Freeze wells may be made of carbon steel. Dewatering wells may enhance the spread of formation fluid from a treatment area. Water produced from dewatering wells may contain a portion of formation fluid. Such water may need to be freated to remove hydrocarbons and other material before the water can be released. Dewatering wells may inhibit the ability to raise pressure within a treatment area to a desired value since dewatering wells are constantly removing fluid from the fonnation.

Water presence in a low temperature zone may allow for the formation of a frozen banier. The frozen banier may be a monolithic, impermeable structure. After the frozen banier is established, the energy requirements needed to maintain the frozen banier may be significantly reduced, as compared to the energy costs needed to establish the frozen banier. In some embodiments, the reduction in cost may be a factor of 10 or more. In other embodiments, the reduction in cost may be less dramatic, such as a reduction by a factor of about 3 or 4.

In many formations, hydrocarbon containing portions of the formation are saturated or contain sufficient amounts of formation water to allow for formation of a frozen banier. hi some formations, water may be added to the formation adjacent to freeze wells after and or during formation of a low temperature zone so that a frozen banier will be formed.

In some in situ conversion embodiments, a low temperature zone may be formed around a freatment area. During heating of the tt-eatment area, water may be released from the treatment area as steam and/or enfrained water in formation fluids. In general, when a freatment area is initially heated, water present in the foπnation is mobilized before substantial quantities of hydrocarbons are produced. The water may be free water and/or released water that was attached or bound to clays or minerals ("bound water"). Mobilized water may flow into the low temperature zone. The water may condense and subsequently solidify in the low temperature zone to form a frozen banier.

Pyrolyzing hydrocarbons and/or oxidizing hydrocarbons may form water vapor during in situ conversion. A significant portion of the generated water vapor may be removed from the foπnation through production wells. A small portion of the generated water vapor may migrate towards the perimeter of the freatment area. As the water approaches the low temperature zone fonned by the freeze wells, a portion of the water may condense to liquid water in the low temperature zone. If the low temperature zone is cold enough, or if the liquid water moves into a cold enough portion of the low temperature zone, the water may solidify.

In some embodiments, freeze wells may form a low temperature zone that does not result in solidification of formation fluid. For example, if there is insufficient water or other fluid with a relatively high freezing point in the foπnation around the freeze wells, then the freeze wells may not form a frozen banier. Instead, a low temperature zone may be formed. During an in situ conversion process, formation fluid may migrate into the low temperature zone. A portion of formation fluid (e.g., low freezing point hydrocarbons) may condense in the low temperature zone. The condensed fluid may fill pore space within the low temperature zone. The condensed fluid may form a banier to additional fluid flow into or out of the low temperature zone. A portion of the formation fluid (e.g., water vapor) may condense and freeze within the low temperature zone to form a frozen banier. Condensed formation fluid and or solidified formation fluid may form a banier to further fluid flow into or out of the low temperature zone.

Freeze wells may be initiated a significant time in advance of mitiation of heat sources that will heat a freatment area. Initiating freeze wells in advance of heat source initiation may allow for the formation of a thick interconnected frozen perimeter banier before formation temperature in a freatment area is raised. In some embodiments, heat sources that are located a large distance away from a perimeter of a freatment area may be initiated before, simultaneously with, or shortly after initiation of freeze wells.

Heat sources may not be able to break through a frozen perimeter banier during thermal freatment of a treatment area. In some embodhnents, a frozen perimeter banier may continue to expand for a significant time after heating is initiated. Thennal diffusivity of a hot, dry formation may be significantly smaller than thermal diffiisivity of a frozen foπnation. The difference in thermal diffusivities between hot, dry formation and frozen formation implies that a cold zone will expand at a faster rate than a hot zone. Even if heat sources are placed relatively close to freeze wells that have foπned a frozen banier (e.g., about 1 m away from freeze wells that have established a frozen barrier), the heat sources will typically not be able to break through the frozen banier if coolant is supplied to the freeze wells. In certain ICP system embodiments, freeze wells are positioned a significant distance away from the heat sources and other ICP wells. The distance may be about 3 m, 5 m, 10 m, 15 m, or greater.

The frozen banier formed by the freeze wells may expand on an outward side of the perhneter banier even when heat sources heat the formation on an inward side of the perimeter banier.

FIG. 213 depicts a representation of freeze wells 8012 installed in a formation to form low temperature zones 8017 around freatment areas 8000. Fluid in low temperature zones 8017 with a freezing point above a temperature of the low temperature zones may solidify in the low temperature zones to form perimeter banier 8002. Typically, the fluid that solidifies to form perimeter banier 8002 will be a portion of formation water. Two or more rows of freeze wells may be installed around treatment area 8000 to form a thicker low temperature zone 8017 than can be formed using a single row of freeze wells. FIG. 221 depicts two rows of freeze wells 8012 around freatment area 8000. Freeze wells 8012 may be placed around all of treatment area 8000, or freeze wells may be placed around a portion of the freatment area. In some embodiments, natural fluid flow baniers (such as unfractured, substantially unpeπneable formation material) and/or artificial baniers (e.g., grout walls or interconnected sheet baniers) sunound remaining portions of the freatment area when freeze wells do not sunound all of the freatment area. If more than one row of freeze wells sunounds a freatment area, the wells in a first row may be staggered relative to wells in a second row. In the freeze well a angement embodhnent depicted in FIG. 221, first separation distance 8018 exists between freeze wells 8012 in a row of freeze wells. Second separation distance 8020 exists between freeze wells 8012 in a first row and a second row. Second separation distance 8020 may be about 10-75% (e.g., 30-60% or 50%) of first separation distance 8018. Other separation distances and freeze well patterns may also be used.

FIG. 217 depicts an embodiment of an ICP system with freeze wells 8012 that form low temperature zone 8017 below a portion of a formation, a low temperature zone above a portion of a formation, and a low temperature zone along a perimeter of a portion of the formation. Portions of heat sources 8022 and portions of production wells 8024 may pass through low temperature zone 8017 formed by freeze wells 8012. The portions of heat sources 8022 and production wells 8024 that pass through low temperature zone 8017 may be insulated to inhibit heat fransfer to the low temperature zone. The insulation may include, but is not limited to, foamed cement, an afr gap between an insulated liner placed in the production well, or a combination thereof.

A portion of a freeze well that is to form a low temperature zone in a formation may be placed in the formation in deshed spaced relation to an adjacent freeze well or freeze wells so that low temperature zones formed by the individual freeze wells interconnect to form a continuous low temperature zone. In some freeze well embodiments, each freeze well may have two or more sections that allow for heat fransfer with an adjacent formation. Other sections of the freeze wells may be insulated to inhibit heat transfer with the adjacent formation. Freeze wells may be placed in the formation so that there is minimal deviation in orientation of one freeze well relative to an adjacent freeze well. Excessive deviation may create a large separation distance between adj acent freeze wells that may not permit formation of an interconnected low temperature zone between the adjacent freeze wells. Factors that may influence the manner in which freeze wells are inserted into the ground include, but are not limited to, freeze well insertion time, depth that the freeze wells are to be inserted, formation properties, desired well orientation, and economics. Relatively low depth freeze wells may be impacted and or vibrationally inserted into some formations. Freeze wells may be impacted and/or vibrationally inserted into formations to depths from about 1 m to about 100 m without excessive deviation in orientation of freeze wells relative to adjacent freeze wells in some types of formations. Freeze wells placed deep in a formation or in formations with layers that are difficult to drill through may be placed in the formation by directional drilling and/or geosteering. Directional drilling with steerable motors uses an inclinometer to guide the drilling assembly. Periodic gyro logs are obtained to conect the path. An example of a dfrectional drilling system is VertiTrak™ available from Baker Hughes Inteq (Houston, Texas). Geosteering uses analysis of geological and survey data from an actively drilling well to estimate stratigraphic and structural position needed to keep the wellbore advancing in a desired direction. Elecfrical, magnetic, and/or other signals produced in an adjacent freeze well may also be used to guide directionally drilled wells so that a desired spacing between adjacent wells is maintained. Relatively tight control of the spacing between freeze wells is an important factor in minimizing the time for completion of a low temperature zone.

FIG. 222 depicts a representation of an embodiment of freeze well 8012 that is directionally drilled into a formation. Freeze well 8012 may enter the formation at a first location and exit the foπnation at a second location so that both ends of the freeze well are above the ground surface. Refrigerant flow through freeze well 8012 may reduce the temperature of the formation adjacent to the freeze well to form low temperature zone 8017. Refrigerant passing through freeze well 8012 may be passed through an adjacent freeze well or freeze wells. Temperature of the refrigerant may be monitored. When the refrigerant temperature exceeds a desired value, the refrigerant may be directed to a refrigeration unit or units to reduce the temperature of the refrigerant before recycling the refrigerant back into the freeze wells. The use of freeze wells that both enter and exit the formation may eliminate the need to accommodate an inlet refrigerant passage and an outlet refrigerant passage in each freeze well. Freeze well 8012 depicted in the embodiment of FIG. 222 forms part of frozen banier 8002 below water body 8026. Water body 8026 may be any type of water body such as a pond, lake, sfream, or river. In some embodiments, the water body may be a subsurface water body such as an underground sfream or river. Freeze well 8012 is one of many freeze wells that may inhibit downward migration of water from water body 8026 to hydrocarbon containing layer 516. FIG. 223 depicts a representation of freeze wells 8012 used to form a low temperature zone on a side of hydrocarbon containing layer 516. In some embodiments, freeze wells 8012 may be placed in a non-hydrocarbon containing layer that is adjacent to hydrocarbon containing layer 516. In the depicted embodhnent, freeze wells 8012 are oriented along dip of hydrocarbon containing layer 516. In some embodiments, freeze wells may be inserted into the formation from two different dfrections or substantially peφendicular to the ground surface to limit the length of the freeze wells. Freeze well 8012' and other freeze wells may be inserted into hydrocarbon containing layer 516 to form a perimeter banier that inhibits fluid flow along the hydrocarbon containing layer. If needed, additional freeze wells may be installed to form perimeter baniers to inhibit fluid flow into or from overburden 540 or underburden 8010.

As depicted in FIG. 216, freeze wells 8012 may be positioned within a portion of a foπnation. Freeze wells 8012 and ICP wells may extend through overburden 540, through hydrocarbon layer 516, and into underburden 8010. In some embodiments, portions of freeze wells and ICP wells extending through the overburden

540 may be insulated to inhibit heat fransfer to or from the sunounding foπnation.

In some embodiments, dewatering wells 8028 may extend into formation 516. Dewatering wells 8028 may be used to remove formation water from hydrocarbon containing layer 516 after freeze wells 8012 form perimeter banier 8002. Water may flow through hydrocarbon containing layer 516 in an existing fracture system and channels. Only a small number of dewatering wells 8028 may be needed to dewater freatment area 8000 because the formation may have a large permeability due to the existing fracture system and channels. Dewatering wells 8028 may be placed relatively close to freeze wells 8012. In some embodiments, dewatering wells may be temporarily sealed after dewatering. If dewatering wells are placed close to freeze wells or to a low temperature zone foπned by freeze wells, the dewatering wells may be filled with water. Expanding low temperature zone 8017 may freeze the water placed in the freeze wells to seal the freeze wells. Dewatering wells 8028 may be re-opened after completion of in situ conversion. After in situ conversion, dewatering wells 8028 may be used during clean up procedures for injection or removal of fluids.

In some embodiments, selected production wells, heat sources, or other types of ICP wells may be temporarily converted to dewatering wells by attaching pumps to the selected wells. The converted wells may supplement dewatering wells or eliminate the need for separate dewatering wells. Converting other wells to dewatering wells may eliminate costs associated with drilling wellbores for dewatering wells.

FIG. 224 depicts a representation of an embodiment of a well system for freating a fonnation. Hydrocarbon containing layer 516 may include leached/fractured portion 8030 and non-leached/non-fractured portion 8032. Formation water may flow through leached/fractured portion 8030. Non-leached/non-fractured portion 8032 may be unsaturated and relatively dry. In some formations, leached/fractured portion 8030 may be beneath 100 m or more of overburden 540, and the leached/fractured portion may extend 200 m or more into the formation. Non-leached/non-fractured portion 8032 may extend 400 m or more deeper into the formation.

Heat sources 8022 may extend to underburden 8010 below non-leached/non-fractured portion 8032. Production wells may extend into the non-leached/non-fractured portion of the foπnation. The production wells may have perforations, or be open wellbores, along the portions extending into the leached/fractured portion and non-leached/non-fractured portions of the hydrocarbon containing layer. Freeze wells 8012 may extend close to, or a short distance into, non-leached non-fractured portion 8032. Freeze wells 8012 may be offset from heat sources 8022 and production wells a distance sufficient to allow hydrocarbon material below the freeze wells to remain unpyrolyzed during freatment of the formation (e.g., about 30 m). Freeze wells 8012 may inhibit formation water from flowing into hydrocarbon containing layer 516. Advantageously, freeze wells 8012 do not need to extend along the full length of hydrocarbon material that is to be subjected to in situ conversion, because non-leached non- fractured portion 8032 beneath freeze wells 8012 may remain untreated. If treatment of the formation generates thermal fractures in the non-leached/non-fractured portion 8032 that propagate towards and/or past freeze wells 8012, the fractures may remain substantially horizontally oriented. Horizontally oriented fractures will not intersect the leached/fractured portion 8030 to allow formation water to enter into freatment area 8000. Various types of refrigeration systems may be used to form a low temperature zone. Determination of an appropriate refrigeration system may be based on many factors, including, but not limited to: type of freeze well; a distance between adjacent freeze wells; refrigerant; time frame in which to form a low temperature zone; depth of the low temperature zone; temperature differential to which the refrigerant will be subjected; chemical and physical properties of the refrigerant; environmental concerns related to potential refrigerant releases, leaks, or spills; economics; formation water flow in the formation; composition and properties of formation water; and various properties of the formation such as thermal conductivity, thennal diffusivity, and heat capacity.

Several different types of freeze wells may be used to form a low temperature zone. The type of freeze well used may depend on the type of refrigeration system used to form a low temperature zone. The type of refrigeration system may be, but is not limited to, a batch operated refrigeration system, a circulated fluid refrigeration system, a refrigeration system that utilizes a vaporization cycle, a refrigeration system that utilizes an adsoφtion-desoφtion refrigeration cycle, or a refrigeration system that uses an absoφtion-desoφtion refrigeration cycle. Different types of refrigeration systems may be used at different times during formation and/or maintenance of a low temperature zone. In some embodiments, freeze wells may include casings. In some embodiments, freeze wells may include perforated casings or casings with other types of openings. In some embodiments, a portion of a freeze well may be an open wellbore.

A batch operated refrigeration system may utilize a plurality of freeze wells. A refrigerant is placed in the freeze wells. Heat fransfers from the formation to the freeze wells. The refrigerant may be replenished or replaced to maintain the freeze wells at desired temperatures.

FIG. 225 depicts an embodiment of batch operated freeze well 8012. Freeze well 8012 may include casing 8034, inlet conduit 8036, vent conduit 8038, and packing 8040. Packing 8040 may be fonned near a top of where a low temperature zone is to be foπned in a formation. In some embodiments, packing is not utilized. Inlet conduit 8036 and/or vent conduit 8038 may extend through packing 8040. Refrigerant 8041 may be inserted into freeze well 8012 through inlet conduit 8036. Inlet conduit 8036 may be insulated, or formed of an insulating material, to inhibit heat fransfer to refrigerant 8041 as the refrigerant is transported through the inlet conduit. In an embodiment, inlet conduit 8036 is foπned of high density polyethylene. Vapor generated by heat fransfer between the formation and refrigerant 8041 may exit freeze well 8012 through vent conduit 8038. In some embodiments, a vent conduit may not be needed.

In some freeze well embodiments, a low temperature zone may be formed by batch operated freeze wells that do not include sealed casings. Portions of freeze wells may be open wellbores, and/or portions of the wellbores may include casings that have perforations or other types of openings. FIG. 226 depicts an embodiment of freeze well 8012 that includes an open wellbore portion. To use freeze wells that include open wellbore portions and/or perforations or other types of openings, water may be infroduced into the freeze wells to fill fractures and/or pore space within the formation adjacent to the wellbore. A pump may be used to remove excess water from the wellbore. In some embodiments, addition of water into the wellbore may not be necessary. Cryogenic refrigerant 8041, such as liquid nitrogen, may be infroduced into the wellbores to freeze material in the formation adjacent to the wellbores and seal any fractures or pore spaces of the formation that are adjacent to the freeze wells. Cryogenic refrigerant 8041 may be periodically replenished so that a frozen banier is formed and maintained. Alternately, a less cold, less expensive fluid, (such as a dry ice and low freezing point liquid bath) may be substituted for the cryogenic refrigerant after evaporation or removal of the cryogenic refrigerant from the wellbores. The less cold fluid may be used to form and/or maintain the frozen banier. A need to replenish refrigerant may make the use of batch operated freeze wells economical only for forming a low temperature zone around a relatively small freatment area. The need to replenish refrigerant may allow for economical operation of batch operated freeze wells only for relatively short periods of time. Batch operated freeze wells may advantageously be able to form a frozen banier in a short period of time, especially if a close freeze well spacing and a cryogenic fluid is used. Batch operated freeze wells may be able to form a frozen barrier even when there is a large fluid flow rate adjacent to the freeze wells. Batch operated freeze wells that use liquid nifrogen may be able to form a frozen banier when formation fluid flows at a rate of up to about 20 m/day. A circulated refrigeration system may utilize a plurality of freeze wells. A refrigerant may be circulated through the freeze wells and through a refrigeration unit. The refrigeration unit may cool the refrigerant to an initial refrigerant temperature. The freeze wells may be coupled together in series, parallel, or series and parallel combinations. The circulated refrigeration system may be a high volume system. When the system is initially started, the temperature difference between refrigerant entering a refrigeration unit and leaving a refrigeration unit may be relatively large (e.g., from about 10 °C to about 30 °C) and may quickly diminish. After formation of a frozen banier, the temperature difference may be 1 °C or less. It may be desirable for the temperature of the circulated refrigerant to be very low after the refrigerant passes through a refrigeration unit so that the refrigerant will be able to form a thick low temperature zone adjacent to the freeze wells. An initial working temperature of the refrigerant may be -25 °C, -40 °C, -50 °C, or lower.

FIG. 227 depicts an embodhnent of a circulated refrigerant type of refrigeration system that may be used to form low temperature zone 8017 around treatment area 8000. The refrigeration system may include refrigeration units 8042, cold side conduit 8044, warm side conduit 8046, and freeze wells 8012. Cold side conduits 8044 and warm side conduits 8046 (as shown in FIG. 224) may be made of insulated polymer piping such as HDPE (high- density polyethylene). Cold side conduits 8044 and warm side conduits 8046 may couple refrigeration units 8042 to freeze wells 8012 in series, parallel, or series and parallel anangements. The type of piping arrangement used to connect freeze wells 8012 to refrigeration units 8042 may depend on the type of refrigeration system, the number of refrigeration units, and the heat load required to be removed from the formation by the refrigerant. In some embodiments, freeze wells 8012 may be connected to refrigeration conduits 8044, 8046 in a parallel configuration as depicted in FIG. 227. Cold side conduit 8044 may fransport refrigerant from a first storage tank of refrigeration unit 8042 to freeze wells 8012. The refrigerant may travel through freeze wells 8012 to warm side conduit 8046. Warm side conduit 8046 may fransport the refrigerant to a second storage tank of refrigeration unit 8042. Parallel configurations for refrigeration systems may be utilized when a low temperature zone extends for a long length (e.g., 50 m or longer). Several refrigeration systems may be needed to form a perhneter banier around a freatment area.

In some embodhnents, freeze wells may be connected to refrigeration conduits in parallel and series configurations. Two or more freeze wells may be coupled together in a series piping anangement to form a group. Each group may be coupled in a parallel piping anangement to the cold side conduit and the warm side conduit. A circulated fluid refrigeration system may utilize a liquid refrigerant that is circulated through freeze wells. A liquid circulation system utilizes heat fransfer between a circulated liquid and the formation without a significant portion of the refrigerant undergoing a phase change. The liquid may be any type of heat fransfer fluid able to function at cold temperatures. Some of the desired properties for a liquid refrigerant are: a low working temperature, low viscosity, high specific heat capacity, high thermal conductivity, low conosiveness, and low toxicity. A low working temperature of the refrigerant allows for formation of a large low temperature zone around a freeze well. A low working temperature of the liquid should be about -20 °C or lower. Fluids having low working temperatures at or below -20 °C may include certain salt solutions (e.g., solutions containing calcium chloride or lithium chloride). Other salt solutions may include salts of certain organic acids (e.g., potassium formate, potassium acetate, potassium citrate, ammonium formate, ammonium acetate, ammonium citrate, sodium cifrate, sodium formate, sodium acetate). One liquid that may be used as a refrigerant below -50 °C is Freezium®, available from Kemfra Chemicals (Helsinki, Finland). Another liquid refrigerant is a solution of ammonia and water with a weight percent of ammonia between about 20 % and about 40 %.

A refrigerant that is capable of being chilled below a freezing temperature of formation water may be used to form a low temperature zone. The following equation (the Sanger equation) may be used to model the time t_t needed to form a frozen banier of radius R around a freeze well having a surface temperature of T_s:

c '_Vvff^v"s

in which:

a_r =

R

In these equations, kf is the thermal conductivity of the frozen material; c_v and c_v„are the volumefric heat capacity of the frozen and unfrozen material, respectively; r₀ is the radius of the freeze well; v_s is the temperature difference between the freeze well surface temperature T_s and the freezing point of water T₀; v₀ is the temperature difference between the ambient ground temperature T_g and the freezing point of water T₀; L is the volumefric latent heat of freezing of the formation; R is the radius at the frozen-unfrozen interface; and R_A is a radius at which there is no influence from the refrigeration pipe. The temperature of the refrigerant is an adjustable variable that may significantly affect the spacing between refrigeration pipes.

It is expected that reducing refrigerant temperature may reduce the time needed to form an interconnected low temperature zone sufficiently cold to freeze formation water. In certain circumstances (e.g., where hydrocarbon containing portions of a formation are deeper than about

300 m), it may be desirable to minimize the number of freeze wells (i.e., increase freeze well spacing) to improve project economics. Using a refrigerant that can go to low temperatures allows for the use of a large freeze well spacing.

ΕQN. 69 implies that a large low temperature zone may be formed by using a refrigerant having an initial temperature that is very low. To form a low temperature zone for in situ conversion processes for formations, the use of a refrigerant having an initial cold temperature of about -50 °C or lower may be desirable. Refrigerants having initial temperatures warmer than about -50 °C may also be used, but such refrigerants may requfre longer times for the low temperature zones produced by individual freeze wells to connect. In addition, such refrigerants may require the use of closer freeze well spacings and/or more freeze wells.

A refrigeration unit may be used to reduce the temperature of a refrigerant liquid to a low working temperature. In some embodiments, the refrigeration unit may utilize an ammonia vaporization cycle. Refrigeration units are available from Cool Man Inc. (Milwaukee, Wisconsin), Gartner Refrigeration &

Manufacturing (Minneapolis, Minnesota), and other suppliers. In some embodiments, a cascading refrigeration system may be utilized with a first stage of ammonia and a second stage of carbon dioxide. The circulating refrigerant through the freeze wells may be 30 weight % ammonia in water (aqua ammonia).

In some embodiments, ref igeration units for chilling refrigerant may utilize an absoφtion-desoφtion cycle. An absoφtion refrigeration unit may produce temperatures down to about -60 °C using thermal energy.

Thermal energy sources used in the desoφtion unit of the absoφtion refrigeration unit may include, but are not limited to, hot water, steam, formation fluid, and/or exhaust gas. In some embodiments, ammonia is used as the refrigerant and water as the absorbent in the absoφtion refrigeration unit. Absoφtion refrigeration units are available from Stork Thermeq B.V. (Hengelo, The Netherlands). A vaporization cycle refrigeration system may be used to form and/or maintain a low temperature zone. A liquid refrigerant may be infroduced into a plurality of wells. The refrigerant may absorb heat from the formation and vaporize. The vaporized refrigerant may be circulated to a refrigeration unit that compresses the refrigerant to a liquid and reinfroduces the refrigerant into the freeze wells. The refrigerant may be, but is not limited to, ammonia, carbon dioxide, or a low molecular weight hydrocarbon (e.g., propane). After vaporization, the fluid may be recompressed to a liquid in a refrigeration unit or refrigeration units and circulated back into the freeze wells. The use of a circulated refrigerant system may allow economical formation and/or maintenance of a long low temperature zone that sunounds a large treatment area. The use of a vaporization cycle refrigeration system may require a high pressure piping system.

FIG. 228 depicts an embodiment of freeze well 8012. Freeze well 8012 may include casing 8034, inlet conduit 8036, spacers 8052, and wellcap 8051. Spacers 8052 may position inlet conduit 8036 within casing 8034 so that an annular space is formed between the casing and the conduit. Spacers 8052 may promote turbulent flow of refrigerant in the annular space between inlet conduit 8036 and casing 8034, but the spacers may also cause a significant fluid pressure drop. Turbulent fluid flow in the annular space may be promoted by roughening the inner surface of casing 8034, by roughening the outer surface of inlet conduit 8036, and or by having a small cross- sectional area annular space that allows for high refrigerant velocity in the annular space. In some embodiments, spacers are not used.

Refrigerant may flow through cold conduit 8044 from a refrigeration unit to inlet conduit 8036 of freeze well 8012. The refrigerant may flow through an annular space between inlet conduit 8036 and casing 8034 to warm side conduit 8046. Heat may fransfer from the formation to casing 8034 and from the casing to the refrigerant in the annular space. Inlet conduit 8036 may be insulated to inhibit heat fransfer to the refrigerant during passage of the refrigerant into freeze well 8012. In an embodiment, inlet conduit 8036 is a high density polyethylene tube. In other embodiments, inlet conduit 8036 is an insulated metal tube.

FIG. 229 depicts an embodiment of circulated refrigerant freeze well 8012. Refrigerant may flow through U-shaped conduit 8054 that is suspended or packed in casing 8034. Suspending conduit 8054 in casing 8034 may advantageously provide thermal contraction and expansion room for the conduit. In some embodiments, spacers may be positioned at selected locations along the length of the conduit to inhibit conduit 8054 from contacting casing 8034. Typically, preventing conduit 8054 from contacting casing 8034 is not needed, so spacers are not used. Casing 8034 may be filled with a low freezing point heat fransfer fluid to enhance thermal contact and promote heat fransfer between the formation, casing, and conduit 8054. In some embodiments, water or other fluid that will solidify when refrigerant flows through conduit 8054 may be placed in casing 8034. The solid formed in casing 8034 may enhance heat fransfer between the formation, casing, and refrigerant within conduit 8054.

Portions of conduit 8054 adjacent to the formation that are not to be cooled may be foπned of an insulating material (e.g., high density polyethylene) and/or the conduit portions may be insulated. Portions of conduit 8054 adjacent to the formation that are to be cooled may be formed of a thermally conductive metal (e.g., copper or a copper alloy) to enhance heat fransfer between the foπnation and refrigerant within the conduit portion. In some freeze well embodiments, U-shaped conduits may be suspended or packed in open wellbores or in perforated casings instead of in sealed casings. FIG. 230 depicts an embodiment of freeze well 8012 having an open wellbore portion. Open wellbores and/or perforated casings may be used when water or other fluid is to be introduced into the formation from the freeze wells. Water may be infroduced into the formation to promote formation of a frozen banier. Water may be introduced into the formation through freeze wells during cleanup procedures after completion of an in situ conversion process (e.g., the freeze wells may be thawed and perforated for introduction of water). In some embodiments, open wellbores and/or perforated casings may be used when the freeze wells will later be converted to heat sources, production wells, and/or injection wells.

As depicted in FIG. 230, outlet leg 8056 of U-shaped conduit 8054 may be wrapped around inlet leg 8058 adjacent to a portion of the formation that is to be cooled. Wrapping outlet leg 8056 around inlet leg 8058 may significantly increase the heat transfer surface area of conduit 8054. Inlet leg and outlet leg adjacent to portions of the formation that are not to be cooled may be insulated and/or made of an insulating material. Conduits with an outlet leg wrapped around an inlet leg are available from Packless Hose, Inc. (Waco, Texas).

A time needed to fonn a low temperature zone may be dependent on a number of factors and variables. Such factors and variables may include, but are not limited to, freeze well spacing, refrigerant temperature, length of the low temperature zone, fluid flow rate into the treatment area, salinity of the fluid flowing into the treatment area, and the refrigeration system type, or refrigerant used to form the banier. The time needed to form the low temperature zone may range from about two days to more than a year depending on the extent and spacing of the freeze wells. In some embodiments, a time needed to form a low temperature zone may be about 6 to 8 months.

Spacing between adjacent freeze wells may be a function of a number of different factors. The factors may include, but are not limited to, physical properties of formation material, type of refrigeration system, type of refrigerant, flow rate of material into or out of a treatment area defined by the freeze wells, time for forming the low temperature zone, and economic considerations. Consolidated or partially consolidated formation material may allow for a large separation distance between freeze wells. A separation distance between freeze wells in consolidated or partially consolidated formation material may be from about 3 m to 10 m or larger. In an embodiment, the spacing between adjacent freeze wells is about 5 m. Spacing between freeze wells in unconsolidated or substantially unconsolidated formation material may need to be smaller than spacing in consolidated formation material. A separation distance between freeze wells in unconsolidated material may be 1 m or more.

Numerical simulations may be used to determine spacing for freeze wells based on known physical properties of the formation. A general puφose simulator, such as the Steam, Thermal and Advanced Processes

Reservofr Shnulator (STARS), may be used for numerical simulation work. Also, a simulator for freeze wells, such as TEMP W available from Geoslope (Calgary, Alberta), may be used for numerical simulations. The numerical simulations may include the effect of heat sources operating within a treatment area defined by the freeze wells.

It is believed that closer freeze well spacing decreases an amount of time required to form an interconnected low temperature zone capable of freezing formation water. A shorter distances between adjacent freeze wells may decrease the time necessary to form an interconnected low temperature zone.

The use of a specific type of refrigerant may be made based on a number of different factors. Such factors may include, but are not limited to, the type of refrigeration system employed, the chemical properties of the refrigerant, and the physical properties of the refrigerant.

Refrigerants may have different equipment requirements. For example, cryogenic refrigerants (e.g., liquid nifrogen) may induce greater temperature differentials than a brine solution. A required flow rate for a circulated cryogenic refrigerant system may be substantially lower than a required flow rate for a brine solution refrigerant to achieve a desired temperature in a formation. A required volume of cryogenic refrigerant for a batch refrigeration system may be large. The use of a cryogenic refrigerant may result in significant equipment savings, but the cost of reducing refrigerant to cryogenic temperatures may make the use of a cryogenic refrigeration system uneconomical. Fluid flow into a freatment area may inhibit formation of a frozen banier. Formations having high peπneability may have high fluid flow rates that inhibit fonnation of a frozen banier. Fluid flow rate may limit a residence time of a fluid in a low temperature zone around a freeze well. If fluid is flowing rapidly adjacent to a freeze well, a residence time of the fluid proximate the freeze well may be insufficient to allow the fluid to freeze in a cylindrical pattern around the freeze well. Fluid flow rate may influence the shape of a banier formed around freeze wells. A high flow rate may result in frregular low temperature zones around freeze wells. FIG. 231 depicts shapes of low temperature zones 8017 around freeze wells 8012 when foπnation water flows by the freeze wells at a rate that allows for formation of frozen perimeter banier 8002. Direction of formation water flow is indicated by anows 8073. As time passes, the frozen banier may expand outwards from the freeze wells. If the formation water flow rate is high enough, the fluid may inhibit overlap of low temperature zones 8017 between adjacent wells, as depicted in FIG. 232. In such a situation, formation fluid would continue to flow into a freatment area and formation of a frozen banier would be inhibited. To alleviate the problem of non-closure of the low temperature zone, additional freeze wells may be installed between the existing freeze wells, dewatering wells may be used to reduce formation fluid flow rate by the freeze wells to allow for formation of an interconnected low temperature zone, or other techniques may be used to reduce formation fluid flow to a rate that will allow low temperature zones from adjacent wells to interconnect so that a frozen banier forms.

In some embodiments, fluid flow into a freatment area may be inhibited to allow formation of a frozen banier by freeze wells. In an embodiment, dewatering wells may be placed in the formation to inhibit fluid flow past freeze wells during formation of a frozen banier. The dewatering wells may be placed far enough away from the freeze wells so that the dewatering wells do not create a flow rate past the freeze wells that inhibits formation of a frozen banier. In some embodiments, injection wells may be used to inject fluid into the formation so that fluid flow by the freeze wells is reduced to a level that will allow for formation of interconnected frozen baniers between adjacent freeze wells.

In an embodiment, freeze wells may be positioned between an inner row and an outer row of dewatering wells. The inner row of dewatering wells and the outer row of dewatering wells may be operated to have a minimal pressure differential so that fluid flow between the inner row of dewatering wells and the outer row of dewatering wells is minimized. The dewatering wells may remove formation water between the outer dewatering row and the inner dewatering row. The freeze wells may be initialized after removal of formation water by the dewatering wells. The freeze wells may cool the formation between the inner row and the outer row to form a low temperature zone. The power supplied to the dewatering wells may be reduced stepwise after the freeze wells foπn an interconnected low temperature zone that is able to solidify foπnation water. Reduction of power to the dewatering wells may allow some water to enter the low temperature zone. The water may freeze to form a frozen banier.

Operation of the dewatering wells may be ended when the frozen banier is fully formed.

In some formations, a combination batch refrigeration system and circulated fluid refrigeration system may be used to form a frozen banier when fluid flow into the foπnation is too high to allow fonnation of the frozen barrier using only the circulated refrigeration system. Batch freeze wells may be placed in the formation and operated with cryogenic refrigerant to form an initial frozen banier that inhibits or stops fluid flow towards freeze wells of a circulated fluid refrigeration system. Circulation freeze wells may be placed on a side of the batch freeze wells towards a freatment area. The batch freeze wells may be operated to form a perimeter banier that stops or reduces fluid flow to the circulation freeze wells. The cfrculation freeze wells may be operated to form a primary perimeter banier. After formation of the primary frozen banier, use of the batch freeze wells may be discontinued. Alternately, some or all of the batch operated freeze wells may be converted to circulation freeze wells that maintain and/or expand the initial banier formed by the batch freeze wells. Converting some or all of the batch freeze wells to circulation freeze wells may allow a thick frozen banier to be formed and maintained around a freatment area. In some embodiments, a combination of dewatering wells and batch operated freeze wells may be used to reduce fluid flow past circulation freeze wells so that the circulation freeze wells form a frozen banier. Open wellbore freeze wells may be utilized in some formations that have very low permeability. Freeze well wellbores may be formed in such formations. A frozen banier may initially be formed using a very cold fluid, such as liquid nitrogen, that is placed in casings of the freeze wells. After the very cold fluid forms an interconnected frozen banier around the treatment area, the very cold cryogenic fluid may be replaced with a circulated refrigerant that will maintain the frozen banier during in situ processing of the formation. For example, liquid nitrogen at a temperature of about -196 °C may be used to form an interconnected frozen banier around a treatment area by placing the liquid nitrogen within the freeze wells and replenishing the liquid nifrogen when necessary. The liquid nifrogen may be placed in an annular space between an inlet line and a casing in each freeze well. After the liquid nitrogen forms an interconnected frozen banier between adjacent freeze wells, the liquid nifrogen may be removed from the freeze wells. A fluid, such as a low freezing point alcohol, may be circulated into and out of the freeze wells to raise the temperature adjacent to the freeze wells. When the temperature of the well casing is sufficiently high to inhibit refrigerant, such as a brine solution, from solidifying in the freeze wells, the fluid may be replaced with the refrigerant. The refrigerant may be used to maintain the frozen banier.

FIG. 213 depicts freeze wells 8012 installed around freatment areas 8000. ICP wells 8004 may be installed in freatment areas 8000 prior to, simultaneously with, or after insertion of freeze wells 8012. In some embodiments, wellbores for ICP wells 8004 and/or freeze wells 8012 may be drilled into a formation. In other embodiments, wellbores may be formed when the wells are vibrationally inserted and/or driven into the formation. In some embodiments, well casings are formed of pipe segments. Connections between lengths of pipe may be self-sealing tapered threaded connections, and/or welded joints. In other embodiments, well casings may be inserted using coiled tubing installation. Integrity of coiled tubing may be tested before installation by hydrotesting at pressure. Coiled tubing installation may reduce a number of welded and/or threaded connections in a length of casing. Welds and or threaded connections in coiled tubing may be pre-tested for integrity (e.g., by hydraulic pressure testing). Coiled tubing may be installed more easily and faster than installation of pipe segments joined together by threaded and/or welded connections.

Embodiments of heat sources, production wells, and/or freeze wells may be installed in a fonnation using coiled tubing installation. Some embodiments of heat sources, production wells, and freeze wells include an element placed within an outer casing. For example, a conductor-in-conduit heater may include an outer casing with a conduit disposed in the casing. A production well may include a heater element or heater elements disposed within a casing. A freeze well may include a refrigerant inlet conduit disposed within a casing, or a U-shaped conduit disposed in a casing. Spacers may be spaced along a length of an element, or elements, positioned within a casing to inhibit the element, or elements, from contacting the casing walls. In some embodiments of heat sources, production wells, and freeze wells, casings may be installed using coiled tube installation. Elements may be placed within the casing after the casing is placed in the formation for heat sources or wells that include elements within the casings. In some embodiments, sections of casings ^'may be threaded and/or welded and inserted into a wellbore using a drilling rig. In some embodiments, elements may be placed within the casing before the casing is wound onto a reel. The elements within a casing are installed in a formation when the casing is installed in the formation. For example, a coiled tubing reel for forming a freeze well such as the freeze well depicted in FIG. 228 may include 8.9 cm (3.5 in.) outer diameter carbon steel coiled tubing with 5.1 cm (2 in.) outer diameter high density polyethylene tubing positioned inside the carbon steel tubing. During installation, a portion of the polyethylene tubing may be cut so that the polyethylene tubing will be recessed within the steel casing. A wellcap may be threaded and/or welded to the steel tubing to seal the end of the tubing. The coiled tubing may be inserted by a coiled tubing unit into the formation.

Care may be taken during design and installation of freeze well casing strings to allow for thermal confraction of the casing string when refrigerant passes through the casing. Allowance for thermal confraction may inhibit the development of sfress fractures and leaks in the casing. If a freeze well casing were to leak, leaking refrigerant may inhibit formation of a frozen banier or degrade an existing frozen banier. Water or other diluent may be used to flush the formation to diffuse released refrigerant if a leak occurs.

Diameters of freeze well casings installed in a fonnation may be oversized as compared to a minimum diameter needed to allow for foπnation of a low temperature zone. For example, if design calculations indicate that 10.2 cm (4 in.) piping is needed to provide sufficient heat transfer area between the formation and the freeze wells, 15.2 cm (6 in.) piping may be placed in the formation. The oversized casing may allow a sleeve or other type of seal to be placed into the casing should a leak develop in the freeze well casing.

In some embodiments, flow meters may be used to monitor for leaks of refrigerant within freeze wells. A first flow meter may measure an amount of refrigerant flow into a freeze well or a group of wells. A second flow meter may measure an amount of flow out of a freeze well or a group of freeze wells. A significant difference between the measurements taken by the first flow meter and the second flow meter may indicate a leak in the freeze well or in a freeze well of the group of freeze wells. A significant difference between the measurements may result in the activation of a solenoid valve that inhibits refrigerant flow to the freeze well or group of freeze wells.

Freeze well placement may vary depending on a number of factors. The factors may include, but are not limited to, predominant direction of fluid flow within the foπnation; type of refrigeration system used; spacing of freeze wells; and characteristics of the formation such as depth, length, thickness, and dip. Placement of freeze wells may also vary across a formation to account for variations in geological strata. In some embodiments, freeze wells may be inserted into hydrocarbon containing portions of a formation. In some embodiments, freeze wells may be placed near hydrocarbon containing portions of a formation. In some embodiments, some freeze wells may be positioned in hydrocarbon containing portions while other freeze wells are placed proximate the hydrocarbon containing portions. Placement of heat sources, dewatering wells, and/or production wells may also vary depending on the factors affecting freeze well placement. ICP wells may be placed a large distance away from freeze wells used to form a low temperature zone around a freatment area. In some embodiments, ICP wells may be positioned far enough away from freeze wells so that a temperature of a portion of formation between the freeze wells and the ICP wells is not influenced by the freeze wells or the ICP wells when the freeze wells have foπned an interconnected frozen banier and ICP wells have raised temperatures throughout a freatment area to pyrolysis temperatures. In some embodiments, ICP wells may be placed 20 m, 30 m, or farther away from freeze wells used to form a low temperature zone.

In some embodiments, ICP wells may be placed in a relatively close proximity to freeze wells. During in situ conversion, a hot zone established by heat sources and a cold zone established by freeze wells may reach an equilibrium condition where the hot zone and the cold zone do not expand towards each other. FIG. 233 depicts thermal simulation results after 1000 days when heat source 8022 at about 650 °C is placed at a center of a ring of freeze wells 8012 that are about 9.1 m away from the heat source and spaced at about 2.4 m intervals. The freeze wells are able to maintain frozen banier 8002 that extends over 1 m inwards towards the heat source. On an outer side of the freeze wells, the freeze banier is much thicker, and the freeze wells influence portions (e.g., low temperature zone 8017) of the formation up to about 15 m away from the freeze wells.

Thermal diffusivities and other properties of both saturated frozen formation material and hot, dry formation material may allow operation of heat sources close to freeze wells. These properties may inhibit the heat provided by the heat sources from breaking through a frozen banier established by the freeze wells. Frozen saturated formation material may have a significantly higher theπnal diffusivity than hot, dry formation material. The difference in the thermal diffusivity of hot, dry formation material and cold, saturated formation material predicts that a cold zone will propagate faster than a hot zone. Fast propagation of a cold zone established and maintained by freeze wells may inhibit a hot zone formed by heat sources from melting through the cold zone during thermal freatment of a freatment area.

In some embodiments, a heat source may be placed relatively close to a frozen banier fonned and maintained by freeze wells without the heat source being able to break through the frozen banier. Although a heat source may be placed close to a frozen banier, heat sources are typically placed 5 m or farther away from a frozen banier formed and maintained by freeze wells. In an embodiment, heat sources are placed about 30 m away from freeze wells. Since the heat sources may be placed relatively close to the frozen banier, a relatively large section of a formation may be treated without an excessive number of freeze wells. A number of freeze wells needed to sunound an area increases at a significantly lower rate than the number of ICP wells needed to thermally treat the surrounded area as the size of the sunounded area increases. This is because the surface-to-volume ratio decreases with the radius of a freated volume.

Measurable properties and/or testing procedures may indicate formation of a frozen banier. For example, if dewatering is taking place on an inner side of freeze wells, the amount of water removed from the fonnation through dewatering wells may significantly decrease as a frozen banier fonns and blocks recharge of water into a freatment area. A freatment area may be saturated with formation water. When a frozen perimeter banier is formed around the freatment area, water recharge and removal from the freatment area is stopped. The frozen perimeter banier may continue to expand. Expansion of the perimeter banier may cause the hydrostatic head (i.e., piezomefric head) in the freatment area to rise as compared to the hydrostatic head of formation outside of the frozen banier. The hydrostatic head in the banier may rise because the water in the formation is confined in an increasingly smaller volume as the frozen banier expands inwards. The hydrostatic change may be relatively small, but still measurable. Piezometers placed inside and outside of a ring of freeze wells may be used to deteπnine when a frozen banier is foπned based on hydrostatic head measurements.

In addition, transient pressure testing (e.g., drawdown tests or injection tests) in the treatment area may indicate foπnation of a frozen banier. Such fransient pressure tests may also indicate the permeability at the banier. Pressure testing is described in Pressure Buildup and Flow Tests in Wells by C. S. Matthews & D.G. Russell (SPE Monograph, 1967).

A fransient fluid pulse test may be used to deteπnine or confirm fonnation of a perimeter banier. A freatment area may be saturated with formation water after formation of a perimeter banier. A pulse may be instigated inside a freatment area sunounded by the perimeter banier. The pulse may be a pressure pulse that is produced by pumping fluid (e.g., water) into or out of a wellbore. In some embodiments, the pressure pulse may be applied in incremental steps, and responses may be monitored after each step. After the pressure pulse is applied, the transient response to the pulse may be measured by, for example, measuring pressures at monitor wells and/or in the well in which the pressure pulse was applied. Monitoring wells used to detect pressure pulses may be located outside and/or inside of the freatment area.

In some embodiments, a pressure pulse may be applied by drawing a vacuum on the formation through a wellbore. If a frozen barrier is formed, a portion of the pulse will be reflected by the frozen banier back towards the source of the pulse. Sensors may be used to measure response to the pulse. In some embodiments, a pulse or pulses are instigated before freeze wells are initialized. Response to the pulses is measured to provide a base line for future responses. After formation of a perimeter banier, a pressure pulse initiated inside of the perimeter banier should not be detected by monitor wells outside of the perimeter banier. Reflections of the pressure pulse measured within the freatment area may be analyzed to provide information on the establishment, thickness, depth, and other characteristics of the frozen banier.

In certain embodhnents, hydrostatic pressures will tend to change due to natural forces (e.g., tides, water recharge, etc.). A sensitive piezometer (e.g., a quartz crystal sensor) may be able to accurately monitor natural hydrostatic pressure changes. Fluctuations in natural hydrostatic pressure changes may indicate formation of a frozen banier around a treatment area. For example, if areas sunounding the treatment area undergo natural hydrostatic pressure changes but the area enclosed by the frozen banier does not, this is an indication of formation of the frozen banier.

In some embodiments, a tracer test may be used to determine or confirm formation of a frozen banier. A tracer fluid may be injected on a first side of a perimeter banier. Monitor wells on a second side of the perimeter banier may be operated to detect the tracer fluid. No detection of the tracer fluid by the monitor wells may indicate that the perimeter banier is formed. The tracer fluid may be, but is not limited to, carbon dioxide, argon, nitrogen, and isotope labeled water or combinations thereof. A gas tracer test may have limited use in saturated formations because the tracer fluid may not be able to travel easily from an injection well to a monitor well through a saturated formation. In a water saturated formation, an isotope labeled water (e.g., deuterated or fritiated water) or a specific ion dissolved in water (e.g., thiocyanate ion) may be used as a tracer fluid. If tests indicate that a frozen perimeter banier has not been foπned by the freeze wells, the location of incomplete sections of the perimeter banier may be determined. Pulse tests may indicate the location of unformed portions of a perhneter banier. Tracer tests may indicate the general direction in which there is an incomplete section of perimeter banier. Temperatures of freeze wells may be monitored to determine the location of an incomplete portion of a perimeter banier around a freatment area. In some freeze well embodiments, such as in the embodiment depicted in FIG. 228 and FIG. 224, freeze well 8012 may include port 8074. Temperature probes, such as resistance temperature devices, may be inserted into port 8074. Refrigerant flow to the freeze wells may be stopped. Dewatering wells may be operated to draw fluid past the perimeter banier. The temperature probes may be moved within ports 8074 to monitor temperature changes along lengths of the freeze wells. The temperature may rise quickly adjacent to areas where a frozen banier has not formed. After the location of the portion of perimeter banier that is unformed is located, refrigerant flow through freeze wells adjacent to the area may be increased and/or an additional freeze well may be installed near the area to allow for completion of a frozen banier around the treatment area. A typical relatively low permeability formation containing heavy hydrocarbons freated by a thermal treatment process may have a thick overburden. Average thickness of an overburden may be greater than about 20 m, 50 m, or 500 m. The overburden may provide a substantially impeπneable banier that inhibits vapor release to the atmosphere. ICP wells passing into the formation may include well completions that cement or otherwise seal well casings from sunounding formation material so that formation fluid cannot pass to the atmosphere adjacent to the wells.

In some embodiments of an in situ conversion process, heat sources may be placed in a hydrocarbon containing portion of the formation such that the heat sources do not heat sections of the hydrocarbon containing portion nearest to the ground surface to pyrolysis temperatures. The heat sources may heat a section of the hydrocarbon containing portion that is below the untreated section to pyrolysis temperatures. The untreated section of hydrocarbon containing material may be considered to be part of the overburden.

Some formations may have relatively thin overburdens over a portion of the foπnation. Some formations may have an outcrop that approaches or extends to ground surface. In some formations, an overburden may have fractures or develop fractures during thermal processing that connect or approach the ground surface. Some formations may have permeable portions that allow formation fluid to escape to the atmosphere when the formation is heated. A ground cover may be provided for a portion of a fonnation that will allow, or potentially allow, formation fluid to escape to the atmosphere during theπnal processing.

A ground cover may include several layers. FIG. 234 depicts an embodiment of ground cover 8076. Ground cover 8076 may include fill material 8078 used to level a surface on which the ground cover is placed, first impermeable layer 8080, insulation 8082, framework 8084, and second impermeable layer 8086. Other embodiments of ground covers may include a different number of layers. For example, a ground cover may only include a first impermeable layer. In some embodiments, first impermeable layer 8080 may be formed of concrete, metal, plastic, clay, or other types of material that inhibit foπnation fluid from passing from the ground to the atmosphere.

Ground cover 8076 may be sealed to the ground, to ICP wells, to freeze wells, and to other equipment that passes through the ground cover. Ground cover 8076 may inhibit release of formation fluid to the atmosphere.

Ground cover 8076 may also inhibit rain and run-off water seepage into a freatment area from the ground surface. The choice of ground cover material may be based on temperatures and chemicals to which ground cover 8076 is subjected. In embodiments in which overburden 540 is sufficiently thick so that temperatures at the ground surface are not influenced, or are only slightly elevated, by heating of the formation, ground cover 8076 may be a polymer sheet. For thinner overburdens 540, where heating the formation may significantly influence the temperature at ground surface, ground cover 8076 may be fonned of metal sheet placed over the treatment area. Ground cover

8076 may be placed on a graded surface, and wellbores for ICP wells and freeze wells may be placed into the formation through the ground cover. Ground cover 8076 may be welded or otherwise sealed to well casings and/or other structures extending through the ground cover. If needed, insulation 8082 may be placed above or below ground cover 8076 to inhibit heat loss to the atmosphere. Ground cover 8076 may include framework 8084. In certain embodiments, framework 8084 supports a portion of ground cover 8076. For example, framework 8084 may support second impermeable layer 8086, which may be a rain cover that extends over a portion or all of the treatment area. In other embodiments, framework 8084 supports well casings, walkways, and/or other structures that provide access to wells within the treatment area, so that personnel do not have to contact ground cover 8076 when accessing a well or equipment within the treatment area.

Perforated piping of a piping system may be placed in the ground or adjacent to the ground surface below a ground cover. The perforated piping may provide a path for transporting foπnation fluid passing through the foπnation towards the surface to surface facilities. In other embodiments, a piping system may be connected to openings that pass through the ground cover. Blowers or other types of drive systems may draw formation fluid adjacent to the ground cover into the piping. Monitor wells may be placed through a ground cover at the ground surface. If the monitor wells detect formation fluid, the drive system may be activated to fransport the fluid to a surface facility.

Ground cover 8076 may be sealed to the ground. In an embodiment of an in situ conversion process, freeze wells 8012 are used to form a low temperature zone around the treatment area. A portion of the refrigerant capacity utilized in freeze wells 8012 may be used to freeze a portion of the formation adjacent to the ground surface. Ground cover 8076 may include a lip that is pushed into wet ground prior to formation of the low temperature zone. When the low temperature zone is fonned, the freeze wells may freeze the ground and the ground cover together. Insulation may be placed over the frozen ground to inhibit heat absoφtion from the atmosphere. In other embodiments, a ground cover may be welded or otherwise sealed to a sheet banier or a grout wall formed in the foπnation around the freatment area.

In some embodiments, an upper layer of a formation (e.g., an outcrop) that allows, or potentially allows, formation fluid to escape to the atmosphere during thermal treatment is excavated. The depth of the excavation opening created may be about 1/3 m, 1 m, 5 m, 10 m, or greater. Perforated piping of a piping system may be placed in the excavation and covered with a permeable layer such as sand and/or gravel. A concrete, clay, or other impermeable layer may be formed as a cover over the excavation opening. Alternately, a similar structure may be built on top of the ground to form an impermeable cover over a portion of a formation. The concrete, clay, or other impermeable layer may function as an artificial overburden.

A treatment area may be subjected to various processes sequentially. Treatment areas may undergo many different processes including, but not limited to, initial heating, production of hydrocarbons, pyrolysis, synthesis gas generation, storage of fluids, sequesfration, remediation, use as a filtration unit, solution mining, and/or upgrading of hydrocarbon containing feed sfreams. Fluids may be stored in a formation as long term storage and/or as temporary storage during unusual situations such as a power failure or surface facilities shutdown. Various factors may be used to determine which processes will be used in particular freatment areas. Factors determining the use of a formation may include, but are not limited to, formation characteristics such as type, size, hydrology, and location; economic viability of a process; available market for products produced from the formation; available surface facilities to process fluid removed from the formation; and/or feedstocks for introduction into a fonnation to produce desired products.

For some processes, a low temperature zone may be used to isolate a freatment area. A freatment area sunounded by a low temperature zone may be used, in certain embodiments, as a storage area for fluids produced or needed on site. Fluids may be diverted from other areas of the foπnation in the event of an emergency. Alternatively, fluids may be stored in a freatment area for later use. A low temperature zone may inhibit flow of stored fluids from a freatment area depending on characteristics of the stored fluids. A frozen banier zone may be necessary to inhibit flow of certain stored fluids from a freatment area. Other processes which may benefit from an isolated freatment zone may include, but are not limited to, synthesis gas generation, upgrading of hydrocarbon containing feed sfreams, filtration of feed stocks, and/or solution mining. In some in situ conversion process embodiments, three or more sets of wells may sunound a freatment area. FIG. 237 depicts a well pattern embodiment for an in situ conversion process. Treatment area 8000 may include a plurality of heat sources and/or production wells. Treatment area 8000 may be sunounded by a first set of freeze wells 8028. The first set of freeze wells 8028 may establish a frozen barrier that inhibits migration of fluid out of freatment area 8000 during the in situ conversion process. The first set of freeze wells 8028 may be sunounded by a set of monitor and/or injection wells 8088.

Monitor and/or injection wells 8088 may be used during the in situ conversion process to monitor temperature and monitor for the presence of formation fluid (e.g., for water, steam, hydrocarbons, etc.). If hydrocarbons or steam are detected, a breach of the frozen banier established by the first set of freeze wells 8028 may be indicated. Measures may be taken to determine the location of the breach in the frozen banier. After determining the location of the breach, measures may be taken to stop the breach. In an embodiment, an additional freeze well or freeze wells may be inserted into the foπnation between the first set of freeze wells and the set of monitor and/or injection wells 8088 to seal the breach.

The set of monitor and or injection wells 8088 may be sunounded by a second set of freeze wells 8029. The second set of freeze wells 8029 may form a frozen banier that inhibits migration of fluid (e.g., water) from outside the second set of freeze wells into treatment area 8000. The second set of freeze wells 8029 may also form a banier that inhibits migration of fluid past the second set of freeze wells should the frozen banier foπned by the first set of freeze wells 8028 develop a breach. A frozen banier formed by the second set of freeze wells 8029 may stop migration of formation fluid and allow sufficient time for the breach in the frozen banier formed by the first set of freeze wells 8028 to be fixed. Should a breach form in the frozen barrier formed by the first set of freeze wells 8028, the frozen banier foπned by the second set of freeze wells 8029 may lhnit the area that formation fluid from the freatment area can flow into, and thus the area that needs to be cleaned after the in situ conversion process is complete.

If the set of monitor and/or injection wells 8088 detect the presence of formation water, a breach of the second set of freeze wells 8029 may be indicated. Measures may be taken to determine the location of the breach in the second set of freeze wells 8029. After determining the location of the breach, measures may be taken to stop the breach. In an embodiment, an additional freeze well or freeze wells may be inserted into the formation between the second set of freeze wells 8029 and the set of monitor and/or injection wells 8088 to seal the breach.

In many embodiments, monitor and/or injection wells 8088 may not detect a breach in the frozen banier formed by the first set of freeze wells 8028 during the in situ conversion process. To clean the freatment area after completion of the in situ conversion processes, the first set of freeze wells 8028 may be deactivated. Fluid may be introduced through monitor and/or injection wells 8088 to raise the temperature of the frozen banier and force fluid back towards freatment area 8000. The fluid forced into freatment area 8000 may be produced from production wells in the freatment area. If a breach of the frozen banier formed by the first set of freeze wells 8028 is detected during the in situ conversion process, monitor and/or injection wells 8088 may be used to remediate the area between the first set of freeze wells 8028 and the second set of freeze wells 8029 before, or simultaneously with, deactivating the first set of freeze wells. The ability to maintain the frozen banier foπned by the second set of freeze wells 8029 after in situ conversion of hydrocarbons in freatment area 8000 is complete may allow for cleansing of the freatment area with little or no possibility of spreading contaminants beyond the second set of freeze wells 8029. The set of monitor and/or injection wells 8088 may be positioned at a distance between the first set of freeze wells 8028 and the second set of freeze wells 8029 to inhibit the monitor and/or injection wells from becoming frozen. In some embodiments, some or all of the monitor and/or injection wells 8088 may include a heat source or heat sources (e.g., an elecfric heater, circulated fluid line, etc.) sufficient to inhibit the monitor and/or injection wells from freezing due to the low temperature zones created by freeze wells 8028 and freeze wells 8029. In some in situ conversion process embodiments, a freatment area may be freated sequentially. An example of sequentially freating a freatment area with different processes includes installing a plurality of freeze wells within a formation around a freatment area. Pumping wells are placed proximate the freeze wells within the freatment area. After a low temperature zone is formed, the pumping wells are engaged to reduce water content in the treatment area. After the pumping wells have reduced the water content, the low temperature zone expands to encompass some of the pumping wells. Heat is applied to the treatment area using heat sources. A mixture is produced from the formation. After a majority of recoverable liquid hydrocarbons is recovered from the formation, synthesis gas generation is initiated. Following synthesis gas generation, the freatment area is used as a storage unit for fluids diverted from other freatment areas within the formation. The diverted fluids are produced from the freatment area. Before the low temperature zone is allowed to thaw, the treatment area is remediated. A first portion of a low temperature zone sunounding the pumping wells is allowed to thaw, exposing an unaltered portion of the formation. Water is provided to a second portion of a low temperature zone to form a frozen banier zone. A drive fluid is provided to the treatment area through the pumping wells. The drive fluid may move some fluids remaining in the formation towards wells through which the fluids are produced. This movement may be the result of steam distillation of organic compounds, leaching of inorganic compounds into the drive fluid solution, and/or the force of the drive fluid "pushing" fluids from the pores. Drive fluid is injected into the freatment area until the removed drive fluid contains concentrations of the remaining fluids that fall below acceptable levels. After remediation of a treatment area, carbon dioxide is injected into the freatment area for sequesfration.

An alternate example of formation use includes a plurality of freeze wells placed within a formation sunounding a freatment area. A low temperature zone may be formed around the freatment area. Pumping wells, heat sources, and production wells are disposed within the treatment area. Hot water, or water heated in situ by heat sources, may be infroduced into the freatment area to solution mine portions of the formation adjacent to selected wells. After solution mining, the treatment area may be dewatered. The temperature of the treatment area may be raised to pyrolysis temperatures, and pyrolysis products may be produced from the treatment area.

After pyrolysis, the freatment area may be subjected to a synthesis gas generation process. After synthesis gas generation, the freatment area may be cleaned. A drive fluid (e.g., water and/or steam) may be infroduced into the treatment area to remove (e.g., by steam distillation) hydrocarbons out of the treatment area. The drive fluid may be infroduced into the freatment area from an outer perimeter of the treatment area. The drive fluid and any materials in front of, or enfrained in, the drive fluid may be produced from production wells in the interior of the freatment area. After cleaning, the freatment area may be used as storage for selected products, as an emergency storage facility, as a carbon dioxide sequesfration bed, or for other uses. In certain embodiments, adjacent freatment areas may be undergoing different processes concunently within separate low temperature zones. These differing processes may have varied requirements, for example, temperature and/or requfred constituents, which may be added to the section. In an embodiment, a low temperature zone may be sufficient to isolate a first freatment area from a second freatment area. An example of differing conditions required by two processes includes a first freatment area undergoing production of hydrocarbons. In situ generation of synthesis gas may requfre temperatures greater than about 400 °C. A second treatment area adjacent to the first may undergo sequesfration, a process, which depending on the component being sequestered, may be optimized at a temperature less than about 100 °C. Alternatively, providing a banier to both mass and heat fransfer may be necessary in some embodiments. A frozen banier zone may be utilized to isolate a treatment area from the sunounding formation both thermally and hydraulically. For example, a first treatment area undergoing pyrolysis should be isolated both thennally and hydraulically from a second freatment area in which fluids are being stored.

As depicted in FIG. 235 and FIG. 236, dewatering wells 8028 may sunound freatment area 8000. Dewatering wells 8028 that sunound treatment area 8000 may be used to provide a banier to fluid flow into the treatment area or migration of fluid out of the treatment area into sunounding formation. In an embodiment, a single ring of dewatering wells 8028 sunounds treatment area 8000. In other embodiments, two or more rings of dewatering wells sunound a freatment area. In some embodiments that use multiple rings of dewatering wells

8028, a pressure differential between adjacent dewatering well rings may be minimized to inhibit fluid flow between the rings of dewatering wells. During processing of treatment area 8000, formation water removed by dewatering wells 8028 in outer rings of wells may be substantially the same as formation water in areas of the formation not subjected to in situ conversion. Such water may be released with no treatment or minimal treatment. If removed water needs treatment before being released, the water may be passed through carbon beds or otherwise freated before being released. Water removed by dewatering wells 8028 in inner rings of wells may contain some hydrocarbons. Water with significant amounts of hydrocarbon may be used for synthesis gas generation. In some embodiments, water with significant amounts of hydrocarbons may be passed through a portion of formation that has been subjected to in situ conversion. Remaining carbon within the portion of the formation may purify the water by adsorbing the hydrocarbons from the water.

In some embodiments, an outer ring of wells may be used to provide a fluid to the formation. In some embodiments, the provided fluids may entrain some formation fluids (e.g., vapors). An inner ring of dewatering wells may be used to recover the provided fluids and inhibit the migration of vapors. Recovered fluids may be separated into fluids to be recycled into the formation and formation fluids. Recycled fluids may then be provided to the formation. In some embodiments, a pressure gradient within a portion of the formation may increase recovery of the provided fluids. Alternatively, an inner ring of wells may be used for dewatering while an outer ring is used to reduce an inflow of groundwater. In certain embodiments, an inner ring of wells is used to dewater the formation and fluid is pumped into the outer ring to confine vapors to the inner area.

Water within freatment area 8000 may be pumped out of the freatment area prior to or during heating of the formation to pyrolysis temperatures. Removing water prior to or during heating may limit the water that needs to be vaporized by heat sources so that the heat sources are able to raise formation temperatures to pyrolysis temperatures more efficiently.

In some embodiments, well spacing between dewatering wells 8028 may be ananged in convenient multiples of heater and/or production well spacing. Some dewatering wells may be converted to heater wells and/or production wells during in situ processing of a hydrocarbon formation. Spacing between dewatering wells may depend on a number of factors, including the hydrology of the formation. In some embodiments, spacing between dewatering wells may be 2 m, 5 m, 10 m, 20 m, or greater.

A spacing between dewatering wells and ICP wells, such as heat sources or production wells, may need to be large. The spacing may need to be large so that the dewatering wells and the in situ process wells are not influenced by each other. In an embodiment, a spacing between dewatering wells and in situ process wells may need to be 30 m or more. Greater or lesser spacings may be used depending on formation properties. Also, a spacing between a property line and dewatering wells may need to be large so that dewatering does not influence water levels on adjacent property.

In some embodiments, a perhneter banier or a portion of a perimeter banier may be a grout wall, a cement banier, and/or a sulfur banier. For shallow formations, a trench may be formed in the foπnation where the perimeter banier is to be formed. The trench may be filled with grout, cement, and or molten sulfur. The material in the trench may be allowed to set to form a perimeter banier or a portion of a perimeter banier.

Some grout, cement, or sulfur baniers may be formed in drilled columns along a perimeter or portion of a perimeter of a treatment area. A first opening may be formed in the formation. A second opening may be formed in the formation adjacent to the first opening. The second opening may be formed so that the second opening intersects a portion of the first opening along a portion of the formation where a banier is to be formed. Additional intersecting openings may be formed so that an interconnected opening is formed along a desired length of freatment area perimeter. After the interconnected openings are formed, a portion of the interconnected opening adjacent to where a banier is to be formed may be filled with material such as grout, cement, and/or sulfur. The material may be allowed to set to form a banier.

In situ freatment of formations may significantly alter foπnation characteristics such as peπneability and structural strength. Production of hydrocarbons from a formation conesponds to removal of hydrocarbon containing material from the foπnation. Heat added to the formation may, in some embodiments, fracture the formation. Removal of hydrocarbon containing material and formation of fractures may influence the structural integrity of the formation. Selected areas of a freatment area may remain untreated to promote structural integrity of the formation, to inhibit subsidence, and/or to inhibit fracture propagation.

FIG. 213 depicts a foπnation separated into a number of freatment areas 8000. Freeze wells 8012 sunounding freatment areas 8000 may form low temperature zones around the freatment areas. Formation material within the low temperature zones may be untreated formation material that is not exposed to high temperatures during an in situ conversion process. Formation water may be frozen in the low temperature zone. The frozen water may provide additional structural sfrength to the formation during the in situ conversion process. After completion of processing and use of a freatment area, maintenance of the low temperature zone may be ended and temperature of material within the low temperature zone may return to ambient conditions. The untreated formation material that was in the low temperature zone may provide structural sfrength to the formation. The regions of unfreated formation may inhibit subsidence of the formation. In some embodiments of in situ conversion processes, portions of a fonnation within a treatment area may not be subjected to temperatures high enough to pyrolyze or otherwise significantly change properties of the formation. Unfreated portions of the formation may stabilize the formation and inhibit subsidence of the formation or overburden. In a freatment area, heat sources are generally placed in patterns with regular spacings between adjacent wells. The spacings may be small enough to allow supeφosition of heat between adjacent heat sources. The supeφosition of heat allows the formation to reach high temperatures. A regular pattern of heat sources may promote relatively uniform heating of the treatment area.

In some embodiments, a disruption of a regular heat source pattern may leave sections of formation within a freatment area unprocessed. A large distance may separate heat sources from sections of the formation that are to remain untreated. The distance should allow the untreated section to be minimally influenced by adjacent heat sources. The distance may be 20 m, 25 m, or greater. In an embodiment ofan in situ treatment process that uses a friangular pattern of heat sources, a well unit (e.g., three heat sources) may be periodically omitted from the pattern to leave an untreated portion of formation when the formation is subjected to in situ conversion. In other embodiments, more wells than a single unit of wells may be omitted from the pattern (e.g., 4, 5, 6, or more heat source wells may be periodically omitted from an equilateral triangle heat source pattern). In some embodiments, selected wellbores of a regular heat source pattern may be utilized to maintain unfreated sections of formation within the pattern. A heat fransfer fluid may be placed or circulated within casings placed in the selected wellbores. The heat fransfer fluid may maintain adjacent portions of the foπnation at low enough temperatures that allow the portions to be uninfluenced or minimally influenced by heat provided to the formation from adjacent heat sources. The use of selected wellbores to maintain unfreated portions of the formation within a treatment area may advantageously eliminate the need to make wellbore pattern alterations during well installation.

In some embodiments, water may be used as a heat transfer fluid placed or circulated in selected casings to maintain unfreated portions of a foπnation. In some embodiments, the heat fransfer fluid circulated in selected casings to maintain unfreated portions of formation may include refrigerant utilized to form a low temperature zone around a freatment area. The refrigerant may be circulated in the selected wells prior to initiation of formation heating so that low temperature zones are formed around the selected freeze wells. Water in the formation may freeze in columns around the selected wells. Heating of the formation may reduce the size of the columns around the freeze wells, but the freeze wells should maintain frozen, unfreated portions of the formation within a heated portion of the formation. The unfreated portions may provide structural strength to the formation during an in situ conversion process and after the in situ conversion process is completed.

Vapor processing facilities that treat production fluid from a foπnation may include facilities for treating generated hydrogen sulfide and other sulfur containing compounds. The sulfur treatment facilities may utilize a modified Claus process or other process that produces elemental sulfur. Sulfur may be produced in large quantities at an in situ conversion process site. Some of the sulfur produced may be liquefied and placed (e.g., injected) in a spent formation. Stabilizers and other additives may be introduced into the sulfur to adjust the properties of the sulfur. For example, aggregate such as sand, conosion inhibitors, and/or plasticizers may be added to the molten sulfur. U.S. Pat. No. 4,518,548 and U.S. Pat. No. 4,428,700, which are both incoφorated by reference as if fully set forth herein, describe sulfur cements.

A spent formation may be highly porous and highly permeable. Liquefied sulfur may diffuse into pore space within the formation formed by thennally processing hydrocarbons within the formation. The sulfur may solidify in the formation when the sulfur cools below the melting temperature of sulfur (approximately 115 °C). Solidified sulfur may provide structural strength to the foπnation and inhibit subsidence of the formation. Solidified sulfur in pore spaces within the formation may provide a banier to fluid flow. If needed at a future time, sulfur may be produced from the formation by heating the fonnation and removing the sulfur from the formation. In some in situ conversion process embodiments, molten sulfur may be placed in a formation to fonn a perimeter banier around a portion of the formation to be subjected to pyrolysis. The perimeter banier formed by solidified sulfur may provide structural sfrength to the formation. The perimeter banier may need to be located a large distance away from ICP wells used during in situ conversion so that heat applied to the freatment area does not affect the sulfur banier. In some embodiments, the perimeter banier may be 20 m, 30 m, or farther away from heat sources of an in situ conversion process system.

Sulfur baniers may be used in conjunction with a low temperature zone formed by freeze wells. A low temperature zone, or freeze wall, may be formed to provide a banier to fluid flow into or out of a treatment area that is subjected to an in situ conversion process. The low temperature zone may also provide structural sfrength to the formation being freated. After the freatment area is processed, water or other fluid may be infroduced into the formation to remediate any contaminants within the freatment area. Heat may be recovered from the formation by removing the water or other fluid from the formation and utilizing the heat fransfened to the water or fluid for other purposes. Recovering heat from the formation may reduce the temperature of the formation to a temperature in the vicinity of the melting temperature of sulfur adjacent to the low temperature zone.

After a temperature of the freatment area is reduced to about the temperature of molten sulfur, molten sulfur may be infroduced into the formation adjacent to the low temperature zone formed by freeze wells, and the molten sulfur may be allowed to diffuse into the formation. In the embodhnent depicted in FIG. 216, the molten sulfur may be introduced into the foπnation through dewatering well 8028. The molten sulfur may solidify against the frozen banier formed by freeze well 8012. After solidification of the sulfur, maintenance of the low temperature zone may be reduced or stopped. Solid sulfur within pore spaces may inhibit fluid from migrating through the sulfur banier. For example, carbon dioxide may be adsorbed onto carbon remaining in a formation that has been processed using an in situ conversion process. If water migrates into the formation, the water may desorb the stored carbon dioxide from the formation. Sulfur injected into wells may solidify in pore spaces within the formation to form a sulfur cement banier. The sulfur cement banier may inhibit water migration into the formation. The banier formed by the sulfur may inhibit removal of stored carbon dioxide from the formation. In some embodiments, sulfur may be infroduced throughout a formation instead of just as a perimeter banier. Sulfur may be stored or used to inhibit subsidence of the formation.

In some instances, shut-in management of the in situ freatment of a formation may become necessary. "Shut-in" may be a reduction or complete termination of production from a formation undergoing in situ freatment. Adverse events of any kind and/or scheduled maintenance may require shut-in of an in situ freatment process. For example, adverse events may include malfunctioning or nonfunctioning surface facilities, lack of fransport facilities to move products away from the project, breakthrough to the surface or an aquifer, and/or sociopolitical events not directly related to a project.

Generally, thermal conduction and conversion of hydrocarbons during in situ freatment are relatively slow processes. Therefore, shut-in of production may require a relatively long period of time. For example, at least some hydrocarbons in the formation may continue to be converted for months or years after heating from the heat sources is terminated. Consequently, hydrocarbons and other vapors may continue to be generated, accompanied by a build up of fluid pressure in the formation. Fluid pressure in the formation may exceed the fracturing sfrength of the formation and create fractures. As a result, hydrocarbons and other vapors, which may include hydrogen sulfide, may migrate through the fractures to the sunounding foπnation, potentially reaching groundwater or the surface.

Shut-in management of an in situ freatment process may include a variety of steps that alleviate problems associated with shut-in of the process. In one embodiment, substantially all heating from heat sources, including heater wells and thermal injection, may be terminated. Termination of heating is particularly important if the adverse event or shut down may be of long duration. In addition, substantially all hydrocarbon vapors generated may be produced from the formation. The produced hydrocarbon vapors may be flared. "Flaring" is oxidation or burning of fluids produced from a formation. It is particularly advantageous for complete combustion of H₂S to take place. Furthermore, it is desirable to flar,e methane since methane may be a much sfronger greenhouse gas than C0₂.

In certain embodiments, the fluid pressure in the formation may be maintained below a safe level. The safe fluid pressure level may be below an established threshold at which fracturing and breakthrough occur in the formation. The fluid pressure in the formation may be monitored by several methods, for example, by passive acoustic monitoring to detect fracturing. "Passive acoustic monitoring" detects and analyzes microseismic events to determine fracturing in a formation. In an embodiment, a short term response to excessive pressure build up may be to release formation fluids to other storage (e.g., a spent, cool portion of the formation). Alternatively, formation fluids may be flared.

In some embodiments, produced formation fluid may be injected and stored in spent formations. A spent formation may be retained specifically for receiving produced fluids should a shut-in situation arise. Fluid communication between the spent formation and the sunounding formation may be limited by a banier (e.g., a frozen banier, a sulfur banier, etc.). The banier may inhibit flow of the produced formation fluid from the spent formation. In an embodiment, the temperature of the spent formation may be low enough to condense a substantial portion of condensable fluids. There may be a conesponding decrease in fluid pressure as fonnation fluid condenses in the spent formation. The decrease in fluid pressure and volume reduction may increase storage capacity of the spent formation. In an embodiment, subsequent heating of the spent formation may allow substantially complete recovery of stored hydrocarbons. In certain embodiments, produced formation fluid may be injected into relatively high temperature formations. The formation may have portions with an average temperature high enough to convert a substantial portion of the injected formation fluid to coke and H₂. H₂ may be flared to produce water vapor in some embodiments.

In an embodiment, produced formation fluid may be injected into partially produced or depleted formations. The depleted formations may include oil fields, gas fields, or water zones with established seal and trap integrity. The trapped formation fluid may be recovered at a later time. In other embodiments, formation fluid may be stored in surface storage units.

FIG. 250 is a flow chart illustrating options for produced fluids from a shut-in formation. Stream 8252 may be produced from shut-in formation 8250. Sfream 8252 may be injected into cooled spent fonnation 8254. Formation 8254 may be reheated at a later time to produce the stored formation fluid, as shown by sfream 8255. In addition, stream 8252 may be injected into hot formation 8256. A substantial portion of the fluids injected into formation 8256 may be converted to coke and H₂. The H₂ may be produced from fonnation 8256 as sfream 8257 and flared. Alternatively, sfream 8252 may be injected into depleted oil or gas field or water zone 8258. Injected foπnation fluid may be produced at a later thne, as sfream 8259 illusfrates. Furtheπnore, stream 8252 may be stored in surface storage facilities 8260.

After completion of an in situ conversion process, formations may be subjected to additional freatment processes in preparation for abandonment. Processes which may be performed in a formation may include, but are not limited to, recovery of thermal energy from the formation, removal of fluids generated during the in situ conversion process through injection of a fluid (water, carbon dioxide, drive fluid), and/or recovery of thermal energy from a frozen banier or freeze well.

Theπnal energy may be recovered from formations through the injection of fluids into the foπnation. Fluids may be injected and/or removed through existing heater wells, dewatering wells, and/or production wells. In some embodhnents, a portion of a formation subjected to an in situ conversion process may be at an average temperature greater than about 300 °C. The portion of the formation may have a relatively high porosity (e.g., greater than about 20%) and a permeability greater than about 0.3 darcy (e.g., 0.4 darcy, 0.6 darcy, 0.9 darcy, 1 darcy, or greater) due to the removal of hydrocarbons from the formation and theπnal fracturing of the formation. The increased porosity and permeability of the section may reduce the number of wells needed to inject and recover fluid. For example, water may be provided to or be removed from the formation using heater wells that allow, or have been reworked to allow, fluid communication between the well and the sunounding formation. In some embodiments, fresh water may be injected into the formation. Alternatively, non-potable water, hydrocarbon containing water, brine, acidic water, alkaline water, or combinations thereof may be injected into the formation. Compounds in the water may be left within the formation after the water is vaporized by heat within the formation. Some compounds within the water may be absorbed and/or adsorbed onto remaining material within the formation. Introduction of several pore volumes of water may be needed to lower the average temperature in the formation below the boiling point of water. In an embodiment, water injection may include geothermal well and other technologies developed for utilizing the steam production from high temperature subtenanean formations. In certain embodiments, applications of steam recovered from the formation may include direct use for power generation and/or use as sensible energy in heat exchange mechanisms. In particular, theπnal energy from recovered steam may be used in project surface facilities (e.g., in heat exchange units, in the desalinization process, or in the distillation of produced water). The theπnal energy from recovered steam may be used for solution mining of nearby mineral resources (e.g., nahcolite, sulfur, phosphates, etc). Thermal energy from recovered steam may also be used in external industrial applications, such as applications that require the use of large volumes of steam. In addition, theπnal energy from recovered steam may be used for municipal puφoses (e.g., heating buildings) and for agricultural puφoses (e.g., heating hothouses or processing products). In an in situ conversion process embodiment during a time prior to abandonment, substantially non- reactive gas (e.g., carbon dioxide) may be used as a heat recovery fluid. The substantially non-reactive gas may be injected into the formation and heat within the formation may be fransfened to the substantially non-reactive gas. In some embodiments, the substantially non-reactive gas may recover a substantial portion of residual freatment fluids (e.g., low molecular weight hydrocarbons). The treatment fluids may be separated from the substantially non-reactive gas at the surface of the formation. For example, some carbon dioxide may be adsorbed onto the surface of the formation, displacing low molecular weight hydrocarbons. In an embodiment, carbon dioxide adsorbed onto formation surfaces during use as a heat recovery fluid may be sequestered within the formation. After completion of heat recovery, additional carbon dioxide may be provided to the fonnation and adsorbed in formation pore spaces for sequesfration.

In an in situ conversion process embodiment, recovery of stored heat in a formation with injected substantially non-reactive gas may require more pore volumes of gas than would have been required had water been used as the heat recovery fluid. This may be due to gases generally having lower sensible heats than liquids. .In addition, substantially non-reactive gas injection may require initial compression of the injected gas sfream. However, injection and recovery in the gas phase may be easier than in the liquid phase. In certain embodiments, recovery of heat from the formation may combine injection of water and substantially non-reactive gas. For example, substantially non-reactive gas injection may be performed first, followed by water injection.

In some embodiments, the formation may be cooled such that an average temperature of the formation is at least below the ambient boiling temperature of water. Injection and recovery of fluid may be repeated until the average temperature of the formation is below the ambient boiling point at the fluid pressure in the formation.

FIG. 238 illustrates a schematic of an embodhnent of heat recovery from a formation previously subjected to an in situ conversion process. FIG. 238 includes formation 8278 with heat recovery fluid injection wellbore 8280 and production wellbore 8282. The wellbores may be members of a larger pattern of wellbores placed throughout a portion of the formation. The temperature in heated portions of the formation that are to be cooled may be between about 300 °C and about 1000 °C. Thermal energy may be recovered from the heated portions of the formation by injecting a heat recovery fluid. Heat recovery fluid 8284, such as water and/or carbon dioxide, may be injected into wellbore 8280. A portion of injected water may be vaporized to form steam. A portion of injected carbon dioxide may adsorb on the surface of the carbon in the formation. Gas mixture 8286 may exit continuously from wellbore 8282. Gas mixture 8286 may include the heat recovery fluid (e.g., steam or carbon dioxide), hydrocarbons, and or components. Components and hydrocarbons may be separated from the gas mixture in a surface facility. The heat recovery fluid may be recycled back into the formation.

In an in situ conversion process embodiment, heat recovery from the formation may be performed in a batch mode. Injection of the heat recovery fluid may continue for a period of time (e.g., until the pore volume of the portion of the formation is substantially filled). After a selected period of time subsequent to ceasing injection of heat recovery fluid, gas mixture 8286 may be produced from the formation through wellbore 8282. In an embodiment, the gas mixture may also exit through wellbore 8280. The selected period of time may be, in some embodiments, about one month.

In one embodiment, gas mixture 8286 may be fed to surface separation unit 8288. Separation unit 8288 may separate gas mixture 8286 into heat recovery fluid 8290 and hydrocarbons and components 8296. The heat recovery fluid may be used in power generation units 8292 or heat exchange mechanisms 8294. In another embodiment, gas mixture 8286 may be fed directly from the formation to power generation units or heat exchange mechanisms. Injection of the heat recovery fluid may be continued until a portion of the formation reaches a desired temperature. For example, if water is used as the heat recovery fluid, water injection may continue until the formation cools to, or is at a temperature below, the boiling point of water at formation pressure. Thermal processing and increasing the permeability of a formation may allow some components (e.g., hydrocarbons, metals and/or residual formation fluids) in the foπnation to migrate from a freatment area to areas adjacent to the foπnation. Such components may be created during thermal processing of the formation. Such components may be present in higher quantities if the formation is not subjected to a synthesis gas generation cycle after pyrolysis. In one embodiment, a recovery fluid may be infroduced into the formation to remove some of the components. The recovery fluid may be provided to the formation prior to and/or after cooling of the formation has begun. The recovery fluid may include, but is not limited to, water, steam, hydrogen, carbon dioxide, air, hydrocarbons (e.g., methane, ethane, and/or propane), and/or a combustible gas. The provided recovery fluid may be recycled from another portion of the formation, another fonnation, and/or the portion of the formation being treated. In some embodiments, a portion of the recovery fluid may react with one or more materials in the formation to volatize and/or neutralize at least some of the material. In alternate embodiments, the recovery fluid may force components in the formation to be produced. After production the recovery fluid may be provided to an energy producing unit (e.g. turbine or combustor). For example, methane may be provided to a portion of the formation. Heat within the formation may fransfer to the methane. The methane may cause production of a mixture including heavier hydrocarbons (e.g., BTEX compounds). The mixture may be provided to a turbine, where some of the mixture is combusted to produce elecfricity. In alternate embodiments, water may be provided to the formation as a recovery fluid. Steam produced from the water may entrain, distill, and/or drive components within the formation to production wells. In an embodiment, organic components may be produced from the formation either by steam distillation and/or entrainment in steam. In some embodiments, inorganic components may be entrained and produced in condensed water in the formation. Water injection and steam recovery may be continued until safe and permissible levels of components are achieved. Removal of these components may occur after an in situ conversion process is complete.

Remediation within a freatment area sunounded by a banier (e.g., a frozen banier) may inhibit the migration of components from the freatment area to the sunounding formation. A plurality of freeze wells 8012 may be used to form frozen banier zone 8002 and define a volume to be treated within hydrocarbon containing material 8006, as illusfrated in FIG. 239. Frozen banier 8002 may inhibit fluid flow into or out of freatment area 6510. In an in situ conversion process embodiment, a recovery fluid may be introduced into the formation near freeze wells 8012 after treatment is complete.

Injection wells 6902 Used for injection of the recovery fluid may include, but are not limited to, pumping wells, heat sources, freeze wells, dewatering wells, and/or production wells that have been converted into injection wells. In certain embodiments, wells used previously may have a sealed casing. The sealed casing may be perforated to permit fluid communication between the well and the sunounding formation. Recovery fluid may move some of the components in the formation towards one or more removal wells 6904. Removal wells 6904 may include wells that were converted from heat sources and/or production wells. In an alternate embodiment, a recovery fluid may be infroduced into a freatment area through an innermost production well, or a production well ring, that is converted into an injection well.

In some embodiments, the recovery fluid may be infroduced into the formation after the frozen banier zone has been partially thawed. When thawing the frozen barrier, thermal energy may be removed from the frozen banier by circulating various fluids through the freeze well. For example, a warm refrigerant may be injected into the freeze well system to be cooled and used in a surface freatment unit, a freeze well system, and/or other freatment area. As the temperature within the freeze well increases, various other fluids (e.g., water, substantially non-reactive gas, etc.) may be utilized to raise the temperature of the freeze well. Thawed freeze wells that are exposed may be converted for use as injection wells 6902 to introduce recovery fluid into the formation. Introduction of the recovery fluid may heat the region adjacent to the inner row of freeze wells to an average temperature of less than a pyrolysis temperature of hydrocarbon material in the foπnation. The heat from the recovery fluid may move mobilized hydrocarbon and inorganic components. Movement of the hydrocarbon and inorganic components may be due in part to steam distillation of the fluids and/or entrainment. Introducing the recovery fluid at a point where the foπnation was previously frozen ensures that the hydrocarbon material at the injection well is unaltered. The unaltered hydrocarbon material may be essentially in its original natural state. As such, the injected fluid may move from a natural zone to the previously freated area and be produced. Thus, fluids formed during the treatment are removed without spreading such fluids to other areas outside of the freatment area. Alternatively, any well previously frozen in a frozen banier zone, such as a pumping well, may be thawed and used as an injection well.

A volume of recovery fluid requfred to remediate a treatment area may be greater than about one pore volume of the treatment area. Two pore volumes or more of recovery fluid may be infroduced to remediate the freatment area. In certain embodiments, injection of a recovery fluid to remediate a freatment area may continue until concenfrations of components in the removed recovery fluid are at acceptable levels deemed appropriate for a site. These acceptable levels may be based on base line surveys, regulatory requirements, future potential uses of the site, geology of the site, and accessibility. After one or more components within a treatment area are removed or reduced to acceptable levels, the freatment system for the formation, including the freeze wells, may be deactivated. If a new banier zone around a new freatment area is to be formed, heat may be fransfened between hydrocarbon containing material, in which a new banier zone is to be formed, and the initial freeze wells using a circulated heat fransfer fluid. Using deactivated freeze wells to cool hydrocarbon containing material in which a low temperature zone is to be formed may allow for recovery of some of the energy expended to form and maintain the initial banier. In addition, using thermal energy extracted from the initial banier to cool hydrocarbon material in which a new banier zone is to be formed may significantly decrease a cost of forming the new banier. In some freatment system embodiments, a low temperature zone may be allowed to reach thermal equilibrium with a sunounding formation naturally.

In some in situ conversion process embodiments, the frozen banier may include an inner ring of freeze wells directly adjacent to the treatment area and an outer ring of freeze wells directly adjacent to the unfreated area. A region of the foπnation near the freeze wells may remain at a temperature below the freezing point of water during pyrolysis and synthesis gas generation. In an embodiment, organic components from pyrolysis may migrate through thermal fractures to a region adjacent to the inner row of freeze wells. The contaminants may become immobilized in fractures and pores in the region due to the relatively low temperatures of the region.

Migration of contaminants from the freatment area may be reduced or prevented by inhibiting groundwater flow through the freatment area. For example, groundwater flow may be inhibited using a banier such as a freeze wall and/or sulfur baniers. As a result, migration of contaminants may be reduced or eliminated even if contaminants were dissolved in formation pore water. In addition, it may be advantageous to inhibit groundwater flow to maintain a reduced state within the formation. Oxidized metals infroduced into the formation from groundwater flow tend to have greater mobility and may be more likely to be released.

An embodiment for inhibiting migration of contaminants may also include sealing off the mineral mafrix and residual carbon by precipitation or evaporation of a sealing mineral phase. The sealing mineral phase may inhibit dissolution of contaminants of fluids in the formation into groundwater.

Carbon dioxide may be produced during an in situ conversion process or during processing of the products produced by the in situ conversion process (e.g., combustion). Confrol and/or reduction of carbon dioxide production from an in situ conversion process may be desirable. "Carbon dioxide life cycle emissions," as used herein, is defined as the amount of C0₂ emissions from a product as it is produced, transported, and used. A base line C0₂ life cycle emission level may be selected for products produced from an in situ conversion process. The foπnation conditions and/or process conditions may be altered to produce products to meet the selected C0₂ base line life cycle emission level. In some embodiments, in situ conversion products may be blended to meet a selected C0₂ base line life cycle emission level. The C0₂ life cycle emission level of a selected product is defined as a number of kilograms of C0₂ per joule of energy (kg C0₂/J).

A hydrogen cycle, a half-way cycle, and a methane cycle are examples of processes that may be used to produce products with selected C0₂ emission levels less than the total C0₂ emission level that would be produced by direct production of natural gas from a gas reservofr. In certain embodiments, products may be combined to produce a product with a selected C0₂ emission level less than the total C0₂ emission from direct production of natural gas. In other embodiments, cycles may be blended to produce products with a C0₂ emission level less than the total C0₂ emission from direct production of natural gas. For example, in an embodiment, a methane cycle may be used in one part of a production field and a half-way cycle may be used in another part of the production field. The products produced from these two processes may be blended to produce a product with a selected C0₂ emission level. In other embodiments, other combinations of products from the hydrogen cycle, the half-way cycle, and the methane cycle may be used to produce a product with a selected C0₂ emission level.

In an in situ conversion process embodiment, a formation may be freated such that hydrocarbons in the formation are converted to a desired product. The product may be produced from the formation, fri some in situ conversion process embodiments, the in situ conversion process may be operated to produce a limited amount of carbon dioxide. In an in situ conversion process embodiment, the in situ conversion process may be operated so that a substantial portion of the product is molecular hydrogen. There may be little or no hydrocarbon fluid recovery. An in situ conversion process that operates at a high temperature to produce a substantial portion of hydrogen may be a "hydrogen cycle process." A portion of the hydrogen produced during the hydrogen cycle process may be used to fuel heat sources that raise and/or maintain a temperature within the formation to a high temperature. During a hydrogen cycle process, a production well and formation adjacent to the production well may be heated to temperatures greater than about 525 °C. At such temperatures, a substantial portion of hydrocarbons present or that flow into the production well and formation adjacent to the production well may be reduced to hydrogen and coke. There may be minimal or no production of carbon dioxide or hydrocarbons. Hydrocarbons in formation fluid produced from the formation may be recycled back into the formation through injection wells to produce hydrogen and coke. Hydrogen produced from a hydrogen cycle process may be produced through heated production wells in the formation. A portion of the produced hydrogen may be used as a fuel for heat sources in the formation. A portion of the hydrogen may be sold or used in fuel cells. In some embodiments, coke produced during a hydrogen cycle process may slowly fill pore space within the formation adjacent to the production well. The coke may provide structural strength to the formation. In some embodiments, the production wells may be freated (e.g., by introducing steam to generate synthesis gas) to remove a portion of formed coke and allow for production of formation fluid. In some embodiments, a coked production well may be blocked, and fonnation fluid may be produced from other production wells.

A hydrogen cycle may allow for very low C0₂ life cycle emission levels. In some embodiments, a hydrogen cycle process may have a C0₂ life cycle emission level of about 3.3 x 10^"9 kg C0₂/J. In other embodiments, a C0₂ life cycle emission level of the hydrogen cycle process may be less than about 1.6 x 10^"10 kg

CO₂/J. In an in situ conversion process embodiment, a portion of formation may be freated to produce a product that is substantially a mixture of molecular hydrogen and methane. There may be little or no other hydrocarbons (i.e., ethane, propane, etc.). A process of converting hydrocarbons in a formation to a product that is substantially molecular hydrogen and methane may be refened to as a "half-way cycle process." A portion of the product may be used as a fuel for heat sources that heat the foπnation to maintain and/or increase the formation temperature.

During a half-way cycle, production wells and formation adjacent to the production wells may be heated to temperatures from about 400 °C to about 525 °C. A substantial portion of hydrocarbons present or that flow into the production wells or formation adjacent to the production wells may be reduced to molecular hydrogen and methane. The hydrogen and methane may be produced as a mixture from the production wells. Produced hydrocarbons having carbon numbers greater than one may be recycled back into the formation through injection wells to generate hydrogen and methane. Foπnation adjacent to the production wells may slowly coke up during a half-way cycle. When production through a production well falls below a certain level, the production well may blocked in. In some embodiments, the production well may be treated (e.g., by introducing steam to generate synthesis gas) to remove a portion of the coke and allow for increased production through the well. In an embodiment of a half-way cycle process, produced hydrogen and methane may be separated from other produced fluid. A portion of the hydrogen and methane may be used as a fuel for heat sources. Further, hydrogen may be separated from the methane of a portion not used as fuel. In some embodiments, a portion of the hydrogen may be used for hydrogenation in another portion of the foπnation and/or in surface facilities. In some embodiments, hydrogen may be sold. In some embodiments, some or all produced methane may be used to fuel heat sources.

A mixture produced using a half-way cycle may have a C0₂ life cycle emission level that is greater than a C0₂ life cycle emission level of a hydrogen cycle. A mixture produced using a half-way cycle may have a C0₂ life cycle emission level of less than about 3.3 x 10^"8 kg C0₂/J.

In an in situ conversion process embodiment, a portion of foπnation may be freated to produce a product that is substantially methane. A process of converting a substantial portion of hydrocarbons within a portion of formation to methane may be refened to as a "methane cycle."

The producing wellbore and the formation proximate the producing wellbore may, in some embodiments, be heated to temperatures from about 300 °C to about 500 °C. For example, the producing wellbore may be heated to about 400 °C. Pyrolysis in this temperature range may allow a substantial portion of hydrocarbons in the formation to be converted to methane. Hydrocarbons with carbon numbers greater than one produced from the formation may be recycled back into the formation through injection wells to generate methane. The methane may be produced in a mixture from the heated wellbores. In an embodhnent, the methane content may be greater than about 80 volume % of the produced fluids.

A mixture produced from a methane cycle may have a C0₂ life cycle emission level that is larger than the C0₂ life cycle emission level for a half-way cycle. In some embodiments of methane cycles, the C0₂ life cycle emission levels are less than about 7.4 x 10^"8 kg C0₂/J.

In an in situ conversion process embodiment, molecular hydrogen may be produced on site using processes such as, but not limited to, Modular and Intensified Steam Reforming (MISR) and/or Steam Methane Reforming (SMR). The produced molecular hydrogen may be blended with other products to produce a product below a selected C0₂ emission level. The C0₂ produced using MISR or other processes may be sequestered in a formation. After completion of pyrolysis and/or synthesis gas generation during an in situ conversion process, at least a portion of the fonnation may be converted into a hot spent reservoir. The hot spent reservoir may have a temperature of greater than about 350 °C. The porosity may have increased by 20 volume % or more. In addition, a penneability in a hot spent reservoir may be greater than about 1 darcy, or in certain embodiments, greater than about 20 darcy. A hot spent reservoir may have a large open volume. The surface area within the volume may have increased significantly due to the in situ conversion process. Utilization of the in situ conversion process may have required the installation and use of production wells and heat sources spaced at a range between about 10 m and about 30 m. A banier (e.g., freeze wells) may also be present to inhibit migration of fluids to or from a treatment area in the formation. In an in situ conversion process embodiment, a heated formation (e.g., a formation that has undergone substantial pyrolysis and/or synthesis gas generation) may be used to produce olefins and/or other desfred products. Hydrocarbons may be provided to (e.g., injected into) a heated portion of a formation. An in situ conversion process in a separate portion of the formation may provide the source of the hydrocarbons. The formation temperature and/or pressure may be confrolled to produce hydrocarbons of a desired composition (e.g., hydrocarbons with a C₂-C₇ carbon chain length). Temperature may be controlled by controlling energy input into heat sources. Pressure may be confrolled by controlling the temperature in the formation and/or by controlling a rate of production of formation fluid from the fonnation. Pressure within a portion of a formation enclosed by a perimeter banier (e.g., a frozen banier and an impermeable overburden and underburden) may be confrolled so that the pressure is substantially uniform throughout the enclosed portion of formation. Many different types of hydrocarbons may be provided to the heated formation as a feed stream.

Examples of hydrocarbons include, but are not limited to, pitch, heavy hydrocarbons, asphaltenes, crude oil, naphtha, and/or condensable hydrocarbons (e.g., methane, ethane, propane, and butane). A portion of heavy and/or condensable hydrocarbons infroduced into a heated portion of the formation may pyrolyze to form shorter chain compounds. The shorter chain compounds may have greater value than the longer chain compounds infroduced into the portion of formation.

A portion of the hydrocarbons infroduced into the formation may react to form olefins. An overall efficiency for producing olefins may be relatively low (as compared to reactors designed to produce olefins), but the volume of heated formation and/or the availability of feed from portions of the formation undergoing an in situ conversion process may make production of olefins from a heated formation economically viable. In certain embodiments, the temperature of a selected portion of the formation (e.g., near production wells) may be confrolled so that hydrocarbon fluid flowing into the selected portion has an increased chance of forming olefins. In certain embodiments, process conditions may be controlled such that the time period in which the compounds are subjected to relatively higher temperatures is confrolled. In certain embodiments, only a small portion of the formation (e.g., near the production wells) is at a high enough temperature to promote olefin formation. Olefins may be formed subsurface in the small portion, but the olefins are produced quickly (e.g., before the olefins can cross-link in the formation and/or further react to form coke).

In an embodiment, olefins are produced from saturated hydrocarbons. Formation of the olefins from saturated hydrocarbons also results in the production of molecular hydrogen. In an embodiment, olefin production may include cracking saturated hydrocarbons in the formation and allowing the cracked hydrocarbons to further react in the foπnation (e.g., via alkylation or dimerization). The foπnation of olefins may involve different reaction mechanisms. Any number of the olefin formation mechanisms may be present in the in situ conversion process. Water may be added to the formation for steam generation and/or temperature confrol.

Examples of olefins produced by providing hydrocarbons to a heated formation may include, but are not limited to, ethene, propene, 1 -butene, 2-butene, higher molecular weight olefins, and/or mixtures thereof. The produced mixture may include from slightly over about 0 weight % to about 80 weight % (e.g., from about 10-50 weight %) olefins in a hydrocarbon portion of a produced mixture.

In an in situ conversion process embodiment, crude oil may be provided to a heated portion of a formation. The crade oil may crack in the heated portion to form a lighter, higher quality oil and an olefin portion. In an in situ conversion process embodiment, pitch and/or asphaltenes may be provided to a heated portion of a formation. The pitch and/or asphaltenes may be in solution and/or entrained in a solvent. The solvent may be a hydrocarbon portion of a fluid produced from a portion of a formation subjected to an in situ conversion process. A portion of the pitch and/or asphaltenes and the solvent may be converted in the formation to high quality hydrocarbons and/or olefins. Similarly, emulsions, bottoms, and/or undesired hydrocarbon compounds that are flowable, entrained in a flowable solution, or dissolved in a solvent may be infroduced into a heated portion of a foπnation to upgrade the introduced fluids and/or produce olefins.

In some embodiments, a temperature in selected portions of a production well wellbore may be confrolled to promote production of olefins. A portion of the wellbore adjacent to a heated portion of the formation may include a heater that maintains the temperature at an elevated temperature. A portion of the wellbore above the heated portion of the wellbore may include a heat fransfer line that reduces the temperature of fluid being removed through the wellbore to a temperature below reaction temperatures of desired components within the wellbore (e.g., olefins). In some embodiments, transfer of heat from the fluids in the wellbore to the overburden may reduce the temperature of fluids in the wellbore quickly enough to obviate the need for a heat fransfer line in the wellbore.

In some in situ conversion process embodiments, hydrocarbon feedstock introduced into a hot portion of a portion may have an API gravity of less than about 20°. The hydrocarbon feedstock may be cracked in the heated portion to produce a plurality of products. The products may include olefins. Molecular hydrogen may also be produced along with a mixture of products. A temperature and/or a pressure of the heated portion of the formation may be controlled such that a substantial portion of the produced product includes olefins. A hydrocarbon portion of the produced mixture may include from about 1 weight % to about 80 weight % (e.g., from about 10-50 weight %) olefins. In some in situ conversion process embodiments, a hydrocarbon mixture produced from a formation may be suitable for use as an olefin plant feedstock. Process conditions in a portion of a formation may be adjusted to produce a hydrocarbon mixture that is suitable for use as an olefin plant feedstock. |The mixture should contain relatively short chain saturated hydrocarbons (e.g., methane, ethane, propane, and or butane). To change formation conditions to produce a hydrocarbon mixture suitable for use as an olefin plant feedstock, backpressure within the formation may be maintained at an increased level (i.e., production from production wells may be low enough to result in an increase in pressure in the formation).

In some in situ conversion process embodiments, low molecular weight olefins (e.g., ethene and propene) may be produced during the in situ conversion process. Fluid produced may be routed through a relatively hot (e.g., greater than about 500 °C) subsurface zone before the fluid is allowed to cool. The fluid may crack at a high temperature to produce low molecular weight olefins. Temperature of the fluid should be subjected to high temperature for only a short period of time to inhibit formation of methane, hydrogen, and/or coke from the low molecular weight olefins.

In some in situ conversion process embodiments, olefin production yield may be facilitated from a formation. Continued processing or recycling of the non-olefinic C₂+ products in the in situ conversion process may maximize ethene and/or propene yield. Confrol of the temperature and residence time within a portion of the formation may be used to maximize non-olefinic C₂+ hydrocarbons and hydrogen content. Some olefins may be produced in this cycle and separated from the produced fluid. The non-olefinic portion may be recycled to a second section of the formation that includes production wells that are heated. A portion of the infroduced hydrocarbons may be converted into olefins by the heated production wells to increase the yield of olefins obtained from the formation.

In some in situ conversion process embodiments, linear alpha olefins in the C₄-C₃₀ range may be produced from a relatively low permeability formation containing heavy hydrocarbons. Formation conditions may be controlled to facilitate formation and production of olefins in a desired range (e.g., C₆-Cι₆ alpha olefins). Shale oil may produce paraffinic (i.e., waxy) and linear compounds during the in situ conversion process. Linear alpha olefins may be produced from the in situ conversion process by varying the temperature, residence time, and/or pressure in the formation being freated. Some other types of relatively low permeability formations containing heavy hydrocarbons may promote the production of shorter chain olefins.

Some in situ conversion processes may be run at sufficient pressure to generate a desirable steam cracker feed. A desirable steam cracker feed may be a feed with relatively high hydrocarbon content (e.g., a relatively high alkane content) and relatively low oxygen, sulfur, and/or nitrogen content. A desirable steam cracker feed may reduce the need to treat the sfream before processing in a steam cracker unit. Therefore, the desirable feed may be run directly from the in situ conversion process to a steam cracker unit. The steam cracker unit may produce olefins from the feed sfream.

In an in situ conversion process embodiment, a heated formation may be used to upgrade materials. Materials to be upgraded may be produced from the same portion of the fonnation and recycled, produced from other formations, or produced from other portions of the same formation.

During some in situ conversion process embodiments in selected formations (e.g., in tar sands formations), only a selected portion of a foπnation may be heated to relatively high temperatures (e.g., a temperature sufficient to cause pyrolysis). Other portions of the formation may still produce heavy hydrocarbons but may not be heated, or may only be partially heated (e.g., by steam, heat sources, or other mechanisms). The heavy hydrocarbons produced from the other less heated or unheated portions of the formation may be infroduced into the portion of the formation that is heated to a relatively high temperature. The high temperature portion of the formation may upgrade the introduced heavy hydrocarbons. Energy savings may be achieved since only a portion of the foimation is heated to a relatively high temperature. In an embodiment, surface mined tar (e.g., from tar sands) may be upgraded in a heated formation. The tar sands may be processed to produce separated hydrocarbons (e.g., tar). A portion of the tar may be heated, enfrained, and/or dissolved in a solvent to produce a flowable fluid. The solvent may be a portion of hydrocarbon fluid produced from the formation. The flowable fluid may be infroduced into the heated portion of the fonnation. Emulsions may be produced during some metal processing and/or hydrocarbon processing procedures. Some emulsions may be flowable. Other emulsions may be made flowable by the introduction of heat and/or a canier fluid. The canier fluid may be water and/or hydrocarbon fluid. The hydrocarbon fluid may be a fluid produced during an in situ process. A flowable emulsion may be introduced into a heated portion of a formation being subjected to in situ processing. In some embodiments, the heated portion may break the emulsion. The components of the emulsion may pyrolyze or react (e.g., undergo synthesis gas reactions) in the heated formation to produce desfred products from production wells. In some embodiments, the emulsion or components of the emulsion may remain in the formation.

Upgrading may include, but is not limited to, changing a product composition, a boiling point, or a freezing point. Examples of materials that may be upgraded include, but are not limited to, heavy hydrocarbons, tar, emulsions (e.g., emulsions from surface separation of tar from sand), naphtha, asphaltenes, and/or crude oil. In certain embodiments, surface mined tar may be injected into a foπnation for upgrading. Such surface mined tar may be partially treated, heated, or emulsified before being provided to a formation for upgrading. The material to be upgraded may be provided to the heated portion of the formation. The material may be upgraded in the formation. For example, upgrading may include providing heavy hydrocarbons having an API gravity of less than about 20°, 15°, 10°, or 5° into a heated portion of the formation. The heavy hydrocarbons may be cracked or distilled in the heated portion. The upgraded heavy hydrocarbons may have an API gravity of greater than about 20° (or above about 25° or above 30°). The upgraded heavy hydrocarbons may also have a reduced amount of sulfur and/or nifrogen. A property of the upgraded hydrocarbons (e.g., API gravity or sulfur content) may be measured to determine the relative upgrading of the hydrocarbons.

In some in situ conversion process embodiments, fluid produced from a formation may be fractionated in an above ground facility to produce selected components. The relatively heavier molecular weight components (e.g., bottom fractions from distillation columns) may be recycled into a formation. The heated formation may upgrade the relatively heavier molecular weight components.

In some in situ conversion process embodiments, heavy hydrocarbons may be produced at a first location. The heavy hydrocarbons may be diluted with a diluent to enable the heavy hydrocarbons to be pumped or otherwise transported to a different location. The mixture of heavy hydrocarbons and diluent may be separated at the heated fonnation prior to providing the heavy hydrocarbons mixture to the heated formation for upgrading. Alternately, the mixture of heavy hydrocarbons and diluent may be directly injected into a heated formation for upgrading and separation in the heated formation. In certain embodiments, a hot fluid (e.g., steam) may be added to the heavy hydrocarbons mixture to allow fluid cracking in the heated foπnation. Steam may inhibit coking in the foπnation, lessen the partial pressure of hydrocarbons in the formation, and/or provide a mechanism to sweep the formation. Controlling the flow of steam may provide a mechanism to control the residence time of the hydrocarbons in the heated formation. The residence time of the hydrocarbons in the heated formation may be used to control or adjust the molecular weight and/or API gravity of a product produced from the heated formation.

In an in situ conversion process embodiment, heavy hydrocarbons may be produced from a heated formation. The heavy hydrocarbons may be recycled back into the same formation to be upgraded. The upgraded products may be produced from the foimation. In another embodiment, the heavy hydrocarbon may be produced from one formation and upgraded in another formation at a different temperature. The residence time and temperature of the formation may be controlled to produce a desirable product. For example, a portion of fluid initially produced from a tar sands formation undergoing an in situ conversion process may be heavy hydrocarbons, especially if the hydrocarbons are produced from a relatively deep depth within a hydrocarbon containing layer of the tar sands formation. The produced heavy hydrocarbons may be reinttoduced into the formation through or adjacent to a heat source to facilitate upgrading of the heavy hydrocarbons. In an in situ conversion process embodiment, crude oil produced from a formation by conventional methods may be upgraded in a heated formation of the in situ conversion process system. The crude oil may be provided to a heated portion of the formation to upgrade the oil. In some embodiments, only a heavy fraction of the crude oil may be infroduced into the heated formation. The heated portion of the foπnation may upgrade the quality of the infroduced portion of the oil and/or remove some of the undesired components within the infroduced portion of the crade oil (e.g., sulfur and/or nifrogen).

In some embodiments, hydrogen or any other hydrogen donor fluid may be added to heavy hydrocarbons injected into a heated formation. The hydrogen or hydrogen donor may increase cracking and upgrading of the heavy hydrocarbons in the heated formation. In certain embodiments, heavy hydrocarbons may be injected with a gas (e.g., hydrogen or carbon dioxide) to increase and/or confrol the pressure within the heated formation.

In an in situ conversion process embodiment, a heated portion of a formation may be used as a hydrofreating zone. A temperature and pressure of a portion of the formation may be controlled so that molecular hydrogen is present in the hydrofreating zone. For example, a heat source or selected heat sources may be operated at high temperatures to produce hydrogen and coke. The hydrogen produced by the heat source or selected heat sources may diffuse or be drawn by a pressure gradient created by production wells towards the hydrofreating zone.

The amount of molecular hydrogen may be controlled by controlling the temperature of the heat source or selected heat sources. In some embodhnents, hydrogen or hydrogen generating fluid (e.g., hydrocarbons infroduced through or adjacent to a hot zone) may be introduced into the formation to provide hydrogen for the hydrotreating zone. In an in situ conversion process embodiment, a compound or compounds may be provided to a hydrofreating zone to hydrofreat the compound or compounds. In some embodiments, the compound or compounds may be generated in the formation by pyrolysis reactions of native hydrocarbons. In other embodiments, the compound or compounds may be infroduced into the hydrotreating zone. Examples of compounds that may be hydrofreated include, but are not limited to, oxygenates, olefins, nifrogen containing carbon compounds, sulfur containing carbon compounds, crude oil, synthetic crade oil, pitch, hydrocarbon mixtures, and/or combinations thereof.

Hydrofreating in a heated formation may provide advantages over conventional hydrotreating. The heated reservoir may function as a large hydrofreating unit, thereby providing a large reactor volume in which to hydrotreat materials. The hydrofreating conditions may allow the reaction to be run at low hydrogen partial pressures and/or at low temperatures (e.g., less than about 0.007 to about 1.4 bars or about 0.14 to about 0.7 bars partial pressure hydrogen and/or about 200 °C to about 450 °C or about 200 °C to about 250 °C). Coking within the formation generates hydrogen, which may be used for hydrofreating. Even though coke may be produced, coking may not cause a decrease in the throughput of the foπnation because of the large pore volume of the reservofr.

The heated foπnation may have lower catalytic activity for hydrotreating compared to commercially available hydrofreating catalysts. The formation provides a long residence time, large volume, and large surface area, such that the process may be economical even with lower catalytic activity. In some formations, metals may be present. These naturally present metals may be incoφorated into the coke and provide some catalytic activity during hydrofreating. Advantageously, a sfream generated or introduced into a hydrofreating zone does not need to be monitored for the presence of catalyst deactivators or destroyers.

In an embodiment, the hydrotreated products produced from an in situ hydrofreating zone may include a hydrocarbon mixture and an inorganic mixture. The produced products may vary depending upon, for example, the compound provided. Examples of products that may be produced from an in situ hydrofreating process include, but are not limited to, hydrocarbons, ammonia, hydrogen sulfide, water, or mixtures thereof. In some embodiments, ammonia, hydrogen sulfide, and/or oxygenated compounds may be less than about 40 weight % of the produced products.

In an in situ conversion process embodiment, a heated formation may be used for separation processes. FIG. 240 illusfrates an embodiment of a temperature gradient formed in a selected section of heated formation 8501.

Formation temperatures may decrease radially from heat source 8500 through the selected section. A fluid (either products from various surface processes and/or products from other sources such as crude oil) may be provided through injection well 8502. The fluid may pass through heated formation 8501. Some production wells 8503 may be located at various positions along the temperature gradient. For vapor phase production wells, different products may be produced from production wells that are at different temperatures. The ability to produce different compositions from production wells depending on the temperature of the production well may allow for production of a desired composition from selected wells based on boiling points of fluids within the formation. Some compounds with boiling points that are below the temperature of a production well may be entrained in vapor and produced from the production well. FIG. 241 illusfrates an embodiment for separating hydrocarbon mixtures in a heated portion of foπnation

8506. Temperature and/or pressure of the heated portion may be controlled by heat source 8504. A hydrocarbon mixture may be provided through injection well 8505 into a portion of the formation that is cooler than a portion of the formation closer to heat sources or production wells. In a cooler portion of fonnation 8506, relatively heavy molecular weight products may condense and remain in the formation. After separation of a desired quantity of hydrocarbon mixture, the cooler portion of the foimation may be heated to result in pyrolysis of a portion of the heavy hydrocarbons to desired products and/or mobilization of a portion of the heavy hydrocarbons to production well 8507.

In an embodhnent, a portion of a formation may be shut in at selected times to provide confrol of residence time of the products in the subsurface formation. Shutting in a portion of the formation by not producing fluid from production wells may result in an increase in pressure in the formation. The increased pressure may result in production of a lighter fluid from the formation when production is resumed. Different products may be produced based on the residence time of fluids in the formation.

Once a formation has undergone an in situ conversion process, heat from the process may remain within the formation. Heat may be recovered from the formation using a heat fransfer fluid. Heat fransfer fluids used to recover energy from a relatively low permeability formation containing heavy hydrocarbons may include, but are not limited to, foπnation fluids, product streams (e.g., a hydrocarbon sfream produced from crude oil infroduced into the formation), inert gases, hydrocarbons, liquid water, and or steam. FIG. 242 illustrates an embodhnent for recovering heat remaining in formation 8509 by providing a product sfream through injection well 8510. Heat remaining in the foπnation may fransfer to the product sfream. The formation heat may be confrolled with heat source 8508. The heated product sfream may be produced from the formation through production well 8511. The heat of the product sfream may be fransfened to any number of surface freatment units 8512 or to other formations.

In an in situ conversion process embodiment, heat recovered from the formation by a heat transfer fluid may be directed to surface freatment units to utilize the heat. For example, a heat transfer fluid may flow to a steam-cracking unit. The heat fransfer fluid may pass through a heat exchange mechanism of the steam-cracking unit to transfer heat from the heat transfer fluid to the steam-cracking unit. The transfened heat may be used to vaporize water or as a source of heat for the steam-cracking unit. In some in situ conversion process embodiments, heat transfer fluid may be used to transfer heat to a hydrofreating unit. The heat transfer fluid may pass through a heat exchange mechanism of the hydrofreating unit. Heat from the product sfream may be transfened from the heat fransfer fluid to the hydrotreating unit. Alternatively, a temperature of the heat fransfer fluid may be increased with a heating unit prior to processing the heat fransfer fluid in a steam cracking unit or hydrotreating unit. In addition, heat of a heat fransfer fluid may be fransfened to any other type of unit (e.g., distillation column, separator, regeneration unit for an activated carbon bed, etc.).

Heat from a heated formation may be recovered for use in heating another fonnation. FIG. 243 illusfrates an embodiment of a heat fransfer fluid provided through injection well 8515 into heated formation 8514. Heat may transfer from the heated formation to the heat fransfer fluid. Heat source 8513 may be used to control formation heat. The heat transfer fluid may be produced from production well 8516. The heat fransfer fluid may be directed through injection well 8517 to fransfer heat from the heat fransfer fluid to formation 8518. Formation conditions subsequent to an in situ conversion process may determine the heat fransfer fluid temperature. The heat fransfer fluid may be produced from production well 8519. In some embodiments, formation 8518 may include U-tube wells or closed casings with fluid insertion ports and fluid removal ports so that heat fransfer fluid does not enter into the rock of the formation.

Movement of the heat fransfer fluid (e.g., product streams, inert gas, steam, and/or hydrocarbons) through the formation may be confrolled such that any associated hydrocarbons in the formation are directed towards the production wells. The formation heat and mass fransfer of the heat fransfer fluid may be controlled such that fluids within the formation are swept towards the production wells. During remediation of a formation, the foπnation heat and mass fransfer of the heat transfer fluid may be confrolled such that transfer of heat from the formation to the heat fransfer fluid is accomplished simultaneously with clean up of the formation.

FIG. 244 illusfrates an in situ conversion process embodiment in which a heat fransfer fluid is provided to formation 8521a through injection well 8522. Heat within formation 8521a may be controlled by heat source 8520. The heat of the heat transfer fluid may be transfened to cooler formation 8521b. The heat fransfer fluid may be produced through production well 8523. In other embodiments, a heat transfer fluid may be directed to a plurality of formations to heat the plurality of formations.

FIG. 245 illustrates an embodiment for controlling foπnation 8525a to produce region of reaction 8525b in the formation. A region of reaction may be any section of the foπnation having a temperature sufficient for a reaction to occur. A region of reaction may be hotter or cooler than a portion of a fonnation proximate the region of reaction. Material may be directed to the region of reaction through injection well 8526. The material may be reacted within the region of reaction. Any number and any type of heat source 8524 may heat the formation and the region of reaction. Appropriate heat sources include, but are not limited to, elecfric heaters, surface burners, flameless disfributed combustors, and/or natural disfributed combustors. The product may be produced through production well 8527.

In some in situ conversion process embodiments, a region of reaction may be heated by transference of heat from a heated product to the region of reaction. In some embodiments, regions of reaction may be in series. A material may flow through the regions of reaction in a serial manner. The regions of reaction may have substantially the same properties. As such, flowing a material through such regions of reaction may increase a residence time of the material in the regions of reaction. Alternatively, the regions of reaction may have different properties (e.g., temperature, pressure, and hydrogen content). Flowing a material through such regions of reaction may include performing several different reactions with the material. Various materials may be reacted in a region of reaction. Examples of such materials include, but are not limited to, materials produced by an in situ conversion process and hydrocarbons produced from petroleum crude (e.g., tar, pitch, asphaltenes, heavy hydrocarbons, naphtha, methane, ethane, propane, and/or butane). In some in situ conversion process embodiments, a region of reaction may be formed by placing conduit

8530 in a heated portion of formation 8529. FIG. 246 depicts such an embodhnent of an in situ conversion process. A portion of conduit 8530 may be heated by the formation to form a region of reaction within the conduit. The conduit may inhibit contact between the material and the formation. The formation temperature and conduit temperature may be controlled by heat source 8528. Material may be provided through injection well 8531. The material may be produced through production well 8532.

A shape of a conduit may be variable. For example, the conduit may be curved, straight, or U-shaped (as shown in FIG. 247). U-shaped conduit 8534 may be placed within a heater well in a heated formation. Any number of materials may be reacted within the conduit. For example, water may be passed through a conduit such that the water is heated to a temperature higher than the initial water temperature. In other embodiments, water may be heated in a conduit to produce steam. Material may be provided through injection site 8535 and produced through production site 8536. The formation temperature may be controlled by heat source 8533.

In some in situ conversion process embodiments, formations may be used to store materials. A first portion of a formation may be subjected to in situ conversion. After in situ conversion, the first portion may be permeable and have a large pore volume. Formation fluid (e.g., pyrolysis fluid or synthesis gas) produced from another portion of the formation may be stored in the first portion. Alternately, the first portion may be used to store a separated component of formation fluid produced from the formation, a compressed gas (e.g., air), crude oil, water, or other fluid. Alternately, the first portion may be used to store carbon dioxide or other fluid that is to be sequestered.

Materials may be stored in a portion of the formation temporarily or for long periods of time. The materials may include inorganic and/or organic compounds and may be in solid, liquid, and/or gaseous form. If the materials are solids, the solid products may be stored as a liquid by dissolving the materials in a suitable solvent. If the materials are liquids or gases, they may be stored in such form. The materials may be produced from the foimation when needed. In some storage embodiments, the stored material may be removed from the formation by heating the formation using heat sources inserted in wellbores in the formation and producing the stored material from production wells. The heat sources may be heat sources used during a pyrolysis and/or synthesis gas generation phase of the in situ conversion process. The production wells may be production wells used during the pyrolysis and/or synthesis gas generation phase of the in situ conversion process. In other embodiments, the heat source and/or production wells may be wells that were originally used for a different purpose and converted to a new puφose. In some embodiments, some or all heat source and/or production wells may be newly foπned wells in the storage portion of the formation.

In a storage process embodiment, oil may be stored in a portion of a formation that has been subjected to an in situ conversion process. In some embodiments, natural gas may be stored in a portion of a formation that has been subjected to an in situ conversion process. If the formation is close to the surface, the shallow depth of the formation may limit gas pressure. In certain embodiments, close spacing of wells may provide for rapid recovery of oil and/or natural gas with high efficiency. In a storage process embodiment, compressed air may be stored in a portion of a formation that has been subjected to an in situ conversion process. The stored compressed air may be used for peak power generation, load leveling, and/or to even out and compensate for the variability of renewable power sources (e.g., solar and/or wind power). A portion of the stored compressed air may be used as an oxygen source for a natural disfributed combustor, flameless distributed combustor, and or a surface burner.

In an in situ conversion process embodiment, water may be provided to a hot formation to produce steam. The water may be applied during pyrolysis to help remove coke adjacent to or on heat sources and/or production wells. Water may also be infroduced into the formation after pyrolysis and/or synthesis gas generation is complete. The produced steam may sweep hydrocarbons towards production wells. The formation heat fransfer and mass transfer may be confrolled to clean the foimation during recovery of heat from the foπnation. The mfroduced water may absorb heat from the formation as the water is transformed to steam, resulting in cooling of the formation. The steam may be produced from the formation. Organic or other components in the steam may be separated from the steam and/or water condensed from the steam. The steam may be used as a heat transfer fluid in a separation unit or in another portion of the formation that is being heated. Cleaned or filtered water may be produced along with subsequent cooling of the formation.

In an in situ conversion process embodiment, a hot formation may treat water to remove dissolved cations (e.g., calcium and/or magnesium ions). The unfreated water may be converted to steam in the formation. The steam may be produced and condensed to provide softened water (e.g., water from which calcium and magnesium salts have been removed). If additional water is provided to the formation, the retained salts in the formation may dissolve in the water and "hard" water may be produced. Therefore, order of treatment may be a factor in water purification within a formation. A hot formation may sterilize infroduced water by destroying microbes.

In certain embodiments, a cooled formation may be used as a large activated carbon bed. After pyrolysis and/or synthesis gas generation a freated, cooled formation may be permeable and may mclude a significant weight percentage of char/coke. The formation may be substantially uniformly permeable without significant fluid passage fractures from wellbore to wellbore within the formation. Contaminated water may be provided to the cooled foimation. The water may pass through the cooled formation to a production well. Material (e.g., hydrocarbons or metal cations) may be adsorbed onto carbon in the cooled formation, thereby cleaning the water. In some embodiments, the formation may be used as a filter to remove microbes from the provided water. The filtration capability of the formation may depend upon the pore size distribution of the foπnation. A freated portion of formation may be used trap and filter out particulates. Water with particulates may be infroduced into a first wellbore. Water may be produced from production wells. When the particulate matter clogs the pore space adjacent to the first wellbore sufficiently to inhibit further introduction of water with particulates, the water with particulates may be infroduced into a different wellbore. A large number of wellbores in a fonnation subject to in situ freatment may provide an opportunity to purify a large volume of water and/or store a large amount of particulate matter in a formation.

Water quality may be improved using a heated formation. For example, after pyrolysis (and/or synthesis gas generation) is completed, formation water that was inhibited from passing into the formation during conversion by freeze wells or other types of baniers may be allowed to pass through the spent formation. The foπnation water may be passed through a hot formation to fonn steam and soften the water (i.e., ionic compounds are not present in significant amounts in the produced steam). The steam produced from the formation may be condensed to foπn formation water. The foπnation water may be passed through a carbon bed (in a surface facility or in a cooled, spent portion of the formation) to treat the formation water by adsoφtion, absoφtion, and/or filtering.

FIG. 248 illusfrates an embodiment for sequestering carbon dioxide as carbonate compounds in a portion of a formation. The carbon dioxide may be sequestered in the formation by forming carbonate compounds from the carbon dioxide through carbonation reactions with pore water. Energy input into heat sources 8537 may be used to confrol a temperature of the heated portion of formation 8540. Valves may be used to confrol a pressure of the heated portion of the foπnation. In other embodiments, carbon dioxide may be sequestered in a cooled formation by adsorbing the carbon dioxide on carbon than remains in the formation.

In the embodiment depicted in FIG. 248, solution 8538 is provided to the lower portion of the formation through well 8541 into dipping foπnation 8540. The solution may be obtained, for example, from natural groundwater flow or from an aquifer in a deeper formation. In an embodiment, the solution may be seawater. In some embodiments, the salt content of the water may be concentrated by evaporation. In certain embodiments, the solution may be obtained from man-made indusfrial solutions (e.g., slaked lime solution) or agricultural runoff. The solution may include sodium, magnesium, calcium, iron, manganese, and/or other dissolved ions. Furthermore, the solution may contact the ash from the spent formation as it is provided to the post treatment foπnation. Contact of the solution with the formation ash may produce a buffered, basic solution.

In some sequesfration embodiments, carbon dioxide 8539 may be provided to the upper portion of the formation through well 8542 simultaneously with providing solution 8538 to the formation. The solution may be provided to the lower portion of the formation, such that the solution rises through a portion of the provided carbon dioxide. Carbonate compounds may form in a dissolution zone at the interface of the solution and the carbon dioxide. In certain embodiments, the carbonate compounds may form by the reaction of the basic solution with the carbonic acid produced when the carbon dioxide dissolves in the solution. Other mechanisms, however, may also cause the formation and precipitation of the carbonate compounds.

The type of carbonate compounds formed may be determined by the dissolved ions in the solution. Examples of carbonate compounds include, but are not limited to, calcite (CaC0₃), magnesite (MgC0₃), siderite

(FeC0₃), rhodochrosite (MnC0₃), ankerite (CaFe(C0₃)₂), dolomite (CaMg(C0₃)₂), fenoan dolomite, magnesium ankerite, nahcolite (NaHC0₃), dawsonite (NaAl(0H)₂C0₃), and/or mixtures thereof. Other carbonate compounds that may be precipitated include, but are not limited to, cerussite (PbC0₃), malachite (Cu₂(OH)₂C0₃, azurite (Cu₃(OH)₂(C0₃)₂), smithsonite (ZnC0₃), witherite (BaC0₃), sfrontianite (SrC0₃), and/or mixtures thereof. A portion of the solution may be slowly withdrawn from the formation to deposit carbonate compounds within the formation. After withdrawal, the solution may be reinserted into the formation to continue precipitation of carbonate compounds in the formation. The solution may rise again through the provided carbon dioxide and additional carbonates may be foπned and precipitated. The solution may be cycled up and down within the fonnation to maximize the precipitation of carbonates within the fonnation. The carbonate compounds may remain within the foπnation.

In an embodiment, chemical compounds (e.g., CaO) may be added to the solution if the amount of ash remaining in the formation is insufficient to provide adequate buffering. In some embodiments, chemical compounds may be added to surface water to produce a solution.

Altering the pH of a solution in which carbon dioxide is dissolved may allow carbonate foπnation. Compounds that hydrolyze in different temperature ranges to produce basic compounds may be included in the solution. Therefore, altering the solution temperature may alter the solution pH, thus allowing carbonate foπnation. Compounds that hydrolyze to produce basic compounds may include cyanates and nitrites. Examples of cyanates and nitrites may include, but are not limited to, potassium cyanate, sodium cyanate, sodium nitrite, potassium nitrite, and/or calcium nitrite. In some embodiments, urea may also hydrolyze to produce a basic compound.

In a sequesfration embodiment, carbon dioxide may be allowed to diffuse throughout a solution within a formation. The solution may include at least one of the compounds that hydrolyze. The formation may be heated such that the compound(s) included in the solution hydrolyzes and produces a basic solution. The carbonate compounds may precipitate when appropriate ions (e.g., calcium and/or magnesium) are present. Altering the solution temperature may provide an ability to alter the occunence and rate of carbonate precipitation in the formation. Heat may be provided from heat sources in the fonnation. In a sequestration embodiment, carbon dioxide may be provided to a dipping formation. A solution may be provided to the dipping formation so that the solution contacts carbon dioxide to allow for precipitation of carbonate in the formation. Carbon dioxide and/or solution addition may be cycled to increase the amount of carbonate formed in the foπnation.

Foπnation of carbonate compounds may inhibit movement of mobile or released hydrocarbon compounds to groundwater. Formation of carbonate compounds may decrease the permeability of the fonnation and inhibit water or other fluid from migrating into or out of a portion of the formation in which carbonates have been formed. Foπnation of carbonates may decrease leaching of metals in the formation to groundwater, decrease formation deformation, and/or decrease well damage by providmg support for the remaining formation overburden. In certain in situ conversion process embodiments, the formation of carbonate compounds may be a part of the abandonment and reclamation process for the formation.

In an embodiment, heating during in situ conversion processes may cause decomposition of calcite (limestone) or dolomite to lime and magnesite. Upon carbonation, the calcite and dolomite may be reconstituted. The reconstitution may result in sequesfration of a significant volume of carbon dioxide.

In a sequesfration embodhnent, existing wellbores may be used during foπnation of carbonates in the formation. A solution may be provided to the formation and recovery of the solution may be provided from adjacent or closely spaced wells to create small circulation cells. In some embodiments with a dipping or thick formation, a counterflow of carbon dioxide and water may be applied. The carbon dioxide may be provided downdip (e.g., a point lower in the formation) and the solution provided updip (e.g., a point higher in the formation). The carbon dioxide and the solution may migrate past each other in a counterflow manner. In other embodhnents, the carbon dioxide may be bubbled up through a solution-filled foimation.

In a sequesfration embodiment, precipitation of mineral phases (e.g., carbonates) may cement together the friable and unconsolidated formation mafrix remaining after an in situ conversion process. In certain embodiments, the formation of minerals in an in situ foπnation may be similar to natural mineral formation and cementation, though significantly accelerated. In an embodiment, vertical and/or horizontal mineral formation near a well may provide at least some well integrity. Mineral precipitation may provide the formation around the well with higher cohesiveness and strength. The increased cohesiveness and strength may inhibit compaction and deformation of the foπnation around the wellbore.

In some in situ conversion process embodiments, non-hydrocarbon materials such as minerals, metals, and other economically viable materials contained within the formation may be economically produced from the formation. In some embodiments, the non-hydrocarbon materials may be mined or extracted from the formation following an in situ conversion process. However, mining or extracting material following an in situ conversion process may not be economically or environmentally favorable. In certain embodiments, non-hydrocarbon materials may be recovered and/or produced prior to, during, and/or after the in situ conversion process for freating hydrocarbons using an additional in situ process of treating the formation for producing the non-hydrocarbon materials.

In an embodiment for producing non-hydrocarbon material, a portion of the foπnation may be subjected to in situ conversion process to produce hydrocarbons and/or synthesis gas from the formation. The temperature of the portion may be reduced below the boiling point of water at formation conditions. A first fluid may be injected into the portion. The first fluid may be injected through a production well, heater well, or injection well. The first fluid may include an agent that reduces, mixes, combines, or fonns a solution with non-hydrocarbon materials to be recovered. The first fluid may be water, a basic solution, an acid solution, and/or a hydrocarbon fluid. In some embodiments, the first fluid may be introduced into the formation as a hot or warm liquid. The first fluid may be heated using heat generated in another portion of the formation and/or using excess heat from another portion of the foπnation. A second fluid may be produced in the formation from formation material and the first fluid. The second fluid may be produced from the formation through production wells. The second fluid may include desfred non- hydrocarbon materials from the formation. The non-hydrocarbon materials may include valuable metals such as, but not limited to, aluminum, nickel, vanadium, and gold. The non-hydrocarbon materials may also include minerals that contain phosphorus, sodium, or magnesium. In certain embodiments, the second fluid may include metals combined with minerals. For example, the second fluid may contain phosphates, carbonates, etc. Metals, minerals, or other non-hydrocarbon materials contained within the second fluid may be produced or extracted from the second fluid.

Producing the non-hydrocarbon materials may include separating the materials from the solution mixture. Producing the non-hydrocarbon materials may include processing the second fluid in a surface facility or refinery. In some embodiments, the first fluid may be circulated through the formation from an injection well to a removal site of the second fluid. Any portion of the first fluid remaining in the second fluid may be recirculated (or re- injected) into the formation as a portion of the first fluid. In other embodiments, the second fluid may be freated at the surface to remove non-hydrocarbon materials from the second fluid. This may reconstitute the first fluid from the second fluid. The reconstituted first fluid may be re-injected into the formation for further material recovery. In certain embodiments, a first fluid may be injected into a portion of the foimation that has been treated using an in situ conversion process. The first fluid may include water. The first fluid may break and/or fragment the foimation into relatively small pieces of mineral mafrix containing hydrocarbons. The relatively small pieces may combine with the first fluid to form a slurry. The slurry may be removed or produced from the formation. The slurry may be treated in a surface facility to separate the first fluid from the relatively small pieces of hydrocarbons. The mineral mafrix containing hydrocarbon pieces may be freated in a refining or exfraction process in a surface facility.

In some embodiments, non-hydrocarbon materials may be produced from a formation prior to treating the formation in situ. Heat may be provided to the formation from heat sources. The formation may reach an average temperature approaching below pyrolysis temperatures (e.g., about 260 °C or less). A first fluid may be injected into the formation. The first fluid may dissolve and or entrain formation material to form a second fluid. The second fluid may be produced from the fonnation. Some relatively low permeability formations containing heavy hydrocarbons may include nahcolite, frona, and/or dawsonite withm the formation. For example, nahcolite may be contained in unleached portions of a foπnation. Unleached portions of a formation are parts of the formation where groundwater has not leached out minerals within the formation Nahcolite is a mineral that includes sodium bicarbonate (NaHC0₃). Greater than about 5 weight %, and in some embodiments even greater than about 10 weight %, or greater than about 20 weight % nahcolite may be present in a formation. Dawsonite is a mineral that includes sodium aluminum carbonate (NaAl(C0₃)(OH)₂). Dawsonite may be present in a foπnation at weight percents greater than about 2 weight % or, in some embodiments, greater than about 5 weight %. The nahcolite and/or dawsonite may dissociate at temperatures used in an in situ conversion process of freating a formation. The dissociation is strongly endotheπnic and may produce large amounts of carbon dioxide. The nahcolite and/or dawsonite may be solution mined prior to, during, and/or following freating a formation in situ to avoid the dissociation reactions. For example, hot water may be used to form a solution with nahcolite. Nahcolite may form sodium ions (Na⁺) and bicarbonate ions (HC0₃ ^") in aqueous solution. The solution may be produced from the formation through production wells. A formation that includes nahcolite and/or dawsonite may be freated using an in situ conversion process.

A perimeter banier may be formed around the portion of the formation to be freated. The perimeter banier may inhibit migration of water into the treatment area. During an in situ conversion process, the perimeter banier may inhibit migration of dissolved minerals and formation fluid from the treatment area. During initial heating, a portion of the formation to be treated may be raised to a temperature below the disassociation temperature of the nahcolite. The first temperature may be less than about 90 °C, or in some embodiments, less than about 80 °C. The first temperature may be, however, any temperature that increases a reaction of a solution with nahcolite, but is also below a temperature at which nahcolite may dissociate (above about 95 °C at atmospheric pressure). A first fluid may be injected into the heated portion. The first fluid may include water, steam, or other fluids that may fonn a solution with nahcolite and/or dawsonite. The first fluid may be at an increased temperature (e.g., about 90 °C or about 100 °C). The increased temperature may be substantially similar to the first temperature of the portion of the formation.

In some embodiments, the portion of the formation may be at ambient temperature and the first fluid may be injected at an increased temperature. The increased temperature may be a temperature below a boiling point of the first fluid (e.g., about 90 °C for water). Providing the first fluid at an increased temperature may increase a temperature of a portion of the formation. Additional heat may be provided from one or more heat sources (e.g., a heater in a heater well) placed in the formation.

In other embodiments, steam is included in the first fluid. Heat from the injection of steam into the formation may be used to provide heat to the formation. The steam may be produced from recovered heat from the formation (e.g., from steam recovered during remediation of a portion) or from heat exchange with formation fluids and/or with surface facilities.

A second fluid may be produced from the formation following injection of the first fluid into the formation. The second fluid may include products of injection of the first fluid into the formation. For example, the second fluid may include carbonic acid or other hydrated carbonate compounds formed from the dissolution of nahcolite in the first fluid. The second fluid may also include minerals and or metals. The minerals and/or metals may include sodium, aluminum, phosphorus, and other elements. Producing the second fluid from the formation may reduce an amount of carbon dioxide produced from the formation during an in situ conversion process. Reducing the amount of carbon dioxide may be advantageous because the production of carbon dioxide from nahcolite is endothermic and uses significant amounts of energy. For example, nahcolite has a heat of decomposition of about 0.66 joules per kilogram (J/kg). The energy required to pyrolyze hydrocarbons in a formation using an in situ process may generally be about 0.35 J/kg. Thus, to decompose nahcolite from a formation having about 20 weight % nahcolite, about 0.13 J/kg additional energy would be needed. Removing nahcolite from a formation using a solution mining process prior to freating the fonnation using an in situ conversion process may significantly reduce carbon dioxide emissions from the formation as well as energy required to heat the formation.

Some minerals (e.g., trona, pirssonite, or gaylussite) may include associated water. Solution mining, or removing, such minerals before heating the formation may reduce costs of heating the formation to pyrolysis temperatures since associated water is removed prior to heating of the formation. Thus, the heat for dissociation of water from the mineral does not have to be provided to the formation.

FIG. 249 depicts an embodiment for solution mining a formation. Banier 6500 (e.g., a frozen banier) may be foπned around a circumference of treatment area 6510 of the formation. Banier 6500 may be any banier formed to inhibit a flow of water into or out of treatment area 6510. For example, banier 6500 may include one or more freeze wells that inhibit a flow of water through the banier. In some embodiments, banier 6500 has a diameter of about 18 m. Banier 6500 may be foπned using one or more banier wells 6502. Banier wells 6502 may have a spacing of about 2.4 m. Formation of banier 6500 may be monitored using monitor wells 6504 and/or by monitoring devices placed in banier wells 6502. Water inside treatment area 6510 may be pumped out of the freatment area through production well 6516.

Water may be pumped until a production rate of water is low. Heat may be provided to treatment area 6510 through heater wells 6514. The provided heat may heat freatment area 6510 to a temperature of about 90 °C or, in some embodiments, to a temperature of about 100 °C, 110 °C, or 120 °C. A temperature of treatment area 6510 may be monitored using temperature measurement devices placed in temperature wells 6518. A first fluid (e.g., water) may be injected through one or more injection wells 6512. The first fluid may also be injected through a heater or production well located in the formation. The first fluid may mix and/or combine with non-hydrocarbon materials (e.g., minerals, metals, nahcolite, and dawsonite) that are soluble in the first fluid to produce a second fluid. The second fluid, containing the non-hydrocarbon materials, may be removed from the freatment area through production well 6516 and/or heater wells 6514. Production well 6516 and heater wells 6514 may be heated during removal of the second fluid. After producing a majority of the non-hydrocarbon materials from freatment area 6510, solution remaining within the freatment area may be removed (e.g., by pumping) from the freatment area through production well 6516 and/or heater wells 6514. A relatively high permeability freatment area 6510 may be produced following removal of the non-hydrocarbon materials from the freatment area. Hydrocarbons within freatment area 6510 may be pyrolyzed and/or produced using an in situ conversion process of treating a formation following removal of the non-hydrocarbon materials. Heat may be provided to treatment area 6510 through heater wells 6514. A mixture of hydrocarbons may be produced from the foπnation through production well 6516 and/or heater wells 6514.

In certain embodiments, during an initial heating up to a temperature near a boiling temperature of water, unleached soluble minerals within the formation may be disaggregated and dissolved in water condensing within the formation. The water may be condensing in cooler portions of the foπnation. Some of these minerals may flow in the condensed water to production wells. The water and minerals are produced through the production wells.

Following an in situ conversion process, treatment area 6510 may be cooled during heat recovery by introduction of water to produce steam from a hot portion of the formation. Introduction of water to produce steam may vaporize some hydrocarbons remaining in the formation. Water may be injected through injection wells 6512.

The injected water may cool the formation. The remaining hydrocarbons and generated steam may be produced through production wells 6516 and or heater wells 6514. Treatment area 6510 may be cooled to a temperature near the boiling point of water.

Treatment area 6510 may be further cooled to a temperature at which water will begin to condense within the foπnation (i.e., a temperature below a boiling temperature of water). Removing the water or other solvents from freatment area 6510 may also remove any materials remaining in the freatment area that are soluble in water. The water may be pumped out of treatment area 6510 through production well 6516 and/or heater wells 6514. Additional water and/or other solvents may be injected into treatment area 6510. This injection and removal of water may be repeated until a sufficient water quality within treatment area 6510 is reached. Water quality may be measured at injection wells 6512, heater wells 6514, and/or production wells 6516. The sufficient water quality may be a water quality that substantially matches a water quality of freatment area 6510 prior to freatment.

In some embodiments, treatment area 6510 may include a leached zone located above an unleached zone. The leached zone may have been leached naturally and/or by a separate leaching process. In certain embodiments, the unleached zone may be at a depth of about 500 m. A thickness of the unleached zone may be about 100 m to about 500 m. However, the depth and thickness of the unleached zone may vary depending on, for example, a location of freatment area 6510 and a type of foimation. A first fluid may be injected into the unleached zone below the leached zone. Heat may also be provided into the unleached zone.

In certain embodiments, a section of a formation may be left unleached or without injection of a solution. The unleached section may be proximate a selected section of the formation that has been leached by providing a first fluid as described above. The unleached section may inhibit the flow of water into the selected section. In some embodiments, more than one unleached section may be proximate a selected section.

Water may be injected into the formation through a heater well or an injection well. The water may be heated and/or injected as steam. The water may be mjected at a temperature at or near the decomposition temperature of nahcolite. For example, the water may be at a temperature of about 70 °C, 90 °C, 100 °C, or 110 °C. Nahcolite within the formation may form an aqueous solution following the injection of water. The aqueous solution may be removed from the formation through a heater well, injection well, or production well. Removing the nahcolite removes material that would otherwise form carbon dioxide during heating of the foπnation to pyrolysis temperature. Removing the nahcolite may also inhibit the endothermic dissociation of nahcolite during an in situ conversion process. Removing the nahcolite may reduce mass within the formation and increase a permeability of the formation. Reducing the mass within the formation may reduce the heat required to heat to temperatures needed for the in situ conversion process. Reducing the mass within the formation may also increase a speed at which a heat front within the formation moves. Increasing the speed of the heat front may reduce a time needed for production to begin. In some embodiments, slightly higher temperatures may be used in the formation (e.g., above about 120 °C) and the nahcolite may begin to decompose. In such a case, nahcolite may be removed from the foπnation as a soda ash (Na₂C0₃). Nahcolite removed from the formation may be heated in a surface facility to form sodium carbonate and/or sodium carbonate brine. Heating nahcolite will form sodium carbonate according to the equation: (70) 2NaHC0₃ → Na₂C0₃ + C0₂ + H₂0.

The sodium carbonate brine may be used to solution mine alumina. The carbon dioxide produced may be used to precipitate alumina. If soda ash is produced from solution mining of nahcolite, the soda ash may be transported to a separate facility for freatment. The soda ash may be transported through a pipeline to the separate facility. Following removal of nahcolite from the formation, the formation may be treated using an in situ conversion process to produce hydrocarbon fluids from the formation. Remaining water is drained from the solution mining area through dewatering wells prior to heating to in situ conversion process temperatures. During the in situ conversion process, a portion of the dawsonite within the formation may decompose. Dawsonite will typically decompose at temperatures above about 270 °C according to the reaction:

(71) 2NaAl(0H)₂C0₃ → Na₂C0₃ + A1₂0₃ + 2H₂0 + C0₂.

The alumina formed from EQN. 71 will tend to be in the form of chi alumina. Chi alumina is relatively soluble in basic fluids.

Alumina within the formation may be solution mined using a relatively basic fluid following reaching pyrolysis temperatures of hydrocarbons within the formation. For example, a dilute sodium carbonate brine, such as 0.5 Normal Na₂C0₃, may be used to solution mine alumina. The sodium carbonate brine may be obtained from solution mining the nahcolite. Obtaining the basic fluid by solution mining the nahcolite may significantly reduce costs associated with obtaining the basic fluid. The basic fluid may be injected into the formation through a heater well and/or an injection well. The basic fluid may form an alumina solution that may be removed from the formation. The alumina solution may be removed through a heater well, injection well, or production well. An excess of basic fluid may have to be maintained throughout an alumina solution mining process.

Alumina may be extracted from the alumina solution in a surface facility. In an embodiment, carbon dioxide may be bubbled through the alumina solution to precipitate the alumina from the basic fluid. Carbon dioxide may be obtained from the in situ conversion process or from decomposition of the dawsonite during the in situ conversion process. In certain embodiments, a foπnation may include portions that are significantly rich in either nahcolite or dawsonite only. For example, a formation may contain significant amounts of nahcolite (e.g., greater than about 20 weight %) in a depocenter of the formation. The depocenter may contain only about 5 weight % or less dawsonite on average. However, in bottom layers of the foπnation, a weight percent of dawsonite may be about 10 weight % or even as high as about 25 weight %. In such formations, it may be advantageous to solution mine for nahcolite only in nahcolite-rich areas, such as the depocenter, and solution mine for dawsonite only in the dawsonite-rich areas, such as the bottom layers. This selective solution mining may significantly reduce a fluid cost, heating cost, and/or equipment cost associated with operating a solution mining process.

Nordsfrandite (Al(OH)₃) is another aluminum bearing mineral that may be found in a formation. Nordsfrandite decomposes at about the same temperatures (about 300 °C) as dawsonite and will produce alumina according to the equation:

(72) 2A1(0H)₃ -* A1₂0₃ + 3H₂0. Nordsfrandite is typically found in foπnations that also contain dawsonite and may be solution mined simultaneously with the dawsonite.

Solution mining dawsonite and nahcolite may be a simple process that produces only aluminum and soda ash from a formation. It may be possible to use some or all hydrocarbons produced from an in situ conversion process to produce direct cunent (DC) elecfricity on a site of the formation. The produced DC electricity may be used on the site to produce aluminum metal from the alumina using the Hall process. Aluminum metal may be produced from the alumina by melting the alumina in a surface facility on the site. Generating the DC elecfricity at the site may save on costs associated with using hydrofreaters, pipelines, or other surface facilities associated with transporting and/or freating hydrocarbons produced from the formation using the in situ conversion process. Some foπnations may also contain amounts of frona. Trona is a sodium sesquicarbonate

(Na₂C0₃-NaHC0₃-2H₂0) that has properties and undergoes reactions (including decomposition) very similar to those of nahcolite. Treatments for solution mining of frona may be substantially similar to treatments used for solution mining of nahcolite.

For certain types of formations, solution mining may be used to recover non-hydrocarbon materials prior to heating the fonnation to hydrocarbon pyrolysis temperatures. Examples of such materials may include nahcolite, dawsonite, and ammonia. Other non-hydrocarbon materials that may be solution mined include carbonates (e.g., frona, eitelite, burbankite, shortite, pirssonite, gaylussite, norsethite, thermonafrite), phosphates, carbonate- phosphates (e.g., bradleyite), carbonate chlorides (e.g., northupite), silicates (e.g., albite, analcite, sepiolite, loughlinite, labuntsovite, acmite, elpidite, magnesioriebeckite, feldspar), borosilicates (e.g., reedmergnerite, searlesite, leucosphenite), and halides (e.g., neighborite, cryolite, halite). Solution mining prior to hydrocarbon pyrolysis may increase a peπneability of the formation and/or improve other features (e.g., porosity) of the formation for the in situ process. Solution mining may also remove significant portions of compounds that will tend to endotheπnically dissociate at increased temperatures. Removing these endothermically dissociating compounds from the formation tends to decrease an amount of heat input required to heat the formation. For some types of formations, it may be advantageous to solution mine a formation after pyrolysis and/or synthesis gas production. Many different types of non-hydrocarbon materials may be removed from a formation following an in situ conversion process.

For example, phosphate may be removed from some foπnations. Recovered phosphate may be used in combination with ammonia and/or sulfur produced during the in situ conversion process to produce useable materials such as fertilizer.

Metals may also be recoverable from formations. Metals such as uranium, chromium, cobalt, nickel, gold, zinc, etc. may be recovered from formations such as bitumen deposits. For example, bitumen deposits may contain amounts of vanadium, nickel, uranium, platinum, or gold.

In one embodiment, oil production in solution mined formations may begin sooner and may befaster than oil production in the non-solution mined oil formationsln another embodiment, less heat may be needed to produce oil from solution mined foπnations than from non-solution mined foπnations.

In certain embodiments a soluble compound (e.g., phosphates, bicarbonates, alumina, metals, minerals, etc.) may be produced from a soluble compound containing formation (e.g., a fonnation that contains nahcolite, dawsonite, nordsfrandite, trona, carbonates, carbonate-phosphates, carbonate chlorides, silicates, borosililcates, etc.) that is different from a relatively low permeability formation containing heavy hydrocarbons. For example, the soluble compound containing formation may be adjacent (lower or higher) than the relatively low permeability formation containing heavy hydrocarbons, or at different non-adjacent depths than the relatively low permeability formation containing heavy hydrocarbons. In other embodiments, the soluble compound containing foπnation may be located at a different geographic location than the relatively low permeability fonnation containing heavy hydrocarbons. In an embodiment, heat is provided from one or more heat sources to at least a portion of a relatively low penneability formation containing heavy hydrocarbons. A mixture, at some point, may be produced from the foπnation. The mixture may include hydrocarbons from the formation as well as other compounds such as C0₂, H₂, etc. Heat from the formation, or heat from the mixture produced from the formation, may be used to adjust or change a quality of a first fluid that is provided to the soluble compound containing formation. Heat may be provided in the form of hot water or steam produced from the formation. In other embodiments, heat may be transfened by heat exchangers to the first fluid. In other embodiments, a heated portion or component from the mixture may be mixed with the first fluid to heat the fluid.

Alternately, or in addition, a component from the mixture produced from the relatively low permeability formation containing heavy hydrocarbons may be used to adjust a quality of a first fluid. For example, acidic compounds (e.g., carbonic acid, organic acids) or basic compounds (e.g., ammonium, carbonate, or hydroxide compounds) from the mixture produced from the relatively low permeability foπnation containing heavy hydrocarbons may be used to adjust the pH of the first fluid. For example, C0₂ from the relatively low permeability formation containing heavy hydrocarbons may be used with water to acidify the first fluid. In certain embodiments, components added to the first fluid (e.g., divalent cations, pyridines, or organic acids such as carboxylic acids or naphthenic acids) may increase the solubility of the soluble compound in the first fluid.

Once adjusted (e.g., heated and/or changed by having at least one component added to the first fluid), the first fluid may be injected into the soluble compound containing formation. The first fluid may, in some embodiments, include hot water or steam. The first fluid may interact with the soluble compound. The soluble compound may at least partially dissolve. A second fluid including the soluble compound may be produced from the soluble compound containing formation. The soluble compound may be separated from the second fluid sfream and freated or processed. Portions of the second fluid may be recycled into the formation.

In certain embodiments, heat from the relatively low permeability formation containing heavy hydrocarbons may migrate and heat at least a portion of the soluble compound containing foπnation. In some embodiments, the soluble compound containing formation may be substantially near, adjacent to, or intermixed with the relatively low permeability foimation containing heavy hydrocarbons. The heat that migrates may be useful to enhance the solubility of the soluble compound when the first fluid is applied to the soluble compound containing formation. Heat that migrates from the relatively low permeability foπnation containing heavy hydrocarbons may be recovered instead of being lost.

Reusing openings (wellbores) for different applications may be cost effective in certain embodiments. In some embodiments, openings used for providing the heat sources (or from producing from the relatively low penneability formation containing heavy hydrocarbons) may be used to provide the first fluid to the soluble compound containing formation or to produce the second fluid from the soluble compound containing formation. In certain embodiments, a solution may be first provided to, or produced from, a foπnation in a solution mining operation. The solution may be provided or produced through openings. One or more of the same openings may later be used as heater wells or producer wells for an in situ conversion process. Additionally, one or more of the same openings may be used again for providing a first fluid to the same formation layer or to a different foπnation layer. For example, the openings may be used to solution mine components such as nahcolite. These openings may further be used as heater wells or producer wells in the relatively low permeability formation containing heavy hydrocarbons. Then the openings may be used to provide the first fluid to either the hydrocarbon containing layer or a different layer at a different depth than the hydrocarbon containing layer. These openings may also be used when producing second fluid from the solution compound containing formation.

Relatively low permeability formations containing heavy hydrocarbons may have varied geometries and shapes. Conventional extraction techniques may not be appropriate for all foπnations. In some formations, rich hydrocarbon containing material may be positioned in layers that are too thin to be economically extracted using conventional methods. FIGS. 214 and 215 depict representations of embodiments of in situ conversion process systems that may be used to produce a thin rich hydrocarbon layer. To produce such layers, directionally drilled wells may be used to heat the thin hydrocarbon layer within the formation, plus a minimum amount of rock above and/or below. In some embodiments, the heat source wells may be placed in the rock above and/or below the thin hydrocarbon layer. The wells may be closely spaced to reduce heat losses and speed the heating process. In addition, drilling technologies such as geosteering, slim well, coiled tubing, and other techniques may be utilized to accurately and economically place the wells. Conductive heat losses to the sunounding formation may be offset by a high oil content of the thin hydrocarbon layer, rapid heating of the thin hydrocarbon layer (e.g., a heating rate in the range of about 1 °C/day to about 15 °C/day), and/or close spacing (meter scale) of heaters. Subsidence may be reduced, or even minimized, by positioning heater wells in a non-hydrocarbon and/or lean section of the fonnation immediately beneath and/or at the base of the thin hydrocarbon layer. A non-hydrocarbon and or lean section of the formation may lose less material than the thin hydrocarbon layer. Therefore, the structural integrity of formation may be maintained.

In some in situ conversion process embodiments, formations may be freated in situ by heating with a heat transfer fluid. A method for freating a formation may include injecting a heat fransfer fluid into the formation. In some embodiments, steam may be used as the heat fransfer fluid. The heat from the heat transfer fluid may fransfer to a selected section of the formation. In conjunction with heat from heat sources, the heat may pyrolyze at least some of the hydrocarbons within the selected section of the foπnation. A vapor mixture that includes pyrolysis products may be produced from the formation. The pyrolysis products may include hydrocarbons having an average API gravity of at least about 25°. The vapor mixture may also include steam.

In one embodhnent, hydrocarbons may be distilled from the fonnation. For example, hydrocarbons may be separated from the formation by steam distillation. The heat from the heat transfer fluid (e.g., steam), and or heat from heat sources, may vaporize some of the hydrocarbons within the selected section of the formation. The vaporized hydrocarbons may include hydrocarbons having a carbon number greater than about 1 and a carbon number less than about 8. The vapor mixture may include the vaporized hydrocarbons. For example, in a heavy hydrocarbon containing formation, pyrolyzation fluids and steam may distill a substantial portion of unconverted heavy hydrocarbons. In addition, coke, sulfur, nitrogen, oxygen, and or metals may be separated from formation fluid in the formation.

It may be advantageous to use steam injection for in situ treatment of heavy hydrocarbon or bitumen containing formations. In an embodhnent, steam injection and soaking with steam may be applied to formations that have sufficiently high permeability and homogeneity. Substantially uniform heating of a substantial portion of the hydrocarbons in a formation to pyrolysis temperatures with heat transfer from steam and heat sources (e.g., elecfric heaters, gas burners, natural disfributed combustors, etc.) may be enhanced if the formation has relatively high permeability and homogeneity. Relatively high permeability and homogeneity may allow the injected steam to contact a large surface area within the formation.

In certain embodiments, in situ freatment of hydrocarbons may be accomplished with a suitable combination of steam pressure, temperature, and residence time of injected steam, together with a selected amount of heat from heat sources, at a selected depth in the formation. For example, at a temperature of about 350 °C, at hydrostatic pressure, and at a depth of about 700 m to about 1000 m, a residence time of at least approximately one month may be requfred for in situ steam freatment of hydrocarbons with steam and heat sources.

In some embodiments, relatively deep foπnations may be particularly suitable for in situ treatment with heat sources and steam injection. Higher steam pressures and temperatures may be readily maintained in relatively deep foπnations. Furthermore, steam may be at or approaching supercritical conditions below a particular depth.

Supercritical steam or near supercritical steam may facilitate pyrolyzation of hydrocarbons. In other embodiments, in situ treatment of a relatively shallow formation may be performed with a sufficient amount of oveφressure (e.g., an oveφressure above a hydrostatic pressure). The amount of oveφressure may depend on the strength of the formation or the overburden of the formation. In an embodiment, in situ treatment of a formation may include heating a selected section of the formation with one or more heat sources, and one or more cycles of steam injection. The cycles of steam may soak the formation with steam for a selected time period. The selected time period may be about one month. In other embodhnents, the selected time period may be about one month to about six months. The selected section may be heated to a temperature between about 275 °C and about 350 °C. In another embodiment, the formation may be heated to a temperature of about 350 °C to about 400 °C. A vapor mixture, which may include pyrolyzation fluids, may be produced from the formation through one or more production wells placed in the formation.

In certain embodiments, in situ freatment of a formation may include continuous steam injection into the foπnation, together with addition of heat from heat sources. Pyrolyzation fluids may be produced from different portions of the formation during such freatment. FIG. 251 illustrates a schematic of an embodiment of continuous production of a vapor mixture from a formation. FIG. 251 includes formation 8262 with heat fransfer fluid injection well 8264 and well 8266. The wells may be members of a larger pattern of wells placed throughout the foπnation. A portion of a foπnation may be heated to pyrolyzation temperatures by heating the formation with heat sources and an injected heat fransfer fluid. Heat fransfer fluid 8268, such as steam, may be injected through injection well 8264. Other wells may be used to provide the steam. Injected heat fransfer fluid may be at a temperature between about 300 °C and about 500 °C. In an embodiment, heat transfer fluid 8268 is steam.

Heat transfer fluid 8268, and heating from the heat sources, may heat region 8263 of the formation between wells 8264 and 8266. Such heating may heat region 8263 into a selected temperature range (e.g., between about 275 °C and about 400 °C). An advantage of a continuous production method may be that the temperature across region 8263 may be substantially uniform and substantially constant with time once the formation has reached substantial thermal equilibrium. Vapor mixture 8270 may exit continuously through well 8266. Vapor mixture 8270 may include pyrolysis fluids and/or steam. In one embodiment, vapor mixture 8270 may be fed to surface separation unit 8272. Separation unit 8272 may separate vapor mixture 8270 into sfream 8274 and hydrocarbons 8276. Sfream 8274 may be composed primarily of steam or water. Sfream 8274 may be re-injected into the formation. Hydrocarbons may include pyrolysis fluids and hydrocarbons distilled from the formation. In an embodiment, production of a vapor mixture from a formation may be performed in a batch mode. Injection of the heat fransfer fluid may continue for a period of time, together with heat from one or more heat sources. In an embodiment, heat from the heat sources may combine with heat from transfer fluid until the temperature of a portion of the formation is at a desired temperature (e.g., between about 275 °C and about 400 °C). Higher or lower temperatures may also be used. Alternatively, injection may continue until a pore volume of the portion of the formation is substantially filled. After a selected period of time subsequent to ceasing injection of the heat fransfer fluid, vapor mixture 8270 may be produced from the foπnation through wellbore 8266. The vapor mixture may include pyrolysis fluids and/or steam. In some embodiments, the vapor mixture may exit through wellbore 8264. In an embodiment, the selected period of time may be about one month. Injected steam may contact a substantial portion of a volume of the formation to be treated. The heat fransfer fluid may be injected through one or more injection wells. Similarly, the heat sources may be placed in one or more heater wells. The injection wells may be located substantially horizontally in the foπnation. Alternatively, the injection wells may be disposed substantially vertically or any desired angle (e.g., along dip of the fonnation). The heat transfer fluid may be injected into regions of relatively high water saturation. Relatively high water saturation may include water concenfrations greater than about 50 volume percent. In some embodiments, the average spacing between injection wells may be between about 40 m and about 50 m. In other embodiments, the average spacing may be between about 50 m and about 60 m.

In an embodiment, the heat from injection of a heat fransfer fluid, together with heat from one or more heat sources, may pyrolyze at least some of the hydrocarbons in the selected first section. In certain embodiments, the heat may mobilize at least some of the hydrocarbons within the selected first section. Injection of a heat transfer fluid, and/or heat from the heat sources, may decrease a viscosity of hydrocarbons in the formation. Decreasing the viscosity of the hydrocarbons may allow the hydrocarbons to be more mobile. In addition, some of the heat may partially upgrade a portion of the hydrocarbons. Partial upgrading may reduce the viscosity and/or mobilize the hydrocarbons. Some of the mobilized hydrocarbons may flow (e.g., due to gravity) from the selected first section of the formation to a selected second section of the fonnation. Heat from the heat fransfer fluid and the heat sources may pyrolyze at least some of the mobilized fluids in the selected second section.

In some embodiments, heat may be provided from one or more heat sources to at least one portion of the formation. The one or more heat sources may include elecfric heaters, flameless disfributed combustors, or natural distributed combustors. Heat from the heat sources may fransfer to the selected first section and the selected second section of the formation. The heat may heat or superheat steam injected into the formation. The heat may also vaporize water in the formation to generate steam. In addition, the heat from the heat sources may mobilize and/or pyrolyze hydrocarbons in the selected first section and/or the selected second section of the foπnation.

In an embodiment, the selected first section and the selected second section may be located in a relatively deep portion of the formation. For example, a relatively deep portion of a formation may be between about 100 m and about 300 m below the surface. Heat from the heat sources and the heat transfer fluid may pyrolyze at least some of the hydrocarbons within the selected second section of the formation. In some embodiments, at least about 20 percent of the hydrocarbons in the formation may be pyrolyzed. The pyrolyzed hydrocarbons may have an average API gravity of at least about 25°.

In an embodiment, a vapor mixture may be produced from the formation. The vapor mixture may contain pyrolyzed fluids. In other embodiments, the vapor mixture may contain pyrolyzed fluids and/or heat fransfer fluid.

The vapor mixture may include hydrocarbons distilled from the formation. The heat fransfer fluid may be separated from the pyrolyzed fluids and distilled hydrocarbons at the surface of the formation. For example, heat fransfer fluid may be separated using a membrane separation method. Alternatively, heat fransfer fluid may be separated from pyrolyzed fluids and distilled hydrocarbons in the formation. The pyrolyzed fluids and distilled hydrocarbons may then be produced from the formation. In an embodiment, the vapor mixture may be produced from the selected second section of the formation.

Alternatively, the vapor mixture may be produced from the selected first section.

In one embodhnent, the mobilized fluids may be partially upgraded in the selected second section. The partially upgraded fluids may be produced from the fonnation and re-injected back into the formation.

In certain embodiments, the vapor mixture may be produced through one or more production wells. In some embodiments, at least some of the vapor mixture may be produced through a heat source wellbore.

In one embodiment, a liquid mixture composed primarily of condensed heat fransfer fluid may accumulate in a portion of the formation. The liquid mixture may be produced from the formation. The liquid mixture may include liquid hydrocarbons. The condensed heat fransfer fluid may be separated from the liquid hydrocarbons in the formation and the condensed heat fransfer fluid may be produced from the formation. Alternatively, the liquid mixture may be produced from the formation and fed to a separation unit. The separation unit may separate the condensed heat transfer fluid from the liquid hydrocarbons. The liquid hydrocarbons may then be re-injected into the formation.

FIG. 252 illusfrates a cross-sectional representation of an embodiment of an in situ treatment process with steam injection. Portion 8300 of the formation may be treated with steam injection. Portion 8301 may be untreated. Horizontal injection and/or heat source wells 8302 may be located in an upper or selected first section of portion 8300. Horizontal production wells 8304 may be located in a lower or selected second section of portion 8300. The wells may be members of a larger pattern of wells placed throughout a portion of the formation.

Steam may be injected into the formation through wells 8302, and/or heat sources may be placed in such wells 8302 and provide heat to the formation and/or to the steam. The heat from the steam and the heat sources may heat the selected first and second sections to pyrolyzation temperatures and pyrolyze some of the hydrocarbons in the sections. In addition, heat from the steam injection and the heat sources may mobilize some hydrocarbons in the sections. The mobilized hydrocarbons in the selected first section may flow (e.g., by gravity and or flow towards low pressure of a pressure gradient established by production wells) to the selected second section as indicated by anows 8306. Some of the mobilized hydrocarbons may be pyrolyzed in the selected second section. Pyrolyzed fluids and or mobilized fluids may be produced through production wells 8304. In an embodiment, condensed fluids (e.g., condensed steam) may be produced through production wells in the selected second section. FIG. 253 illusfrates a cross-sectional representation of an embodiment of an in situ freatment process with steam injection and heat sources. Portion 8310 of the formation may be treated with heat from heat sources and steam injection. Portion 8311 may be unfreated. Portion 8310 may include a horizontal heat source and/or injection well 8314 located in an upper or selected first section. Horizontal production well 8312 may be located above the injection well in the selected first section of portion 8310. The production well and/or the injection well may include a heat source. Water and oil production well 8316 may be placed in the selected second section of the formation. The wells may be members of a larger pattern of wells placed throughout a portion of the formation.

Heat and/or steam may be provided to the formation through well 8314. Such heat and steam may heat the selected ffrst and second sections to pyrolyzation temperatures. Hydrocarbons may be pyrolyzed in the selected first section between well 8312 and well 8314. In addition, the heat may mobilize some hydrocarbons in the sections. The mobilized hydrocarbons in the selected first section may flow through region 8319 to the selected second section as indicated by anows 8318. Some of the mobilized hydrocarbons may be pyrolyzed in the selected second section. Pyrolyzed fluids and/or mobilized fluids may be produced tiirough production well 8312. In addition, condensed fluids (e.g., steam) may be produced through production well 8316 in the selected second section.

In one embodiment, a method of freating a hydrocarbon containing formation in situ may include heating the formation with heat sources, and also injecting a heat fransfer fluid into a formation and allowing the heat transfer fluid to flow through the formation. Heat transfer fluid may be injected into the formation through one or more injection wells. The injection wells may be located substantially horizontally in the formation. Alternatively, the injection wells may be disposed substantially vertically in the formation or at a desired angle. The size of a selected section of the formation may increase as a heat fransfer fluid front migrates through the foimation. "Heat transfer fluid front" is a moving boundary between the portion of the formation freated by heat fransfer fluid and the portion unfreated by heat fransfer fluid. The selected section may be a portion of the formation freated or contacted by the heat fransfer fluid. Heat from the heat transfer fluid, together with heat from one or more heat sources, may pyrolyze at least some of the hydrocarbons within the selected section of the formation. In an embodiment, the average temperature of the selected section may be about 300 °C, which conesponds to a heat fransfer fluid pressure of about 90 bars.

In some embodiments, heat from the heat fransfer fluid and/or one or more heat sources may mobilize at least some of the hydrocarbons at the heat fransfer fluid front. The mobilized hydrocarbons may flow substantially parallel to the heat fransfer fluid front. Heat from the heat transfer fluid, in conjunction with heat from the heat sources, may pyrolyze at least some of the hydrocarbons in the mobilized fluid.

In an embodiment, a vapor mixture may migrate to an upper portion of the formation. The vapor mixture may include pyrolysis fluids. The vapor mixture may also include heat fransfer fluid and/or distilled hydrocarbons. In an embodiment, the vapor mixture may be produced from an upper portion of the formation. The vapor mixture may be produced through one or more production wells located substantially horizontally in the formation.

In one embodiment, a portion of the heat fransfer fluid may condense and flow to a lower portion of the selected section. A portion of the condensed heat fransfer fluid may be produced from a lower portion of the selected section. The condensed heat fransfer fluid may be produced through one or more production wells. Production wells may be located substantially horizontally in the foπnation. FIG. 254 illustrates a cross-sectional representation of an embodiment of an in situ freatment process with heat sources and steam injection. Portion 8320 of the formation may be freated with heat sources and steam injection. Portion 8321 may be untreated. Portion 8320 may include horizontal heat source and/or injection well 8326. Alternatively or in addition, portion 8320 may include vertical heat source and/or injection well 8324. Horizontal production well 8328 may be located in an upper portion of the formation. Portion 8320 may also include condensed fluid production well 8330 (production well 8330 may contain one or more heat sources). The wells may be members of a larger pattern of wells placed throughout a portion of the foπnation.

Heat and/or steam may be provided into the formation through wells 8326 or 8324. The heat and or steam may flow through the formation in the direction indicated by anows 8332. A size of a section treated by the heat and/or steam (i.e., a selected section) increases as the heat and/or steam flows through the unfreated portion of the formation. The formation may include migrating heat and/or steam front 8339 at a boundary between portion 8320 and portion 8321. Mobilized fluids may flow in the direction of anows 8334 toward production well 8328. Fluids may be pyrolyzed and produced through production well 8328. Steam and distilled hydrocarbons may also be produced through well 8328. In addition, condensed fluids may flow downward in the direction of anows 8336. The condensed fluids may be produced through production well 8330. The heat source in production well 8330 may pyrolyze some of the produced hydrocarbons.

Heat form the heat sources and or steam may mobilize some hydrocarbons at the migrating steam front. The mobilized hydrocarbons may flow downward in a direction substantially parallel to the front as indicated by anow 8338. A portion of the mobilized hydrocarbons may be pyrolyzed. At least some of the mobilized hydrocarbons may be produced through production well 8328 or production well 8330. In certain embodiments, existing steam freatment processes/systems may be enhanced by the addition of one or more heat sources to the process/system. Heat sources may be placed in locations such that heat from the heat source openings will heat areas of the formation that are not heated (or that are less heated) by the steam. For example, if the steam is preferentially flowing in certain pathways through the fonnation, the heat sources may be placed in locations that heat areas of the foπnations that are less heated by steam in these pathways. In some embodiments, hydrocarbon fluids may be produced through a heel portion of a wellbore of a heat source. The heel portion of the heat source may be at a lower temperature than the toe portion of the heat source. Efficiency and production of hydrocarbons from a steam flood may be enhanced.

Some hydrocarbon containing formations may contain a significant portion of adsorbed and/or absorbed methane. Often such methane is present in foπnations saturated with formation water. The formation may be in a water recharge zone. A small portion of the methane may be produced from hydrocarbon containing formations by removing the formation water. The removal of formation water may reduce pressure in the hydrocarbon containing formation and cause the release of some adsorbed methane. In some embodiments, the dewatering process may result in recovery of up to about 30 % of adsorbed methane from a portion of the formation.

Increasing the average temperature of a formation with entrained methane may increase the yield of methane from the foimation. Substantial recovery of enfrained methane may be achieved at a temperature at or above approximately the boiling point of water in the formation. During heating, substantially all free moisture may be removed from a portion of the formation after the portion has reached an average temperature of about the ambient boiling point of water.

In certain embodiments, substantially complete recovery of methane from a coal formation may yield between about 1 m³/ton and about 30 mVton. Methane recovered from thermal desoφtion during heating may be used as fuel for an in situ freatment process. For example, methane may be used for power generation to run electric heater wells. In addition, methane may be used as fuel for gas fired heater wells or combustion heaters.

All or almost all methane that is entrained in a hydrocarbon fonnation may be produced during an in situ conversion process. In an embodiment, freeze wells may be installed around a portion of a formation that includes adsorbed methane to define a freatment area. Heat sources, production wells, and/or dewatering wells may be installed in the treatment area prior to, simultaneously with, or after installation of the freeze wells. The freeze wells may be activated to form a frozen banier that inhibits water inflow into the freatment area. After formation of the frozen banier, dewatering wells and/or selected production wells may be used to remove formation water from the treatment area. Some of the methane enfrained within the formation may be released from the formation and recovered as the water is removed. Heat sources may be activated to begin heating the formation. Heat from the heat sources may release methane enfrained in the formation. The methane may be produced from production wells hi the freatment area. Early production of adsorbed methane may significantly improve the economics of an in situ conversion process.

Freeze wells may be used to isolate deep coal beds (e.g., coal in the Powder River Basin). Isolating the coal bed allows dewatering to remove coal bed methane gas. The coal beds often include aquifers with flow rates that would otherwise inhibit production of coal bed methane. The use of freeze wells may enable the dewatering of these coal beds and production of coal bed methane.

Water, in the form of saline or a solution with high levels of dissolved solids, may be provided to a hot spent reservofr. Water to be desalinated in a hot spent reservoir may originate from the ocean and/or from deep non-potable reservoirs. As water flows into the hot spent reservoir, the water may be evaporated and produced from the formation as steam. This water may be condensed into potable water having a low total dissolved solids content. Condensation of the produced water may occur in surface facilities or in subsurface conduits. Salts and other dissolved solids may remain in the reservofr. The salts and dissolved solids may be stored in the reservoir. Alternatively, effluent from surface facilities may be provided to a hot spent formation for desalinization and/or disposal. Utilizing a hot spent formation to desalinate fluids may recover some heat from the formation. After a temperature within the formation falls below a boiling point of a fluid, desalinization may cease. Alternatively, a section of a formation may be continually heated to maintain conditions appropriate for desalinization. Desalinization may continue until a peπneability and/or a porosity of a section is significantly reduced from the precipitation of solids. In some embodiments, heat from surface facilities may be used to run a surface desalinization plant, with produced salts and solids being injected into a portion of the foπnation, or to preheat fluids being injected into the formation to minimize temperature change within the formation.

Water generated from a desalination process may be sold to a local market for use as potable and/or agricultural water. The desalinated water may provide additional resources to geographical areas that have severe water supply limitations. Combustion of gaseous by-products from an in situ conversion process as well as fluids generated in surface facilities may be utilized to generate heat and/or energy for use in the in situ conversion process. For example, a low heating value stream (LHV stream), such as tail gas from the treating/recovery operations, may be catalytically combusted to generate heat and increase temperatures to a range needed for the in situ conversion process. A monolithic substrate (i.e., honeycomb such as Torvex (Du Pont) and/or Cordierite (Coming)) with good flow geometry and/or minimal pressure drops may be used in the combustor. In a conventional process, a gaseous by-product sfream may be flared, since the heating value is considered too low to sustain stable thermal combustion. Utilizing energy in these sfreams may increase an overall efficiency of the treatment system for formations.

U.S. Patent No. 4,640,352 to Van Meurs et al., which is incoφorated by reference as if fully set forth herein, describes a method for recovering hydrocarbons (e.g., heavy hydrocarbons) from a low permeability subtenanean reservoir of the type comprised primarily of diatomite. At least two wells may be completed into a freatment interval having a thickness of at least about 30 m within an oil and water-containing zone. The zone may be both undesirably impermeable and non-productive in response to injections of oil-displacing fluids. The wells may be ananged to provide at least one each of heat-injecting and fluid-producing wells having boreholes. The wells may, substantially throughout the freatment interval, be substantially parallel and separated by substantially equal distances of at least about 6 m. In each heat-injecting well, substantially throughout the treatment interval, the face of the reservoir formation may be sealed with a solid material or cement which is relatively heat conductive and substantially fluid impermeable. Sealing of each heat-injecting well may inhibit fluid from flowing between the interior of the borehole and the reservoir. In each fluid-producing well, substantially throughout the treatment interval, fluid communication may be established between the well borehole and the reservoir foimation and the well is ananged for producing fluid from that formation. Heavy hydrocarbons may be contained in diatomite formations. The term "diatomite formation" is defined as a fonnation of a siliceous sedimentary rock composed of the siliceous skeletal remains of single-celled aquatic plants called "diatoms."

Heavy hydrocarbons containing diatomite fonnations may have a relatively high porosity, high internal surface area, high absoφtive capacity, relatively low permeability, and relatively high oil saturation. "Relatively high porosity" is, with respect to diatomite or portions thereof, an average porosity of greater than about 50 %. The low permeability of diatomite formations may be due to the scarcity of flow channels or fractures through which oil may flow and, ultimately, be recovered. Such deposits, in addition to the oil saturated diatomaceous particles, may also contain some fine clay, silt, and water.

An "oil containing formation" is a rock formation that includes microscopic pores in coarser sediments of rock. The rock may be composed of shales, limestone, and carbonates. Oil may be present in interstices between rocks and within the pores. An oil containing formation generally has a relatively high porosity and relatively high oil saturation. The average porosity may be greater than about 15 %. The average oil saturation may be greater than about 40 %. Oil containing formations may have sections greater than about 10 m in thickness.

In an embodiment, heat sources may be initiated in stages to confrol the volumefric production rate. Staging may allow substantially constant production throughout production from the formation (e.g., ignoring initial heating time of the ffrst stage).

In certain embodiments, a portion of the formation fluids in relatively deep sections of a formation may reach a supercritical state. Condensable and non-condensable formation fluids in a supercritical state may become miscible, which may allow single-phase flow through the deep sections of the formation. Fractures may be created by expansion of the heated portion of the formation mafrix. In addition, fractures may also be created by increased pressure from expanding formation fluids and products generated from pyrolysis. In some embodiments, hydrocarbons such as kerogen, pyrobitumen, and/or bitumen may block pores in a portion of the formation. Such hydrocarbons may dissolve or pyrolyze during heating, resulting in an increase in the permeability of the portion of the formation. In one embodiment, vaporization of the aqueous fluids in pores of the formation may result in separation of hydrocarbons from water. The vaporizing water may cause some local fracturing of the rock matrix. Hydrocarbons may migrate by film drainage, which may further increase the effective permeability of the formation. The relatively low viscosity of the hydrocarbons may increase the possibility of migration of hydrocarbons by film drainage. The relatively low viscosity may be due to the relatively high temperature in the formation.

In certain embodiments, heat from the heat sources may shrink clays present in a portion of the formation. Shrinkage of the clay may increase permeability of the portion.

In an embodiment, a method of freating an oil containing formation in situ may include injecting a recovery fluid into a formation. The recovery fluid may be water. Heat from one or more heat sources may provide heat to the formation. At least one of the heat sources may be an electric heater. In one embodiment, at least one of the heat sources may be located in a heater well. A heater well may include a conduit through which flows a hot fluid that transfers heat to the formation. At least some of the recovery fluid in a selected section of the formation may be vaporized by heat from the heat sources. For example, water may be vaporized into steam. Heat from the heat sources and the vaporized recovery fluid may pyrolyze at least some hydrocarbons within the selected section. A temperature for pyrolysis may be from about 270 °C to about 400 °C. A gas mixture that includes pyrolyzation fluids and steam may be produced from the formation. In one embodiment, fluids may be produced tiirough a production well. The pressure at or near the heat sources may increase due to theπnal expansion of the formation and vaporization of the recovery fluid. The pressure differential between the heat sources and production wells may force steam and/or pyrolyzation fluids toward the production wells. In one embodiment, the gas mixture may include hydrocarbons having an average API gravity greater than about 25°.

FIG. 255 illustrates a schematic of an embodhnent of in situ freatment of an oil containing formation. FIG. 255 includes formation 8340 with heat source well 8342 and production well 8344. The wells may be members of a larger pattern of wells placed throughout a portion of the formation. Recovery fluid 8346 may be injected into the formation through heat source well 8342. Water may be used as a heat recovery fluid. Heat from heat source well 8342 may vaporize some of the water in the formation to produce steam. Heat from the heat sources and/or the steam may pyrolyze hydrocarbons in the formation.

In an embodiment, a pressure differential may be created in region 8341 between heat source well 8342 and production well 8344 due to thermal expansion of the foπnation and vaporization of the steam. Steam and pyrolyzation fluids may be forced by the pressure gradient from heat source well 8342 towards production well 8344. Steam and pyrolyzation fluids stream 8348 may be produced from production well 8344.

Stream 8348 may be fed to surface separation unit 8350. Separation unit 8350 may separate stream 8348 into sfream 8354 and hydrocarbons 8352. Sfream 8354 may be composed primarily of steam or water. Steam may be used in power generation units 8356 or heat exchange mechanisms 8358 or injected back into the foimation. In this patent, certain U.S. patents, U.S. patent applications, and other materials (e.g., articles) have been incoφorated by reference. The text of such U.S. patents, U.S. patent applications, and other materials is, however, only incoφorated by reference to the extent that no conflict exists between such text and the other statements and drawings set forth herein. In the event of such conflict, then any such conflicting text in such incoφorated by reference U.S. patents, U.S. patent applications, and other materials is specifically not incoφorated by reference in this patent. Further modifications and alternative embodiments of various aspects of the invention may be apparent to those skilled in the art in view of this description. Accordingly, this description is to be construed as illustrative only and is for the ptupose of teaching those skilled in the art the general manner of carrying out the invention. It is to be understood that the forms of the invention shown and described herein are to be taken as the presently prefened embodiments. Elements and materials may be substituted for those illusfrated and described herein, parts and processes may be reversed, and certain features of the invention may be utilized independently, all as would be apparent to one skilled in the art after having the benefit of this description of the invention. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as described in the following claims.

Claims

WHAT IS CLAIMED IS:

1. A method of freating a relatively low peπneability fonnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; confrolling the heat from the one or more heat sources such that an average temperature within at least a majority of the selected section of the foπnation is less than about 375 °C; and producing a mixture from the formation.

2. The method of claim 1, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

3. The method of claim 1 , wherein controlling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

4. The method of claim 1, wherein the one or more heat sources comprise electrical heaters.

5. The method of claim 1, wherein the one or more heat sources comprise surface burners.

6. The method of claim 1, wherein the one or more heat sources comprise flameless disfributed combustors.

7. The method of claim 1, wherein the one or more heat sources comprise natural distributed combustors.

8. The method of claim 1, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

9. The method of claim 1 , further comprising confrolling a pressure within at least a majority of the selected section of the formation with a valve coupled to at least one of the one or more heat sources.

10. The method of claim 1, further comprising confrolling a pressure within at least a majority of the selected section of the formation with a valve coupled to a production well located in the formation.

11. The method of claim 1, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

12. The method of claim 1, wherein providing heat from the one or more heat sources to at least the portion of foπnation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

13. The method of claim 1, wherein allowing the heat to transfer from the one or more heat sources to the selected section comprises fransfening heat substantially by conduction.

14. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

15. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

16. The method of claim 1, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

17. The method of claim 1, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

18. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

19. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

20. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

21. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

22. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

23. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

24. The method of claim 1, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

25. The method of claim 1, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable component and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

26. The method of claim 1, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

27. The method of claim 1, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

28. The method of claim 1, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

29. The method of claim 1, further comprising confrolling formation conditions such that the produced mixture comprises a partial pressure of H₂ within the mixture greater than about 0.5 bars.

30. The method of claim 29, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

31. The method of claim 1, wherein controlling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

32. The method of claim 1, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

33. The method of claim 1, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

34. The method of claim 1, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

35. The method of claim 1, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

36. The method of claim 34, wherein at least about 20 heat sources are disposed in the foπnation for each production well.

37. The method of claim 1, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

38. The method of claim 1, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the fonnation to form a repetitive pattern of units.

39. The method of clahn 1, further comprising separating the produced mixture into a gas stream and a liquid sfream.

40. The method of claim 1, further comprising separating the produced mixture into a gas sfream and a liquid stream and separating the liquid sfream into an aqueous sfream and a non-aqueous sfream.

41. The method of claim 1, wherein the produced mixture comprises H₂S, the method further comprising separating a portion of the H₂S from non-condensable hydrocarbons.

42. The method of claim 1, wherein the produced mixture comprises C0₂, the method further comprising separating a portion of the C0₂ from non-condensable hydrocarbons.

43. The method of claim 1, wherein the mixture is produced from a production well, wherein the heating is confrolled such that the mixture can be produced from the formation as a vapor.

44. The method of claim 1, wherein the mixture is produced from a production well, the method further comprising heating a wellbore of the production well to inhibit condensation of the mixture within the wellbore.

45. The method of claim 1, wherein the mixture is produced from a production well, wherein a wellbore of the production well comprises a heater element configured to heat the foπnation adjacent to the wellbore, and further comprising heatmg the formation with the heater element to produce the mixture, wherein the mixture comprises a large non-condensable hydrocarbon gas component and H₂.

46. The method of claim 1, wherein the minimum pyrolysis temperature is about 270 °C.

47. The method of claim 1, further comprising maintaining the pressure within the formation above about 2.0 bars absolute to inhibit production of fluids having carbon numbers above 25.

48. The method of claim 1, further comprising controlling pressure within the formation in a range from about atmospheric pressure to about 100 bars, as measured at a wellhead of a production well, to confrol an amount of condensable hydrocarbons within the produced mixture, wherein the pressure is reduced to increase production of condensable hydrocarbons, and wherein the pressure is increased to increase production of non-condensable hydrocarbons.

49. The method of clahn 1, further comprising confrolling pressure within the formation in a range from about atmospheric pressure to about 100 bars, as measured at a wellhead of a production well, to control an API gravity of condensable hydrocarbons within the produced mixture, wherein the pressure is reduced to decrease the API gravity, and wherein the pressure is increased to reduce the API gravity.

50. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from at least the portion to a selected section of the formation substantially by conduction of heat; pyrolyzing at least some hydrocarbons within the selected section of the foπnation; and producing a mixture from the formation.

51. The method of claim 50, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

52. The method of claim 50, wherein the one or more heat sources comprise elecfrical heaters.

53. The method of claim 50, wherein the one or more heat sources comprise surface burners.

54. The method of clahn 50, wherein the one or more heat sources comprise flameless disfributed combustors.

55. The method of claim 50, wherein the one or more heat sources comprise natural disfributed combustors.

56. The method of claim 50, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

57. The method of claim 50, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1.0 ° C per day during pyrolysis.

58. The method of claim 50, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability foπnation containing heavy hydrocarbons from the one or more heat sources, wherein the foimation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

59. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

60. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

61. The method of claim 50, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

62. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

63.^' The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

64. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

65. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

66. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

67. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

68. The method of claim 50, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

69. The method of clahn 50, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

70. The method of claim 50, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

71. The method of claim 50, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

72. The method of claim 50, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

73. The method of clahn 50, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

74. The method of claim 73, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

75. The method of claim 50, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

76. The method of claim 50, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

77. The method of claim 50, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

78. The method of claim 50, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

79. The method of claim 50, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

80. The method of claim 79, wherein at least about 20 heat sources are disposed in the formation for each production well.

81. The method of claim 50, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

82. The method of claim 50, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to foπn a repetitive pattern of units.

83. A method of treating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; confrolling the heat from the one or more heat sources such that an average temperature within at least a majority of the selected section of the foπnation is less than about 370 °C such that production of a substantial amount of hydrocarbons having carbon numbers greater than 25 is inhibited; controlling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least 2.0 bars absolute; and producing a mixture from the foπnation, wherein about 0.1 % by weight of the produced mixture to about 15 % by weight of the produced mixture are olefins, and wherein an average carbon number of the produced mixture ranges from 1-25.

84. The method of claim 83, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

85. The method of claim 83, wherein confrolling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

86. The method of claim 83, wherein the one or more heat sources comprise elecfrical heaters.

87. The method of claim 83, wherein the one or more heat sources comprise surface burners.

88. The method of claim 83, wherein the one or more heat sources comprise flameless disfributed combustors.

89. The method of claim 83, wherein the one or more heat sources comprise natural distributed combustors.

90. The method of claim 83, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

91. The method of claim 83 , further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

92. The method of claim 83, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability foπnation containing heavy hydrocarbons from the one or more heat sources, wherem the formation has an average heat capacity (C_v), and wherem the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

93. The method of claim 83, wherein allowing the heat to fransfer comprises transfening heat substantially by conduction.

94. The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

95. The method of claim 83, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

96. The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

97. The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

98. The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

99. The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds. lOO.The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

lOl.The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

102.The method of claim 83, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

103. The method of clahn 83, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

104.The method of claim 83, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

105. The method of claim 83, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

106.The method of claim 83, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

107.The method of claim 106, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

108.The method of claim 83, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

109.The method of claim 83, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1 lO.The method of claim 83, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

I ll .The method of claim 83, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

112.The method of claim 111, wherein at least about 20 heat sources are disposed in the formation for each production well.

113.The method of claim 83, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

114.The method of claim 83, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

115. The method of claim 83, further comprising separating the produced mixture into a gas stream and a liquid stream.

116.The method of claim 83, further comprising separating the produced mixture into a gas stream and a liquid sfream and separating the liquid sfream into an aqueous sfream and a non-aqueous stream.

117.The method of claim 83, wherein the produced mixture comprises H₂S, the method further comprising separating a portion of the H₂S from non-condensable hydrocarbons.

118. The method of claim 83, wherein the produced mixture comprises C0₂, the method further comprising separating a portion of the C0₂ from non-condensable hydrocarbons.

119. The method of claim 83, wherein the mixture is produced from a production well, wherein the heating is confrolled such that the mixture can be produced from the formation as a vapor.

120.The method of claim 83, wherein the mixture is produced from a production well, the method further comprising heating a wellbore of the production well to inhibit condensation of the mixture within the wellbore.

121. The method of claim 83, wherein the mixture is produced from a production well, wherein a wellbore of the production well comprises a heater element configured to heat the formation adjacent to the wellbore, and further comprising heating the formation with the heater element to produce the mixture, wherein the produced mixture comprise a large non-condensable hydrocarbon gas component and H₂.

122.The method of claim 83, wherein the minimum pyrolysis temperature is about 270 °C.

123. The method of claim 83, further comprising maintaining the pressure within the formation above about 2.0 bars absolute to inhibit production of fluids having carbon numbers above 25.

124. The method of claim 83, further comprising confrolling pressure within the formation in a range from about atmospheric pressure to about 100 bars absolute, as measured at a wellhead of a production well, to control an amount of condensable fluids within the produced mixture, wherein the pressure is reduced to increase production of condensable fluids, and wherein the pressure is increased to increase production of non-condensable fluids.

125. The method of claim 83, further comprising controlling pressure within the formation in a range from about atmospheric pressure to about 100 bars absolute, as measured at a wellhead of a production well, to confrol an API gravity of condensable fluids within the produced mixture, wherein the pressure is reduced to decrease the API gravity, and wherein the pressure is increased to reduce the API gravity.

126.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute; and producing a mixture from the formation.

127.The method of claim 126, wherein confrolling the pressure comprises confrolling the pressure with a valve coupled to at least one of the one or more heat sources.

128.The method of claim 126, wherein confrolling the pressure comprises controlling the pressure with a valve coupled to a production well located in the formation.

129.The method of claim 126, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

130.The method of claim 126, wherein confrolling foimation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

131.The method of claim 126, wherein the one or more heat sources comprise electrical heaters.

132.The method of claim 126, wherein the one or more heat sources comprise surface burners.

133. The method of claim 126, wherein the one or more heat sources comprise flameless distributed combustors.

134.The method of claim 126, wherein the one or more heat sources comprise natural distributed combustors.

135.The method of clahn 126, further comprising controlling a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

136.The method of claim 126, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

137. The method of clahn 126, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C,,), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foimation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C *p_B wherein w is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

138.The method of claim 126, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

139.The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

140.The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

141. The method of claim 126, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

142.The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

143. The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

144.The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

145. The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

146.The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

147.The method of claim 126, wherein the produced mixture comprises condensable hydrocarbons, and wherem less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

148.The method of clahn 126, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

149.The method of claim 126, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

150.The method of claim 126, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

151.The method of claim 126, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

152. The method of claim 126, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

153. The method of claim 152, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

154. The method of claim 126, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

155.The method of claim 126, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

156.The method of claim 126, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

157.The method of claim 126, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

158.The method of claim 126, wherein producing the mixture from the formation comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the fonnation for each production well.

159.The method of claim 158, wherein at least about 20 heat sources are disposed in the formation for each production well.

160.A method of freating a relatively low penneability foimation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; and confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute; confrolling the heat from the one or more heat sources such that an average temperature within at least a majority of the selected section of the formation is less than about 375 °C; and producing a mixture from the foπnation.

161. The method of claim 159, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

162.The method of claim 159, wherein confrolling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

163. The method of claim 159, wherein the one or more heat sources comprise elecfrical heaters.

164.The method of claim 159, wherein the one or more heat sources comprise surface burners.

165. The method of claim 159, wherein the one or more heat sources comprise flameless disfributed combustors.

166.The method of claim 159, wherein the one or more heat sources comprise natural distributed combustors.

167. The method of claim 159, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

168.The method of claim 159, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

169.The method of claim 159, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherehi heating energy/day provided to the volume is equal to or less than Pwr, wherehi Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

170.The method of claim 159, wherein allowing the heat to fransfer comprises transfening heat substantially by conduction.

171. The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

172.The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

173. The method of claim 159, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

174.The method of claim 159, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

175.The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

176.The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

177. The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

178. The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

179.The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

180. The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

181. The method of claim 159, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

182.The method of claim 159, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

183. The method of claim 159, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

184.The method of clahn 159, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

185.The method of claim 159, wherein controlling the heat further comprises confrolling the heat such that coke production is inhibited.

186.The method of claim 159, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

187.The method of claim 186, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

188. The method of claim 159, further comprising altering the pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

189.The method of claim 159, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

190.The method of claim 159, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

191. The method of claim 159, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

192.The method of claim 159, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

193. The method of claim 192, wherein at least about 20 heat sources are disposed in the formation for each production well.

194. The method of claim 159, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

195.The method of claim 159, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

196. A method of freating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; producing a mixture from the formation, wherein at least a portion of the mixture is produced during the pyrolysis and the mixture moves through the formation in a vapor phase; and maintaining a pressure within at least a majority of the selected section above about 2.0 bars absolute.

197.The method of claim 196, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foπnation.

198. The method of claim 196, wherein confrolling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

199.The method of claim 196, wherein the one or more heat sources comprise electrical heaters.

200. The method of claim 196, wherein the one or more heat sources comprise surface burners.

201. The method of claim 196, wherein the one or more heat sources comprise flameless disfributed combustors.

202,The method of claim 196, wherein the one or more heat sources comprise natural disfributed combustors.

203.The method of claim 196, further comprising controlling the pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

204.The method of claim 196, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

205.The method of claim 196, wherein providing heat from the one or more heat sources to at least the portion of fonnation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherehi the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

206. The method of claim 196, wherein allowing the heat to fransfer comprises ttansfening heat substantially by conduction.

" 207.The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

208.The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

209.The method of claim 196, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

210.The method of claim 196, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

211. The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

212.The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

213. The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

214.The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

215. The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

216.The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

217. The method of claim 196, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

218. The method of claim 196, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

219.The method of claim 196, wherem the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

220.The method of claim 196, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

221. The method of claim 196, wherein the pressure is measured at a wellhead of a production well.

222.The method of claim 196, wherein the pressure is measured at a location within a wellbore of the production well.

223. The method of claim 196, wherein the pressure is maintained below about 100 bars absolute.

224.The method of claim 196, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

225.The method of claim 224, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

226. The method of claim 196, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

227.The method of clahn 196, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the foimation.

228. The method of claim 196, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

229.The method of claim 196, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

230. The method of claim 196, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

231. The method of claim 230, wherein at least about 20 heat sources are disposed in the formation for each production well.

232.The method of claim 196, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

233. The method of claim 196, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

234.A method of treating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; maintaining a pressure within at least a majority of the selected section of the formation above 2.0 bars absolute; and producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity higher than an API gravity of condensable hydrocarbons in a mixture producible from the formation at the same temperature and at atmospheric pressure.

235,The method of claim 234, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foπnation.

236.The method of claim 234, wherein controlling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

237. The method of claim 234, wherein the one or more heat sources comprise elecfrical heaters.

238.The method of claim 234, wherem the one or more heat sources comprise surface burners.

239.The method of claim 234, wherein the one or more heat sources comprise flameless distributed combustors.

240. The method of claim 234, wherein the one or more heat sources comprise natural distributed combustors.

241. The method of claim 234, further comprising confrolling the pressure and a temperature within at least a majority of the selected section of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

242.The method of claim 234, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

243. The method of claim 234, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

244.The method of claim 234, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

245. The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

246.The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

247.The method of claim 234, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

248.The method of claim 234, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

249.The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

250. The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

251.The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

252.The method of clahn 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

253. The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

254.The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

255. The method of claim 234, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

256.The method of claim 234, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

257.The method of claim 234, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

258.The method of claim 234, wherehi the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

259.The method of claim 234, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

260.The method of claim 234, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

261. The method of claim 234, further comprising altering a pressure within the foπnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

262.The method of claim 234, wherein controlling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

263. The method of claim 234, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

264.The method of claim 234, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

265.The method of claim 234, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

266.The method of claim 265, wherein at least about 20 heat sources are disposed in the formation for each production well.

267.The method of claim 234, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

268. The method of claim 234, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

269.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; maintaining a pressure within at least a majority of the selected section of the formation to above 2.0 bars absolute; and producing a fluid from the formation, wherein condensable hydrocarbons within the fluid comprise an atomic hydrogen to atomic carbon ratio of greater than about 1J5.

270.The method of claim 269, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

271. The method of claim 269, wherein confrolling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

272.The method of claim 269, wherein the one or more heat sources comprise electrical heaters.

273. The method of claim 269, wherein the one or more heat sources comprise surface burners.

274.The method of claim 269, wherein the one or more heat sources comprise flameless distributed combustors.

275.The method of claim 269, wherein the one or more heat sources comprise natural disfributed combustors.

276.The method of claim 269, further comprising confrolling the pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

277.The method of claim 269, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

278.The method of clahn 269, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

279.The method of claim 269, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

280.The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

281. The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

282.The method of claim 269, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

283.The method of claim 269, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

284.The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

285. The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

286.The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

287.The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

288.The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

289. The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

290.The method of claim 269, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

291. The method of claim 269, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

292. The method of claim 269, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

293. The method of claim 269, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

294.The method of claim 269, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

295. The method of claim 269, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

296. The method of claim 269, further comprising altering the pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

291. The method of claim 269, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

298. The method of claim 269, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

299.The method of claim 269, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

300.The method of claim 269, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

301.The method of claim 300, wherein at least about 20 heat sources are disposed in the formation for each production well.

302.The method of claim 269, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

303. The method of claim 269, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

304. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; maintaining a pressure within at least a majority of the selected section of the foimation to above 2.0 bars absolute; and producing a mixture from the formation, wherein the produced mixture comprises a higher amount of non- condensable components as compared to non-condensable components producible from the foπnation under the same temperature conditions and at atmospheric pressure.

305. The method of claim 304, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

306.The method of claim 304, wherein controlling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

307. The method of claim 304, wherein the one or more heat sources comprise electrical heaters.

308.The method of claim 304, wherein the one or more heat sources comprise surface burners.

309.The method of claim 304, wherein the one or more heat sources comprise flameless disfributed combustors.

3 lO.The method of claim 304, wherein the one or more heat sources comprise natural distributed combustors.

311.The method of claim 304, further comprising controlling the pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

312.The method of claim 304, furtlier comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

313. The method of claim 304, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, ρ_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

314.The method of claim 304, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

315. The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

316.The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

317.The method of claim 304, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

318.The method of claim 304, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

319.The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

320.The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

321. The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

322.The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

323. The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

324.The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

325.The method of claim 304, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

326. The method of claim 304, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

327. The method of claim 304, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

328. The method of clahn 304, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

329. The method of claim 304, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

330.The method of claim 304, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

331. The method of claim 304, further comprising altering the pressure within the formation to inhibit production of hydrocarbons from the foπnation having carbon numbers greater than about 25.

332.The method of claim 304, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

333. The method of claim 304, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

334.The method of claim 304, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

335. The method of claim 334, wherein at least about 20 heat sources are disposed in the formation for each production well.

336. The method of claim 304, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

337.The method of claim 304, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

338. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that superhnposed heat from the one or more heat sources pyrolyzes at least about 20 % by weight of hydrocarbons within the selected section of the formation; and producing a mixture from the foπnation.

339. The method of claim 338, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

340.The method of claim 338, wherein controlling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

341.The method of claim 338, wherein the one or more heat sources comprise electrical heaters.

342.The method of claim 338, wherein the one or more heat sources comprise surface burners.

343. The method of claim 338, wherein the one or more heat sources comprise flameless distributed combustors.

344.The method of claim 338, wherein the one or more heat sources comprise natural distributed combustors.

345.The method of claim 338, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

346.The method of claim 338, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

347. The method of claim 338, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the fonnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

348.The method of claim 338, wherein allowing the heat to fransfer comprises transferring heat substantially by conduction.

349. The method of claim 338, wherein providing heat from the one or more heat sources comprises heating the selected foπnation such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

350.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

351. The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

352.The method of claim 338, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

353. The method of claim 338, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

354.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

355.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

356.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

357.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

358.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

359. The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

360.The method of claim 338, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

361.The method of claim 338, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

362.The method of claim 338, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

363.The method of claim 338, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

364.The method of claim 338, further comprising controlling a pressure within at least a majority of the selected section of the foimation, wherein the controlled pressure is at least about 2.0 bars absolute.

365. The method of claim 338, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

366.The method of claim 338, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

367.The method of claim 338, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

368.The method of claim 338, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

369.The method of claim 338, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

370.The method of claim 338, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

371.The method of claim 338, wherehi allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

372.The method of claim 338, wherein allowing the heat to fransfer comprises substantially uniformly increasing a permeability of a majority of the selected section.

373. The method of claim 338, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

374.The method of claim 373, wherein at least about 20 heat sources are disposed in the formation for each production well.

375.The method of claim 338, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

376.The method of claim 338, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

377. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more -heat sources to a selected section of the formation such that superimposed heat from the one or more heat sources pyrolyzes at least about 20 % of hydrocarbons within the selected section of the formation; and producing a mixture from the formation, wherem the mixture comprises a condensable component having an API gravity of at least about 25°.

378. The method of claim 377, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

379. The method of claim 377, wherein controlling foimation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

380.The method of claim 377, wherein the one or more heat sources comprise elecfrical heaters.

381. The method of claim 377, wherein the one or more heat sources comprise surface burners.

382. The method of claim 377, wherein the one or more heat sources comprise flameless distributed combustors.

383. The method of claim 377, wherein the one or more heat sources comprise natural distributed combustors.

384. The method of claim 377, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

385. The method of claim 377, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

386. The method of claim 377, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

387. The method of claim 377, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

388. The method of claim 377, wherein providing heat from the one or more heat sources comprises heating the selected section such that a theπnal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

389.The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

390.The method of claim 377, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

391. The method of claim 377, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

392.The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

393.The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

394.The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

395. The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

396.The method of clahn 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

397.The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

398.The method of claim 377, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

399.The method of claim 377, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

400.The method of claim 377, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

401.The method of claim 377, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

402.The method of claim 377, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

403. The method of claim 377, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

404.The method of claim 377, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

405. The method of claim 377, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

406.The method of claim 377, wherein controlling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

407.The method of claim 377, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

408.The method of claim 377, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

409.The method of claim 377, wherein allowing the heat to transfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

410.The method of claim 377, wherein allowing the heat to fransfer comprises substantially uniformly increasing a permeability of a majority of the selected section.

41 l.The method of claim 377, wherem producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

412.The method of claim 411, wherein at least about 20 heat sources are disposed in the formation for each production well.

413. The method of claim 377, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

414.The method of claim 377, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

415. A method of freating a layer of a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the layer, wherein the one or more heat sources are positioned proximate an edge of the layer; allowing the heat to transfer from the one or more heat sources to a selected section of the layer such that superimposed heat from the one or more heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation; and producing a mixture from the formation.

416.The method of claim 415, wherein the one or more heat sources are laterally spaced from a center of the layer.

417.The method of claim 415, wherein the one or more heat sources are positioned in a staggered line.

418. The method of claim 415, wherein the one or more heat sources positioned proximate the edge of the layer can increase an amount of hydrocarbons produced per unit of energy input to the one or more heat sources.

419. The method of claim 415, wherein the one or more heat sources positioned proximate the edge of the layer can increase the volume of foπnation undergoing pyrolysis per unit of energy input to the one or more heat sources.

420. The method of claim 415, wherein the one or more heat sources comprise elecfrical heaters.

421. The method of claim 415, wherein the one or more heat sources comprise surface burners.

422.The method of claim 415, wherein the one or more heat sources comprise flameless disfributed combustors.

423. The method of claim 415, wherein the one or more heat sources comprise natural disfributed combustors.

424.The method of claim 415, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

425.The method of claim 415, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1.0 ° C per day during pyrolysis.

426. The method of claim 415, wherein providing heat from the one or more heat sources to at least the portion of the layer comprises: heating a selected volume (V) of the relatively low peπneability formation-containing heavy hydrocarbons from the one or more heat sources, wherein the foπnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

427. The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

428.The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

429.The method of claim 415, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

430.The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

43 l.The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

432. The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

433.The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

434.The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

435. The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

436.The method of claim 415, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

437. The method of claim 415, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

438.The method of claim 415, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

439.The method of claim 415, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

440.The method of claim 415, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

441. The method of clahn 415, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherehi a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

442.The method of claim 441, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

443. The method of claim 415, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foπnation having carbon numbers greater than about 25.

444.The method of claim 415, further comprising confrolling formation conditions, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

445.The method of claim 415, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

446. The method of claim 415, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

447.The method of claim 415, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

448.The method of claim 447, wherein at least about 20 heat sources are disposed in the formation for each production well.

449.The method of claim 415, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

450.The method of claim 415, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

451.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure; and producing a mixture from the formation.

452.The method of claim 451, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foπnation.

453. The method of claim 451, wherein confrolling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

454.The method of claim 451, wherein the one or more heat sources comprise electrical heaters.

455.The method of clahn 451, wherein the one or more heat sources comprise surface burners.

456.The method of claim 451, wherein the one or more heat sources comprise flameless disfributed combustors.

457.The method of claim 451, wherein the one or more heat sources comprise natural disfributed combustors.

458.The method of claim 451, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

459. The method of claim 451, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (Cv), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

460.The method of claim 451, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

461.The method of claim 451 , wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

462.The method of claim 451, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

463.The method of claim 451, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

464.The method of claim 451, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

465.The method of claim 451 , wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

466. The method of claim 451, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

467.The method of claim 451, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

468.The method of claim 451, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

469.The method of claim 451, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

470.The method of claim 451 , wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

47 l.The method of claim 451, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

472.The method of claim 451, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

473. The method of claim 451, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

474.The method of clahn 451, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

475. The method of claim 451, wherein the controlled pressure is at least about 2.0 bars absolute.

476.The method of claim 451, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

477.The method of claim 451, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

478.The method of claim 451, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

479.The method of claim 451, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

480.The method of clahn 451, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

481.The method of claim 451, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

482. The method of claim 451 , wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

483. The method of clahn 482, wherein at least about 20 heat sources are disposed in the foπnation for each production well.

484. The method of claim 451, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

485.The method of claim 451, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

486. A method of freating a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the foπnation to raise an average temperature within the selected section to, or above, a temperature that will pyrolyze hydrocarbons within the selected section; producing a mixture from the formation; and confrolling API gravity of the produced mixture to be greater than about 25 degrees API by confrolling average pressure and average temperature in the selected section such that the average pressure in the selected section is greater than the pressure (p) set forth in the following equation for an assessed average temperature (T) in the selected section:

_ _e f-44000 T+ 67]

where/? is measured in psia and Tis measured in ° Kelvin.

487.The method of claim 486, wherein the API gravity of the produced mixture is controlled to be greater than about 30 degrees API, and wherein the equation is:

488.The method of claim 486, wherein the API gravity of the produced mixture is controlled to be greater than about 35 degrees API, and wherein the equation is:

_ [-22000/T+ 38]

489.The method of claim 486, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

490.The method of claim 486, wherein confrolling the average temperature comprises maintaining a temperature in the selected section within a pyrolysis temperature range.

491. The method of clahn 486, wherein the one or more heat sources comprise elecfrical heaters.

492.The method of claim 486, wherein the one or more heat sources comprise surface burners.

493. The method of claim 486, wherein the one or more heat sources comprise flameless distributed combustors.

494.The method of clahn 486, wherein the one or more heat sources comprise natural distributed combustors.

495.The method of claim 486, further comprising confrolling a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

496.The method of claim 486, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

497.The method of claim 486, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low penneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherehi heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

498.The method of claim 486, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

499.The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

500.The method of clahn 486, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

501. The method of clahn 486, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

502.The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

503. The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

504.The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

505.The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

506.The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

507.The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

508. The method of claim 486, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

509.The method of claim 486, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

5 lO.The method of claim 486, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

51 l.The method of claim 486, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

512.The method of claim 486, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

513. The method of claim 486, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

514.The method of claim 486, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foπnation having carbon numbers greater than about 25.

515. The method of claim 486, wherein controlling foπnation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

516.The method of claim 486, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

517.The method of clahn 486, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

518. The method of claim 486, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

519.The method of claim 518, wherein at least about 20 heat sources are disposed in the formation for each production well.

520. The method of claim 486, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

521. The method of claim 486, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

522.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat to at least a portion of a relatively low permeability foπnation containing heavy hydrocarbons such that a temperature (7) in a substantial part of the heated portion exceeds 270 °C and hydrocarbons are pyrolyzed within the heated portion of the formation; confrolling a pressure (p) within at least a substantial part of the heated portion of the formation; vthexe p_bar> e ^[<-^{Λ /τ}> ÷^B- ^6744] ; wherein p is the pressure in bars absolute and T is the temperature in degrees K, and A and B are parameters that are larger than 10 and are selected in relation to the characteristics and composition of the relatively low peπneability formation containing heavy hydrocarbons and on the required olefin content and carbon number of the pyrolyzed hydrocarbon fluids; and producing pyrolyzed hydrocarbon fluids from the heated portion of the formation.

523.The method of claim 522, wherein A is greater than 14000 and B is greater than about 25 and a majority of the produced pyrolyzed hydrocarbon fluids have an average carbon number lower than 25 and comprise less than about 10 % by weight of olefins.

524.The method of claim 522, wherein T is less than about 390 °C, p is greater than about 1.4 bars, A is greater than about 44000, and b is greater than about 67, and a majority of the produced pyrolyzed hydrocarbon fluids have an average carbon number less than 25 and comprise less than 10 % by weight of olefins.

525. The method of claim 522, wherein Tis less than about 390 °C, p is greater than about 2 bars, A is less than about 57000, and b is less than about 83, and a majority of the produced pyrolyzed hydrocarbon fluids have an average carbon number lower than about 21.

526.The method of claim 522, further comprising confrolling the heat such that an average heating rate of the heated portion is less than about 3°C per day during pyrolysis.

527.The method of claim 522, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

528.The method of claim 522, wherein heat is fransfened substantially by conduction from one or more heat sources to the heated portion of the formation.

529.The method of claim 528, wherein the heat sources comprise heaters in which hydrocarbons are either injected into a heaters or released by the relatively low permeability formation containing heavy hydrocarbons adjacent to a heater by an oxidant injected into the heater in or adjacent to which the combustion occurs and wherein at least part of the produced combustion gases are vented to surface via the heater in which the combustion occurs.

530.The method of clahn 522, further comprising controlling formation conditions to produce a mixture of hydrocarbon fluids and H₂, wherein a partial pressure of H₂ within the mixture flowing through the formation is greater than 0.5 bars.

53 l.The method of claim 530, further comprising, hydrogenating a portion of the produced pyrolyzed hydrocarbon fluids with at least a portion of the produced hydrogen and heating the fluids with heat from hydrogenation.

532. The method of claim 522, wherein the substantially gaseous pyrolyzed hydrocarbon fluids are produced from a production well, the method further comprising heating a wellbore of the production well to inhibit condensation of the hydrocarbon fluids within the wellbore.

533.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation to raise an average temperature within the selected section to, or above, a temperature that will pyrolyze hydrocarbons within the selected section; producing a mixture from the foimation; and controlling a weight percentage of olefins of the produced mixture to be less than about 20 % by weight by controlling average pressure and average temperature in the selected section such that the average pressure in the selected section is greater than the pressure (p) set forth in the following equation for an assessed average temperature (T) in the selected section:

_ _e [-57000/T+ 83]

where p is measured in psia and Tis measured in ° Kelvin.

534.The method of clahn 533, wherein the weight percentage of olefins of the produced mixture is confrolled to be less than about 10 % by weight, and wherein the equation is: p _ e [-16000/7 + 28]

535.The method of claim 533, wherein the weight percentage of olefins of the produced mixture is confrolled to be less than about 5 % by weight, and wherein the equation is: p _ e [-I2000/T÷ 22J

536.The method of claim 533, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

537.The method of claim 533, wherein the one or more heat sources comprise elecfrical heaters.

538.The method of claim 533, wherein the one or more heat sources comprise surface burners.

539.The method of claim 533, wherein the one or more heat sources comprise flameless disfributed combustors.

540.The method of claim 533, wherein the one or more heat sources comprise natural disfributed combustors.

541.The method of claim 533, further comprising confrolling a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

542.The method of claim 541, wherein confrolling an average temperature comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

543. The method of claim 533, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 3.0 °C per day during pyrolysis.

544.The method of claim 533, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

545. The method of claim 533, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the foπnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

546.The method of claim 533, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

547.The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

548. The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

549.The method of claim 533, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

550.The method of claim 533, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

55 l.The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

552.The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

553. The method of clahn 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

554.The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

555.The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

556.The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

557. The method of claim 533, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

558.The method of claim 533, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

559.The method of clahn 533, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

560.The method of claim 533, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer. 56 l.The method of claim 533, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

562.The method of claim 533, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

563. The method of claim 533, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

564.The method of claim 533, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

565. The method of claim 533, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

566. The method of claim 533, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

567.The method of claim 533, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

568.The method of claim 567, wherein at least about 20 heat sources are disposed in the foimation for each production well.

569. The method of claim 533, further comprising providing heat from three or more heat sources to at least a portion of the fonnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

570.The method of claim 533, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the foπnation to form a repetitive pattern of units.

571.A method of freating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation to raise an average temperature within the selected section to, or above, a temperature that will pyrolyze hydrocarbons within the selected section; producing a mixture from the formation; and controlling hydrocarbons having carbon numbers greater than 20 of the produced mixture to be less than about 20 % by weight by confrolling average pressure and average temperature in the selected section such that the average pressure in the selected section is greater than the pressure (p) set forth in the following equation for an assessed average temperature (7) in the selected section:

_ [-14000,'T + 25]

where p is measured in psia and T is measured in ° Kelvin. •

572.The method of claim 571, wherein the hydrocarbons having carbon numbers greater than 20 of the produced mixture is confrolled to be less than about 15 % by weight, and wherein the equation is: _p = _e [-18000 T + 32]_

573.The method of claim 571, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

574.The method of claim 571, wherein the one or more heat sources comprise elecfrical heaters.

575. The method of claim 571, wherein the one or more heat sources comprise surface burners.

576.The method of claim 571, wherein the one or more heat sources comprise flameless disfributed combustors.

577.The method of claim 571, wherein the one or more heat sources comprise natural distributed combustors.

578.The method of claim 571, further comprising confrolling a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

579.The method of claim 578, wherein confrolling the temperature comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

580.The method of claim 571, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

581.The method of claim 571, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherehi heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

582.The method of clahn 571, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

583.The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

584.The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

585. The method of claim 571, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

586.The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

587.The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

588. The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

589.The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

590.The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

591. The method of clahn 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

592. The method of claim 571, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

593. The method of claim 571, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

594.The method of claim 571, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

595.The method of claim 571, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

596.The method of claim 571, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

597.The method of claim 571, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

598. The method of claim 571, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

599.The method of claim 571, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

600.The method of claim 571, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method fiirther comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

60 l.The method of claim 571, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foimation for each production well.

602.The method of claim 601, wherein at least about 20 heat sources are disposed in the formation for each production well.

603. The method of claim 571, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

604.The method of claim 571, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

605.A method of treating a relatively low permeability fonnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foimation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation to raise an average temperature within the selected section to, or above, a temperature that will pyrolyze hydrocarbons within the selected section; producing a mixture from the formation; and confrolling an atomic hydrogen to carbon ratio of the produced mixture to be greater than about 1.7 by controlling average pressure and average temperature in the selected section such that the average pressure in the selected section is greater than the pressure (p) set forth in the following equation for an assessed average temperature (T) in the selected section:

_ [-38000/T + 61]

where p is measured in psia and Tis measured in ° Kelvin.

606.The method of claim 605, wherem the atomic hydrogen to carbon ratio of the produced mixture is confrolled to be greater than about 1.8, and wherein the equation is:

_ _ef-13000 T + 24J_

607.The method of claim 605, wherein the atomic hydrogen to carbon ratio of the produced mixture is controlled to be greater than about 1.9, and wherein the equation is:

608.The method of claim 605, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foπnation.

609.The method of claim 605, wherein the one or more heat sources comprise electrical heaters.

610.The method of claim 605, wherein the one or more heat sources comprise surface burners.

611.The method of claim 605, wherein the one or more heat sources comprise flameless disfributed combustors.

612.The method of claim 605, wherein the one or more heat sources comprise natural distributed combustors.

613. The method of claim 605, further comprising controlling a temperature within at least a majority of the selected section of the foimation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

614.The method of claim 613, wherein confrolling the temperature comprises maintaining a temperature within the ' selected section within a pyrolysis temperature range.

615. The method of claim 605, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

616.The method of claim 605, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

617.The method of claim 605, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

618.The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

619.The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

620.The method of claim 605, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

62 l.The method of claim 605, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

622.The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

623. The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

624.The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

625. The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

626. The method of clahn 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

627.The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

628. The method of claim 605, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

629. The method of claim 605, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

630.The method of claim 605, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

63 l.The method of clahn 605, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

632.The method of claim 605, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

633. The method of claim 605, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

634.The method of claim 605, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

635. The method of claim 605, wherein controlling formation conditions comprises recirculating a portion of hydrogen from the mixture into the foπnation.

636.The method of claim 605, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

637.The method of claim 605, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

638.The method of claim 605, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

639.The method of claim 638, wherein at least about 20 heat sources are disposed in the foimation for each production well.

640. The method of claim 605, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

641.The method of claim 605, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the fonnation to form a repetitive pattern of units.

642.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; controlling a pressure-temperature relationship within at least the selected section of the formation by selected energy input into the one or more heat sources and by pressure release from the selected section through wellbores of the one or more heat sources; and producing a mixture from the formation.

643. The method of claim 642, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

644. The method of claim 642, wherein the one or more heat sources comprise at least two heat sources.

645. The method of claim 642, wherein the one or more heat sources comprise surface burners.

646.The method of claim 642, wherein the one or more heat sources comprise flameless disfributed combustors.

647.The method of claim 642, wherein the one or more heat sources comprise natural disfributed combustors.

648. The method of claim 642, further comprising confrolling the pressure-temperature relationship by confrolling a rate of removal of fluid from the foπnation.

649.The method of claim 642, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

650.The method of claim 642, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability foimation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

65 l.The method of claim 642, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

652. The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

653. The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

654.The method of claim 642, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

655. The method of claim 642, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

656. The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

657.The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

658.The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

659.The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

660.The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

66 l.The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

662. The method of claim 642, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

663. The method of claim 642, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

664. The method of claim 642, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

665.The method of claim 642, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

666.The method of claim 642, further comprising controlling a pressure within at least a majority of the selected section of the foimation, wherein the confrolled pressure is at least about 2.0 bars absolute.

667.The method of claim 642, further comprising controlling formation conditions to produce a mixture of hydrocarbon fluids and H₂, wherein the partial pressure of H₂ within the mixture is greater than about 0.5 bars.

668. The method of claim 642, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

669. The method of claim 642, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

670. The method of claim 642, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

671.The method of claim 642, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

672.The method of claim 642, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

673. The method of claim 642, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

674.The method of clahn 642, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

675.The method of clahn 674, wherein at least about 20 heat sources are disposed in the formation for each production well.

676.The method of claim 642, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

677.The method of claim 642, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

678.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: heating a selected volume (V) of the relatively low permeability foπnation containing heavy hydrocarbons, wherein foimation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

679.The method of claim 678, wherein heating a selected volume comprises heating with an elecfrical heater.

680.The method of claim 678, wherein heating a selected volume comprises heating with a surface burner.

68 l.The method of claim 678, wherein heating a selected volume comprises heating with a flameless disfributed combustor.

682.The method of clahn 678, wherein heating a selected volume comprises heating with at least one natural disfributed combustor.

683.The method of claim 678, further comprising controlling a pressure and a temperature within at least a majority of the selected volume of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

684.The method of clahn 678, further comprising controlling the heating such that an average heating rate of the selected volume is less than about 1 °C per day during pyrolysis.

685.The method of claim 678, wherein a value for C_v is determined as an average heat capacity of two or more samples taken from the relatively low permeability foπnation containing heavy hydrocarbons.

686.The method of claim 678, wherein heating the selected volume comprises fransfening heat substantially by conduction.

687.The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

688.The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

689.The method of claim 678, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

690.The method of clahn 678, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

691. The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

692.The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

693. The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

694.The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

695. The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

696.The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

697.The method of claim 678, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

698.The method of claim 678, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

699.The method of clahn 678, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

700.The method of claim 678, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer

70 l.The method of claim 678, further comprising confrolling a pressure within at least a majority of the selected volume of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

702.The method of claim 678, further comprising controlling formation conditions to produce a mixture from the formation comprising condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

703. The method of claim 678, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

704.The method of clahn 678, further comprising altering a pressure within the foimation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

705.The method of claim 678, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

706.The method of claim 678, further comprising: providing hydrogen (H₂) to the heated volume to hydrogenate hydrocarbons within the volume; and heating a portion of the volume with heat from hydrogenation.

707.The method of claim 678, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

708. The method of claim 678, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

709. The method of claim 708, wherein at least about 20 heat sources are disposed in the foπnation for each production well.

710.The method of claim 678, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

71 l.The method of claim 678, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

712.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation to raise an average temperature within the selected section to, or above, a temperature that will pyrolyze hydrocarbons within the selected section; controlling heat output from the one or more heat sources such that an average heating rate of the selected section rises by less than about 3 °C per day when the average temperature of the selected section is at, or above, the temperature that will pyrolyze hydrocarbons within the selected section; and producing a mixture from the formation.

713. The method of claim 712, wherein confrolling heat output comprises: raising the average temperature within the selected section to a first temperature that is at or above a minimum pyrolysis temperature of hydrocarbons within the formation; limiting energy input into the one or more heat sources to inhibit increase in temperature of the selected section; and increasing energy input into the formation to raise an average temperature of the selected section above the ffrst temperature when production of formation fluid declines below a desired production rate.

714.The method of claim 712, wherein controlling heat output comprises: raising the average temperature within the selected section to a first temperature that is at or above a minimum pyrolysis temperature of hydrocarbons within the formation; limiting energy input into the one or more heat sources to inhibit increase in temperature of the selected section; and increasing energy input into the formation to raise an average temperature of the selected section above the ffrst temperature when quality of formation fluid produced from the formation falls below a deshed quality.

715. The method of claim 712, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section.

716.The method of claim 712, wherein the one or more heat sources comprise electrical heaters.

717. The method of claim 712, wherein the one or more heat sources comprise surface burners.

718.The method of claim 712, wherein the one or more heat sources comprise flameless disfributed combustors.

719.The method of claim 712, wherein the one or more heat sources comprise natural distributed combustors.

720. The method of claim 712, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

721.The method of claim 712, wherein the heat is confrolled such that an average heating rate of the selected section is less than about 1.5 °C per day during pyrolysis.

722.The method of claim 712, wherein the heat is controlled such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

723. The method of claim 712, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density.

724.The method of claim 712, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

725. The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

726.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

727.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, wherein the condensable hydrocarbons have an olefin content less than about 2.5 % by weight of the condensable hydrocarbons, and wherein the olefin content is greater than about 0.1 % by weight of the condensable hydrocarbons.

728.The method of claim 712, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

729.The method of clahn 712, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.10 and wherein the ratio of ethene to ethane is greater than about 0.001.

730. The method of claim 712, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.05 and wherein the ratio of ethene to ethane is greater than about 0.001.

731.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

732.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

733.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

734.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

735.The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

736. The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

737. The method of claim 712, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

738.The method of claim 712, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

739.The method of claim 712, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

740.The method of claim 712, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

741. The method of claim 712, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

742.The method of claim 712, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

743. The method of claim 712, wherein a partial pressure of H₂ is measured when the mixture is at a production well.

744.The method of claim 712, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

745. The method of claim 712, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

746.The method of clahn 712, further comprising: providing H₂ to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

747.The method of claim 712, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

748. The method of claim 712, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

749. The method of claim 748, wherein at least about 20 heat sources are disposed in the formation for each production well.

750.The method of clahn 712, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

75 l.The method of claim 712, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to foπn a repetitive pattern of units.

752. A method of treating a relatively low peπneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; to heat a selected section of the formation to an average temperature above about 270 °C; allowing the heat to transfer from the one or more heat sources to the selected section of the formation; confrolling the heat from the one or more heat sources such that an average heating rate of the selected section is less than about 3 °C per day during pyrolysis; and producing a mixture from the formation.

753.The method of claim 752, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

754.The method of claim 752, wherein the one or more heat sources comprise elecfrical heaters.

755.The method of claim 752, further comprising supplying elecfricity to the elecfrical heaters substantially during non-peak hours.

756. The method of claim 752, wherein the one or more heat sources comprise surface burners.

757. The method of claim 752, wherein the one or more heat sources comprise flameless distributed combustors.

758.The method of claim 752, wherein the one or more heat sources comprise natural distributed combustors.

759.The method of claim 752, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

760.The method of claim 752, wherein the heat is further controlled such that an average heating rate of the selected section is less than about 3 °C/day until production of condensable hydrocarbons substantially ceases.

761. The method of claim 752, wherein the heat is further controlled that an average heating rate of the selected section is less than about 1.5 °C per day during pyrolysis.

762.The method of clahn 752, wherein the heat is further controlled such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

763. The method of claim 752, wherein providing heat from the one or more heat sources to at least the portion of foπnation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density.

764.The method of claim 752, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

765. The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

766. The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

767.The method of claim 752, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

768. The method of claim 752, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

769. The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

770. The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

77 l.The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

772.The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

773. The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

774. The method of clahn 752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

775. The method of claim 752, wherein the produced mixture comprises condensable hydrocarbons, and wherehi about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

776. The method of claim 752, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

777. The method of claim 752, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

778. The method of claim 752, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

779.The method of claim 752, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

780. The method of claim 752, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

78 l.The method of claim 780, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

782.The method of claim 752, further comprising altering a pressure within the fonnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

783. The method of claim 752, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

784.The method of claim 752, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

785.The method of claim 752, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

786.The method of claim 752, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

787.The method of claim 786, wherein at least about 20 heat sources are disposed in the formation for each production well.

788. The method of clahn 752, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

789.The method of claim 752, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

790.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; producing a mixture from the formation through at least one production well; monitoring a temperature at or in the production well; and confrolling heat input to raise the monitored temperature at a rate of less than about 3 °C per day.

791.The method of claim 790, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

792.The method of claim 790, wherein the one or more heat sources comprise electrical heaters.

793. The method of claim 790, wherein the one or more heat sources comprise surface burners.

794.The method of claim 790, wherein the one or more heat sources comprise flameless disfributed combustors.

795. The method of claim 790, wherein the one or more heat sources comprise natural distributed combustors.

796. The method of claim 790, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

797.The method of claim 790, wherein the heat is confrolled such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

798.The method of claim 790, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the foπnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherehi Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density.

799.The method of claim 790, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

800. The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

801. The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

802.The method of claim 790, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

803. The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

804.The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

805. The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

806.The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

807.The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

808. The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

809.The method of claim 790, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

8 lO.The method of claim 790, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volmne of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

81 l.The method of claim 790, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

812.The method of claim 790, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

813. The method of claim 790, further comprising controlling a pressure within at least a maj ority of the selected section of the foimation, wherein the confrolled pressure is at least about 2.0 bars absolute.

814.The method of claim 790, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

815.The method of claim 814, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

816.The method of claim 790, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

817.The method of claim 790, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the foπnation.

818. The method of claim 790, further comprising: providing H₂ to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

819.The method of claim 790, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

820.The method of claim 790, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well. 82 l.The method of claim 820, wherein at least about 20 heat sources are disposed in the formation for each production well.

822.The method of claim 790, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

823. The method of claim 790, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

824.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: heating a portion of the formation to a temperature sufficient to support oxidation of hydrocarbons within the portion, wherehi the portion is located substantially adjacent to a wellbore; flowing an oxidant through a conduit positioned within the wellbore to a heat source zone within the portion, wherein the heat source zone supports an oxidation reaction between hydrocarbons and the oxidant; reacting a portion of the oxidant with hydrocarbons to generate heat; and fransfening generated heat substantially by conduction to a pyrolysis zone of the foπnation to pyrolyze at least a portion of the hydrocarbons within the pyrolysis zone.

825. The method of claim 824, wherein heating the portion of the formation comprises raising a temperature of the portion above about 400 °C.

826.The method of claim 824, wherein the conduit comprises critical flow orifices, the method further comprising flowing the oxidant through the critical flow orifices to the heat source zone.

827.The method of claim 824, further comprising removing reaction products from the heat source zone through the wellbore.

828.The method of claim 824, further comprising removing excess oxidant from the heat source zone to inhibit transport of the oxidant to the pyrolysis zone.

829.The method of claim 824, further comprising transporting the oxidant from the conduit to the heat source zone substantially by diffusion.

830.The method of claim 824, further comprising heating the conduit with reaction products being removed through the wellbore.

831.The method of claim 824, wherein the oxidant comprises hydrogen peroxide.

832. The method of claim 824, wherein the oxidant comprises air.

833. The method of claim 824, wherein the oxidant comprises a fluid substantially free of nifrogen.

834.The method of claim 824, further comprising limiting an amount of oxidant to maintain a temperature of the heat source zone less than about 1200 °C.

835. The method of clahn 824, wherein heating the portion of the fonnation comprises electrically heating the formation.

836.The method of claim 824, wherein heating the portion of the formation comprises heating the portion using exhaust gases from a surface burner.

837.The method of claim 824, wherein heating the portion of the formation comprises heating the portion with a flameless disfributed combustor.

838. The method of clahn 824, further comprising confrolling a pressure and a temperature within at least a majority of the pyrolysis zone, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

839. The method of claim 824, further comprising confrolling the heat such that an average heating rate of the pyrolysis zone is less than about 1 °C per day during pyrolysis.

840.The method of claim 824, further comprising confrolling a pressure within at least a majority of the pyrolysis zone of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

84 l.The method of claim 824, further comprising: providing hydrogen (H₂) to the pyrolysis zone to hydrogenate hydrocarbons within the pyrolysis zone; and heating a portion of the pyrolysis zone with heat from hydrogenation.

842.The method of claim 824, wherein the wellbore is located along sfrike to reduce pressure differentials along a heated length of the wellbore.

843.The method of claim 824, wherein the wellbore is located along sfrike to increase uniformity of heating along a heated length of the wellbore.

844.The method of claim 824, wherein the wellbore is located along sfrike to increase control of heating along a heated length of the wellbore.

845.A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons within the portion of the formation with an oxidant; flowing the oxidant into a conduit, and wherein the conduit is connected such that the oxidant can flow from the conduit to the hydrocarbons; allowing the oxidant and the hydrocarbons to react to produce heat in a heat source zone; allowing heat to transfer from the heat source zone to a pyrolysis zone in the formation to pyrolyze at least a portion of the hydrocarbons within the pyrolysis zone; and removing reaction products such that the reaction products are inhibited from flowing from the heat source zone to the pyrolysis zone.

846.The method of claim 845, wherein heating the portion of the formation comprises raising the temperature of the portion above about 400 °C.

847.The method of claim 845, wherein heating the portion of the formation comprises elecfrically heating the formation.

848.The method of claim 845, wherein heating the portion of the formation comprises heating the portion using exhaust gases from a surface burner.

849.The method of claim 845, wherein the conduit comprises critical flow orifices, the method further comprising flowing the oxidant through the critical flow orifices to the heat source zone.

850.The method of claim 845, wherein the conduit is located within a wellbore, wherein removing reaction products comprises removing reaction products from the heat source zone through the wellbore.

85 l.The method of claim 845, further comprising removing excess oxidant from the heat source zone to inhibit fransport of the oxidant to the pyrolysis zone.

852.The method of claim 845, further comprising ttansporting the oxidant from the conduit to the heat source zone substantially by diffusion.

853. The method of claim 845, wherein the conduit is located within a wellbore, the method further comprising heating the conduit with reaction products being removed through the wellbore to raise a temperature of the oxidant passing through the conduit.

854.The method of claim 845, wherein the oxidant comprises hydrogen peroxide.

855. The method of claim 845, wherein the oxidant comprises air.

856.The method of claim 845, wherein the oxidant comprises a fluid substantially free of nifrogen.

857. The method of claim 845, further comprising limiting an amount of oxidant to maintain a temperature of the heat source zone less than about 1200 °C.

858. The method of claim 845, further comprising limiting an amount of oxidant to maintain a temperature of the heat source zone at a temperature that inhibits production of oxides of nifrogen.

859. The method of claim 845, wherein heating a portion of the foπnation to a temperature sufficient to support oxidation of hydrocarbons within the portion further comprises heating with a flameless distributed combustor.

860.The method of claim 845, further comprising confrolling a pressure and a temperature within at least a majority of the pyrolysis zone of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

861. The method of claim 845, further comprising confrolling the heat such that an average heating rate of the pyrolysis zone is less than about 1 °C per day during pyrolysis.

862.The method of claim 845, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

863.The method of claim 845, further comprising confrolling a pressure within at least a majority of the pyrolysis zone, wherein the controlled pressure is at least about 2.0 bars absolute.

864.The method of claim 845, further comprising: providing hydrogen (H₂) to the pyrolysis zone to hydrogenate hydrocarbons within the pyrolysis zone; and heating a portion of the pyrolysis zone with heat from hydrogenation.

865. An in situ method for heating a relatively low permeability foπnation containing heavy hydrocarbons, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons within the portion of the foimation with an oxidizing fluid, wherein the portion is located substantially adjacent to an opening in the formation; providing the oxidizing fluid to a heat source zone in the formation; allowing the oxidizing gas to react with at least a portion of the hydrocarbons at the heat source zone to generate heat in the heat source zone; and fransfening the generated heat substantially by conduction from the heat source zone to a pyrolysis zone in the formation.

866. The method of claim 865, further comprising transporting the oxidizing fluid through the heat source zone by diffusion.

867.The method of claim 865, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

868.The method of claim 865, further comprising confrolling a flow of the oxidizing fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

869.The method of claim 865, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit.

870.The method of claim 865, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and fransfening substantial heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

87 l.The method of claim 865, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

872. The method of claim 865, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foimation through the conduit and confrolling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

873. The method of claim 865, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

874. The method of claim 865, wherein the heat source zone extends radially from the opening a width of less than approximately 0.15 m.

875. The method of claim 865, wherein heating the portion comprises applying electrical cunent to an electric heater disposed within the opening.

876. The method of claim 865, wherein the pyrolysis zone is substantially adjacent to the heat source zone.

877.The method of claim 865, further comprising confrolling a pressure and a temperature within at least a majority of the pyrolysis zone of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

878. The method of claim 865, further comprising controlling the heat such that an average heating rate of the pyrolysis zone is less than about 1 °C per day during pyrolysis.

879.The method of claim 865, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

880.The method of claim 865, further comprising controlling a pressure within at least a majority of the pyrolysis zone, wherein the confrolled pressure is at least about 2.0 bars absolute.

881. The method of claim 865, further comprising: providing hydrogen (H₂) to the pyrolysis zone to hydrogenate hydrocarbons within the pyrolysis zone; and heating a portion of the pyrolysis zone with heat from hydrogenation.

882.A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; producing a mixture from the formation; and maintaining an average temperature within the selected section above a minimum pyrolysis temperature and below a vaporization temperature of hydrocarbons having carbon numbers greater than 25 to inhibit production of a substantial amount of hydrocarbons having carbon numbers greater than 25 in the mixture.

883. The method of claim 882, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

884.The method of clahn 882, wherein maintaining the average temperature within the selected section comprises maintaining the temperature within a pyrolysis temperature range.

885.The method of clahn 882, wherein the one or more heat sources comprise electrical heaters.

886.The method of claim 882, wherein the one or more heat sources comprise surface burners.

887.The method of claim 882, wherein the one or πiore heat sources comprise flameless distributed combustors.

888. The method of claim 882, wherein the one or more heat sources comprise natural distributed combustors.

889. The method of claim 882, wherein the minimum pyrolysis temperature is greater than about 270 °C.

890.The method of claim 882, wherein the vaporization temperature is less than approximately 450 °C at atmospheric pressure.

891.The method of claim 882, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

892.The method of claim 882, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

893. The method of claim 882, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C„), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

894.The method of claim 882, wherein allowmg the heat to fransfer comprises fransfening heat substantially by conduction.

895.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

896.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

897. The method of claim 882, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

898.The method of claim 882, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

899.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

900.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

90 l.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

902.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

903. The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

904.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

905.The method of claim 882, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

906.The method of claim 882, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

907. The method of claim 882, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

908.The method of claim 882, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

909.The method of claim 882, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

910.The method of claim 882, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

91 l.The method of claim 910, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

912.The method of claim 882, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

913. The method of claim 882, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

914.The method of claim 882, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

915. The method of claim 882, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

916.The method of claim 915, wherein at least about 20 heat sources are disposed in the formation for each production well.

917.The method of claim 882, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are Ideated in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

918.The method of claim 882, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

919.A method of treating a relatively low permeability foimation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foimation; confrolling a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than 25; and producing a mixture from the formation.

920.The method of claim 919, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

921. The method of claim 919, wherein the one or more heat sources comprise elecfrical heaters.

922.The method of claim 919, wherein the one or more heat sources comprise surface burners.

923.The method of claim 919, wherein the one or more heat sources comprise flameless distributed combustors.

924.The method of claim 919, wherein the one or more heat sources comprise natural disfributed combustors.

925.The method of claim 919, further comprising confrolling a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

926.The method of claim 925, wherein controlling the temperature comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

927.The method of claim 919, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

928.The method of claim 919, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the fonnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

929.The method of claim 919, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

930.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

93 l.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

932.The method of claim 919, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

933. The method of claim 919, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

934.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

935. The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

936.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

937.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

938.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

939.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

940.The method of claim 919, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

94 l.The method of claim 919, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

942.The method of claim 919, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

943. The method of claim 919, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

944.The method of claim 919, further comprising controlling the pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

945. The method of claim 919, further comprising confrolling foimation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

946.The method of claim 945, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

947.The method of claim 919, wherein controlling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

948. The method of claim 919, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

949.The method of claim 919, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

950.The method of claim 919, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

951. The method of claim 950, wherein at least about 20 heat sources are disposed in the formation for each production well.

952.The method of claim 919, further comprising providmg heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

953. The method of claim 919, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

954.A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the fonnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

955. The method of claim 954, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

956.The method of claim 954, wherein the one or more heat sources comprise elecfrical heaters.

957.The method of claim 954, wherein the one or more heat sources comprise surface burners.

958.The method of claim 954, wherein the one or more heat sources comprise flameless disfributed combustors.

959.The method of claim 954, wherein the one or more heat sources comprise natural distributed combustors.

960.The method of clahn 954, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

961. The method of claim 954, wherein confrolling the temperature comprises maintaining the temperature within the selected section within a pyrolysis temperature range.

962.The method of claim 954, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

963. The method of claim 954, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, ρ_B is formation bulk density, and wherein the heathig rate is less than about 10 °C/day.

964.The method of claim 954, wherein allowing the heat to transfer comprises transfening heat substantially by conduction.

965.The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

966. The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

967.The method of claim 954, wherehi the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

968. The method of claim 954, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

969.The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

970.The method of clahn 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

97 l.The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

972.The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

973. The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

974.The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

975. The method of claim 954, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

976.The method of claim 954, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non- condensable component.

977.The method of claim 954, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

978.The method of claim 954, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

979. The method of claim 954, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

980.The method of claim 954, further comprising confrolling foπnation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

981. The method of claim 980, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

982.The method of clahn 954, further comprising altering a pressure within the foπnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

983. The method of claim 954, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

984.The method of claim 954, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

985.The method of claim 954, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

986.The method of claim 954, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

987.The method of claim 986, wherein at least about 20 heat sources are disposed in the formation for each production well.

988.The method of claim 954, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

989.The method of claim 954, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

990. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: heating a section of the foπnation to a pyrolysis temperature from at least a first heat source, a second heat source and a third heat source, and wherein the first heat source, the second heat source and the third heat source are located along a perimeter of the section; confrolling heat input to the first heat source, the second heat source and the thfrd heat source to limit a heating rate of the section to a rate configured to produce a mixture from the formation with an olefin content of less than about 15% by weight of condensable fluids (on a dry basis) within the produced mixture; and producing the mixture from the foπnation through a production well.

99 l.The method of claim 990, wherem supeφosition of heat form the first heat source, second heat source, and third heat source pyrolyzes a portion of the hydrocarbons within the foπnation to fluids.

992.The method of claim 990, wherein the pyrolysis temperature is between about 270 °C and about 400 °C.

993. The method of claim 990, wherein the first heat source is operated for less than about twenty four hours a day.

994.The method of clahn 990, wherein the first heat source comprises an electrical heater.

995. The method of claim 990, wherein the first heat source comprises a surface burner.

996.The method of claim 990, wherein the first heat source comprises a flameless disfributed combustor.

997.The method of claim 990, wherein the first heat source, second heat source and third heat source are positioned substantially at apexes of an equilateral triangle.

998. The method of claim 990, wherein the production well is located substantially at a geometrical center of the first heat source, second heat source, and third heat source.

999.The method of claim 990, further comprising a fourth heat source, fifth heat source, and sixth heat source located along the perimeter of the section.

1000. The method of claim 999, wherein the heat sources are located substantially at apexes of a regular hexagon.

1001. The method of claim 1000, wherein the production well is located substantially at a center of the hexagon.

1002. The method of claim 990, further comprising confrolling a pressure and a temperature within at least a majority of the section of the foπnation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1003. The method of claim 990, wherein confrolling the temperature comprises maintaining the temperature within the selected section within a pyrolysis temperature range.

1004. The method of claim 990, further comprising controlling the heat such that an average heating rate of the section is less than about 3 °C per day during pyrolysis.

1005. The method of claim 990, further comprising confrolling the heat such that an average heating rate of the section is less than about 1 °C per day during pyrolysis.

1006. The method of claim 990, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume ( ) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C„), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1007. The method of claim 990, wherein heating the section of the formation comprises fransfening heat substantially by conduction.

1008. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1009. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1010. The method of claim 990, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherehi the ratio of ethene to ethane is greater than about 0.001.

1011. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1012. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1013. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1014. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1015. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1016. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1017. The method of claim 990, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1018. The method of claim 990, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1019. The method of claim 990, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1020. The method of claim 990, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1021. The method of claim 990, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1022. The method of claim 990, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1023. The method of claim 1022, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

1024. The method of claim 990, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1025. The method of claim 990, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

1026. The method of clahn 990, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1027. The method of claim 990, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprismg hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1028. The method of claim 990, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

1029. The method of claim 1028, wherein at least about 20 heat sources are disposed in the formation for each production well.

1030. The method of claim 990, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1031. The method of claim 990, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1032. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the fonnation; and producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1033. The method of claim 1032, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foimation.

1034. The method of claim 1032, wherein the one or more heat sources comprise electrical heaters.

1035. The method of claim 1032, wherein the one or more heat sources comprise surface burners.

1036. The method of claim 1032, wherein the one or more heat sources comprise flameless disfributed combustors.

1037. The method of claim 1032, wherein the one or more heat sources comprise natural distributed combustors.

1038. The method of claim 1032, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1039. The method of clahn 1038, wherein confrolling the temperature comprises maintaining the temperature within the selected section within a pyrolysis temperature range.

1040. The method of claim 1032, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1041. The method of clahn 1032, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1042. The method of claim 1032, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1043. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1044. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1045. The method of claim 1032, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

1046. The method of claim 1032, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

1047. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1048. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1049. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1050. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1051. The method of claim 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1052. The method of clahn 1032, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1053. The method of claim 1032, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1054. The method of claim 1032, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1055. The method of claim 1032, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1056. The method of claim 1032, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1057. The method of clahn 1032, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1058. The method of claim 1057, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

1059. The method of claim 1032, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foimation having carbon numbers greater than about 25.

1060. The method of claim 1032, wherein controlling foimation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

1061. The method of claim 1032, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1062. The method of claim 1032, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprismg hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1063. The method of claim 1032, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1064. The method of clahn 1063, wherein at least about 20 heat sources are disposed in the formation for each production well.

1065. The method of claim 1032, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1066. The method of claim 1032, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1067. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foimation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1068. The method of claim 1067, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1069. The method of claim 1067, wherein the one or more heat sources comprise elecfrical heaters.

1070. The method of claim 1067, wherein the one or more heat sources comprise surface burners.

1071. The method of claim 1067, wherein the one or more heat sources comprise flameless disfributed combustors.

1072. The method of claim 1067, wherein the one or more heat sources comprise natural distributed combustors.

1073. The method of claim 1067, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the foimation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1074. The method of claim 1073, wherein controlling the temperature comprises maintaining the temperature within the selected section within a pyrolysis temperature range.

1075. The method of claim 1067, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1076. The method of claim 1067, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

1077. The method of claim 1067, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1078. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1079. The method of claim 1067, wherehi the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1080. The method of claim 1067, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

1081. The method of claim 1067, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

1082. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1083. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1084. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherehi less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1085. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1086. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1087. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1088. The method of claim 1067, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1089. The method of claim 1067, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1090. The method of claim 1067, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1091. The method of claim 1067, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1092. The method of claim 1067, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1093. The method of clahn 1067, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1094. The method of claim 1093, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

1095. The method of claim 1067, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1096. The method of claim 1067, wherein controlling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

1097. The method of claim 1067, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1098. The method of claim 1067, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1099. The method of claim 1067, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1100. The method of claim 1099, wherein at least about 20 heat sources are disposed in the formation for each production well.

1101. The method of claim 1067, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1102. The method of claim 1067, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1103. A method of freating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the foimation; and producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1104. The method of claim 1103, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1105. The method of claim 1103, wherein the one or more heat sources comprise elecfrical heaters.

1106. The method of claim 1103, wherein the one or more heat sources comprise surface burners.

1107. The method of claim 1103, wherein the one or more heat sources comprise flameless distributed combustors.

1108. The method of claim 1103, wherein the one or more heat sources comprise natural distributed combustors.

1109. The method of clahn 1103, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1110. The method of claim 1109, wherein controlling the temperature comprises maintaining the temperature within the selected section within a pyrolysis temperature range.

llll. The method of claim 1103, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1112. The method of claim 1103, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1113. The method of claim 1103, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

1114. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1115. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1116. The method of claim 1103, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

1117. The method of claim 1103, wherein the produced mixture comprises non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15, and wherein the ratio of ethene to ethane is greater than about 0.001.

1118. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1119. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1120. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1121. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1122. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1123. The method of claim 1103, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1124. The method of claim 1103, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1125. The method of claim 1103, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1126. The method of claim 1103, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1127. The method of claim 1103, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1128. The method of claim 1103, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1129. The method of claim 1128, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

1130. The method of clahn 1103, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foimation having carbon numbers greater than about 25.

1131. The method of clahn 1103, wherein confrolling formation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

1132. The method of claim 1103, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1133. The method of claim 1103, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1134. The method of claim 1103, wherehi producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1135. The method of claim 1134, wherein at least about 20 heat sources are disposed in the formation for each production well.

1136. The method of claim 1103, further comprising providmg heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1137. The method of claim 1103, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1138. A method of freating a relatively low peπneability foπnation containing heavy hydrocarbons in situ, comprising: raising a temperature of a first section of the fonnation with one or more heat sources to a first pyrolysis temperature; heating the first section to an upper pyrolysis temperature, wherein heat is supplied to the first section at a rate configured to inhibit olefin production; producing a first mixture from the foimation, wherein the first mixture comprises condensable hydrocarbons and H₂; creating a second mixture from the first mixture, wherein the second mixture comprises a higher concentration of H₂ than the first mixture; raising a temperature of a second section of the formation with one or more heat sources to a second pyrolysis temperature; providing a portion of the second mixture to the second section; heatmg the second section to an upper pyrolysis temperature, wherein heat is supplied to the second section at a rate configured to inhibit olefin production; and producing a third mixture from the second section.

1139. The method of clahn 1138, wherein creating the second mixture comprises removing condensable hydrocarbons from the first mixture.

1140. The method of claim 1138, wherein creating the second mixture comprises removing water from the first mixture.

1141. The method of claim 1138, wherein creating the second mixture comprises removing carbon dioxide from the first mixture.

1142. The method of claim 1138, wherein the first pyrolysis temperature is greater than about 270 °C.

1143. The method of claim 1138, wherein the second pyrolysis temperature is greater than about 270 °C.

1144. The method of claim 1138, wherein the upper pyrolysis temperature is about 500 °C.

1145. The method of claim 1138, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the first or second selected section of the formation.

1146. The method of clahn 1138, wherein the one or more heat sources comprise elecfrical heaters.

1147. The method of clahn 1138, wherein the one or more heat sources comprise surface burners.

1148. The method of claim 1138, wherein the one or more heat sources comprise flameless disfributed combustors.

1149. The method of claim 1138, wherein the one or more heat sources comprise natural distributed combustors.

1150. The method of claim 1138, further comprising controlling a pressure and a temperature within at least a majority of the first section and the second section of the fonnation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

1151. The method of claim 1138, further comprising controlling the heat to the first and second sections such that an average heating rate of the first and second sections is less than about 1 °C per day during pyrolysis.

1152. The method of claim 1138, wherein heating the first and the second sections comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heathig pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

1153. The method of claim 1138, wherein heating the first and second sections comprises fransfening heat substantially by conduction.

1154. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1155. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1156. The method of claim 1138, wherein the first or third mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1157. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1158. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1159. The method of claim 1138, wherein the first or thfrd mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1160. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1161. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1162. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1163. The method of claim 1138, wherein the first or third mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1164. The method of claim 1138, wherein the first or third mixture comprises a non-condensable component, and wherein the non-condensable component comprises hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable component and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1165. The method of claim 1138, wherein the ffrst or third mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1166. The method of claim 1138, wherein the ffrst or third mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1167. The method of claim 1138, further comprising confrolling a pressure within at least a majority of the first or second sections of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1168. The method of claim 1138, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1169. The method of claim 1168, wherein the partial pressure of H₂ within a mixture is measured when the mixture is at a production well.

1170. The method of claim 1138, further comprising altering a pressure within the foimation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1171. The method of claim 1138, further comprising: providing hydrogen (H₂) to the first or second section to hydrogenate hydrocarbons within the first or second section; and heating a portion of the first or second section with heat from hydrogenation.

1172. The method of claim 1138, further comprising: producing hydrogen and condensable hydrocarbons from the foimation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1173. The method of claim 1138, wherein producing the first or thfrd mixture comprises producing the first or thfrd mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1174. The method of clahn 1173, wherein at least about 20 heat sources are disposed in the formation for each production well.

1175. The method of claim 1138, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the fonnation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1176. The method of claim 1138, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1177. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foimation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; producing a mixture from the formation; and hydrogenating a portion of the produced mixture with H₂ produced from the foπnation.

1178. The method of claim 1177, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foπnation.

1179. The method of claim 1177, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1180. The method of claim 1177, wherein the one or more heat sources comprise electrical heaters.

1181. The method of claim 1177, wherein the one or more heat sources comprise surface burners.

1182. The method of claim 1177, wherein the one or more heat sources comprise flameless disfributed combustors.

1183. The method of claim 1177, wherein the one or more heat sources comprise natural distributed combustors.

1184. The method of claim 1177, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1185. The method of claim 1177, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1186. The method of claim 1177, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, ρ_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1187. The method of claim 1177, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

1188. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1189. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1190. The method of claim 1177, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1191. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1192. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1193. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1194. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1195. The method of clahn 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1196. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1197. The method of claim 1177, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1198. The method of claim 1177, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1199. The method of claim 1177, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1200. The method of claim 1177, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1201. The method of claim 1177, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1202. The method of claim 1177, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1203. The method of claim 1177, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1204. The method of claim 1177, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1205. The method of claim 1177, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1206. The method of claim 1177, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1207. The method of claim 1206, wherein at least about 20 heat sources are disposed in the formation for each production well.

1208. The method of claim 1177, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1209. The method of claim 1177, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1210. A method of freating a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: heating a first section of the formation; producing H₂ from the first section of formation; heating a second section of the formation; and recirculating a portion of the H₂ from the first section into the second section of the formation to provide a reducing environment within the second section of the formation.

1211. The method of claim 1210, wherein heating the first section or heating the second section comprises heating with an electrical heater.

1212. The method of claim 1210, wherein heating the first section or heating the second section comprises heating with a surface burner.

1213. The method of claim 1210, wherein heating the ffrst section or heating the second section comprises heating with a flameless disfributed combustor.

1214. The method of claim 1210, wherein heating the first section or heating the second section comprises heating with a natural distributed combustor.

1215. The method of claim 1210, further comprising controlling a pressure and a temperature within at least a majority of the first or second section of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1216. The method of claim 1210, further comprising confrolling the heat such that an average heating rate of the first or second section is less than about 1 °C per day during pyrolysis.

1217. The method of claim 1210, wherein heating the first section or heating the second section further comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1218. The method of claim 1210, wherein heating the first section or heating the second section comprises fransfening heat substantially by conduction.

1219. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1220. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1221. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1222. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1223. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1224. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1225. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1226. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherehi less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1227. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1228. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1229. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1230. The method of clahn 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1231. The method of claim 1210, further comprising producing a mixture from the second section, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1232. The method of claim 1210, further comprising confrolling a pressure within at least a majority of the first or second section of the foπnation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1233. The method of claim 1210, further comprising controlling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1234. The method of claim 1233, wherein the partial pressure of H₂ within a mixture is measured when the mixture is at a production well.

1235. The method of claim 1210, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1236. The method of claim 1210, further comprising: providing hydrogen (H₂) to the second section to hydrogenate hydrocarbons within the section; and heating a portion of the second section with heat from hydrogenation.

1237. The method of claim 1210, further comprising: producing hydrogen and condensable hydrocarbons from the fonnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1238. The method of claim 1210, further comprising producing a mixture from the formation hi a production well, and wherein at least about 7 heat sources are disposed in the fonnation for each production well.

1239. The method of claim 1238, wherein at least about 20 heat sources are disposed in the formation for each production well.

1240. The method of claim 1210, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1241. The method of claim 1210, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1242. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; producing a mixture from the formation; and confrolling formation conditions such that the mixture produced from the formation comprises condensable hydrocarbons including H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1243. The method of clahn 1242, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foimation.

1244. The method of claim 1242, wherein controlling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

1245. The method of claim 1242, wherein the one or more heat sources comprise electrical heaters.

1246. The method of claim 1242, wherein the one or more heat sources comprise surface burners.

1247. The method of claim 1242, wherein the one or more heat sources comprise flameless distributed combustors.

1248. The method of claim 1242, wherein the one or more heat sources comprise natural distributed combustors.

1249. The method of claim 1242, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1250. The method of claim 1242, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1251. The method of claim 1242, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low penneability foπnation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1252. The method of claim 1242, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

1253. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1254. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1255. The method of claim 1242, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1256. The method of claim 1242, wherehi the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1257. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1258. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherehi less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1259. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1260. The method of clahn 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1261. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1262. The method of claim 1242, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1263. The method of claim 1242, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1264. The method of claim 1242, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1265. The method of claim 1242, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1266. The method of claim 1242, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1267. The method of claim 1242, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1268. The method of claim 1242, wherein confrolling foπnation conditions comprises recirculating a portion of hydrogen from the mixture into the formation.

1269. The method of clahn 1242, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1270. The method of clahn 1242, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1271. The method of claim 1242, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1272. The method of claim 1271, wherein at least about 20 heat sources are disposed in the formation for each production well.

1273. The method of claim 1242, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1274. The method of claim 1242, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1275. The method of claim 1242, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1276. A method of freating a relatively low peπneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; maintaining a pressure of the selected section above atmospheric pressure to increase a partial pressure of H₂, as compared to the partial pressure of H₂ at atmospheric pressure, in at least a majority of the selected section; and producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1277. The method of claim 1276, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1278. The method of claim 1276, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1279. The method of claim 1276, wherein the one or more heat sources comprise elecfrical heaters.

1280. The method of claim 1276, wherein the one or more heat sources comprise surface burners.

1281. The method of claim 1276, wherein the one or more heat sources comprise flameless disfributed combustors.

1282. The method of claim 1276, wherein the one or more heat sources comprise natural distributed combustors.

1283. The method of claim 1276, further comprising controlling the pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1284. The method of claim 1276, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1285. The method of claim 1276, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1286. The method of claim 1276, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1287. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1288. The method of claim 1276, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1289. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1290. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1291. The method of clahn 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1292. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1293. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1294. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1295. The method of claim 1276, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1296. The method of claim 1276, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1297. The method of claim 1276, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1298. The method of claim 1276, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1299. The method of clahn 1276, further comprising controlling the pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1300. The method of claim 1276, further comprising increasing the pressure of the selected section, to an upper limit of about 21 bars absolute, to increase an amount of non-condensable hydrocarbons produced from the formation.

1301. The method of claim 1276, further comprising decreasing pressure of the selected section, to a lower lhnit of about atmospheric pressure, to increase an amount of condensable hydrocarbons produced from the fonnation.

1302. The method of claim 1276, wherein the partial pressure comprises a partial pressure based on properties measured at a production well.

1303. The method of claim 1276, further comprising altering the pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1304. The method of claim 1276, further comprising confrolling formation conditions by recirculating a portion of hydrogen from the mixture into the formation.

1305. The method of claim 1276, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1306. The method of claim 1276, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1307. The method of claim 1276, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1308. The method of claim 1307, wherein at least about 20 heat sources are disposed in the formation for each production well.

1309. The method of claim 1276, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1310. The method of claim 1276, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1311. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the fonnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; providing H₂ to the foπnation to produce a reducing environment in at least some of the fonnation; producing a mixture from the formation.

1312. The method of claim 1311, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1313. The method of claim 1311, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1314. The method of claim 1311, further comprising separating a portion ofhydrogen within the mixture and recirculating the portion into the foπnation.

1315. The method of claim 1311, wherein the one or more heat sources comprise elecfrical heaters.

1316. The method of claim 1311, wherein the one or more heat sources comprise surface burners.

1317. The method of clahn 1311, wherein the one or more heat sources comprise flameless disfributed combustors.

1318. The method of claim 1311, wherein the one or more heat sources comprise natural disfributed combustors.

1319. The method of claim 1311, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1320. The method of claim 1311, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1321. The method of claim 1311, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (1 of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1322. The method of claim 1311, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

1323. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1324. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1325. The method of claim 1311, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about

0.15.

1326. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1327. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1328. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1329. The method of clahn 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1330. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1331. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1332. The method of claim 1311, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1333. The method of claim 1311, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1334. The method of claim 1311, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1335. The method of claim 1311, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1336. The method of claim 1311, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1337. The method of claim 1311, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1338. The method of claim 1311, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1339. The method of claim 1311, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1340. The method of claim 1311, wherein providing hydrogen (H₂) to the formation further comprises: hydrogenating hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1341. The method of claim 1311, further comprising: producing hydrogen and condensable hydrocarbons from the foπnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1342. The method of clahn 1311, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1343. The method of claim 1342, wherein at least about 20 heat sources are disposed in the formation for each production well.

1344. The method of clahn 1311, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1345. The method of claim 1311, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1346. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; providing H₂ to the selected section to hydrogenate hydrocarbons within the selected section and to heat a portion of the section with heat from the hydrogenation; and confrolling heating of the selected section by controlling amounts of H₂ provided to the selected section.

1347. The method of claim 1346, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1348. The method of claim 1346, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1349. The method of claim 1346, wherein the one or more heat sources comprise electrical heaters.

1350. The method of claim 1346, wherein the one or more heat sources comprise surface burners.

1351. The method of claim 1346, wherein the one or more heat sources comprise flameless disfributed combustors.

1352. The method of claim 1346, wherein the one or more heat sources comprise natural disfributed combustors.

1353. The method of claim 1346, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1354. The method of claim 1346, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1355. The method of claim 1346, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

1356. The method of claim 1346, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1357. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1358. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1359. The method of clahn 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1360. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1361. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1362. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1363. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1364. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1365. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1366. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1367. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1368. The method of claim 1346, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1369. The method of claim 1346, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1370. The method of claim 1346, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1371. The method of claim 1346, further comprising confrolling formation conditions to produce a mixture from the formation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1372. The method of claim 1371, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1373. The method of claim 1346, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foimation having carbon numbers greater than about 25.

1374. The method of claim 1346, further comprising confrolling foimation conditions by recirculating a portion ofhydrogen from a produced mixture into the formation.

1375. The method of clahn 1346, further comprising: producing hydrogen and condensable hydrocarbons from the foimation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1376. The method of claim 1346, further comprising producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1377. The method of claim 1376, wherein at least about 20 heat sources are disposed in the formation for each production well.

1378. The method of claim 1346, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1379. The method of claim 1346, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to foπn a repetitive pattern of units.

1380. An in situ method for producing H₂ from a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation, wherein a H₂ partial pressure within the mixture is greater than about 0.5 bars.

1381. The method of claim 1380, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1382. The method of claim 1380, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1383. The method of claim 1380, wherein the one or more heat sources comprise electrical heaters.

1384. The method of claim 1380, wherein the one or more heat sources comprise surface burners.

1385. The method of claim 1380, wherein the one or more heat sources comprise flameless disfributed combustors.

1386. The method of claim 1380, wherein the one or more heat sources comprise natural distributed combustors.

1387. The method of claim 1380, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1388. The method of claim 1380, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1389. The method of claim 1380, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability foimation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1390. The method of claim 1380, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1391. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1392. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1393. The method of claim 1380, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1394. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1395. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1396. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1397. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1398. The method of clahn 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1399. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1400. The method of claim 1380, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1401. The method of clahn 1380, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1402. The method of claim 1380, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1403. The method of claim 1380, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1404. The method of claim 1380, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1405. The method of claim 1380, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1406. The method of clahn 1380, further comprising recirculating a portion of the hydrogen within the mixture into the formation.

1407. The method of claim 1380, further comprising condensing a hydrocarbon component from the produced mixture and hydrogenating the condensed hydrocarbons with a portion of the hydrogen.

1408. The method of claim 1380, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1409. The method of clahn 1380, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1410. The method of claim 1409, wherein at least about 20 heat sources are disposed in the formation for each production well.

1411. The method of claim 1380, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1412. The method of claim 1380, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherehi three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

1413. The method of claim 1380, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1414. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; wherein the selected section has been selected for heating using an atomic hydrogen weight percentage of at least a portion of hydrocarbons in the selected section, and wherein at least the portion of the hydrocarbons in the selected section comprises an atomic hydrogen weight percentage, when measured on a dry, ash-free basis, of greater than about 4.0 %; and producing a mixture from the formation.

1415. The method of claim 1414, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1416. The method of claim 1414, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1417. The method of claim 1414, wherein the one or more heat sources comprise electrical heaters.

1418. The method of claim 1414, wherein the one or more heat sources comprise surface burners.

1419. The method of clahn 1414, wherein the one or more heat sources comprise flameless disfributed combustors.

1420. The method of claim 1414, wherein the one or more heat sources comprise natural distributed combustors.

1421. The method of claim 1414, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1422. The method of claim 1414, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1423. The method of clahn 1414, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1424. The method of clahn 1414, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1425. The method of claim 1414, wherein providing heat from the one or more heat sources comprises heating the selected section such that a theπnal conductivity of at least a portion of the selected section is greater than about

0.5 W/(m °C).

1426. The method of claim 1414, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1427. The method of claim 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1428. The method of claim 1414, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1429. The method of claim 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1430. The method of claim 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1431. The method of claim 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1432. The method of clahn 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1433. The method of clahn 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1434. The method of clahn 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1435. The method of claim 1414, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1436. The method of claim 1414, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1437. The method of claim 1414, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1438. The method of claim 1414, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1439. The method of claim 1414, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1440. The method of claim 1414, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1441. The method of claim 1440, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1442. The method of claim 1414, further comprising altering a pressure within the foπnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1443. The method of claim 1414, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1444. The method of claim 1414, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1445. The method of claim 1414, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1446. The method of claim 1414, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1447. The method of claim 1414, wherein allowing the heat to fransfer comprises substantially uniformly increasing a permeability of a majority of the selected section.

1448. The method of claim 1414, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1449. The method of claim 1448, wherein at least about 20 heat sources are disposed in the formation for each production well.

1450. The method of claim 1414, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1451. The method of claim 1414, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to foπn a repetitive pattern of units.

1452. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; wherein at least some hydrocarbons within the selected section have an initial atomic hydrogen weight percentage of greater than about 4.0 %; and producing a mixture from the formation.

1453. The method of claim 1452, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1454. The method of claim 1452, further comprismg maintaining a temperature within the selected section within a pyrolysis temperature range.

1455. The method of claim 1452, wherein the one or more heat sources comprise elecfrical heaters.

1456. The method of clahn 1452, wherein the one or more heat sources comprise surface burners.

1457. The method of claim 1452, wherein the one or more heat sources comprise flameless disfributed combustors.

1458. The method of claim 1452, wherein the one or more heat sources comprise natural disfributed combustors.

1459. The method of claim 1452, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1460. The method of claim 1452, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1461. The method of claim 1452, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C„), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the fonnation, ρ_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1462. The method of claim 1452, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1463. The method of claim 1452, wherein providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 /(m °C).

1464. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1465. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1466. The method of claim 1452, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1467. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1468. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1469. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1470. The method of clahn 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1471. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1472. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1473. The method of claim 1452, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1474. The method of claim 1452, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1475. The method of claim 1452, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1476. The method of claim 1452, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1477. The method of claim 1452, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1478. The method of claim 1452, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1479. The method of claim 1478, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1480. The method of claim 1452, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1481. The method of claim 1452, further comprising controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1482. The method of claim 1452, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1483. The method of claim 1452, further comprising: producing hydrogen and condensable hydrocarbons from the foπnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1484. The method of claim 1452, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1485. The method of claim 1452, wherein allowing the heat to fransfer comprises substantially uniformly increasing a peπneability of a majority of the selected section.

1486. The method of claim 1452, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1487. The method of clahn 1486, wherein at least about 20 heat sources are disposed in the formation for each production well.

1488. The method of claim 1452, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1489. The method of claim 1452, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1490. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; wherein the selected section has been selected for heating using a total organic matter weight percentage of at least a portion of the selected section, and wherein at least the portion of the selected section comprises a total organic matter weight percentage, of at least about 5.0 %; and producing a mixture from the formation.

1491. The method of clahn 1490, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1492. The method of claim 1490, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1493. The method of claim 1490, wherein the one or more heat sources comprise electrical heaters.

1494. The method of claim 1490, wherein the one or more heat sources comprise surface burners.

1495. The method of claim 1490, wherein the one or more heat sources comprise flameless distributed combustors.

1496. The method of claim 1490, wherein the one or more heat sources comprise natural disfributed combustors.

1497. The method of claim 1490, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1498. The method of claim 1490, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1499. The method of claim 1490, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low penneability foπnation containing heavy hydrocarbons from the one or more heat sources, wherein the fonnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foπnation bulk density, and wherein the heating rate is less than about 10 °C/day.

1500. The method of clahn 1490, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1501. The method of claim 1490, wherem providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about

0.5 W/(m °C).

1502. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1503. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1504. The method of claim 1490, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about

0.15.

1505. The method of clahn 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1506. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1507. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1508. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1509. The method of clahn 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1510. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1511. The method of claim 1490, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1512. The method of claim 1490, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volmne of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1513. The method of claim 1490, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1514. The method of claim 1490, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1515. The method of claim 1490, further comprising confrolling a pressure within at least a maj ority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1516. The method of claim 1490, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1517. The method of claim 1516, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1518. The method of claim 1490, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1519. The method of claim 1490, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1520. The method of claim 1490, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1521. The method of claim 1490, further comprising: producing hydrogen and condensable hydrocarbons from the foπnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1522. The method of claim 1490, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

The method of claim 1490, wherein allowing the heat to fransfer comprises substantially uniformly increasing a permeability of a majority of the selected section.

1523. The method of claim 1490, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

1524. The method of claim 1523, wherein at least about 20 heat sources are disposed in the formation for each production well.

1525. The method of claim 1490, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1526. The method of claim 1490, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1527. A method of treating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the fonnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foimation; wherem at least some hydrocarbons within the selected section have an initial total organic matter weight percentage of at least about 5.0%; and producing a mixture from the foπnation.

1528. The method of claim 1527, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1529. The method of claim 1527, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1530. The method of claim 1527, wherein the one or more heat sources comprise electrical heaters.

1531. The method of claim 1527, wherein the one or more heat sources comprise surface burners.

1532. The method of claim 1527, wherein the one or more heat sources comprise flameless disfributed combustors.

1533. The method of claim 1527, wherein the one or more heat sources comprise natural disfributed combustors.

1534. The method of claim 1527, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1535. The method of claim 1527, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1536. The method of claim 1527, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the fonnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, ρ_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

1537. The method of claim 1527, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1538. The method of claim 1527, wherein providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

1539. The method of claim 1527, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1540. The method of clahn 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1541. The method of claim 1527, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1542. The method of claim 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1543. The method of claim 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1544. The method of claim 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1545. The method of claim 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1546. The method of claim 1527, wherehi the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1547. The method of clahn 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1548. The method of claim 1527, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1549. The method of claim 1527, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1550. The method of claim 1527, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1551. The method of claim 1527, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1552. The method of claim 1527, further comprising controlling a pressure within at least a majority of the selected section of the foimation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1553. The method of claim 1527, further comprising controlling foimation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1554. The method of claim 1553, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1555. The method of claim 1527, further comprising altering a pressure within the foimation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1556. The method of claim 1527, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1557. The method of claim 1527, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1558. The method of claim 1527, further comprising: producing hydrogen and condensable hydrocarbons from the fonnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1559. The method of claim 1527, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

The method of claim 1527, wherein allowing the heat to fransfer comprises substantially uniformly increasing a penneability of a majority of the selected section.

1561. The method of claim 1527, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1562. The method of claim 1561, wherein at least about 20 heat sources are disposed in the formation for each production well.

1563. The method of claim 1527, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1564. The method of claim 1527, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1565. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; wherein the selected section has been selected for heating using an atomic hydrogen to carbon ratio of at least a portion of hydrocarbons in the selected section, wherein at least a portion of the hydrocarbons in the selected section comprises an atomic hydrogen to carbon ratio greater than about 0.70, and wherein the atomic hydrogen to carbon ratio is less than about 1.65; and producing a mixture from the formation.

1566. The method of claim 1565, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foimation.

1567. The method of claim 1565, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1568. The method of claim 1565, wherein the one or more heat sources comprise elecfrical heaters.

1569. The method of claim 1565, wherein the one or more heat sources comprise surface burners.

1570. The method of claim 1565, wherein the one or more heat sources comprise flameless distributed combustors.

1571. The method of claim 1565, wherein the one or more heat sources comprise natural distributed combustors.

1572. The method of claim 1565, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1573. The method of claim 1565, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1574. The method of claim 1565, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volmne of the fonnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1575. The method of claim 1565, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1576. The method of claim 1565, wherein providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

1577. The method of clahn 1565, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1578. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1579. The method of claim 1565, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1580. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1581. The method of clahn 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1582. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1583. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1584. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1585. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1586. The method of claim 1565, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1587. The method of claim 1565, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1588. The method of claim 1565, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1589. The method of claim 1565, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1590. The method of clahn 1565, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1591. The method of clahn 1565, further comprising controlling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1592. The method of clahn 1591, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1593. The method of claim 1565, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1594. The method of clahn 1565, further comprising controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1595. The method of claim 1565, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1596. The method of claim 1565, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1597. The method of claim 1565, wherein allowing the heat to transfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1598. The method of clahn 1565, wherein allowing the heat to transfer comprises substantially uniformly increasing a peπneability of a maj ority of the selected section.

1599. The method of claim 1565, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1600. The method of claim 1599, wherein at least about 20 heat sources are disposed in the formation for each production well.

1601. The method of claim 1565, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1602. The method of claim 1565, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1603. A method of freating a relatively low penneability fonnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to a selected section of the formation; allowing the heat to fransfer from the one or more heat sources to the selected section of the formation to pyrolyze hydrocarbons within the selected section; wherein at least some hydrocarbons within the selected section have an initial atomic hydrogen to carbon ratio greater than about 0.70; wherein the initial atomic hydrogen to carbon ration is less than about 1.65; and producing a mixture from the foimation.

1604. The method of claim 1603, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1605. The method of claim 1603, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1606. The method of claim 1603, wherein the one or more heat sources comprise electrical heaters.

1607. The method of claim 1603, wherein the one or more heat sources comprise surface burners.

1608. The method of claim 1603, wherein the one or more heat sources comprise flameless disfributed combustors.

1609. The method of claim 1603, wherein the one or more heat sources comprise natural distributed combustors.

1610. The method of claim 1603, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1611. The method of claim 1603 , further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1612. The method of claim 1603, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low peπneability fonnation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

1613. The method of claim 1603, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1614. The method of claim 1603, wherein providing heat from the one or more heat sources comprises heathig the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

1615. The method of claim 1603, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1616. The method of clahn 1603, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1617. The method of claim 1603, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1618. The method of claim 1603 , wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1619. The method of claim 1603, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1620. The method of claim 1603, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1621. The method of claim 1603, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1622. The method of claim 1603, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1623. The method of claim 1603, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1624. The method of claim 1603, wherein the produced mixttire comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1625. The method of claim 1603, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1626. The method of claim 1603, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1627. The method of claim 1603, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1628. The method of claim 1603, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1629. The method of claim 1603, further comprising controlling fonnation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1630. The method of claim 1629, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1631. The method of claim 1603, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1632. The method of claim 1603, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1633. The method of claim 1603, further comprismg: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1634. The method of claim 1603, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1635. The method of claim 1603, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1636. The method of claim 1603, wherein allowing the heat to fransfer comprises substantially uniformly increasing a permeability of a majority of the selected section.

1637. The method of claim 1603, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1638. The method of claim 1637, wherein at least about 20 heat sources are disposed in the foimation for each production well.

1639. The method of claim 1603, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1640. The method of claim 1603, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1641. A method of freating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; wherein the selected section has been selected for heating using a moisture content in the selected section, and wherein at least a portion of the selected section comprises a moisture content of less than about 15 % by weight; and producing a mixture from the formation.

1642. The method of claim 1641, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the* selected section of the formation.

1643. The method of claim 1641 , further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1644. The method of claim 1641, wherein the one or more heat sources comprise electrical heaters.

1645. The method of claim 1641 , wherein the one or more heat sources comprise surface burners.

1646. The method of claim 1641, wherein the one or more heat sources comprise flameless distributed combustors.

1647. The method of claim 1641, wherein the one or more heat sources comprise natural disfributed combustors.

1648. The method of claim 1641, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1649. The method of claim 1641, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1650. The method of claim 1641 , wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the foπnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1651. The method of claim 1641 , wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

1652. The method of claim 1641, wherein providing heat from the one or more heat sources comprises heating the selected section such that a theπnal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

1653. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1654. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1655. The method of claim 1641, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about

0.15.

1656. The method of clahn 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1657. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherehi less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1658. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1659. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1660. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1661. The method of claim 1641 , wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1662. The method of claim 1641, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1663. The method of claim 1641 , wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1664. The method of claim 1641, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1665. The method of claim 1641, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1666. The method of clahn 1641, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1667. The method of claim 1641, further comprismg controlling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1668. The method of claim 1667, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1669. The method of claim 1641, further comprising altering a pressure within the foimation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1670. The method of claim 1641, further comprising controlling foπnation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1671. The method of claim 1641 , further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1672. The method of claim 1641, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1673. The method of claim 1641 , wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1674. The method of claim 1641, wherein allowing the heat to fransfer further comprises substantially uniformly increasing a peπneability of a majority of the selected section.

1675. The method of claim 1641 , wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1676. The method of claim 1675, wherein at least about 20 heat sources are disposed in the formation for each production well.

1677. The method of claim 1641, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foπnation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1678. The method of claim 1641, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1679. A method of freating a relatively low peπneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to a selected section of the formation; allowing the heat to ttansfer from the one or more heat sources to the selected section of the foπnation; wherein at least a portion of the selected section has an initial moisture content of less than about 15 % by weight; and producing a mixture from the formation.

1680. The method of claim 1679, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1681. The method of claim 1679, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1682. The method of claim 1679, wherein the one or more heat sources comprise elecfrical heaters.

1683. The method of claim 1679, wherein the one or more heat sources comprise surface burners.

1684. The method of claim 1679, wherein the one or more heat sources comprise flameless disfributed combustors.

1685. The method of claim 1679, wherein the one or more heat sources comprise natural distributed combustors.

1686. The method of claim 1679, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1687. The method of claim 1679, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1688. The method of claim 1679, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, A is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1689. The method of claim 1679, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1690. The method of claim 1679, wherein providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about

0.5 W/(m °C).

1691. The method of clahn 1679, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1692. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1693. The method of claim 1679, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about

0.15.

1694. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1695. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1696. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1697. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1698. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1699. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1700. The method of claim 1679, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1701. The method of claim 1679, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1702. The method of claim 1679, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1703. The method of claim 1679, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1704. The method of claim 1679, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1705. The method of claim 1679, further comprising controlling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1706. The method of claim 1705, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1707. The method of claim 1679, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1708. The method of claim 1679, further comprising controlling foπnation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1709. The method of claim 1679, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1710. The method of claim 1679, further comprising: producing hydrogen and condensable hydrocarbons from the foπnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1711. The method of claim 1679, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1712. The method of claim 1679, wherein allowing the heat to fransfer further comprises substantially uniformly increasing a permeability of a majority of the selected section.

1713. The method of claim 1679, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1714. The method of clahn 1713, wherein at least about 20 heat sources are disposed in the formation for each production well.

1715. The method of claim 1679, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1716. The method of claim 1679, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1717. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to transfer from the one or more heat sources to a selected section of the foπnation; wherein the selected section is heated in a reducing environment during at least a portion of the time that the selected section is being heated; and producing a mixture from the formation.

1718. The method of claim 1717, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foπnation.

1719. The method of claim 1717, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1720. The method of claim 1717, wherein the one or more heat sources comprise electrical heaters.

1721. The method of claim 1717, wherein the one or more heat sources comprise surface burners.

1722. The method of claim 1717, wherein the one or more heat sources comprise flameless disfributed combustors.

1723. The method of claim 1717, wherein the one or more heat sources comprise natural disfributed combustors.

1724. The method of claim 1717, further comprising confrolling a pressure and a temperature withhi at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

1725. The method of claim 1717, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1726. The method of claim 1717, wherein providing heat from the one or more heat sources to at least the portion of foimation comprises: heating a selected volume ( V) of the relatively low permeability foπnation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1727. The method of claim 1717, wherein allowing the heat to ttansfer comprises fransfening heat substantially by conduction.

1728. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1729. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1730. The method of claim 1717, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1731. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1732. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1733. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1734. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1735. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1736. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1737. The method of claim 1717, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1738. The method of claim 1717, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1739. The method of claim 1717, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1740. The method of claim 1717, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1741. The method of claim 1717, further comprising controlling a pressure within at least a maj ority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1742. The method of claim 1717, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1743. The method of claim 1742, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1744. The method of claim 1717, further comprising altering a pressure within the fonnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1745. The method of claim 1717, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1746. The method of claim 1717, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1747. The method of claim 1717, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1748. The method of claim 1717, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

1749. The method of claim 1748, wherein at least about 20 heat sources are disposed in the formation for each production well.

1750. The method of claim 1717, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1751. The method of claim 1717, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

1752. A method of freating a relatively low permeability foimation containing heavy hydrocarbons in situ, comprising: heating a first section of the formation to produce a mixture from the foπnation; heating a second section of the formation; and recirculating a portion of the produced mixture from the first section into the second section of the foimation to provide a reducing environment within the second section of the formation.

1753. The method of claim 1752, further comprising maintaining a temperature within the first section or the second section within a pyrolysis temperature range.

1754. The method of claim 1752, wherein heating the first or the second section comprises heating with an electrical heater.

1755. The method of claim 1752, wherein heating the first or the second section comprises heating with a surface burner.

1756. The method of claim 1752, wherein heating the first or the second section comprises heating with a flameless distributed combustor.

1757. The method of claim 1752, wherein heating the first or the second section comprises heating with a natural disfributed combustor.

1758.^' The method of claim 1752, further comprising controlling a pressure and a temperature within at least a majority of the first or second section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1759. The method of claim 1752, further comprising controlling the heat such that an average heating rate of the first or the second section is less than about 1 °C per day during pyrolysis.

1760. The method of claim 1752, wherein heating the first or the second section comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from one or more heat sources, wherein the foπnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1761. The method of claim 1752, wherein heating the first or the second section comprises fransfening heat substantially by conduction.

1762. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1763. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1764. The method of claim 1752, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1765. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1766. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1767. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1768. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1769. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1770. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1771. The method of claim 1752, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1772. The method of claim 1752, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1773. The method of claim 1752, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1774. The method of claim 1752, wherein the produced mixture comprises ammonia, and wherehi the ammonia is used to produce fertilizer.

1775. The method of claim 1752, further comprising confrolling a pressure within at least a majority of the first or second section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1776. The method of claim 1752, further comprising controlling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1777. The method of claim 1776, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1778. The method of claim 1752, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foπnation having carbon numbers greater than about 25.

1779. The method of claim 1752, further comprising: providing hydrogen (H₂) to the first or second section to hydrogenate hydrocarbons within the ffrst or second section; and heating a portion of the first or second section with heat from hydrogenation.

1780. The method of claim 1752, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1781. The method of claim 1752, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1782. The method of claim 1781, wherein at least about 20 heat sources are disposed in the fonnation for each production well.

1783. The method of claim 1752, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1784. The method of claim 1752, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1785. A method of freating a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foπnation; and allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that a permeability of a majority of at least a portion of the selected section increases substantially uniformly.

1786. The method of claim 1785, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foimation.

1787. The method of claim 1785, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1788. The method of claim 1785, wherein the one or more heat sources comprise electrical heaters.

1789. The method of claim 1785, wherein the one or more heat sources comprise surface burners.

1790. The method of claim 1785, wherein the one or more heat sources comprise flameless disfributed combustors.

1791. The method of claim 1785, wherein the one or more heat sources comprise natural distributed combustors.

1792. The method of claim 1785, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a fimction of pressure.

1793. The method of claim 1785, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1794. The method of claim 1785, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volmne (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherehi heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1795. The method of claim 1785, wherein allowing the heat to ttansfer comprises fransfening heat substantially by conduction.

1796. The method of claim 1785, wherein providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

1797. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1798. The method of claim 1785, further comprismg producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1799. The method of clahn 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1800. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1801. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1802. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1803. The method of claim 1785, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1804. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1805. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1806. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1807. The method of claim 1785, further comprising producing a mixture from the foimation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1808. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1809. The method of claim 1785, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1810. The method of claim 1785, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1811. The method of claim 1785, further comprising confrolling formation conditions to produce a mixture from the formation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1812. The method of claim 1785, further comprising producing a mixture from the foπnation, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well. ^'

1813. The method of claim 1785, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1814. The method of claim 1785, further comprising producing a mixture from the formation and controlling foimation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1815. The method of claim 1785, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1816. The method of claim 1785, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1817. The method of claim 1785, wherein allowing the heat to ttansfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1818. The method of claim 1785, further comprising producing a mixture in a production well, wherein at least about 7 heat sources are disposed in the foπnation for each production well.

1819. The method of claim 1818, wherein at least about 20 heat sources are disposed in the formation for each production well.

1820. The method of claim 1785, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1821. The method of clahn 1785, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1822. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the fonnation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and confrolling the heat to yield at least about 15 % by weight of a total organic carbon content of at least some of the relatively low permeability formation containing heavy hydrocarbons into condensable hydrocarbons.

1823. The method of claim 1822, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1824. The method of claim 1822, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1825. The method of claim 1822, wherein the one or more heat sources comprise electrical heaters.

1826. The method of claim 1822, wherein the one or more heat sources comprise surface burners.

1827. The method of claim 1822, wherein the one or more heat sources comprise flameless disfributed combustors.

1828. The method of clahn 1822, wherein the one pr more heat sources comprise natural distributed combustors.

1829. The method of claim 1822, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1830. The method of claim 1822, further comprising controlling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1831. The method of claim 1822, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heatmg pyrolyzes at least some hydrocarbons within the selected volume of the fonnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1832. The method of claim 1822, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

1833. The method of claim 1822, wherein providing heat from the one or more heat sources comprises heating the selected section such that a thermal conductivity of at least a portion of the selected section is greater than about 0.5 W/(m °C).

1834. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1835. The method of claim 1822, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1836. The method of claim 1822, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1837. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1838. The method of claim 1822, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1839. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1840. The method of claim 1822, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1841. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1842. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1843. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1844. The method of claim 1822, further comprising producing a mixture from the fonnation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1845. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1846. The method of claim 1822, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherehi the ammonia is used to produce fertilizer.

1847. The method of claim 1822, further comprising confrolling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1848. The method of claim 1822, further comprising confrolling formation conditions to produce a mixture from the formation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1849. The method of claim 1822, further comprising producing a mixture from the formation, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1850. The method of claim 1822, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1851. The method of claim 1822, further comprising producing a mixture from the formation and controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1852. The method of claim 1822, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1853. The method of claim 1822, further comprismg: producing hydrogen and condensable hydrocarbons from the foπnation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1854. The method of claim 1822, wherein allowing the heat to fransfer comprises increasing a permeability of a majority of the selected section to greater than about 100 millidarcy.

1855. The method of clahn 1822, wherein allowing the heat to fransfer comprises substantially uniformly increasing a permeability of a majority of the selected section.

1856. The method of claim 1822, further comprismg producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the foπnation for each production well.

1857. The method of claim 1856, wherein at least about 20 heat sources are disposed in the formation for each production well.

1858. The method of claim 1822, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1859. The method of claim 1822, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1860. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and confrolling the heat to yield greater than about 60 % by weight of hydrocarbons.

1861. The method of claim 1860, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

1862. The method of claim 1860, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1863. The method of claim 1860, wherein the one or more heat sources comprise electrical heaters.

1864. The method of claim 1860, wherein the one or more heat sources comprise surface burners.

1865. The method of claim 1860, wherein the one or more heat sources comprise flameless distributed combustors.

1866. The method of claim 1860, wherein the one or more heat sources comprise natural disfributed combustors.

1867. The method of claim 1860, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1868. The method of clahn 1860, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1869. The method of claim 1860, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (F) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherem heating energy/day provided to the volmne is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1870. The method of claim 1860, wherein allowing the heat to transfer comprises fransfening heat substantially by conduction.

1871. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1872. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1873. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1874. The method of claim 1860, further comprismg producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1875. The method of claim 1860, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1876. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1877. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1878. The method of claim 1860, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1879. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1880. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1881. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1882. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1883. The method of claim 1860, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1884. The method of claim 1860, further comprising controlling a pressure within at least a majority of the selected section of the foπnation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1885. The method of claim 1860, further comprising confrolling fonnation conditions to produce a mixture from the formation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1886. The method of claim 1860, further comprising producing a mixture from the formation, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1887. The method of claim 1860, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1888. The method of claim 1860, further comprising producing a mixture from the formation and controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

1889. The method of claim 1860, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1890. The method of claim 1860, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1891. The method of claim 1860, further comprising producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1892. The method of claim 1891 , wherein at least about 20 heat sources are disposed in the formation for each production well.

1893. The method of claim 1860, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

1894. The method of clahn 1860, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

1895. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: heating a first section of the formation to pyrolyze at least some hydrocarbons in the first section and produce a first mixture from the formation; heating a second section of the formation to pyrolyze at least some hydrocarbons in the second section and produce a second mixture from the formation; and leaving an unpyrolyzed section between the first section and the second section to inhibit subsidence of the formation.

1896. The method of claim 1895, further comprising mahitaining a temperature within the first section or the second section within a pyrolysis temperature range.

1897. The method of claim 1895, wherein heating the first section or heating the second section comprises heating with an electrical heater.

1898. The method of claim 1895, wherein heating the first section or heating the second section comprises heating with a surface burner.

1899. The method of claim 1895, wherein heating the first section or heating the second section comprises heating with a flameless disfributed combustor.

1900. The method of claim 1895, wherein heating the first section or heating the second section comprises heating with a natural distributed combustor.

1901. The method of claim 1895, further comprising confrolling a pressure and a temperature within at least a majority of the first or second section of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

1902. The method of claim 1895, further comprising controlling the heat such that an average heating rate of the first or second section is less than about 1 °C per day during pyrolysis.

1903. The method of clahn 1895, wherein heating the first section or heating the second section comprises: heating a selected volume (V) of the relatively low peπneability fonnation containing heavy hydrocarbons from one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1904. The method of claim 1895, wherein heating the first section or heating the second section comprises fransfening heat substantially by conduction.

1905. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1906. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1907. The method of claim 1895, wherein the first or second mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1908. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

1909. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1910. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1911. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1912. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1913. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1914. The method of claim 1895, wherein the first or second mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1915. The method of claim 1895, wherein the first or second mixture comprises a non-condensable component, and wherein the non-condensable component comprises hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable component and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1916. The method of claim 1895, wherein the ffrst or second mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the first or second mixture is ammonia.

1917. The method of clahn 1895, wherein the first or second mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1918. The method of claim 1895, further comprising controlling a pressure within at least a majority of the first or second section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

1919. The method of claim 1895, further comprising confrolling foπnation conditions to produce the first or second mixture, wherein a partial pressure of H₂ within the first or second mixture is greater than about 0.5 bars.

1920. The method of claim 1895, wherein a partial pressure of H₂ within the first or second mixture is measured when the first or second mixture is at a production well.

1921. The method of claim 1895, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1922. The method of claim 1895, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the first or second mixture into the formation.

1923. The method of claim 1895, further comprising: providing hydrogen (H₂) to the first or second section to hydrogenate hydrocarbons within the first or second section, respectively; and heating a portion of the first or second section, respectively, with heat from hydrogenation.

1924. The method of claim 1895, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1925. The method of claim 1895, wherein producing the first or second mixture comprises producing the first or second mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1926. The method of claim 1925, wherein at least about 20 heat sources are disposed in the formation for each production well.

1927. The method of claim 1895, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1928. The method of claim 1895, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the foπnation to form a repetitive pattern of units.

1929. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation through one or more production wells, wherein the heating is confrolled such that the mixture can be produced from the formation as a vapor, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1930. The method of claim 1929, wherein at least about 20 heat sources are disposed in the formation for each production well.

1931. The method of claim 1929, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foimation.

1932. The method of claim 1929, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

1933. The method of clahn 1929, wherein the one or more heat sources comprise elecfrical heaters.

1934. The method of claim 1929, wherein the one or more heat sources comprise surface burners.

1935. The method of claim 1929, wherein the one or more heat sources comprise flameless disfributed combustors.

1936. The method of claim 1929, wherein the one or more heat sources comprise natural distributed combustors.

1937. The method of claim 1929, further comprising controlling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

1938. The method of claim 1929, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

1939. The method of claim 1929, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherem the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foimation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is fonnation bulk density, and wherein the heating rate is less than about 10 °C/day.

1940. The method of claim 1929, wherein allowing the heat to transfer comprises transferring heat substantially by conduction.

1941. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1942. The method of clahn 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1943. The method of claim 1929, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about

0.15.

1944. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1945. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1946. The method of clahn 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1947. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1948. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

1949. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1950. The method of claim 1929, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1951. The method of claim 1929, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1952. The method of claim 1929, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1953. The method of claim 1929, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1954. The method of claim 1929, further comprising controlling a pressure within at least a majority of the selected section of the foπnation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1955. The method of claim 1929, further comprising controlling foimation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1956. The method of claim 1955, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

1957. The method of claim 1929, further comprising altering a pressure within the foπnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1958. The method of claim 1929, further comprising controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the fonnation.

1959. The method of claim 1929, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1960. The method of claim 1929, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1961. The method of claim 1929, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1962. The method of claim 1929, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1963. A method of treating a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation, wherein the one or more heat sources are disposed within one or more first wells; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation through one or more second wells, wherein one or more of the first or second wells are initially used for a first pmpose and are then used for one or more other puφoses.

1964. The method of claim 1963, wherein the first ptupose comprises removing water from the formation, and wherein the second pmpose comprises providing heat to the formation.

1965. The method of claim 1963, wherein the first pmpose comprises removing water from the formation, and wherein the second pmpose comprises producing the mixture.

1966. The method of claim 1963, wherein the first ptupose comprises heating, and wherein the second pmpose comprises removing water from the formation.

1967. The method of clahn 1963, wherein the first puφose comprises producing the mixture, and wherein the second puφose comprises removing water from the formation.

1968. The method of claim 1963, wherein the one or more heat sources comprise elecfrical heaters.

1969. The method of claim 1963, wherein the one or more heat sources comprise surface burners.

1970. The method of claim 1963, wherein the one or more heat sources comprise flameless distributed combustors.

1971. The method of claim 1963, wherein the one or more heat sources comprise natural disfributed combustors.

1972. The method of claim 1963, further comprismg controlling a pressure and a temperature within at least a majority of the selected section of the fonnation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

1973. The method of claim 1963, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1.0 ° C per day during pyrolysis.

1974. The method of claim 1963, wherein providing heat from the one or more heat sources to at least the portion of the formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

1975. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

1976. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

1977. The method of claim 1963, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

1978. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

1979. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

1980. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

1981. The method of claim 1963, wherehi the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

1982. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings. _«

1983. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

1984. The method of claim 1963, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

1985. The method of claim 1963, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

1986. The method of claim 1963, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

1987. The method of claim 1963, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

1988. The method of claim 1963, further comprising confrolling a pressure within at least a majority of the selected section of the foπnation, wherein the confrolled pressure is at least about 2.0 bars absolute.

1989. The method of claim 1963, further comprising confrolling formation conditions to produce a mixture of condensable hydrocarbons and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

1990. The method of claim 1989, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

1991. The method of claim 1963, further comprising altering a pressure within the foimation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

1992. The method of claim 1963, further comprising controlling formation conditions, wherein confrolling foπnation conditions comprises recirculating a portion ofhydrogen from the mixture into the formation.

1993. The method of claim 1963 , further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

1994. The method of claim 1963, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

1995. The method of claim 1963, wherein producing the mixture comprises producing the mixttire in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

1996. The method of claim 1995, wherein at least about 20 heat sources are disposed in the formation for each production well.

1997. The method of claim 1963, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

1998. The method of claim 1963, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

1999. A method for forming heater wells in a relatively low permeability foπnation containing heavy hydrocarbons, comprising: forming a first wellbore in the formation; forming a second wellbore in the formation using magnetic tracking such that the second wellbore is ananged substantially parallel to the first wellbore; and providing at least one heat source within the first wellbore and at least one heat source within the second wellbore such that the heat sources can provide heat to at least a portion of the formation.

2000. The method of claim 1999, wherein supeφosition of heat from the at least one heat source within the first wellbore and the at least one heat source within the second wellbore pyrolyzes at least some hydrocarbons within a selected section of the formation.

2001. The method of claim 1999, further comprising maintaining a temperature within a selected section within a pyrolysis temperature range.

2002. The method of claim 1999, wherein the heat sources comprise electrical heaters.

2003. The method of claim 1999, wherein the heat sources comprise surface burners.

2004. The method of claim 1999, wherein the heat sources comprise flameless distributed combustors.

2005. The method of claim 1999, wherein the heat sources comprise natural disfributed combustors.

2006. The method of claim 1999, further comprising confrolling a pressure and a temperature within at least a majority of a selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

2007. The method of clahn 1999, further comprising controlling the heat from the heat sources such that heat fransfened from the heat sources to at least the portion of the hydrocarbons is less than about 1 °C per day during pyrolysis.

2008. The method of claim 1999, further comprising: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy /day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is fonnation bulk density, and wherein the heating rate is less than about 10 °C/day.

2009. The method of claim 1999, further comprising allowing the heat to fransfer from the heat sources to at least the portion of the formation substantially by conduction.

2010. The method of clahn 1999, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2011. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2012. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2013. The method of claim 1999, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

2014. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2015. The method of claim 1999, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2016. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2017. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2018. The method of claim 1999, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2019. The method of claim 1999, further comprising producing a mixture from the formation, wherehi the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2020. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

2021. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2022. The method of claim 1999, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2023. The method of claim 1999, further comprising controlling a pressure within at least a maj ority of a selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

2024. The method of claim 2023, wherein the partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2025. The method of claim 1999, further comprising producing a mixture from the formation, wherein a partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2026. The method of claim 1999, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

2027. The method of claim 1999, further comprising producing a mixture from the formation and confrolling foπnation conditions by recirculating a portion ofhydrogen from the mixture mto the formation.

2028. The method of claim 1999, further comprising: providing hydrogen (H₂) to the portion to hydrogenate hydrocarbons within the formation; and heating a portion of the formation with heat from hydrogenation.

2029. The method of claim 1999, further comprising: producing hydrogen and condensable hydrocarbons from the foimation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2030. The method of claim 1999, further comprising producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

2031. The method of claim 2030, wherein at least about 20 heat sources are disposed in the formation for each production well.

2032. The method of clahn 1999, further comprising forming a production well in the foπnation using magnetic tracking such that the production well is substantially parallel to the first wellbore and coupling a wellhead to the thfrd wellbore.

2033. The method of clahn 1999, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

2034. The method of claim 1999, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

2035. A method for installing a heater well into a relatively low permeability formation containing heavy hydrocarbons, comprising: forming a bore in the ground using a steerable motor and an accelerometer; and providing a heat source within the bore such that the heat source can fransfer heat to at least a portion of the foπnation.

2036. The method of clahn 2035, further comprising installing at least two heater wells, and wherein supeφosition of heat from at least the two heater wells pyrolyzes at least some hydrocarbons within a selected section of the formation.

2037. The method of claim 2035, further comprising maintaining a temperature within a selected section within a pyrolysis temperature range.

2038. The method of claim 2035, wherein the heat source comprises an elecfrical heater.

2039. The method of clahn 2035, wherein the heat source comprises a surface burner.

2040. The method of claim 2035, wherein the heat source comprises a flameless distributed combustor.

2041. The method of clahn 2035, wherein the heat source comprises a natural distributed combustor.

2042. The method of clahn 2035, further comprising confrolling a pressure and a temperature within at least a majority of a selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

2043. The method of claim 2035, further comprising controlling the heat from the heat source such that heat fransfened from the heat source to at least the portion of the formation is less than about 1 °C per day during pyrolysis.

2044. The method of claim 2035, further comprising: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the heat source, wherein the formation has an average heat capacity (C_v), and wherehi the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

2045. The method of claim 2035, further comprising allowing the heat to fransfer from the heat source to at least the portion of the formation substantially by conduction.

2046. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2047. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2048. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2049. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

2050. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2051. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2052. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2053. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2054. The method of claim 2035, further comprising producing a mixture from the foimation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2055. The method of clahn 2035, furtlier comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2056. The method of claim 2035, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

2057. The method of clahn 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2058. The method of claim 2035, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2059. The method of claim 2035, further comprising confrolling a pressure within at least a majority of a selected section of the fonnation, wherein the confrolled pressure is at least about 2.0 bars absolute.

2060. The method of claim 2035, further comprising confrolling formation conditions to produce a mixture from the foimation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2061. The method of claim 2060, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2062. The method of claim 2035, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

2063. The method of claim 2035, further comprising producing a mixture from the formation and controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the foπnation.

2064. The method of claim 2035, further comprising: providing hydrogen (H₂) to the at least the heated portion to hydrogenate hydrocarbons within the formation; and heating a portion of the formation with heat from hydrogenation.

2065. The method of claim 2035, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2066. The method of claim 2035, further comprising producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the fonnation for each production well.

2067. The method of claim 2066, wherein at least about 20 heat sources are disposed in the formation for each production well.

2068. The method of claim 2035, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

2069. The method of claim 2035, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

2070. A method for installing of wells in a relatively low permeability formation containing heavy hydrocarbons, comprising: forming a wellbore in the formation by geosteered drilling; and providing a heat source within the wellbore such that the heat source can fransfer heat to at least a portion of the formation.

2071. The method of claim 2070, further comprising maintaining a temperature within a selected section within a pyrolysis temperature range.

2072. The method of claim 2070, wherein the heat source comprises an elecfrical heater.

2073. The method of clahn 2070, wherein the heat source comprises a surface burner.

2074. The method of claim 2070, wherein the heat source comprises a flameless disfributed combustor.

2075. The method of claim 2070, wherein the heat source comprises a natural distributed combustor.

2076. The method of claim 2070, further comprising controlling a pressure and a temperature within at least a majority of a selected section of the foimation, wherein the pressure is confrolled as a function of temperature, or the temperature is controlled as a function of pressure.

2077. The method of claim 2070, further comprising confrolling the heat from the heat source such that heat fransfened from the heat source to at least the portion of the foπnation is less than about 1 °C per day during pyrolysis.

2078. The method of claim 2070, further comprising: heating a selected volume (V) of the relatively low peπneability formation containing heavy hydrocarbons from the heat source, wherem the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

2079. The method of claim 2070, further comprising allowing the heat to fransfer from the heat source to at least the portion of the formation substantially by conduction.

2080. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2081. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2082. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2083. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

2084. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2085. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2086. The method of clahn 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2087. The method of claim 2070, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2088. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2089. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2090. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

2091. The method of claim 2070, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2092. The method of claim 2070, further comprising producing a mixture from the formation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2093. The method of claim 2070, further comprising confrolling a pressure within at least a majority of a selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

2094. The method of claim 2070, further comprising controlling foimation conditions to produce a mixture from the formation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2095. The method of claim 2094, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2096. The method of claim 2070, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the foimation having carbon numbers greater than about 25.

2097. The method of claim 2070, further comprising producing a mixture from the formation and confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the foπnation.

2098. The method of claim 2070, further comprising: providing hydrogen (H₂) to at least the heated portion to hydrogenate hydrocarbons within the foπnation; and heating a portion of the formation with heat from hydrogenation.

2099. The method of claim 2070, further comprising: producing hydrogen and condensable hydrocarbons from the foimation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2100. The method of claim 2070, further comprising producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

2101. The method of claim 2100, wherein at least about 20 heat sources are disposed in the formation for each production well.

2102. The method of claim 2070, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

2103. The method of claim 2070, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the foimation to form a repetitive pattern of units.

2104. A method of freating a relatively low permeability foimation containing heavy hydrocarbons in situ, comprising: heating a selected section of the formation with a heating element placed within a wellbore, wherein at least one end of the heating element is free to move axially within the wellbore to allow for thermal expansion of the heating element.

2105. The method of claim 2104, further comprising at least two heating elements within at least two wellbores, and wherein supeφosition of heat from at least the two heating elements pyrolyzes at least some hydrocarbons within a selected section of the formation.

2106. The method of claim 2104, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

2107. The method of claim 2104, wherein the heating element comprises a pipe-in-pipe heater.

2108. The method of claim 2104, wherein the heating element comprises a flameless distributed combustor.

2109. The method of claim 2104, wherein the heating element comprises a mineral insulated cable coupled to a support, and wherein the support is free to move within the wellbore.

2110. The method of claim 2104, wherein the heating element comprises a mineral insulated cable suspended from a wellhead.

2111. The method of clahn 2104, further comprising confrolling a pressure and a temperature within at least a majority of a heated section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

2112. The method of claim 2104, further comprising controlling the heat such that an average heating rate of the heated section is less than about 1 °C per day during pyrolysis.

2113. The method of claim 2104, wherein heating the section of the formation further comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the heating element, wherein the fonnation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the foπnation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

2114. The method of claim 2104, wherein heating the section of the formation comprises fransfening heat substantially by conduction.

2115. The method of clahn 2104, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2116. The method of claim 2104, further comprising producing a mixture from the fonnation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2117. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2118. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

2119. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2120. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2121. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2122. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2123. The method of claim 2104, further comprising producing a mixture from the formation, wherehi the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2124. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2125. The method of claim 2104, further comprising producing a mixture from the formation, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

2126. The method of claim 2104, further comprising producing a mixture from the fonnation, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2127. The method of claim 2104, further comprising producing a mixture from the foπnation, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2128. The method of claim 2104, further comprising confrolling a pressure within the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

2129. The method of claim 2104, further comprising confrolling formation conditions to produce a mixture from the formation, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2130. The method of claim 2129, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2131. The method of claim 2104, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

2132. The method of claim 2104, further comprising producing a mixture from the formation and confrolling foimation conditions by recirculating a portion ofhydrogen from the mixture into the formation.

2133. The method of claim 2104, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the heated section; and heating a portion of the section with heat from hydrogenation.

2134. The method of claim 2104, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2135. The method of claim 2104, further comprising producing a mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

2136. The method of claim 2135, wherein at least about 20 heat sources are disposed in the fonnation for each production well.

2137. The method of claim 2104, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

2138. The method of claim 2104, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

2139. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the foimation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation through a production well, wherein the production well is located such that a majority of the mixture produced from the formation comprises non-condensable hydrocarbons and a non-condensable component comprising hydrogen.

2140. The method of claim 2139, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

2141. The method of claim 2139, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

2142. The method of claim 2139, wherein the production well is less than approximately 6 m from a heat source of the one or more heat sources.

2143. The method of claim 2139, wherein the production well is less than approximately 3 m from a heat source of the one or more heat sources.

2144. The method of claim 2139, wherein the production well is less than approxhnately 1.5 m from a heat source of the one or more heat sources.

2145. The method of claim 2139, wherein an additional heat source is positioned within a wellbore of the production well.

2146. The method of claim 2139, wherein the one or more heat sources comprise electrical heaters.

2147. The method of claim 2139, wherein the one or more heat sources comprise surface burners.

2148. The method of claim 2139, wherein the one or more heat sources comprise flameless disfributed combustors.

2149. The method of claim 2139, wherein the one or more heat sources comprise natural distributed combustors.

2150. The method of claim 2139, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

2151. The method of claim 2139, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

2152. The method of claim 2139, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation: Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foimation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

2153. The method of claim 2139, wherein allowing the heat to fransfer from the one or more heat sources to the selected section comprises fransfening heat substantially by conduction.

2154. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2155. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2156. The method of claim 2139, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2157. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

2158. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2159. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2160. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2161. The method of clahn 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2162. The method of claim 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2163. The method of clahn 2139, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2164. The method of claim 2139, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

2165. The method of claim 2139, wherehi the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2166. The method of claim 2139, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2167. The method of claim 2139, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

2168. The method of claim 2139, further comprising controlling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2169. The method of claim 2168, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2170. The method of claim 2139, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

2171. The method of claim 2139, further comprishig confrolling fonnation conditions by recfrculatmg a portion of the hydrogen from the mixture into the formation.

2172. The method of claim 2139, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

2173. The method of claim 2139, further comprising: producing condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2174. The method of clahn 2139, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

2175. The method of claim 2174, wherein at least about 20 heat sources are disposed in the fonnation for each production well.

2176. The method of claim 2139, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

2177. The method of claim 2139, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

2178. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat to at least a portion of the formation from one or more first heat sources placed within a pattern in the formation; allowing the heat to fransfer from the one or more first heat sources to a first section of the formation; heating a second section of the foπnation with at least one second heat source, wherein the second section is located within the first section, and wherein at least the one second heat source is configured to raise an average temperature of a portion of the second section to a higher temperature than an average temperature of the first section; and producing a mixture from the foπnation through a production well positioned within the second section, wherein a majority of the produced mixture comprises non-condensable hydrocarbons and a non-condensable component comprising H₂ components.

2179. The method of claim 2178, wherehi the one or more ffrst heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the first section of the formation.

2180. The method of claim 2178, further comprising maintaining a temperature within the first section within a pyrolysis temperature range.

2181. The method of claim 2178, wherein at least the one heat source comprises a heater element positioned within the production well.

2182. The method of claim 2178, wherein at least the one second heat source comprises an electrical heater.

2183. The method of claim 2178, wherein at least the one second heat source comprises a surface burner.

2184. The method of claim 2178, wherein at least the one second heat source comprises a flameless disfributed combustor.

2185. The method of claim 2178, wherein at least the one second heat source comprises a natural distributed combustor.

2186. The method of claim 2178, further comprising confrolling a pressure and a temperature within at least a majority of the first or the second section of the formation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

2187. The method of clahn 2178, further comprising confrolling the heat such that an average heating rate of the first section is less than about 1 °C per day during pyrolysis.

2188. The method of claim 2178, wherein providing heat to the formation further comprises: heating a selected volume (I⁷) of the relatively low penneability formation containing heavy hydrocarbons from the one or more first heat sources, wherein the foπnation has an average heat capacity (C„), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volmne is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

2189. The method of claim 2178, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

2190. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2191. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2192. The method of clahn 2178, wherem a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2193. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

«

2194. The method of clahn 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2195. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2196. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2197. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2198. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2199. The method of claim 2178, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2200. The method of claim 2178, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherehi the hydrogen is less than about 80 % by volume of the non-condensable component.

2201. The method of claim 2178, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2202. The method of claim 2178, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2203. The method of claim 2178, further comprising confrolling a pressure within at least a majority of the first or the second section of the foπnation, wherein the confrolled pressure is at least about 2.0 bars absolute.

2204. The method of claim 2178, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2205. The method of claim 2204, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2206. The method of claim 2178, further comprising altering a pressure within the fonnation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

2207. The method of claim 2178, further comprising confrolling formation conditions by recirculating a portion ofhydrogen from the mixture into the foπnation.

2208. The method of claim 2178, further comprising: providing hydrogen (H₂) to the first or second section to hydrogenate hydrocarbons within the first or second section, respectively; and heating a portion of the ffrst or second section, respectively, with heat from hydrogenation.

2209. The method of claim 2178, further comprising: producing condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2210. The method of clahn 2178, wherein at least about 7 heat sources are disposed in the formation for each production well.

2211. The method of claim 2210, wherein at least about 20 heat sources are disposed in the foπnation for each production well.

2212. The method of claim 2178, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a ttiangular pattern.

2213. The method of claim 2178, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

2214. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat into the foπnation from a plurality of heat sources placed in a pattern within the formation, wherein a spacing between heat sources is greater than about 6 m; allowing the heat to transfer from the plurality of heat sources to a selected section of the formation; producing a mixture from the formation from a plurality of production wells, wherein the plurality of production wells are positioned within the pattern, and wherein a spacing between production wells is greater than about 12 m.

2215. The method of claim 2214, wherein supeφosition of heat from the plurality of heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

2216. The method of claim 2214, further comprising maintaining a temperature within the selected section within a pyrolysis temperature range.

2217. The method of claim 2214, wherein the plurality of heat sources comprises elecfrical heaters.

2218. The method of claim 2214, wherein the plurality of heat sources comprises surface burners.

2219. The method of claim 2214, wherein the plurality of heat sources comprises flameless disfributed combustors.

2220. The method of claim 2214, wherein the plurality of heat sources comprises natural disfributed combustors.

2221. The method of claim 2214, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the formation, wherein the pressure is confrolled as a function of temperature, or the temperature is confrolled as a function of pressure.

2222. The method of claim 2214, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

2223. The method of claim 2214, wherein providing heat from the plurality of heat sources comprises: heating a selected volume (V) of the relatively low permeability foπnation containing heavy hydrocarbons from the plurality of heat sources, wherein the fonnation has an ayerage heat capacity (C_v), and wherein the heating pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is foimation bulk density, and wherein the heating rate is less than about 10 °C/day.

2224. The method of claim 2214, wherein allowing the heat to fransfer comprises fransfening heat substantially by conduction.

2225. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

2226. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherehi about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

2227. The method of claim 2214, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

2228. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

2229. The method of claim 2214, wherein the produced mixttire comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

2230. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

2231. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

2232. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

2233. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

2234. The method of claim 2214, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

2235. The method of claim 2214, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

2236. The method of claim 2214, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

2237. The method of claim 2214, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

2238. The method of claim 2214, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the confrolled pressure is at least about 2.0 bars absolute.

2239. The method of claim 2214, further comprising confrolling formation conditions to produce the mixture, wherein a partial pressure of H₂ within the mixture is greater than about 0.5 bars.

2240. The method of claim 2239, wherein the partial pressure of H₂ within the mixture is measured when the mixture is at a production well.

2241. The method of clahn 2214, further comprising altering a pressure within the foimation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

2242. The method of claim 2214, further comprismg confrolling formation conditions by recirculating a portion of hydrogen from the mixture into the formation.

2243. The method of claim 2214, further comprising: providing hydrogen (H₂) to the selected section to hydrogenate hydrocarbons within the selected section; and heating a portion of the selected section with heat from hydrogenation.

2244. The method of claim 2214, further comprising: producing hydrogen and condensable hydrocarbons from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

2245. The method of clahn 2214, wherein at least about 7 heat sources are disposed in the formation for each production well.

2246. The method of claim 2245, wherein at least about 20 heat sources are disposed in the formation for each production well.

2247. The method of claim 2214, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

2248. The method of claim 2214, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

2249. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a heater disposed in an opening in the formation, wherein the heater is configured to provide heat to at least a portion of the foimation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to transfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2250. The system of claim 2249, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2251. The system of claim 2249, wherein the conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2252. The system of claim 2249, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configured to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2253. The system of claim 2249, wherein the conduit is further configured to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2254. The system of claim 2249, wherein the conduit is further configured to remove an oxidation product.

2255. The system of claim 2249, wherein the conduit is further configured to remove an oxidation product such that the oxidation product transfers substantial heat to the oxidizing fluid.

2256. The system of claim 2249, wherein the conduit is further configured to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2257. The system of claim 2249, wherein the conduit is further configured to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are controlled to reduce contamination of the oxidation product by the oxidizing fluid.

2258. The system of claim 2249, wherein the conduit is further configured to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2259. The system of claim 2249, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2260. The system of claim 2249, further comprising a center conduit disposed within the conduit, wherein the center conduit is configured to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configured to remove an oxidation product during use.

2261. The system of clahn 2249, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m. ■

2262. The system of claim 2249, further comprising a conductor disposed in a second conduit, wherein the second conduit is disposed within the opening, and wherein the conductor is configured to heat at least a portion of the formation during application of an electrical cunent to the conductor.

2263. The system of clahn 2249, further comprising an insulated conductor disposed within the opening, wherein the insulated conductor is configured to heat at least a portion of the formation during application of an elecfrical cunent to the insulated conductor.

2264. The system of claim 2249, further comprising at least one elongated member disposed within the opening, wherein the at least the one elongated member is configured to heat at least a portion of the formation during application of an electrical cunent to the at least the one elongated member.

2265. The system of claim 2249, further comprising a heat exchanger disposed external to the formation, wherein the heat exchanger is configured to heat the oxidizing fluid, wherein the conduit is further configured to provide the heated oxidizing fluid into the openmg during use, and wherein the heated oxidizing fluid is configured to heat at least a portion of the formation during use.

2266. The system of claim 2249, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2267. The system of claim 2249, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing comprises steel.

2268. The system of claim 2249, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2269. The system of claim 2249, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2270. The system of claim 2249, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2271. The system of claim 2249, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2272. The system of claim 2249, wherein the system is further configured such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2273. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a heater configurable to be disposed in an opening in the formation, wherein the heater is further configurable to provide heat to at least a portion of the formation during use; a conduit configurable to be disposed in the opening, wherein the conduit is configurable to provide an oxidizing fluid from an oxidizing fluid source to a reaction zone in the formation during use, and wherein the system is configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is further configurable to allow heat to transfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2274. The system of claim 2273, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2275. The system of claim 2273, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2276. The system of clahn 2273, wherehi the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2277. The system of claim 2273, wherein the conduit is further configurable to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2278. The system of claim 2273, wherein the conduit is further configurable to remove an oxidation product.

2279. The system of claim 2273, wherein the conduit is further configurable to remove an oxidation product, such that the oxidation product fransfers heat to the oxidizing fluid.

2280. The system of claim 2273, wherein the conduit is further configurable to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approxhnately equal to a flow rate of the oxidation product in the conduit.

2281. The system of claim 2273, wherein the conduit is further configurable to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2282. The system of claim 2273, wherein the conduit is further configurable to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the fonnation beyond the reaction zone.

2283. The system of claim 2273, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2284. The system of claim 2273, further comprising a center conduit disposed within the conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configurable to remove an oxidation product during use.

2285. The system of claim 2273, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2286. The system of claim 2273, further comprising a conductor disposed in a second conduit, wherein the second conduit is disposed within the opening, and wherein the conductor is configurable to heat at least a portion of the foπnation during application of an elecfrical cunent to the conductor.

2287. The system of claim 2273, further comprising an insulated conductor disposed within the opening, wherein the insulated conductor is configurable to heat at least a portion of the fonnation during application of an electrical cunent to the insulated conductor.

2288. The system of claim 2273, further comprising at least one elongated member disposed withhi the opening, wherein the at least the one elongated member is configurable to heat at least a portion of the formation during application of an elecfrical cunent to the at least the one elongated member.

2289. The system of claim 2273, further comprising a heat exchanger disposed external to the formation, wherein the heat exchanger is configurable to heat the oxidizing fluid, wherein the conduit is further configurable to provide the heated oxidizing fluid into the opening during use, and wherein the heated oxidizing fluid is configurable to heat at least a portion of the formation during use.

2290. The system of claim 2273, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2291. The system of claim 2273, further comprising an overburden casing coupled to the opening, wherehi the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2292. The system of claim 2273, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2293. The system of clahn 2273, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2294. The system of clahn 2273, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2295. The system of claim 2273, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2296. The system of claim 2273, wherein the system is further configurable such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2297. The system of claim 2273, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a heater disposed in an opening in the foimation, wherein the heater is configured to provide heat to at least a portion of the foimation during use; r an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherehi the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to transfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2298. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons within the portion of the formation with an oxidizing fluid; providing the oxidizing fluid to a reaction zone in the formation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and fransfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the foπnation.

2299. The method of claim 2298, further comprising transporting the oxidizing fluid through the reaction zone by diffusion.

2300. The method of claim 2298, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

2301. The method of claim 2298, further comprising confrolling a flow of the oxidizing fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

2302. The method of claim 2298, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

2303. The method of claim 2298, wherein a conduit is disposed in the opening, the method further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

2304. The method of claim 2298, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit.

2305. The method of claim 2298, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foπnation through the conduit and fransfening heat from the oxidation product in the conduit to oxidizing fluid in the conduit.

2306. The method of claim 2298, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foπnation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2307. The method of claim 2298, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foπnation through the conduit and controlling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2308. The method of claim 2298, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2309. The method of claim 2298, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2310. The method of claim 2298, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

2311. The method of claim 2298, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2312. The method of claim 2298, wherein heating the portion comprises applying elecfrical cunent to a conductor disposed in a conduit, wherein the conduit is disposed within the opening.

2313. The method of claim 2298, wherein heating the portion comprises applying elecfrical cunent to an insulated conductor disposed within the opening.

2314. The method of claim 2298, wherein heating the portion comprises applying elecfrical cunent to at least one elongated member disposed within the opening.

2315. The method of claim 2298, wherein heating the portion comprises heatmg the oxidizing fluid in a heat exchanger disposed external to the fonnation such that providing the oxidizing fluid into the opening comprises fransfening heat from the heated oxidizing fluid to the portion.

2316. The method of claim 2298, further comprising removing water from the formation prior to heating the portion.

2317. The method of claim 2298, further comprising confrollmg the temperature of the formation to substantially inhibit production of oxides of nitrogen during oxidation.

2318. The method of claim 2298, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2319. The method of claim 2298, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2320. The method of claim 2298, further comprising coupling an overburden casing to the opening, wherehi the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2321. The method of claim 2298, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2322. The method of clahn 2298, wherein the pyrolysis zone is substantially adjacent to the reaction zone.

2323. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a heater disposed in an opening in the formation, wherein the heater is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizmg fluid from the oxidizing fluid source to a reaction zone in the formation during use, wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone, and wherein the conduit is further configured to remove an oxidation product from the formation during use; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2324. The system of claim 2323, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2325. The system of claim 2323, wherein the conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2326. The system of claim 2323, wherehi the conduit comprises critical flow orifices, and wherein the critical flow orifices are configured to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled.

2327. The system of claim 2323, wherein the conduit is further configured to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2328. The system of claim 2323, wherein the conduit is further configured such that the oxidation product fransfers heat to the oxidizing fluid.

2329. The system of clahn 2323, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2330. The system of claim 2323, wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are controlled to reduce contamination of the oxidation product by the oxidizing fluid.

2331. The system of claim 2323, wherehi the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2332. The system of claim 2323, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2333. The system of clahn 2323, further comprising a center conduit disposed within the conduit, wherein the center conduit is configured to provide the oxidizing fluid into the opening during use.

2334. The system of claim 2323, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2335. The system of claim 2323, further comprising a conductor disposed in a second conduit, wherein the second conduit is disposed within the opening, and wherein the conductor is configured to heat at least a portion of the foimation during application of an elecfrical cunent to the conductor.

2336. The system of claim 2323, further comprising an insulated conductor disposed within the opening, wherein the insulated conductor is configured to heat at least a portion of the formation during application of an elecfrical cunent to the insulated conductor.

2337. The system of claim 2323, further comprising at least one elongated member disposed within the opening, wherein the at least the one elongated member is configured to heat at least a portion of the formation during application of an elecfrical cunent to the at least the one elongated member.

2338. The system of claim 2323, further comprising a heat exchanger disposed external to the formation, wherehi the heat exchanger is configured to heat the oxidizing fluid, wherein the conduit is further configured to provide the heated oxidizing fluid into the opening during use, and wherein the heated oxidizing fluid is configured to heat at least a portion of the foimation during use.

2339. The system of claim 2323, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2340. The system of claim 2323, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2341. The system of claim 2323, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2342. The system of claim 2323, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2343. The system of claim 2323, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherem a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2344. The system of claim 2323, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2345. The system of claim 2323, wherein the system is further configured such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2346. A system configurable to heat a relatively low penneability formation containing heavy hydrocarbons, comprising: a heater configurable to be disposed in an opening in the fonnation, wherein the heater is further configurable to provide heat to at least a portion of the formation during use; a conduit configurable to be disposed in the opening, wherein the conduit is further configurable to provide an oxidizing fluid from an oxidizing fluid source to a reaction zone in the foπnation during use, wherehi the system is configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone, and wherein the conduit is further configurable to remove an oxidation product from the formation during use; and wherein the system is further configurable to allow heat to ttansfer substantially by conduction from the reaction zone to a pyrolysis zone during use.

2347. The system of claim 2346, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2348. The system of claim 2346, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2349. The system of claim 2346, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled.

2350. The system of claim 2346, wherein the conduit is further configurable to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2351. The system of claim 2346, wherein the conduit is further configurable such that the oxidation product transfers heat to the oxidizing fluid.

2352. The system of claim 2346, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2353. The system of claim 2346, wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2354. The system of claim 2346, wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2355. The system of claim 2346, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2356. The system of claim 2346, further comprising a center conduit disposed within the conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use.

2357. The system of claim 2346, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2358. The system of claim 2346, further comprising a conductor disposed in a second conduit, wherein the second conduit is disposed within the opening, and wherein the conductor is configurable to heat at least a portion of the foπnation during application of an electrical cunent to the conductor.

2359. The system of claim 2346, further comprising an insulated conductor disposed within the opening, wherein the insulated conductor is configurable to heat at least a portion of the formation during application of an electrical cunent to the insulated conductor.

2360. The system of claim 2346, further comprising at least one elongated member disposed within the opening, wherein the at least the one elongated member is configurable to heat at least a portion of the foπnation during application of an electrical cunent to the at least the one elongated member.

2361. The system of clahn 2346, further comprising a heat exchanger disposed external to the formation, wherein the heat exchanger is configurable to heat the oxidizing fluid, wherein the conduit is further configurable to provide the heated oxidizing fluid into the opening during use, and wherein the heated oxidizing fluid is configurable to heat at least a portion of the formation during use.

2362. The system of claim 2346, further comprismg an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2363. The system of claim 2346, further comprising an overburden casing coupled to the openmg, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing comprises steel.

2364. The system of claim 2346, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2365. The system of claim 2346, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2366. The system of claim 2346, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2367. The system of claim 2346, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2368. The system of claim 2346, wherein the system is further configurable such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2369. The system of claim 2346, wherein the system is configured to heat a relatively low permeability foimation containing heavy hydrocarbons, and wherein the system comprises: a heater disposed in an opening in the formation, wherein the heater is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the foπnation during use, wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone, and wherein the conduit is further configured to remove an oxidation product from the foimation during use; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2370. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons within the portion of the formation with an oxidizing fluid, wherein the portion is located substantially adjacent to an opening in the formation; providing the oxidizing fluid to a reaction zone in the formation; allowing the oxidizing gas to react with at least a portion of the hydrocarbons at the reaction zone to generate heat in the reaction zone; removing at least a portion of an oxidation product through the opening; and fransfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the foπnation.

2371. The method of claim 2370, further comprising transporting the oxidizing fluid through the reaction zone by diffusion.

2372. The method of claim 2370, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

2373. The method of claim 2370, further comprising controlling a flow of the oxidizhig fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

2374. The method of claim 2370, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially maintained within the reaction zone.

2375. The method of claim 2370, wherein a conduit is disposed in the opening, the method furtlier comprising cooling the conduit with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2376. The method of claim 2370, wherein a conduit is disposed within the opening, and wherein removing at least the portion of the oxidation product through the opening comprises removing at least the portion of the oxidation product tiirough the conduit.

2377. The method of claim 2370, wherein a conduit is disposed within the opening, and wherein removing at least the portion of the oxidation product through the opening comprises removing at least the portion of the oxidation product through the conduit, the method further comprising ttansfening substantial heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

2378. The method of claim 2370, wherein a conduit is disposed within the opening, wherein removing at least the portion of the oxidation product through the opening comprises removing at least the portion of the oxidation product through the conduit, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2379. The method of claim 2370, wherein a conduit is disposed within the opening, and wherein removing at least the portion of the oxidation product through the opening comprises removing at least the portion of the oxidation product through the conduit, the method further comprising confrolling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2380. The method of claim 2370, wherehi a conduit is disposed within the opening, and wherein removing at least the portion of the oxidation product through the opening comprises removing at least the portion of the oxidation product through the conduit, the method further comprising substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2381. The method of claim 2370, further comprishig substantially inhibiting the oxidizing fluid from flowing into portions of the foπnation beyond the reaction zone.

2382. The method of claim 2370, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizmg fluid into the opening through the center conduit and removing at least a portion of the oxidation product through the outer conduit.

2383. The method of claim 2370, wherein the portion of the formation extends radially from the openhig a width of less than approximately 0.2 m.

2384. The method of claim 2370, wherein heating the portion comprises applying elecfrical cunent to a conductor disposed in a conduit, wherein the conduit is disposed within the opening.

2385. The method of clahn 2370, wherein heating the portion comprises applying elecfrical cunent to an insulated conductor disposed within the opening.

2386. The method of claim 2370, wherein heating the portion comprises applying electrical cunent to at least one elongated member disposed within the opening.

2387. The method of claim 2370, wherein heating the portion comprises heating the oxidizing fluid in a heat exchanger disposed external to the formation such that providing the oxidizing fluid into the opening comprises fransfening heat from the heated oxidizing fluid to the portion.

2388. The method of claim 2370, further comprising removing water from the formation prior to heating the portion.

2389. The method of claim 2370, further comprising controlling the temperature of the formation to substantially inhibit production of oxides of nifrogen during oxidation.

2390. The method of claim 2370, further comprising coupling an overburden casing to the openhig, wherein the overburden casing is disposed in an overburden of the formation.

2391. The method of clahn 2370, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2392. The method of claim 2370, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2393. The method of claim 2370, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2394. The method of claim 2370, wherein the pyrolysis zone is substantially adjacent to the reaction.

2395. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: an electric heater disposed in an opening in the fonnation, wherein the elecfric heater is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2396. The system of claim 2395, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2397. The system of claim 2395, wherein the conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2398. The system of clahn 2395, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configured to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled.

2399. The system of claim 2395, wherein the conduit is further configured to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2400. The system of claim 2395, wherein the conduit is further configured to remove an oxidation product.

2401. The system of claim 2395, wherein the conduit is further configured to remove an oxidation product, such that the oxidation product fransfers heat to the oxidizing fluid.

2402. The system of claim 2395, wherein the conduit is further configured to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approxunately equal to a flow rate of the oxidation product in the conduit.

2403. The system of claim 2395, wherein the conduit is further configured to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2404. The system of claim 2395, wherein the conduit is further configured to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2405. The system of claim 2395, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2406. The system of claim 2395, further comprising a center conduit disposed within the conduit, wherein the center conduit is configured to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configured to remove an oxidation product during use.

2407. The system of claim 2395, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2408. The system of claim 2395, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2409. The system of claim 2395, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2410. The system of clahn 2395, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2411. The system of claim 2395, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2412. The system of claim 2395, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2413. The system of claim 2395, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2414. The system of claim 2395, wherein the system is further configured such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2415. A system configurable to heat a relatively low peπneability fonnation containing heavy hydrocarbons, comprising: an elecfric heater configurable to be disposed in an opening in the formation, wherein the elecfric heater is further configurable to provide heat to at least a portion of the formation during use, and wherein at least the portion is located substantially adjacent to the opening; a conduit configurable to be disposed in the opening, wherein the conduit is further configurable to provide an oxidizing fluid from an oxidizing fluid source to a reaction zone hi the formation during use, and wherein the system is configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is further configurable to allow heat to transfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2416. The system of claim 2415, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2417. The system of claim 2415, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2418. The system of claim 2415, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled.

2419. The system of claim 2415, wherein the conduit is further configurable to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2420. The system of claim 2415, wherein the conduit is further configurable to remove an oxidation product.

2421. The system of claim 2415, wherein the conduit is further configurable to remove an oxidation product such that the oxidation product fransfers heat to the oxidizing fluid.

2422. The system of clahn 2415, wherein the conduit is further configurable to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2423. The system of claim 2415, wherein the conduit is further configurable to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2424. The system of claim 2415, wherein the conduit is further configurable to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2425. The system of claim 2415, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2426. The system of claim 2415, further comprising a center conduit disposed within the conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configurable to remove an oxidation product during use.

2427. The system of claim 2415, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2428. The system of claim 2415, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2429. The system of claim 2415, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2430. The system of claim 2415, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed hi an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2431. The system of claim 2415, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2432. The system of claim 2415, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packhig material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2433. The system of claim 2415 , further comprishig an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2434. The system of claim 2415, wherein the system is further configurable such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2435. The system of claim 2415, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: an electric heater disposed in an opening in the foπnation, wherein the electric heater is configured to provide heat to at least a portion of the foimation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the foimation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2436. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a conductor disposed in a first conduit, wherein the first conduit is disposed in an opening in the formation, and wherein the conductor is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a second conduit disposed in the opening, wherein the second conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to transfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2437. The system of claim 2436, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2438. The system of claim 2436, wherein the second conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2439. The system of claim 2436, wherein the second conduit comprises critical flow orifices, and wherehi the critical flow orifices are configured to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2440. The system of claim 2436, wherein the second conduit is further configured to be cooled with the oxidizing fluid to reduce heating of the second conduit by oxidation.

2441. The system of claim 2436, wherein the second conduit is further configured to remove an oxidation product.

2442. The system of claim 2436, wherein the second conduit is further configured to remove an oxidation product such that the oxidation product fransfers heat to the oxidizing fluid.

2443. The system of claim 2436, wherein the second conduit is further configured to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the second conduit.

2444. The system of clahn 2436, wherein the second conduit is further configured to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the second conduit and a pressure of the oxidation product in the second conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2445. The system of claim 2436, wherehi the second conduit is further configured to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2446. The system of claim 2436, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2447. The system of claim 2436, further comprising a center conduit disposed within the second conduit, wherein the center conduit is configured to provide the oxidizing fluid into the opening during use, and wherein the second conduit is further configured to remove an oxidation product during use.

2448. The system of claim 2436, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2449. The system of claim 2436, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2450. The system of claim 2436, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2451. The system of claim 2436, further comprishig an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2452. The system of claim 2436, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2453. The system of claim 2436, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2454. The system of claim 2436, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2455. The system of claim 2436, wherein the system is further configured such that transfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2456. A system configurable to heat a relatively low peπneability fonnation containing heavy hydrocarbons, comprising: a conductor configurable to be disposed in a first conduit, wherein the first conduit is configurable to be disposed in an opening in the formation, and wherein the conductor is further configurable to provide heat to at least a portion of the foπnation during use; a second conduit configurable to be disposed in the opening, wherein the second conduit is further configurable to provide an oxidizing fluid from an oxidizing fluid source to a reaction zone in the foπnation during use, and wherein the system is configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is further configurable to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2457. The system of claim 2456, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2458. The system of claim 2456, wherein the second conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2459. The system of claim 2456, wherein the second conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2460. The system of claim 2456, wherein the second conduit is further configurable to be cooled with the oxidizing fluid to reduce heating of the second conduit by oxidation.

2461. The system of claim 2456, wherein the second conduit is further configurable to remove an oxidation product.

2462. The system of claim 2456, wherein the second conduit is further configurable to remove an oxidation product such that the oxidation product transfers heat to the oxidizing fluid.

2463. The system of clahn 2456, wherein the second conduit is further configurable to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the second conduit.

2464. The system of claim 2456, wherein the second conduit is further configurable to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the second conduit and a pressure of the oxidation product in the second conduit are controlled to reduce contamination of the oxidation product by the oxidizing fluid.

2465. The system of claim 2456, wherein the second conduit is further configurable to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2466. The system of claim 2456, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2467. The system of claim 2456, further comprismg a center conduit disposed within the second conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use, and wherein the second conduit is further configurable to remove an oxidation product during use.

2468. The system of claim 2456, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2469. The system of claim 2456, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2470. The system of claim 2456, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2471. The system of claim 2456, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed hi an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2472. The system of claim 2456, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2473. The system of claim 2456, furtlier comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2474. The system of claim 2456, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2475. The system of claim 2456, wherein the system is further configurable such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2476. The system of claim 2456, wherein the system is configured to heat a relatively low peπneability formation containing heavy hydrocarbons, and wherein the system comprises: a conductor disposed in a ffrst conduit, wherein the first conduit is disposed in an opening in the foimation, and wherein the conductor is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a second conduit disposed in the opening, wherein the second conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the foimation during use.

2477. An in situ method for heating a relatively low permeability fonnation containing heavy hydrocarbons, comprising: heating a portion of the foπnation to a temperature sufficient to support reaction of hydrocarbons within the portion of the fonnation with an oxidizing fluid, wherein heating comprises applying an elecfrical cunent to a conductor disposed in a first conduit to provide heat to the portion, and wherein the first conduit is disposed within the opening; providing the oxidizing fluid to a reaction zone in the foπnation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and fransfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the formation.

2478. The method of claim 2477, further comprising transporting the oxidizing fluid through the reaction zone by diffusion.

2479. The method of claim 2477, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a second conduit disposed in the opening.

2480. The method of claim 2477, furtlier comprishig controlling a flow of the oxidizing fluid with critical flow orifices of a second conduit disposed in the opening such that a rate of oxidation is controlled.

2481. The method of claim 2477, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over thne within the reaction zone.

2482. The method of claim 2477, wherein a second conduit is disposed in the opening, the method further comprising cooling the second conduit with the oxidizing fluid to reduce heating of the second conduit by oxidation.

2483. The method of claim 2477, wherein a second conduit is disposed within the opening, the method further comprising removing an oxidation product from the fonnation through the second conduit.

2484. The method of claim 2477, wherein a second conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation tiirough the second conduit and fransfening heat from the oxidation product in the conduit to the oxidizing fluid in the second conduit.

2485. The method of claim 2477, wherein a second conduit is disposed within the opening, the method further comprishig removing an oxidation product from the foimation through the second conduit, wherein a flow rate of the oxidizhig fluid in the second conduit is approximately equal to a flow rate of the oxidation product in the second conduit.

2486. The method of claim 2477, wherein a second conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the second conduit and confrolling a pressure between the oxidizing fluid and the oxidation product in the second conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2487. The method of claim 2477, wherein a second conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2488. The method of claim 2477, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2489. The method of claim 2477, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

2490. The method of claim 2477, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2491. The method of claim 2477, further comprising removing water from the formation prior to heating the portion.

2492. The method of claim 2477, further comprising confrolling the temperature of the formation to substantially inhibit production of oxides of nitrogen during oxidation.

2493. The method of claim 2477, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation.

2494. The method of claim 2477, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2495. The method of claim 2477, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2496. The method of claim 2477, further comprising coupling an overburden casing to the opening, wherehi a packing material is disposed at ajunction of the overburden casing and the opening.

2497. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: an insulated conductor disposed in an opening in the formation, wherein the insulated conductor is configured to provide heat to at least a portion of the formation during use; an oxidizhig fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2498. The system of claim 2497, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2499. The system of claim 2497, wherein the conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2500. The system of claim 2497, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configured to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2501. The system of claim 2497, wherein the conduit is configured to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2502. The system of claim 2497, wherein the conduit is further configured to remove an oxidation product.

2503. The system of claim 2497, wherein the conduit is further configured to remove an oxidation product, and wherein the conduit is further configured such that the oxidation product fransfers substantial heat to the oxidizing fluid.

2504. The system of claim 2497, wherein the conduit is further configured to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2505. The system of claim 2497, wherein the conduit is further configured to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the second conduit and a pressure of the oxidation product in the conduit are controlled to reduce contamination of the oxidation product by the oxidizing fluid.

2506. The system of claim 2497, wherein the conduit is further configured to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2507. The system of claim 2497, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2508. The system of claim 2497, further comprising a center conduit disposed within the conduit, wherehi the center conduit is configured to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configured to remove an oxidation product during use.

2509. The system of claim 2497, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2510. The system of claim 2497, furtlier comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation.

2511. The system of claim 2497, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2512. The system of claim 2497, further comprising an overburden casing coupled to the opening, wherehi the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

2513. The system of claim 2497, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2514. The system of claim 2497, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2515. The system of claim 2497, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2516. The system of clahn 2497, wherein the system is further configured such that transfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2517. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: an insulated conductor configurable to be disposed in an opening in the foπnation, wherein the insulated conductor is further configurable to provide heat to at least a portion of the foπnation during use; a conduit configurable to be disposed in the opening, wherein the conduit is further configurable to provide an oxidizing fluid from an oxidizing fluid source to a reaction zone in the formation during use, and wherein the system is configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is further configurable to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2518. The system of claim 2517, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2519. The system of claim 2517, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2520. The system of claim 2517, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled.

2521. The system of claim 2517, wherein the conduit is further configurable to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2522. The system of claim 2517, wherein the conduit is further configurable to remove an oxidation product.

2523. The system of claim 2517, wherein the conduit is further configurable to remove an oxidation product, such that the oxidation product transfers heat to the oxidizing fluid.

2524. The system of claim 2517, wherein the conduit is further configurable to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2525. The system of clahn 2517, wherein the conduit is further configurable to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2526. The system of claim 2517, wherein the conduit is further configurable to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2527. The system of claim 2517, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2528. The system of claim 2517, further comprising a center conduit disposed within the conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configurable to remove an oxidation product during use.

2529. The system of claim 2517, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2530. The system of claim 2517, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation.

2531. The system of claim 2517, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing comprises steel.

2532. The system of claim 2517, further comprismg an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2533. The system of claim 2517, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2534. The system of claim 2517, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherehi the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2535. The system of claim 2517, further comprismg an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2536. The system of claim 2517, wherein the system is further configurable such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2537. The system of claim 2517, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: an insulated conductor disposed in an opening in the formation, wherein the insulated conductor is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to transfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2538. An in situ method for heating a relatively low peπneability formation containing heavy hydrocarbons, comprising: heating a portion of the foimation to a temperature sufficient to support reaction of hydrocarbons within the portion of the foπnation with an oxidizing fluid, wherein heating comprises applying an electrical cunent to an insulated conductor to provide heat to the portion, and wherein the insulated conductor is disposed within the opening; providing the oxidizing fluid to a reaction zone in the foπnation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and fransfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the formation.

2539. The method of claim 2538, further comprising transporting the oxidizing fluid through the reaction zone by diffusion.

2540. The method of claim 2538, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

2541. The method of claim 2538, further comprising confrolling a flow of the oxidizing fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

2542. The method of claim 2538, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

2543. The method of clahn 2538, wherein a conduit is disposed in the opening, the method further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

2544. The method of claim 2538, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit.

2545. The method of claim 2538, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and fransfening heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

2546. The method of claim 2538, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2547. The method of claim 2538, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and controlling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2548. The method of claim 2538, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2549. The method of claim 2538, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2550. The method of claim 2538, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

2551. The method of claim 2538, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2552. The method of claim 2538, further comprising removing water from the formation prior to heating the portion.

2553. The method of claim 2538, further comprising controlling the temperature of the formation to substantially inhibit production of oxides of nitrogen during oxidation.

2554. The method of clahn 2538, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2555. The method of clahn 2538, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2556. The method of claim 2538, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2557. The method of claim 2538, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2558. The method of claim 2538, wherein the pyrolysis zone is substantially adjacent to the reaction zone.

2559. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the foπnation to a temperature sufficient to support reaction of hydrocarbons within the portion of the foπnation with an oxidizing fluid, wherein the portion is located substantially adjacent to an opening in the foπnation, wherein heating comprises applying an electrical cunent to an insulated conductor to provide heat to the portion, wherein the insulated conductor is coupled to a conduit, wherein the conduit comprises critical flow orifices, and wherein the conduit is disposed within the opening; providing the oxidizing fluid to a reaction zone in the formation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and fransfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the formation.

2560. The method of claim 2559, further comprising transporting the oxidizing fluid through the reaction zone by diffusion.

2561. The method of claim 2559, further comprising confrolling a flow of the oxidizing fluid with the critical flow orifices such that a rate of oxidation is controlled.

2562. The method of claim 2559, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

2563. The method of claim 2559, further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

2564. The method of clahn 2559, further comprising removing an oxidation product from the formation through the conduit.

2565. The method of claim 2559, further comprising removing an oxidation product from the formation through the conduit and fransfening heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

2566. The method of claim 2559, further comprising removing an oxidation product from the formation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2567. The method of claim 2559, further comprising removing an oxidation product from the formation through the conduit and confrolling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2568. The method of claim 2559, fuither comprising removing an oxidation product from the formation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2569. The method of claim 2559, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2570. The method of clahn 2559, wherein a center conduit is disposed within the conduit, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the conduit.

2571. The method of claim 2559, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2572. The method of claim 2559, further comprising removing water from the formation prior to heating the portion.

2573. The method of claim 2559, further comprising confrolling the temperature of the foimation to substantially inhibit production of oxides of nifrogen during oxidation.

2574. The method of claim 2559, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2575. The method of clahn 2559, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2576. The method of claim 2559, further comprising coupling an overburden casing to the openhig, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2577. The method of clahn 2559, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2578. The method of claim 2559, wherein the pyrolysis zone is substantially adjacent to the reaction zone.

2579. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: at least one elongated member disposed in an opening in the foπnation, wherein at least the one elongated member is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2580. The system of claim 2579, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2581. The system ofclaim 2579, wherein the conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2582. The system ofclaim 2579, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configured to control a flow of the oxidizing fluid such that a rate of oxidation in the foπnation is controlled.

2583. The system ofclaim 2579, wherein the conduit is further configured to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2584. The system of claim 2579, wherein the conduit is further configured to remove an oxidation product.

2585. The system ofclaim 2579, wherein the conduit is further configured to remove an oxidation product such that the oxidation product transfers heat to the oxidizhig fluid.

2586. The system ofclaim 2579, wherein the conduit is further configured to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2587. The system ofclaim 2579, wherein the conduit is fuither configured to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2588. The system ofclaim 2579, wherein the conduit is further configured to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2589. The system ofclaim 2579, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2590. The system ofclaim 2579, furtlier comprising a center conduit disposed within the conduit, wherein the center conduit is configured to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configured to remove an oxidation product during use.

2591. The system of claim 2579, wherein the portion of the fonnation extends radially from the opening a width of less than approximately 0.2 m.

2592. The system of clahn 2579, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation.

2593. The system ofclaim 2579, further comprising an overburden casing coupled to die opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2594. The system ofclaim 2579, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2595. The system ofclaim 2579, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2596. The system ofclaim 2579, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2597. The system ofclaim 2579, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packhig material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2598. The system of claim 2579, wherein the system is further configured such that transfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2599. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: at least one elongated member configurable to be disposed in an opening in the formation, wherein at least the one elongated member is further configurable to provide heat to at least a portion of the formation during use; a conduit configurable to be disposed in the opening, wherein the conduit is further configurable to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the formation during use, and wherein the system is configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is further configurable to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2600. The system of claim 2599, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2601. The system ofclaim 2599, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2602. The system ofclaim 2599, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to confrol a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled.

2603. The system of claim 2599, wherein the conduit is further configurable to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2604. The system ofclaim 2599, wherein the conduit is further configurable to remove an oxidation product.

2605. The system of claim 2599, wherein the conduit is further configurable to remove an oxidation product such that the oxidation product fransfers heat to the oxidizing fluid.

2606. The system of claim 2599, wherein the conduit is further configurable to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approxhnately equal to a flow rate of the oxidation product in the conduit.

2607. The system of claim 2599, wherein the conduit is further configurable to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2608. The system ofclaim 2599, wherein the conduit is further configurable to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2609. The system of claim 2599, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone.

2610. The system ofclaim 2599, further comprising a center conduit disposed within the conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configurable to remove an oxidation product during use.

2611. The system ofclaim 2599, wherein the portion of the foπnation extends radially from the opening a width of less than approximately 0.2 m.

2612. The system ofclaim 2599, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation.

2613. The system of claim 2599, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2614. The system ofclaim 2599, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2615. The system ofclaim 2599, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2616. The system of claim 2599, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2617. The system ofclaim 2599, further comprising an overburden casing coupled to the openhig, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2618. The system ofclaim 2599, wherein the system is further configurable such that transfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

2619. The system of claim 2599, wherein the system is configured to heat a relatively low permeability foimation containing heavy hydrocarbons, and wherein the system comprises: at least one elongated member disposed in an opening in the fonnation, wherein at least the one elongated member is configured to provide heat to at least a portion of the foπnation during use; an oxidizing fluid source; a conduit disposed in the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to a reaction zone in the foπnation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at the reaction zone during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2620. An in situ method for heating a relatively low penneability fonnation containing heavy hydrocarbons, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons within the portion of the foπnation with an oxidizing fluid, wherein heating comprises applying an elecfrical cunent to at least one elongated member to provide heat to the portion, and wherein at least the one elongated member is disposed within the opening; providing the oxidizing fluid to a reaction zone in the formation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and fransfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the formation.

2621. The method of claim 2620, further comprising ttansporting the oxidizing fluid through the reaction zone by diffusion.

2622. The method ofclaim 2620, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

2623. The method ofclaim 2620, further comprising controlling a flow of the oxidizing fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

2624. The method of clahn 2620, further comprishig increasing a flow of the oxidizing fluid in the opening to accoimnodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

2625. The method of claim 2620, wherein a conduit is disposed in the opening, the method further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

2626. The method of claim 2620, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit.

2627. The method ofclaim 2620, wherehi a conduit is disposed within the opening, the method further comprising removmg an oxidation product from the formation through the conduit and fransfening heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

2628. The method of claim 2620, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foimation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2629. The method of claim 2620, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and controlling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2630. The method of claim 2620, wherein a conduit is disposed within the opening, the method further comprishig removing an oxidation product from the formation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the foimation beyond the reaction zone.

2631. The method of claim 2620, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2632. The method of claim 2620, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

2633. The method ofclaim 2620, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2634. The method of claim 2620, further comprising removing water from the foπnation prior to heating the portion.

2635. The method o claim 2620, further comprising confrolling the temperature of the foπnation to substantially inhibit production of oxides of nifrogen during oxidation.

2636. The method of claim 2620, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2637. The method of clahn 2620, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2638. The method ofclaim 2620, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2639. The method ofclaim 2620, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2640. The method ofclaim 2620, wherein the pyrolysis zone is substantially adjacent to the reaction zone.

2641. A system configured to heat a relatively low permeability fonnation containing heavy hydrocarbons, comprising: a heat exchanger disposed external to the formation, wherein the heat exchanger is configured to heat an oxidizing fluid during use; a conduit disposed in the openhig, wherein the conduit is configured to provide the heated oxidizing fluid from the heat exchanger to at least a portion of the foimation during use, wherein the system is configured to allow heat to fransfer from the heated oxidizing fluid to at least the portion of the formation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at a reaction zone in the foimation during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2642. The system ofclaim 2641, wherein the oxidizing fluid is configured to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2643. The system ofclaim 2641, wherein the conduit comprises orifices, and wherein the orifices are configured to provide the oxidizing fluid into the opening.

2644. The system ofclaim 2641, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configured to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2645. The system ofclaim 2641, wherein the conduit is further configured to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2646. The system ofclaim 2641, wherehi the conduit is further configured to remove an oxidation product.

2647. The system ofclaim 2641, wherein the conduit is further configured to remove an oxidation product, such that the oxidation product transfers heat to the oxidizing fluid.

2648. The system ofclaim 2641, wherein the conduit is further configured to remove an oxidation product, and wherehi a flow rate of the oxidizing fluid in the conduit is approxhnately equal to a flow rate of the oxidation product in the conduit.

2649. The system ofclaim 2641, wherein the conduit is further configured to remove an oxidation product, and wherein a pressure of the oxidizhig fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2650. The system ofclaim 2641, wherein the conduit is further configured to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2651. The system of claim 2641 , wherein the oxidizing fluid is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2652. The system of clahn 2641, further comprising a center conduit disposed within the conduit, wherehi the center conduit is configured to provide the oxidizing fluid into the opening during use, and wherein the conduit is further configured to remove an oxidation product during use.

2653. The system ofclaim 2641, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2654. The system of claim 2641 , further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2655. The system ofclaim 2641, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2656. The system ofclaim 2641, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2657. The system ofclaim 2641, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2658. The system ofclaim 2641, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2659. The system ofclaim 2641, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2660. A system configurable to heat a relatively low peπneability formation containing heavy hydrocarbons, comprising: a heat exchanger configurable to be disposed external to the formation, wherein the heat exchanger is further configurable to heat an oxidizhig fluid during use; a conduit configurable to be disposed in the opening, wherein the conduit is further configurable to provide the heated oxidizing fluid from the heat exchanger to at least a portion of the formation during use, wherein the system is configurable to allow heat to transfer from the heated oxidizing fluid to at least the portion of the formation during use, and wherein the system is further configurable to allow the oxidizing fluid to oxidize at least some hydrocarbons at a reaction zone in the fonnation during use such that heat is generated at the reaction zone; and wherein the system is further configurable to allow heat to ttansfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2661. The system ofclaim 2660, wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

2662. The system ofclaim 2660, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening.

2663. The system ofclaim 2660, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled.

2664. The system ofclaim 2660, wherein the conduit is further configurable to be cooled with the oxidizing fluid such that the conduit is not substantially heated by oxidation.

2665. The system ofclaim 2660, wherein the conduit is further configurable to remove an oxidation product.

2666. The system ofclaim 2660, wherein the conduit is further configurable to remove an oxidation product such that the oxidation product transfers heat to the oxidizing fluid.

2667. The system ofclaim 2660, wherein the conduit is fuither configurable to remove an oxidation product, and wherein a flow rate of the oxidizing fluid in the conduit is approxhnately equal to a flow rate of the oxidation product in the conduit.

2668. The system of clahn 2660, wherein the conduit is further configurable to remove an oxidation product, and wherein a pressure of the oxidizing fluid in the conduit and a pressure of the oxidation product in the conduit are confrolled to reduce contamination of the oxidation product by the oxidizing fluid.

2669. The system of claim 2660, wherein the conduit is further configurable to remove an oxidation product, and wherein the oxidation product is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2670. The system ofclaim 2660, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the foπnation beyond the reaction zone.

2671. The system of claim 2660, further comprising a center conduit disposed within the conduit, wherein the center conduit is configurable to provide the oxidizing fluid into the opening during use, and wherein the second conduit is further configurable to remove an oxidation product during use.

2672. The system of claim 2660, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2673. The system ofclaim 2660, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foimation.

2674. The system ofclaim 2660, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2675. The system ofclaim 2660, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2676. The system ofclaim 2660, further comprising an overburden casing coupled to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2677. The system of clahn 2660, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the openmg, and wherehi the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2678. The system ofclaim 2660, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2679. The system ofclaim 2660, wherein the system is configured to heat a relatively low permeability foimation containing heavy hydrocarbons, and wherein the system comprises: a heat exchanger disposed external to the formation, wherein the heat exchanger is configured to heat an oxidizing fluid during use; a conduit disposed in the opening, wherein the conduit is configured to provide the heated oxidizing fluid from the heat exchanger to at least a portion of the fonnation during use, wherein the system is configured to allow heat to fransfer from the heated oxidizing fluid to at least the portion of the foimation during use, and wherein the oxidizing fluid is selected to oxidize at least some hydrocarbons at a reaction zone in the foπnation during use such that heat is generated at the reaction zone; and wherein the system is configured to allow heat to fransfer substantially by conduction from the reaction zone to a pyrolysis zone of the formation during use.

2680. An in situ method for heating a relatively low peπneability formation containing heavy hydrocarbons, comprising: heating a portion of the foimation to a temperature sufficient to support reaction of hydrocarbons within the portion of the formation with an oxidizing fluid, wherein heating comprises: heating the oxidizhig fluid with a heat exchanger, wherein the heat exchanger is disposed external to the formation; providing the heated oxidizing fluid from the heat exchanger to the portion of the formation; and allowing heat to ttansfer from the heated oxidizing fluid to the portion of the formation; providing the oxidizhig fluid to a reaction zone in the formation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and transferring the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the fonnation.

2681. The method of claim 2680, further comprising fransporting the oxidizing fluid through the reaction zone by diffusion.

2682. The method of clahn 2680, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

2683. The method of clahn 2680, further comprising confrolling a flow of the oxidizing fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

2684. The method of clahn 2680, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

2685. The method of claim 2680, wherein a conduit is disposed in the opening, the method further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

2686. The method ofclaim 2680, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit.

2687. The method of claim 2680, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foimation through the conduit and fransfening heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

2688. The method ofclaim 2680, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2689. The method ofclaim 2680, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foπnation through the conduit and controlling a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2690. The method of claim 2680, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the fonnation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2691. The method of claim 2680, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2692. The method ofclaim 2680, wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

2693. The method of clahn 2680, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2694. The method of claim 2680, fuither comprising removing water from the formation prior to heating the portion.

2695. The method of claim 2680, further comprising controlling the temperature of the formation to substantially inhibit production of oxides of nitrogen during oxidation.

2696. The method ofclaim 2680, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2697. The method ofclaim 2680, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2698. The method ofclaim 2680, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2699. The method of claim 2680, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the openhig.

2700. The method of claim 2680, wherein the pyrolysis zone is substantially adjacent to the reaction zone.

2701. An in situ method for heating a relatively low permeability foimation containing heavy hydrocarbons, comprising: heating a portion of the foimation to a temperature sufficient to support reaction of hydrocarbons within the portion of the foimation with an oxidizing fluid, wherein heating comprises: oxidizing a fuel gas in a heater, wherein the heater is disposed external to the foimation; providing the oxidized fuel gas from the heater to the portion of the formation; and allowing heat to transfer from the oxidized fuel gas to the portion of the formation; providing the oxidizing fluid to a reaction zone in the formation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons at the reaction zone to generate heat at the reaction zone; and transfening the generated heat substantially by conduction from the reaction zone to a pyrolysis zone in the formation.

2702. The method of claim 2701, further comprising fransporting the oxidizing fluid through the reaction zone by diffusion.

2703. The method of clahn 2701, further comprising directing at least a portion of the oxidizing fluid into the opening through orifices of a conduit disposed in the opening.

2704. The method ofclaim 2701, further comprising confrolling a flow of the oxidizing fluid with critical flow orifices of a conduit disposed in the opening such that a rate of oxidation is confrolled.

2705. The method ofclaim 2701, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

2706. The method of claim 2701 , wherein a conduit is disposed in the opening, the method further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

2707. The method ofclaim 2701, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foπnation through the conduit.

2708. The method of claim 2701 , wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and transfening heat from the oxidation product in the conduit to the oxidizing fluid in the conduit.

2709. The method ofclaim 2701, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit, wherein a flow rate of the oxidizing fluid in the conduit is approximately equal to a flow rate of the oxidation product in the conduit.

2710. The method of claim 2701 , wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the formation through the conduit and confroUhig a pressure between the oxidizing fluid and the oxidation product in the conduit to reduce contamination of the oxidation product by the oxidizing fluid.

2711. The method of claim 2701, wherein a conduit is disposed within the opening, the method further comprising removing an oxidation product from the foπnation through the conduit and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

2712. The method of claim 2701 , further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

2713. The method of claim 2701 , wherein a center conduit is disposed within an outer conduit, and wherein the outer conduit is disposed within the opening, the method further comprising providing the oxidizing fluid into the opening through the center conduit and removing an oxidation product through the outer conduit.

2714. The method of clahn 2701, wherein the portion of the formation extends radially from the opening a width of less than approximately 0.2 m.

2715. The method of claim 2701 , further comprising removing water from the formation prior to heating the portion.

2716. The method ofclaim 2701, further comprising controlling the temperature of the formation to substantially inhibit production of oxides of nifrogen during oxidation.

2717. The method ofclaim 2701, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2718. The method ofclaim 2701, fuither comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2719. The method ofclaim 2701, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

2720. The method ofclaim 2701, further comprising coupling an overburden cashig to the openhig, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

2721. The method of claim 2701 , wherein the pyrolysis zone is substantially adj acent to the reaction zone.

2722. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: an insulated conductor disposed within an open wellbore in the formation, wherein the insulated conductor is configured to provide radiant heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to transfer from the insulated conductor to a selected section of the formation during use.

2723. The system ofclaim 2722, wherein the insulated conductor is further configured to generate heat during application of an elecfrical cunent to the insulated conductor during use.

2724. The system of clahn 2722, further comprising a support member, wherein the support member is configured to support the insulated conductor.

2725. The system ofclaim 2722, further comprising a support member and a centralizer, wherein the support member is configured to support the insulated conductor, and wherein the cenfralizer is configured to maintain a location of the insulated conductor on the support member.

2726. The system ofclaim 2722, wherein the open wellbore comprises a diameter of at least approximately 5 cm.

2727. The system ofclaim 2722, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

2728. The system of claim 2722, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a rubber insulated conductor.

2729. The system ofclaim 2722, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a copper wire.

2730. The system ofclaim 2722, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin fransition conductor.

2731. The system of claim 2722, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin transition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

2732. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the electrically insulating material is disposed in a sheath.

2733. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

2734. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approxhnately 7 % nickel by weight to approximately 12 % nickel by weight.

2735. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 2 % nickel by weight to approximately 6 % nickel by weight.

2736. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the electrically insulating material comprises a thermally conductive material.

2737. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the electrically insulating material comprises magnesium oxide.

2738. The system of claim 2722, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the electrically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

2739. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the electrically insulating material comprises aluminum oxide and magnesium oxide.

2740. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the electrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configured to occupy porous spaces within the magnesium oxide.

2741. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2742. The system ofclaim 2722, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2743. The system ofclaim 2722, further comprising two additional insulated conductors, wherehi the insulated conductor and the two additional insulated conductors are configured in a 3-phase Y configuration.

2744. The system ofclaim 2722, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configured in a series electrical configuration.

2745. The system ofclaim 2722, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configured in a parallel electrical configuration.

2746. The system ofclaim 2722, wherein the insulated conductor is configured to generate radiant heat of approximately 500 W/m to approxhnately 1150 W/m during use.

2747. The system ofclaim 2722, further comprishig a support member configured to support the insulated conductor, wherehi the support member comprises orifices configured to provide fluid flow through the support member into the open wellbore during use.

2748. The system of claim 2722, further comprishig a support member configured to support the insulated conductor, wherein the support member comprises critical flow orifices configured to provide a substantially constant amount of fluid flow through the support member into the open wellbore during use.

2749. The system of claim 2722, further comprising a tube coupled to the insulated conductor, wherein the tube is configured to provide a flow of fluid into the open wellbore during use.

2750. The system of claim 2722, further comprising a tube coupled to the insulated conductor, wherein the tube comprises critical flow orifices configured to provide a substantially constant amount of fluid flow through the support member into the open wellbore during use.

2751. The system ofclaim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the foimation.

2752. The system ofclaim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2753. The system ofclaim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2754. The system ofclaim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packhig material is disposed at ajunction of the overburden casing and the open wellbore.

2755. The system ofclaim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the open wellbore, and wherein the packing material is configured to substantially inhibit a flow of fluid between the open wellbore and the overburden casing during use.

2756. The system of claim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the open wellbore, and wherein the packing material comprises cement.

2757. The system of claim 2722, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, the system further comprising a wellhead coupled to the overburden casing and a lead-in conductor coupled to the insulated conductor, wherein the wellhead is disposed external to the overburden, wherein the wellhead comprises at least one sealing flange, and wherein at least the one sealing flange is configured to couple to the lead-in conductor.

2758. The system of claim 2722, wherein the system is further configured to transfer heat such that the fransfened heat can pyrolyze at least some of the hydrocarbons in the selected section.

2759. A system configurable to heat a relatively low permeability foimation containing heavy hydrocarbons, comprising: an insulated conductor configurable to be disposed within an open wellbore in the formation, wherein the insulated conductor is further configurable to provide radiant heat to at least a portion of the formation during use; and wherein the system is configurable to allow heat to transfer from the insulated conductor to a selected section of the formation during use.

2760. The system ofclaim 2759, wherein the insulated conductor is further configurable to generate heat during application of an elecfrical cunent to the insulated conductor during use.

2761. The system of claim 2759, further comprising a support member, wherein the support member is configurable to support the insulated conductor.

2762. The system ofclaim 2759, further comprising a support member and a cenfralizer, wherein the support member is configurable to support the insulated conductor, and wherein the centralizer is configurable to maintain a location of the insulated conductor on the support member.

2763. The system ofclaim 2759, wherein the open wellbore comprises a diameter of at least approximately 5 cm.

2764. The system of clahn 2759, further comprismg a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

2765. The system ofclaim 2759, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a rubber insulated conductor.

2766. The system ofclaim 2759, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a copper wire.

2767. The system ofclaim 2759, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin transition conductor.

2768. The system of claim 2759, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin transition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

2769. The system ofclaim 2759, wherehi the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath.

2770. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

2771. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight.

2772. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 2 % nickel by weight to approximately 6 % nickel by weight.

2773. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises a thennally conductive material.

2774. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

2775. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

2776. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

2777. The system of claim 2759, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configurable to occupy porous spaces within the magnesium oxide.

2778. The system ofclaim 2759, wherehi the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2779. The system ofclaim 2759, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2780. The system ofclaim 2759, further comprising two additional insulated conductors, wherein the insulated conductor and the two additional insulated conductors are configurable in a 3 -phase Y configuration.

2781. The system of claim 2759, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configurable in a series elecfrical configuration.

2782. The system ofclaim 2759, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configurable in a parallel electrical configuration.

2783. The system of claim 2759, wherein the insulated conductor is configurable to generate radiant heat of approxhnately 500 W/m to approximately 1150 W/m during use.

2784. The system ofclaim 2759, further comprising a support member configurable to support the insulated conductor, wherein the support member comprises orifices configurable to provide fluid flow through the support member into the open wellbore during use.

2785. The system of claim 2759, further comprising a support member configurable to support the msulated conductor, wherein the support member comprises critical flow orifices configurable to provide a substantially constant amount of fluid flow through the support member into the open wellbore during use.

2786. The system of claim 2759, further comprising a tube coupled to the insulated conductor, wherein the tube is configurable to provide a flow of fluid into the open wellbore during use.

2787. The system of claim 2759, further comprising a tube coupled to the first insulated conductor, wherein the tube comprises critical flow orifices configurable to provide a substantially constant amount of fluid flow through the support member into the open wellbore during use.

2788. The system ofclaim 2759, further comprising an overburden casing coupled to the open wellbore, wherehi the overburden casing is disposed in an overburden of the formation.

2789. The system of claim 2759, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2790. The system ofclaim 2759, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2791. The system of claim 2759, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at ajunction of the overburden casing and the open wellbore.

2792. The system of clahn 2759, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the open wellbore, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the open wellbore and the overburden casing during use.

2793. The system of claim 2759, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the open wellbore, and wherein the packing material comprises cement.

2794. The system ofclaim 2759, further comprising an overburden casing coupled to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, the system further comprising a wellhead coupled to the overburden casing and a lead-in conductor coupled to the insulated conductor, wherein the wellhead is disposed external to the overburden, wherein the wellhead comprises at least one sealing flange, and wherein at least the one sealing flange is configurable to couple to the lead-in conductor.

2795. The system of claim 2759, wherein the system is further configured to ttansfer heat such that the transfened heat can pyrolyze at least some hydrocarbons in the selected section.

2796. The system of claim 2759, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: an insulated conductor disposed within an open wellbore in the fonnation, wherein the insulated conductor is configured to provide radiant heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to transfer from the insulated conductor to a selected section of the formation during use.

2797. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an electrical current to an insulated conductor to provide radiant heat to at least a portion of the formation, wherein the insulated conductor is disposed within an open wellbore in the formation; and allowing the radiant heat to ttansfer from the insulated conductor to a selected section of the formation.

2798. The method of clahn 2797, further comprising supporting the insulated conductor on a support member.

2799. The method of claim 2797, further comprising supporting the insulated conductor on a support member and maintaining a location of the insulated conductor on the support member with a cenfralizer.

2800. The method of claim 2797, wherein the insulated conductor is coupled to two additional insulated conductors, wherein the insulated conductor and the two insulated conductors are disposed within the open wellbore, and wherein the three insulated conductors are elecfrically coupled in a 3-phase Y configuration.

2801. The method of claim 2797, wherein an additional insulated conductor is disposed within the open wellbore.

2802. The method ofclaim 2797, wherein an additional insulated conductor is disposed within the open wellbore, and wherein the insulated conductor and the additional insulated conductor are elecfrically coupled in a series configuration.

2803. The method of claim 2797, wherein an additional insulated conductor is disposed within the open wellbore, and wherein the insulated conductor and the additional insulated conductor are electrically coupled in a parallel configuration.

2804. The method ofclaim 2797, wherein the provided heat comprises approximately 500 W/m to approximately 1150 W/m.

2805. The method of claim 2797, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

2806. The method of claim 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight.

2807. The method of claim 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 2 % nickel by weight to approximately 6 % nickel by weight.

2808. The method of clahn 2797, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, and wherein the electrically insulating material comprises magnesium oxide.

2809. The method of claim 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the electrically insulating material comprises magnesium oxide, and wherehi the magnesium oxide comprises a thickness of at least approximately 1 mm.

2810. The method of clahn 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

2811. The method of claim 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configured to occupy porous spaces within the magnesium oxide.

2812. The method of claim 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2813. The method ofclaim 2797, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2814. The method of claim 2797, further comprising supporting the insulated conductor on a support member and flowing a fluid into the open wellbore through an orifice in the support member.

2815. The method ofclaim 2797, further comprising supporting the insulated conductor on a support member and flowing a substantially constant amount of fluid into the open wellbore through critical flow orifices in the support member.

2816. The method ofclaim 2797, wherein a perforated tube is disposed in the open wellbore proxunate to the insulated conductor, the method further comprising flowing a fluid into the open wellbore through the perforated tube.

2817. The method of claim 2797, wherein a tube is disposed in the open wellbore proximate to the insulated conductor, the method further comprising flowing a substantially constant amount of fluid into the open wellbore through critical flow orifices in the tube.

2818. The method of claim 2797, further comprising supporting the insulated conductor on a support member and flowing a conosion inhibiting fluid into the open wellbore through an orifice in the support member.

2819. The method ofclaim 2797, wherein a perforated tube is disposed in the open wellbore proximate to the insulated conductor, the method further comprising flowing a conosion inhibiting fluid into the open wellbore through the perforated tube.

2820. The method of claim 2797, further comprising determining a temperature distribution in the insulated conductor using an electromagnetic signal provided to the insulated conductor.

2821. The method ofclaim 2797, fuither comprising monitoring a leakage cunent of the insulated conductor.

2822. The method of clahn 2797, further comprising monitoring the applied electrical cunent.

2823. The method ofclaim 2797, further comprising monitoring a voltage applied to the insulated conductor.

2824. The method of claim 2797, further comprising monitoring a temperature in the insulated conductor with at least one thermocouple.

2825. The method of claim 2797, further comprising electrically coupling a lead-in conductor to the insulated conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

2826. The method ofclaim 2797, further comprising electrically coupling a lead-in conductor to the insulated conductor using a cold pin fransition conductor.

2827. The method ofclaim 2797, further comprising electrically coupling a lead-in conductor to the insulated conductor using a cold pin transition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

2828. The method ofclaim 2797, further comprising coupling an overburden casing to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation.

2829. The method of claim 2797, further comprising coupling an overburden casing to the open wellbore, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing comprises steel.

2830. The method ofclaim 2797, further comprising coupling an overburden casing to the open wellbore, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

2831. The method of claim 2797, further comprising coupling an overburden casing to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at ajunction of the overburden casing and the open wellbore.

2832. The method of claim 2797, further comprising coupling an overburden casing to the open wellbore, wherein the overburden casing is disposed in an overburden of the formation, and wherein the method further comprises inhibiting a flow of fluid between the open wellbore and the overburden cashig with a packing material.

2833. The method ofclaim 2797, further comprising heating at least the portion of the foπnation to pyrolyze at least some hydrocarbons within the formation.

2834. An in situ method for heating a relatively low peπneability formation containing heavy hydrocarbons, comprising: applying an elecfrical cunent to an insulated conductor to provide heat to at least a portion of the foπnation, wherein the insulated conductor is disposed within an openhig in the formation; and allowing the heat to fransfer from the insulated conductor to a section of the fonnation.

2835. The method ofclaim 2834, further comprising supporting the insulated conductor on a support member.

2836. The method ofclaim 2834, further comprising supporting the insulated conductor on a support member and maintaining a location of the first insulated conductor on the support member with a cenfralizer.

2837. The method ofclaim 2834, wherein the insulated conductor is coupled to two additional insulated conductors, wherein the insulated conductor and the two insulated conductors are disposed within the opening, and wherein the three insulated conductors are electrically coupled in a 3-phase Y configuration.

2838. The method ofclaim 2834, wherein an additional insulated conductor is disposed within the openhig.

2839. The method ofclaim 2834, wherein an additional insulated conductor is disposed within the opening, and wherein the insulated conductor and the additional insulated conductor are electrically coupled in a series configuration.

2840. The method o claim 2834, wherein an additional insulated conductor is disposed within the opening, and wherein the insulated conductor and the additional insulated conductor are elecfrically coupled in a parallel configuration.

2841. The method of claim 2834, wherein the provided heat comprises approximately 500 W/m to approximately 1150 W/m.

2842. The method ofclaim 2834, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

2843. The method ofclaim 2834, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight.

2844. The method of clahn 2834, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper- nickel alloy comprises approximately 2 % nickel by weight to approximately 6 % nickel by weight.

2845. The method of claim 2834, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

2846. The method of clahn 2834, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

2847. The method of claim 2834, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

2848. The method of claim 2834, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the electrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configured to occupy porous spaces within the magnesium oxide.

2849. The method ofclaim 2834, wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2850. The method ofclaim 2834, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2851. The method of claim 2834, further comprising supporting the insulated conductor on a support member and flowing a fluid into the opening through an orifice in the support member.

2852. The method of claim 2834, further comprising supporting the insulated conductor on a support member and flowing a substantially constant amount of fluid into the opening through critical flow orifices in the support member.

2853. The method of claim 2834, wherein a perforated tube is disposed in the opening proxhnate to the insulated conductor, the method further comprishig flowing a fluid into the opening through the perforated tube.

2854. The method of claim 2834, wherein a tube is disposed in the opening proximate to the insulated conductor, the method further comprising flowing a substantially constant amount of fluid into the opening through critical flow orifices in the tube.

2855. The method of claim 2834, fuither comprising supporting the insulated conductor on a support member and flowing a conosion inhibiting fluid into the opening through an orifice in the support member.

2856. The method of claim 2834, wherein a perforated tube is disposed in the opening proxhnate to the insulated conductor, the method further comprishig flowing a conosion inhibiting fluid into the opening through the perforated tube.

2857. The method of clahn 2834, further comprishig deteπnining a temperature disttibution in the insulated conductor using an electromagnetic signal provided to the insulated conductor.

2858. The method ofclaim 2834, further comprising monitoring a leakage cunent of the insulated conductor.

2859. The method ofclaim 2834, further comprising monitoring the applied elecfrical cunent.

2860. The method ofclaim 2834, further comprising monitoring a voltage applied to the insulated conductor.

2861. The method of claim 2834, further comprising monitoring a temperature in the insulated conductor with at least one thermocouple.

2862. The method of claim 2834, further comprising electrically coupling a lead-in conductor to the insulated conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

2863. The method ofclaim 2834, further comprising electrically coupling a lead-in conductor to the insulated conductor using a cold pin fransition conductor.

2864. The method ofclaim 2834, further comprising electrically coupling a lead-in conductor to the insulated conductor using a cold pin fransition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

2865. The method ofclaim 2834, further comprising coupling an overburden cashig to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2866. The method of claim 2834, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2867. The method of clahn 2834, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

2868. The method of claim 2834, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

2869. The method of clahn 2834, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with a packing material.

2870. The method of claim 2834, further comprising heating at least the portion of the foπnation to substantially pyrolyze at least some hydrocarbons within the foπnation.

2871. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: an insulated conductor disposed withhi an opening in the formation, wherein the insulated conductor is configured to provide heat to at least a portion of the formation during use, wherein the insulated conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight; and wherein the system is configured to allow heat to ttansfer from the insulated conductor to a selected section of the foπnation during use.

2872. The system ofclaim 2871, wherein the insulated conductor is further configured to generate heat during application of an elecfrical cunent to the insulated conductor during use.

2873. The system ofclaim 2871, further comprismg a support member, wherein the support member is configured to support the insulated conductor.

2874. The system ofclaim 2871, further comprising a support member and a cenfralizer, wherein the support member is configured to support the insulated conductor, and wherem the cenfralizer is configured to maintain a location of the insulated conductor on the support member.

2875. The system ofclaim 2871, wherein the opening comprises a diameter of at least approximately 5 cm.

2876. The system ofclaim 2871, further comprising a lead-in conductor coupled to the insulated conductor, wherehi the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

2877. The system ofclaim 2871, further comprismg a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a rubber insulated conductor.

2878. The system ofclaim 2871, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a copper wire.

2879. The system ofclaim 2871, fuither comprising a lead-in conductor coupled to the insulated conductor with a cold pin transition conductor.

2880. The system ofclaim 2871, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin fransition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

2881. The system ofclaim 2871, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, and wherein the electrically insulating material comprises a thermally conductive material.

2882. The system ofclaim 2871, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

2883. The system ofclaim 2871, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, and wherein the magnesimn oxide comprises a thickness of at least approximately 1 mm.

2884. The system of claim 2871 , wherein the copper-nickel alloy is disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

2885. The system ofclaim 2871, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, wherein the electrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherehi the grain particles are configured to occupy porous spaces within the magnesium oxide.

2886. The system ofclaim 2871, wherein the copper-nickel alloy is disposed in an electrically insulating material, wherein the electrically insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2887. The system ofclaim 2871, wherein the copper-nickel alloy is disposed in an electrically insulating material, wherein the electrically insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2888. The system ofclaim 2871, further comprising two additional insulated conductors, wherein the insulated conductor and the two additional insulated conductors are configured in a 3-phase Y configuration.

2889. The system ofclaim 2871, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configured in a series electrical configuration.

2890. The system ofclaim 2871, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configured in a parallel electrical configuration.

2891. The system ofclaim 2871, wherein the insulated conductor is configured to generate radiant heat of approximately 500 W/m to approximately 1150 W/m during use.

2892. The system ofclaim 2871, further comprising a support member configured to support the insulated conductor, wherein the support member comprises orifices configured to provide fluid flow through the support member into the opening during use.

2893. The system of claim 2871 , further comprising a support member configured to support the insulated conductor, wherein the support member comprises critical flow orifices configured to provide a substantially constant amount of fluid flow through the support member into the opening during use.

2894. The system of claim 2871 , further comprising a tube coupled to the insulated conductor, wherein the tube is configured to provide a flow of fluid into the opening during use.

2895. The system of claim 2871 , further comprising a tube coupled to the insulated conductor, wherein the tube comprises critical flow orifices configured to provide a substantially constant amount of fluid flow through the support member into the opening during use.

2896. The system ofclaim 2871, further comprising an overburden casing coupled to the openhig, wherein the overburden casing is disposed in an overburden of the formation.

2897. The system ofclaim 2871, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2898. The system ofclaim 2871, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2899. The system of claim 2871, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherehi a packing material is disposed at a junction of the overburden casing and the opening.

2900. The system ofclaim 2871, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the openmg, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2901. The system ofclaim 2871, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden cashig and the opening, and wherein the packing material comprises cement.

2902. The system ofclaim 2871, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, the system further comprising a wellhead coupled to the overburden casing and a lead-in conductor coupled to the insulated conductor, wherein the wellhead is disposed external to the overburden, wherein the wellhead comprises at least one sealing flange, and wherein at least the one sealing flange is configured to couple to the lead-in conductor.

2903. The system ofclaim 2871, wherein the system is further configured to fransfer heat such that the fransfened heat can pyrolyze at least some hydrocarbons in the selected section.

2904. A system configurable to heat a relatively low permeability foπnation containing heavy hydrocarbons, comprising: an insulated conductor configurable to be disposed within an opening in the formation, wherein the insulated conductor is further configurable to provide heat to at least a portion of the foimation during use, wherein the insulated conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight; wherein the system is configurable to allow heat to fransfer from the insulated conductor to a selected section of the formation during use.

2905. The system ofclaim 2904, wherein the insulated conductor is further configurable to generate heat during application of an electrical cunent to the insulated conductor during use.

2906. The system of claim 2904, further comprising a support member, wherein the support member is configurable to support the insulated conductor.

2907. The system ofclaim 2904, further comprising a support member and a cenfralizer, wherein the support member is configurable to support the insulated conductor, and wherein the centtalizer is configurable to maintain a location of the insulated conductor on the support member.

2908. The system ofclaim 2904, wherein the opening comprises a diameter of at least approxhnately 5 cm.

2909. The system ofclaim 2904, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

2910. The system ofclaim 2904, further comprising a lead-in conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a rubber insulated conductor.

2911. The system of clahn 2904, further comprishig a lead-hi conductor coupled to the insulated conductor, wherein the lead-in conductor comprises a copper wire.

2912. The system ofclaim 2904, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin transition conductor.

2913. The system ofclaim 2904, further comprising a lead-in conductor coupled to the insulated conductor with a cold pin transition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

2914. The system ofclaim 2904, wherein the copper-nickel alloy is disposed in an electrically insulating material, and wherein the electtically insulating material comprises a thermally conductive material.

2915. The system ofclaim 2904, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

2916. The system ofclaim 2904, wherem the copper-nickel alloy is disposed in an elecfrically insulating material, wherein the elecfrically insulating material comprises magnesimn oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

2917. The system ofclaim 2904, wherein the copper-nickel alloy is disposed in an electrically insulating material, and wherein the electtically insulating material comprises aluminum oxide and magnesium oxide.

2918. The system ofclaim 2904, wherein the copper-nickel alloy is disposed in an electrically insulating material, wherein the electtically insulating material comprises magnesium oxide, wherein the magnesimn oxide comprises grain particles, and wherein the grain particles are configurable to occupy porous spaces within the magnesium oxide.

2919. The system ofclaim 2904, wherein the copper-nickel alloy is disposed in an electrically insulating material, wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2920. The system ofclaim 2904, wherein the copper-nickel alloy is disposed in an electrically insulating material, wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2921. The system of claim 2904, further comprising two additional insulated conductors, wherein the insulated conductor and the two additional insulated conductors are configurable in a 3-phase Y configuration.

2922. The system ofclaim 2904, further comprising an additional insulated conductor, wherehi the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configurable in a series elecfrical configuration.

2923. The system ofclaim 2904, further comprising an additional insulated conductor, wherein the insulated conductor and the additional insulated conductor are coupled to a support member, and wherein the insulated conductor and the additional insulated conductor are configurable in a parallel elecfrical configuration.

2924. The system of claim 2904, wherein the insulated conductor is configurable to generate radiant heat of approxhnately 500 W/m to approximately 1 150 W/m during use.

2925. The system ofclaim 2904, further comprising a support member configurable to support the insulated conductor, wherein the support member comprises orifices configurable to provide fluid flow through the support member into the open wellbore during use.

2926. The system of claim 2904, further comprising a support member configurable to support the insulated conductor, wherein the support member comprises critical flow orifices configurable to provide a substantially constant amount of fluid flow through the support member into the opening during use.

2927. The system of claim 2904, further comprising a tube coupled to the insulated conductor, wherein the tube is configurable to provide a flow of fluid into the opening during use.

2928. The system of claim 2904, further comprising a tube coupled to the insulated conductor, wherein the tube comprises critical flow orifices configurable to provide a substantially constant amount of fluid flow through the support member into the opening during use.

2929. The system ofclaim 2904, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

2930. The system of claim 2904, further comprising an overburden cashig coupled to the opening, wherein the overburden cashig is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2931. The system ofclaim 2904, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2932. The system ofclaim 2904, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

2933. The system ofclaim 2904, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

2934. The system ofclaim 2904, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

2935. The system ofclaim 2904, further comprising an overburden casing coupled to the opening, wherein the overburden cashig is disposed in an overburden of the foπnation, the system further comprising a wellhead coupled to the overburden casing and a lead-in conductor coupled to the insulated conductor, wherein the wellhead is disposed external to the overburden, wherein the wellhead comprises at least one sealing flange, and wherein at least the one sealing flange is configurable to couple to the lead-in conductor.

2936. The system ofclaim 2904, wherein the system is further configured to fransfer heat such that the fransfened heat can pyrolyze at least some hydrocarbons in the selected section.

2937. The system of claim 2904, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: an insulated conductor disposed within an opening in the foimation, wherein the insulated conductor is configured to provide heat to at least a portion of the formation during use, wherein the insulated conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight; and wherein the system is configured to allow heat to fransfer from the insulated conductor to a selected section of the formation during use.

2938. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an elecfrical cunent to an insulated conductor to provide heat to at least a portion of the formation, wherein the insulated conductor is disposed within an opening in the foimation, and wherein the insulated conductor comprises a copper-nickel alloy of approximately 7 % nickel by weight to approximately 12 % nickel by weight; and allowing the heat to ttansfer from the insulated conductor to a selected section of the formation.

2939. The method of claim 2938, further comprising supporting the insulated conductor on a support member.

2940. The method ofclaim 2938, further comprising supporting the insulated conductor on a support member and maintaining a location of the first insulated conductor on the support member with a centralizer.

2941. The method of claim 2938, wherein the insulated conductor is coupled to two additional insulated conductors, wherein the insulated conductor and the two insulated conductors are disposed within the opening, and wherein the three insulated conductors are electrically coupled in a 3-phase Y configuration.

2942. The method ofclaim 2938, wherein an additional insulated conductor is disposed within the opening.

2943. The method of claim 2938, wherein an additional insulated conductor is disposed within the opening, and wherehi the insulated conductor and the additional insulated conductor are electrically coupled in a series configuration.

2944. The method ofclaim 2938, wherein an additional insulated conductor is disposed within the opening, and wherein the insulated conductor and the additional insulated conductor are elecfrically coupled in a parallel configuration.

2945. The method ofclaim 2938, wherein the provided heat comprises approximately 500 W/m to approximately 1150 W/m.

2946. The method ofclaim 2938, wherehi the copper-nickel alloy is disposed in an elecfrically insulating material.

2947. The method ofclaim 2938, wherein the copper-nickel alloy is disposed in an electrically insulating material, and wherein the electrically insulating material comprises magnesium oxide.

2948. The method of claim 2938, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

2949. The method of claim 2938, wherein the copper-nickel alloy is disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

2950. The method ofclaim 2938, wherein the copper-nickel alloy is disposed in an electrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configured to occupy porous spaces within the magnesium oxide.

2951. The method of claim 2938, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises a conosion- resistant material.

2952. The method of claim 2938, wherein the copper-nickel alloy is disposed in an elecfrically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2953. The method of claim 2938, further comprising supporting the insulated conductor on a support member and flowing a fluid into the opening through an orifice in the support member.

2954. The method ofclaim 2938, further comprising supporting the insulated conductor on a support member and flowing a substantially constant amount of fluid into the opening through critical flow orifices in the support member.

2955. The method of clahn 2938, wherein a perforated tube is disposed in the opening proximate to the insulated conductor, the method further comprising flowing a fluid into the opening through the perforated tube.

2956. The method ofclaim 2938, wherein a tube is disposed in the opening proxhnate to the insulated conductor, the method further comprising flowing a substantially constant amount of fluid into the opening through critical flow orifices in the tube.

2957. The method of claim 2938, further comprising supporting the insulated conductor on a support member and flowing a conosion inhibiting fluid into the opening through an orifice in the support member.

2958. The method ofclaim 2938, wherein a perforated tube is disposed in the opening proximate to the insulated conductor, the method further comprising flowing a conosion inhibiting fluid into the opening through the perforated tube.

2959. The method ofclaim 2938, further comprising determining a temperature disfribution in the insulated conductor using an electromagnetic signal provided to the insulated conductor.

2960. The method ofclaim 2938, further comprising monitoring a leakage cunent of the insulated conductor.

2961. The method of claim 2938, further comprising monitoring the applied electrical cunent.

2962. The method of clahn 2938, further comprising monitoring a voltage applied to the insulated conductor.

2963. The method of claim 2938, further comprising monitoring a temperature in the insulated conductor with at least one theπnocouple.

2964. The method ofclaim 2938, further comprising elecfrically coupling a lead-in conductor to the insulated conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

2965. The method of claim 2938, further comprising elecfrically coupling a lead-in conductor to the insulated conductor using a cold pin fransition conductor.

2966. The method ofclaim 2938, further comprising elecfrically coupling a lead-in conductor to the insulated conductor using a cold pin fransition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

2967. The method ofclaim 2938, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the fonnation.

2968. The method of claim 2938, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

2969. The method of claim 2938, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

2970. The method of claim 2938, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

2971. The method ofclaim 2938, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with a packing material.

2972. The method of clahn 2938, further comprising heating at least the portion of the formation to substantially pyrolyze at least some hydrocarbons within the formation.

2973. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprismg: at least three insulated conductors disposed within an opening in the foπnation, wherein at least the three insulated conductors are electtically coupled in a 3-phase Y configuration, and wherein at least the three insulated conductors are configured to provide heat to at least a portion of the foπnation during use; and wherein the system is configured to allow heat to fransfer from at least the three insulated conductors to a selected section of the formation during use.

2974. The system ofclaim 2973, wherein at least the three insulated conductors are further configured to generate heat during application of an elecfrical cunent to at least the three insulated conductors during use.

2975. The system of claim 2973, further comprising a support member, wherein the support member is configured to support at least the three insulated conductors.

2976. The system ofclaim 2973, further comprising a support member and a cenfralizer, wherein the support member is configured to support at least the three insulated conductors, and wherein the cenfralizer is configured to maintain a location of at least the three insulated conductors on the support member.

2977. The system ofclaim 2973, wherein the opening comprises a diameter of at least approximately 5 cm.

2978. The system of claim 2973, further comprising at least one lead-in conductor coupled to at least the three insulated conductors, wherein at least the one lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

2979. The system ofclaim 2973, further comprising at least one lead-in conductor coupled to at least the three insulated conductors, wherein at least the one lead-in conductor comprises a rubber insulated conductor.

2980. The system of claim 2973, further comprising at least one lead-in conductor coupled to at least the three insulated conductors, wherein at least the one lead-in conductor comprises a copper wire.

2981. The system of claim 2973, further comprising at least one lead-in conductor coupled to at least the three insulated conductors with a cold pin transition conductor.

2982. The system of claim 2973, further comprising at least one lead-in conductor coupled to at least the three insulated conductors with a cold pin fransition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

2983. The system ofclaim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the electrically insulating material is disposed in a sheath.

2984. The system of claim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

2985. The system of claim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight.

2986. The system ofclaim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 2 % nickel by weight to approxhnately 6 % nickel by weight.

2987. The system of claim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises a thermally conductive material.

2988. The system ofclaim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

2989. The system ofclaim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, wherein the electrically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

2990. The system ofclaim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the electrically insulating material comprises aluminum oxide and magnesimn oxide.

2991. The system of claim 2973 , wherein the insulated conductor comprises a conductor disposed in an elecfrically insulating material, wherein the electtically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configured to occupy porous spaces within the magnesium oxide.

2992. The system ofclaim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an electtically insulating material, and wherein the electtically insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

2993. The system of claim 2973, wherein at least the three insulated conductors comprise a conductor disposed in an electtically insulating material, and wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

2994. The system of claim 2973, wherein at least the three insulated conductors are configured to generate radiant heat of approximately 500 W/m to approximately 1150 W/m of at least the three insulated conductors during use.

2995. The system of clahn 2973, further comprising a support member configured to support at least the three insulated conductors, wherein the support member comprises orifices configured to provide fluid flow through the support member into the opening during use.

2996. The system ofclaim 2973, further comprising a support member configured to support at least the three insulated conductors, wherein the support member comprises critical flow orifices configured to provide a substantially constant amount of fluid flow through the support member into the opening during use.

2997. The system ofclaim 2973, further comprising a tube coupled to at least the three insulated conductors, wherein the tube is configured to provide a flow of fluid into the opening during use.

2998. The system ofclaim 2973, further comprising a tube coupled to at least the three insulated conductors, wherein the tube comprises critical flow orifices configured to provide a substantially constant amount of fluid flow through the support member into the opening during use.

2999. The system ofclaim 2973, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation.

3000. The system of claim 2973, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing comprises steel.

3001. The system of claim 2973 , further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foimation, and wherein the overburden casing is further disposed in cement.

3002. The system ofclaim 2973, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3003. The system ofclaim 2973, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foimation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3004. The system ofclaim 2973, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

3005. The system of claim 2973 , further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, the system further comprising a wellhead coupled to the overburden casing and a lead-in conductor coupled to the insulated conductor, wherein the wellhead is disposed external to the overburden, wherein the wellhead comprises at least one sealing flange, and wherein at least the one sealing flange is configured to couple to the lead-in conductor.

3006. The system ofclaim 2973, wherein the system is further configured to fransfer heat such that the transfened heat can pyrolyze at least some hydrocarbons in the selected section.

3007. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: at least three insulated conductors configurable to be disposed within an opening in the formation, wherein at least the three insulated conductors are elecfrically coupled in a 3-phase Y configuration, and wherein at least the three insulated conductors are further configurable to provide heat to at least a portion of the fonnation during use; and wherein the system is configurable to allow heat to ttansfer from at least the three insulated conductors to a selected section of the formation during use.

3008. The system ofclaim 3007, wherein at least the three insulated conductors are further configurable to generate heat during application of an elecfrical cunent to at least the three insulated conductors during use.

3009. The system ofclaim 3007, further comprising a support member, wherein the support member is configurable to support at least the three insulated conductors.

3010. The system ofclaim 3007, further comprising a support member and a cenfralizer, wherein the support member is configurable to support at least the three insulated conductors, and wherein the centralizer is configurable to maintain a location of at least the three insulated conductors on the support member.

3011. The system ofclaim 3007, wherein the opening comprises a diameter of at least approximately 5 cm.

3012. The system ofclaim 3007, further comprising at least one lead-in conductor coupled to at least the three insulated conductors, wherehi at least the one lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

3013. The system ofclaim 3007, further comprising at least one lead-in conductor coupled to at least the three insulated conductors, wherein at least the one lead-in conductor comprises a rubber insulated conductor.

3014. The system ofclaim 3007, further comprising at least one lead-in conductor coupled to at least the three insulated conductors, wherein at least the one lead-in conductor comprises a copper wire.

3015. The system ofclaim 3007, further comprising at least one lead-in conductor coupled to at least the three insulated conductors with a cold pin fransition conductor.

3016. The system ofclaim 3007, further comprising at least one lead-in conductor coupled to at least the three insulated conductors with a cold pin fransition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

3017. The system ofclaim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath.

3018. The system of clahn 3007, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

3019. The system ofclaim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight.

3020. The system ofclaim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 2 % nickel by weight to approximately 6 % nickel by weight.

3021. The system of claim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises a thermally conductive material.

3022. The system of claim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

3023. The system ofclaim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, wherein the electtically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

3024. The system of claim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

3025. The system of claim 3007, wherein the insulated conductor comprises a conductor disposed in an electrically insulating material, wherein the elecfrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configurable to occupy porous spaces within the magnesium oxide.

3026. The system of clahn 3007, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the electrically insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

3027. The system ofclaim 3007, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

3028. The system of claim 3007, wherein at least the three insulated conductors are configurable to generate radiant heat of approximately 500 W/m to approximately 1150 W/m during use.

3029. The system ofclaim 3007, further comprising a support member configurable to support at least the three insulated conductors, wherein the support member comprises orifices configurable to provide fluid flow through the support member into the opening during use.

3030. The system of claim 3007, further comprising a support member configurable to support at least the three insulated conductors, wherein the support member comprises critical flow orifices configurable to provide a substantially constant amount of fluid flow through the support member into the opening during use.

3031. The system of claim 3007, further comprising a tube coupled to at least the three insulated conductors, wherein the tube is configurable to provide a flow of fluid into the opening during use.

3032. The system ofclaim 3007, further comprising a tube coupled to at least the three insulated conductors, wherein the tube comprises critical flow orifices configurable to provide a substantially constant amount of fluid flow through the support member into the openhig during use.

3033. The system ofclaim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3034. The system ofclaim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3035. The system of claim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3036. The system of claim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the openhig.

3037. The system ofclaim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherehi the packing material is configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3038. The system ofclaim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

3039. The system ofclaim 3007, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed hi an overburden of the fonnation, the system fiirther comprising a wellhead coupled to the overburden casing and a lead-in conductor coupled to the insulated conductor, wherein the wellhead is disposed external to the overburden, wherein the wellhead comprises at least one sealing flange, and wherein at least the one sealing flange is configurable to couple to the lead-in conductor.

3040. The system of claim 3007, wherein the system is further configured to fransfer heat such that the fransfened heat can pyrolyze at least some hydrocarbons in the selected section.

3041. The system ofclaim 3007, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: at least three insulated conductors disposed within an opening in the formation, wherein at least the three insulated conductors are elecfrically coupled in a 3-phase Y configuration, and wherein at least the three insulated conductors are configured to provide heat to at least a portion of the foimation during use; and wherein the system is configured to allow heat to fransfer from at least the three insulated conductors to a selected section of the formation during use.

3042. An in situ method for heating a relatively low permeability foπnation containing heavy hydrocarbons, comprising: applying an electrical cunent to at least three insulated conductors to provide heat to at least a portion of the formation, wherein at least the three insulated conductors are disposed within an opening in the foπnation; and allowing the heat to fransfer from at least the three insulated conductors to a selected section of the formation.

3043. The method ofclaim 3042, further comprising supporting at least the three insulated conductors on a support member.

3044. The method of claim 3042, further comprising supporting at least the three insulated conductors on a support member and maintaining a location of at least the three insulated conductors on the support member with a centralizer.

3045. The method ofclaim 3042, wherein the provided heat comprises approximately 500 W/m to approximately 1150 W/m.

3046. The method ofclaim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the conductor comprises a copper-nickel alloy.

3047. The method of claim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 7 % nickel by weight to approximately 12 % nickel by weight.

3048. The method ofclaim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, wherein the conductor comprises a copper-nickel alloy, and wherein the copper-nickel alloy comprises approximately 2 % nickel by weight to approximately 6 % nickel by weight.

3049. The method ofclaim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, and wherein the elecfrically insulating material comprises magnesium oxide.

3050. The method ofclaim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, wherein the electtically insulating material comprises magnesium oxide, and wherein the magnesium oxide comprises a thickness of at least approximately 1 mm.

3051. The method of claim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an electrically insulating material, and wherein the elecfrically insulating material comprises aluminum oxide and magnesium oxide.

3052. The method ofclaim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an elecfrically insulating material, wherein the electrically insulating material comprises magnesium oxide, wherein the magnesium oxide comprises grain particles, and wherein the grain particles are configured to occupy porous spaces within the magnesium oxide.

3053. The method ofclaim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an electtically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises a conosion-resistant material.

3054. The method of claim 3042, wherein at least the three insulated conductors comprise a conductor disposed in an electtically insulating material, wherein the insulating material is disposed in a sheath, and wherein the sheath comprises stainless steel.

3055. The method of clahn 3042, further comprising supporting at least the three insulated conductors on a support member and flowing a fluid into the opening through an orifice in the support member.

3056. The method ofclaim 3042, further comprising supporting at least the three insulated conductors on a support member and flowing a substantially constant amount of fluid into the opening through critical flow orifices in the support member.

3057. The method of clahn 3042, wherein a perforated tube is disposed in the opening proximate to at least the three insulated conductors, the method further comprising flowing a fluid into the opening through the perforated tube.

3058. The method of claim 3042, wherein a tube is disposed in the opening proximate to at least the three insulated conductors, the method further comprising flowing a substantially constant amount of fluid into the opening through critical flow orifices in the tube.

3059. The method ofclaim 3042, further comprising supporting at least the three insulated conductors on a support member and flowing a conosion inhibiting fluid into the opening through an orifice in the support member.

3060. The method of claim 3042, wherein a perforated tube is disposed in the opening proximate to at least the three insulated conductors, the method further comprising flowing a conosion inhibiting fluid into the opening through the perforated tube.

3061. The method ofclaim 3042, further comprising determining a temperature disttibution in at least the three insulated conductors using an electromagnetic signal provided to the insulated conductor.

3062. The method of claim 3042, further comprising monitoring a leakage cunent of at least the three insulated conductors.

3063. The method ofclaim 3042, further comprising monitoring the applied elecfrical cunent.

3064. The method of claim 3042, further comprising monitoring a voltage applied to at least the three insulated conductors.

3065. The method ofclaim 3042, further comprising monitoring a temperature in at least the three insulated conductors with at least one thermocouple.

3066. The method of clahn 3042, further comprising electrically coupling a lead-in conductor to at least the three insulated conductors, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3067. The method of claim 3042, fuither comprising electrically coupling a lead-in conductor to at least the three insulated conductors using a cold pin transition conductor.

3068. The method of claim 3042, further comprising electrically coupling a lead-in conductor to at least the three insulated conductors using a cold pin fransition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance msulated conductor.

3069. The method of claim 3042, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3070. The method of claim 3042, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3071. The method ofclaim 3042, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

3072. The method of claim 3042, further comprising couplmg an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3073. The method ofclaim 3042, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with a packing material.

3074. The method of claim 3042, further comprising heating at least the portion of the formation to substantially pyrolyze at least some of the hydrocarbons within the formation.

3075. A system configured to heat a relatively low permeability foπnation containing heavy hydrocarbons, comprising: a first conductor disposed in a first conduit, wherein the first conduit is disposed within an opening in the foπnation, and wherein the first conductor is configured to provide heat to at least a portion of the foπnation during use; and wherein the system is configured to allow heat to fransfer from the first conductor to a section of the formation during use.

3076. The system ofclaim 3075, wherein the first conductor is further configured to generate heat during application of an elecfrical cunent to the first conductor.

3077. The system ofclaim 3075, wherein the first conductor comprises a pipe.

3078. The system ofclaim 3075, wherein the first conductor comprises stainless steel.

3079. The system ofclaim 3075, wherein the first conduit comprises stainless steel.

3080. The system of claim 3075, further comprising a centralizer configured to maintain a location of the ffrst conductor within the ffrst conduit.

3081. The system of claim 3075, further comprising a cenfralizer configured to maintain a location of the first conductor within the first conduit, wherein the centralizer comprises ceramic material.

3082. The system ofclaim 3075, further comprising a centralizer configured to maintain a location of the first conductor within the first conduit, wherein the cenfralizer comprises ceramic material and stainless steel.

3083. The system ofclaim 3075, wherein the opening comprises a diameter of at least approximately 5 cm.

3084. The system ofclaim 3075, further comprising a lead-in conductor coupled to the first conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3085. The system ofclaim 3075, further comprising a lead-in conductor coupled to the first conductor, wherein the lead-in conductor comprises copper.

3086. The system of claim 3075, further comprising a sliding electrical connector coupled to the first conductor.

3087. The system ofclaim 3075, further comprising a sliding electrical connector coupled to the first conductor, wherein the sliding electrical connector is further coupled to the first conduit.

3088. The system of claim 3075, further comprising a sliding electrical connector coupled to the first conductor, wherein the sliding electrical connector is further coupled to the first conduit, and wherein the sliding electrical connector is configured to complete an electrical circuit with the first conductor and the first conduit.

3089. The system ofclaim 3075, further comprising a second conductor disposed within the first conduit and at least one sliding electrical connector coupled to the first conductor and the second conductor, wherein at least the one sliding elecfrical connector is configured to generate less heat than the first conductor or the second conductor during use.

3090. The system ofclaim 3075, wherein the first conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the first conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3091. The system ofclaim 3075, further comprising a fluid disposed within the ffrst conduit, wherein the fluid is configured to maintain a pressure within the first conduit to substantially inhibit deformation of the first conduit during use.

3092. The system of claim 3075, further comprising a thermally conductive fluid disposed withhi the first conduit.

3093. The system ofclaim 3075, further comprising a thennally conductive fluid disposed within the first conduit, wherein the thermally conductive fluid comprises helium.

3094. The system ofclaim 3075, further comprising a fluid disposed within the first conduit, wherein the fluid is configured to substantially inhibit arcing between the first conductor and the first conduit during use.

3095. The system ofclaim 3075, further comprising a tube disposed within the opening external to the first conduit, wherein the tube is configured to remove vapor produced from at least the heated portion of the formation such that a pressure balance is maintained between the first conduit and the opening to substantially inhibit deformation of the first conduit during use.

3096. The system of claim 3075, wherein the first conductor is further configured to generate radiant heat of approximately 650 W/ni to approximately 1650 W/m during use.

3097. The system of clahn 3075, further comprising a second conductor disposed within a second conduit and a third conductor disposed within a thfrd conduit, wherein the ffrst conduit, the second conduit and the third conduit are disposed in different openings of the formation, wherein the first conductor is elecfrically coupled to the second conductor and the third conductor, and wherein the first, second, and third conductors are configured to operate in a 3-phase Y configuration during use.

3098. The system of claim 3075, further comprising a second conductor disposed within the first conduit, wherein the second conductor is electrically coupled to the first conductor to form an elecfrical circuit.

3099. The system ofclaim 3075, further comprising a second conductor disposed within the first conduit, wherein the second conductor is elecfrically coupled to the first conductor to form an electrical circuit with a connector.

3100. The system ofclaim 3075, further comprising an overburden casing coupled to the opening, wherein the overburden cashig is disposed in an overburden of the foπnation.

3101. The system ofclaim 3075, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3102. The system ofclaim 3075, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3103. The system of clahn 3075, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3104. The system ofclaim 3075, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3105. The system ofclaim 3075, furtlier comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is electtically coupled to the first conductor.

3106. The system of claim 3075, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is electtically coupled to the first conductor, and wherein the substantially low resistance conductor comprises carbon steel.

3107. The system ofclaim 3075, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing and a centtalizer configured to support the substantially low resistance conductor within the overburden casing.

3108. The system ofclaim 3075, wherein the heated section of the formation is substantially pyrolyzed.

3109. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a first conductor configurable to be disposed in a first conduit, wherein the first conduit is configurable to be disposed within an opening in the formation, and wherein the first conductor is further configurable to provide heat to at least a portion of the formation during use; and wherein the system is configurable to allow heat to transfer from the first conductor to a section of the foπnation during use.

3110. The system ofclaim 3109, wherein the first conductor is further configurable to generate heat during application of an electrical cunent to the first conductor.

3111. The system of claim 3109, wherein the first conductor comprises a pipe.

3112. The system ofclaim 3109, wherein the first conductor comprises stainless steel.

3113. The system of claim 3109, wherein the first conduit comprises stainless steel.

3114. The system of claim 3109, further comprising a cenfralizer configurable to maintain a location of the first conductor within the ffrst conduit.

3115. The system ofclaim 3109, further comprising a centtalizer configurable to maintain a location of the first conductor within the first conduit, wherein the centralizer comprises ceramic material.

3116. The system ofclaim 3109, further comprising a cenfralizer configurable to maintain a location of the first conductor within the first conduit, wherein the centralizer comprises ceramic material and stateless steel.

3117. The system of claim 3109, wherehi the opening comprises a diameter of at least approximately 5 cm.

3118. The system of claim 3109, further comprising a lead-in conductor coupled to the first conductor, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

3119. The system of claim 3109, further comprising a lead-in conductor coupled to the first conductor, wherein the lead-in conductor comprises copper.

3120. The system ofclaim 3109, further comprising a sliding electrical connector coupled to the first conductor.

3121. The system of claim 3109, further comprising a sliding electrical connector coupled to the first conductor, wherein the sliding elecfrical connector is further coupled to the first conduit.

3122. The system of claim 3109, further comprising a sliding electrical connector coupled to the first conductor, wherein the sliding elecfrical connector is further coupled to the first conduit, and wherein the sliding electrical connector is configurable to complete an elecfrical circuit with the first conductor and the first conduit.

3123. The system of claim 3109, further comprising a second conductor disposed within the first conduit and at least one sliding elecfrical connector coupled to the first conductor and the second conductor, wherein at least the one sliding elecfrical connector is configurable to generate less heat than the first conductor or the second conductor during use.

3124. The system of claim 3109, wherein the first conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the ffrst conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3125. The system ofclaim 3109, further comprismg a fluid disposed within the first conduit, wherein the fluid is configurable to maintain a pressure within the first conduit to substantially inhibit deformation of the first conduit during use.

3126. The system ofclaim 3109, further comprising a thermally conductive fluid disposed within the first conduit.

3127. The system of claim 3109, further comprising a thennally conductive fluid disposed within the first conduit, wherein the thermally conductive fluid comprises helium.

3128. The system of claim 3109, further comprising a fluid disposed within the first conduit, wherein the fluid is configurable to substantially inhibit arcing between the first conductor and the first conduit during use.

3129. The system of claim 3109, further comprising a tube disposed within the opening external to the first conduit, wherein the tube is configurable to remove vapor produced from at least the heated portion of the foimation such that a pressure balance is maintained between the first conduit and the opening to substantially inhibit defoπnation of the first conduit during use.

3130. The system of claim 3109, wherein the first conductor is further configurable to generate radiant heat of approximately 650 W/m to approximately 1650 W/m during use.

3131. The system of claim 3109, further comprising a second conductor disposed within a second conduit and a third conductor disposed within a thfrd conduit, wherein the first conduit, the second conduit and the third conduit are disposed in different openings of the formation, wherein the first conductor is elecfrically coupled to the second conductor and the third conductor, and wherein the first, second, and third conductors are configurable to operate in a 3-phase Y configuration during use.

3132. The system of claim 3109, further comprising a second conductor disposed within the first conduit, wherein the second conductor is elecfrically coupled to the first conductor to form an electrical circuit.

3133. The system of claim 3109, further comprising a second conductor disposed within the first conduit, wherein the second conductor is electrically coupled to the first conductor to form an elecfrical circuit with a connector.

3134. The system ofclaim 3109, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foimation.

3135. The system of claim 3109, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3136. The system ofclaim 3109, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is fuither disposed in cement.

3137. The system ofclaim 3109, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherehi a packing material is disposed at a junction of the overburden casing and the opening.

3138.* The system of claim 3109, further comprising an overburden casing coupled to the openmg, wherein the overburden casing is disposed hi an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3139. The system of claim 3109, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is electrically coupled to the first conductor.

3140. The system of claim 3109, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is electrically coupled to the first conductor, and wherein the substantially low resistance conductor comprises carbon steel.

3141. The system ofclaim 3109, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing and a centtalizer configurable to support the substantially low resistance conductor within the overburden casing.

3142. The system of claim 3109, wherein the heated section of the formation is substantially pyrolyzed.

3143. The system ofclaim 3109, wherein the system is configured to heat a relatively low permeability foimation containing heavy hydrocarbons, and wherein the system comprises: a first conductor disposed in a first conduit, wherein the first conduit is disposed within an opening in the formation, and wherein the first conductor is configured to provide heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to fransfer from the first conductor to a section of the formation during use.

3144. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an electrical cunent to a first conductor to provide heat to at least a portion of the formation, wherein the first conductor is disposed in a first conduit, and wherein the first conduit is disposed withhi an opening in the formation; and allowing the heat to fransfer from the first conductor to a section of the fonnation.

3145. The method of claim 3144, wherein the first conductor comprises a pipe.

3146. The method of claim 3144, wherein the first conductor comprises stainless steel.

3147. The method ofclaim 3144, wherein the first conduit comprises stainless steel.

3148. The method of claim 3144, further comprising maintaining a location of the first conductor in the ffrst conduit with a cenfralizer.

3149. The method of claim 3144, further comprising maintaining a location of the first conductor in the first conduit with a cenfralizer, wherein the cenfralizer comprises ceramic material.

3150. The method ofclaim 3144, further comprising maintaining a location of the first conductor in the first conduit with a cenfralizer, wherein the centtalizer comprises ceramic material and stainless steel.

3151. The method of claim 3144, further comprising couplmg a sliding elecfrical connector to the first conductor.

3152. The method of claim 3144, further comprising elecfrically coupling a sliding elecfrical connector to the first conductor and the first conduit, wherein the first conduit comprises an elecfrical lead configured to complete an elecfrical circuit with the first conductor.

3153. The method of claim 3144, further comprising coupling a sliding elecfrical connector to the first conductor and the first conduit, wherein the first conduit comprises an electrical lead configured to complete an elecfrical circuit with the first conductor, and wherein the generated heat comprises approximately 20 percent generated by the first conduit.

3154. The method of claim 3144, wherein the provided heat comprises approximately 650 W/m to approximately 1650 W/m.

3155. The method of claim 3144, further comprising deteπnining a temperature distribution in the first conduit using an electromagnetic signal provided to the conduit.

3156. The method of claim 3144, further comprising monitoring the applied electrical cunent.

3157. The method of claim 3144, fuither comprising monitoring a voltage applied to the first conductor.

3158. The method of clahn 3144, further comprising monitoring a temperature in the conduit with at least one thermocouple.

3159. The method of claim 3144, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3160. The method of claim 3144, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed hi an overburden of the formation, and wherein the overburden casing comprises steel.

3161. The method of claim 3144, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing is further disposed in cement.

3162. The method of claim 3144, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3163. The method ofclaim 3144, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with a packing material.

3164. The method of claim 3144, further comprising coupling an overburden casing to the opening, wherein a substantially low resistance conductor is disposed within the overburden casing, and wherein the substantially low resistance conductor is electrically coupled to the first conductor.

3165. The method of claim 3144, further comprising coupling an overburden casing to the opening, wherein a substantially low resistance conductor is disposed within the overburden casing, wherein the substantially low resistance conductor is electrically coupled to the first conductor, and wherein the substantially low resistance conductor comprises carbon steel.

3166. The method of claim 3144, further comprishig coupling an overburden casing to the opening, wherein a substantially low resistance conductor is disposed within the overburden casing, wherein the substantially low resistance conductor is electtically coupled to the first conductor, and wherein the method further comprises maintaining a location of the substantially low resistance conductor in the overburden casing with a centralizer support.

3167. The method ofclaim 3144, further comprismg electtically coupling a lead-in conductor to the first conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3168. The method of claim 3144, further comprising elecfrically coupling a lead-in conductor to the first conductor, wherein the lead-in conductor comprises copper.

3169. The method of claim 3144, further comprising maintaining a sufficient pressure between the first conduit and the formation to substantially inhibit deformation of the first conduit.

3170. The method of claim 3144, fuither comprising providing a thennally conductive fluid within the first conduit.

3171. The method of claim 3144, further comprising providing a thermally conductive fluid within the first conduit, wherein the thermally conductive fluid comprises helium.

3172. The method ofclaim 3144, further comprising inhibiting arcing between the first conductor and the first conduit with a fluid disposed within the first conduit.

3173. The method ofclaim 3144, further comprising removing a vapor from the opening using a perforated tube disposed proximate to the first conduit in the openhig to control a pressure in the opening.

3174. The method of claim 3144, further comprising flowing a conosion inhibiting fluid through a perforated tube disposed proximate to the first conduit in the opening.

3175. The method ofclaim 3144, wherein a second conductor is disposed within the first conduit, wherein the second conductor is elecfrically coupled to the first conductor to form an elecfrical circuit.

3176. The method of claim 3144, wherein a second conductor is disposed within the first conduit, wherein the second conductor is electrically coupled to the first conductor with a connector.

3177. The method ofclaim 3144, wherein a second conductor is disposed within a second conduit and a third conductor is disposed within a third conduit, wherein the second conduit and the thfrd conduit are disposed in different openings of the formation, wherein the first conductor is electrically coupled to the second conductor and the third conductor, and wherein the first, second, and third conductors are configured to operate in a 3-phase Y configuration.

3178. The method of claim 3144, wherein a second conductor is disposed within the first conduit, wherein at least one sliding elecfrical connector is coupled to the first conductor and the second conductor, and wherein heat generated by at least the one sliding electrical connector is less than heat generated by the ffrst conductor or the second conductor.

3179. The method of claim 3144, wherein the first conduit comprises a first section and a second section, wherehi a thickness of the first section is greater than a thickness of the second section such that heat radiated from the first conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3180. The method of clahn 3144, further comprising flowing an oxidizing fluid through an orifice in the first conduit.

3181. The method of claim 3144, further comprising disposing a perforated tube proximate to the first conduit and flowing an oxidizing fluid through the perforated tube.

3182. The method of claim 3144, fuither comprismg heating at least the portion of the foπnation to substantially pyrolyze at least some hydrocarbons within the formation.

3183. A system configured to heat a relatively low peπneability foπnation containing heavy hydrocarbons, comprising: a first conductor disposed in a first conduit, wherein the first conduit is disposed within a first opening in the formation; a second conductor disposed in a second conduit, wherein the second conduit is disposed within a second opening in the formation; a thfrd conductor disposed in a thfrd conduit, wherein the third conduit is disposed within a third opening in the formation, wherein the ffrst, second, and thfrd conductors are electrically coupled in a 3-phase Y configuration, and wherehi the first, second, and third conductors are configured to provide heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to fransfer from the first, second, and third conductors to a selected section of the foπnation during use.

3184. The system of claim 3183, wherein the first, second, and third conductors are further configured to generate heat during application of an electrical cunent to the fh-st conductor.

3185. The system of claim 3183, wherein the first, second, and third conductors comprise a pipe.

3186. The system of claim 3183 , wherein the first, second, and third conductors comprise stainless steel.

3187. The system ofclaim 3183, wherein the first, second, and thfrd openings comprise a diameter of at least approximately 5 cm.

3188. The system of claim 3183, further comprishig a first sliding elecfrical connector coupled to the first conductor and a second sliding elecfrical connector coupled to the second conductor and a third sliding elecfrical connector coupled to the third conductor.

3189. The system of claim 3183, further comprising a first sliding electrical connector coupled to the first conductor, wherein the first sliding elecfrical connector is further coupled to the first conduit.

3190. The system ofclaim 3183, further comprising a second sliding elecfrical connector coupled to the second conductor, wherein the second sliding elecfrical connector is further coupled to the second conduit.

3191. The system ofclaim 3183, further comprising a third sliding elecfrical connector coupled to the third conductor, wherein the third sliding elecfrical connector is furtlier coupled to the third conduit.

3192. The system ofclaim 3183, wherein each of the first, second, and third conduits comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from each of the first, second, and third conductors to the section along the first section of each of the conduits is less than heat radiated from the first, second, and third conductors to the section along the second section of each of the conduits.

3193. The system ofclaim 3183, further comprising a fluid disposed within the first, second, and third conduits, wherein the fluid is configured to maintain a pressure within the first conduit to substantially inhibit deformation of the first, second, and third conduits during use.

3194. The system ofclaim 3183, further comprising a thermally conductive fluid disposed within the first, second, and third conduits.

3195. The system of claim 3183, further comprising a thermally conductive fluid disposed within the first, second, and thfrd conduits, wherein the thermally conductive fluid comprises helium.

3196. The system ofclaim 3183, further comprising a fluid disposed within the first, second, and third conduits, wherein the fluid is configured to substantiaUy inhibit arcing between the first, second, and third conductors and the first, second, and third conduits during use.

3197. The system ofclaim 3183, further comprising at least one tube disposed within the first, second, and third openings external to the first, second, and thfrd conduits, wherein at least the one tube is configured to remove vapor produced from at least the heated portion of the formation such that a pressure balance is maintained between the first, second, and third conduits and the ffrst, second, and third openings to substantially inhibit deformation of the first, second, and third conduits during use.

3198. The system ofclaim 3183, wherein the first, second, and third conductors are further configured to generate radiant heat of approxhnately 650 W/m to approximately 1650 W/m during use.

3199. The system of claim 3183, furtlier comprising at least one overburden casing coupled to the first, second, and third openings, wherein at least the one overburden casing is disposed in an overburden of the formation.

3200. The system ofclaim 3183, further comprising at least one overburden cashig coupled to the first, second, and third openings, wherein at least the one overburden casing is disposed in an overburden of the formation, and wherein at least the one overburden casing comprises steel.

3201. The system of claim 3183 , further comprising at least one overburden casing coupled to the first, second, and third openings, wherein at least the one overburden casing is disposed in an overburden of the fonnation, and wherein at least the one overburden casing is further disposed in cement.

3202. The system ofclaim 3183, further comprising at least one overburden casing coupled to the first, second, and thfrd openings, wherein at least the one overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at ajunction of at least the one overburden casing and the first, second, and third openings.

3203. The system ofclaim 3183, further comprising at least one overburden casing coupled to the first, second, and thfrd openings, wherein at least the one overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at ajunction of at least the one overburden casing and the first, second, and thfrd openings, and wherein the packing material is further configured to substantially inhibit a flow of fluid between the first, second, and third openings and at least the one overburden casing during use.

3204. The system of claim 3183, wherein the heated section of the foπnation is substantially pyrolyzed.

3205. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a first conductor configurable to be disposed in a first conduit, wherein the first conduit is configurable to be disposed within a first opening in the formation; a second conductor configurable to be disposed in a second conduit, wherein the second conduit is configurable to be disposed within a second opening in the formation; a third conductor configurable to be disposed in a thfrd conduit, wherein the third conduit is configurable to be disposed within a third opening in the foπnation, wherein the first, second, and third conductors are further configurable to be elecfrically coupled in a 3-phase Y configuration, and wherein the first, second, and thfrd conductors are further configurable to provide heat to at least a portion of the formation during use; and wherein the system is configurable to allow heat to fransfer from the first, second, and third conductors to a selected section of the formation during use.

3206. The system ofclaim 3205, wherehi the first, second, and third conductors are further configurable to generate heat during application of an electrical cunent to the first conductor.

3207. The system ofclaim 3205, wherein the first, second, and third conductors comprise a pipe.

3208. The system of claim 3205, wherein the first, second, and third conductors comprise stainless steel.

3209. The system ofclaim 3205, wherein each of the first, second, and third openings comprises a diameter of at least approxhnately 5 cm.

3210. The system ofclaim 3205, further comprising a first sliding elecfrical connector coupled to the first conductor and a second sliding elecfrical connector coupled to the second conductor and a third sliding elecfrical connector coupled to the third conductor.

3211. The system ofclaim 3205, further comprising a first sliding electrical connector coupled to the first conductor, wherein the first sliding elecfrical connector is further coupled to the first conduit.

3212. The system ofclaim 3205, further comprising a second sliding electrical connector coupled to the second conductor, wherein the second sliding electrical connector is further coupled to the second conduit.

3213. The system of claim 3205, further comprising a third sliding elecfrical connector coupled to the third conductor, wherein the third sliding electrical connector is further coupled to the third conduit.

3214. The system of claim 3205, wherein each of the first, second, and thfrd conduits comprises a first section and a second section, wherehi a thickness of the ffrst section is greater than a thickness of the second section such that heat radiated from each of the first, second, and third conductors to the section along the first section of each of the conduits is less than heat radiated from the first, second_hand third conductors to the section along the second section of each of the conduits.

3215. The system of claim 3205, further comprising a fluid disposed within the first, second, and third conduits, wherein the fluid is configurable to maintain a pressure within the ffrst conduit to substantially inhibit deformation of the first, second, and third conduits during use.

3216. The system of claim 3205, further comprising a thermally conductive fluid disposed within the first, second, and third conduits.

3217. The system ofclaim 3205, further comprising a thermally conductive fluid disposed within the first, second, and third conduits, wherein the thermally conductive fluid comprises helium.

3218. The system of claim 3205, further comprising a fluid disposed withhi the first, second, and third conduits, wherein the fluid is configurable to substantially inhibit arcing between the first, second, and third conductors and the first, second, and third conduits during use.

3219. The system of claim 3205, further comprishig at least one tube disposed within the first, second, and third openings external to the first, second, and third conduits, wherein at least the one tube is configurable to remove vapor produced from at least the heated portion of the formation such that a pressure balance is maintained between the first, second, and third conduits and the fnst, second, and thfrd openings to substantially inhibit deformation of the first, second, and third conduits during use.

3220. The system ofclaim 3205, wherein the first, second, and third conductors are further configurable to generate radiant heat of approximately 650 W/m to approximately 1650 W/m during use.

3221. The system ofclaim 3205, further comprising at least one overburden casing coupled to the first, second, and third openings, wherein at least the one overburden casing is disposed in an overburden of the fonnation.

3222. The system ofclaim 3205, further comprising at least one overburden casing coupled to the first, second, and third openings, wherein at least the one overburden casing is disposed in an overburden of the formation, and wherein at least the one overburden casing comprises steel.

3223. The system ofclaim 3205, furtlier comprising at least one overburden casing coupled to the first, second, and third openings, wherein at least the one overburden casing is disposed in an overburden of the formation, and wherein at least the one overburden casing is further disposed in cement.

3224. The system ofclaim 3205, further comprishig at least one overburden casing coupled to the ffrst, second, and thfrd openings, wherein at least the one overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at ajunction of at least the one overburden casing and the first, second, and third openings.

3225. The system ofclaim 3205, further comprising at least one overburden casing coupled to the first, second, and third openings, wherein at least the one overburden cashig is disposed in an overburden of the formation, wherein a packing material is disposed at ajunction of at least the one overburden casing and the first, second, and third openings, and wherein the packing material is further configurable to substantially inhibit a flow of fluid between the first, second, and thfrd openings and at least the one overburden casing during use.

3226. The system ofclaim 3205, wherein the heated section of the foπnation is substantially pyrolyzed.

3227. The system ofclaim 3205 wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a first conductor disposed in a first conduit, wherein the first conduit is disposed within a first opening in the foπnation; a second conductor disposed in a second conduit, wherein the second conduit is disposed within a second opening in the formation; a third conductor disposed in a third conduit, wherehi the third conduit is disposed within a thfrd opening in the formation, wherein the ffrst, second, and third conductors are electrically coupled in a 3-phase Y configuration, and wherein the ffrst, second, and third conductors are configured to provide heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to transfer from the first, second, and third conductors to a selected section of the formation during use.

3228. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprishig: applying an elecfrical cunent to a first conductor to provide heat to at least a portion of the formation, wherein the first conductor is disposed in a first conduit, and wherein the first conduit is disposed within a first opening in the foπnation; applying an elecfrical cunent to a second conductor to provide heat to at least a portion of the formation, wherein the second conductor is disposed in a second conduit, and wherehi the second conduit is disposed within a second opening in the formation; applying an electrical cunent to a thfrd conductor to provide heat to at least a portion of the foπnation, wherein the third conductor is disposed in a thfrd conduit, and wherein the third conduit is disposed within a third opening in the formation; and allowing the heat to fransfer from the first, second, and third conductors to a selected section of the formation.

3229. The method ofclaim 3228, wherein the ffrst, second, and thfrd conductors comprise a pipe.

3230. The method ofclaim 3228, wherein the ffrst, second, and third conductors comprise stainless steel.

3231. The method of claim 3228, wherein the first, second, and third conduits comprise stainless steel.

3232. The method of claim 3228, wherein the provided heat comprises approximately 650 W/m to approximately 1650 W/m.

3233. The method ofclaim 3228, further comprising determining a temperature distribution in the first, second, and third conduits using an electromagnetic signal provided to the first, second, and third conduits.

3234. The method of claim 3228, further comprising monitoring the applied electrical cunent.

3235. The method of claim 3228, further comprising monitoring a voltage applied to the first, second, and third conductors.

3236. The method of clahn 3228, further comprising monitoring a temperature in the first, second, and thfrd conduits with at least one thermocouple.

3237. The method of claim 3228, fuither comprising maintaining a sufficient pressure between the first, second, and third conduits and the first, second, and third openings to substantially inhibit deformation of the first, second, and third conduits.

3238. The method of clahn 3228, further comprising providing a thermally conductive fluid within the first, second, and third conduits.

3239. The method of clahn 3228, further comprising providing a thermally conductive fluid within the first, second, and third conduits, wherein the thermally conductive fluid comprises helium.

3240. The method ofclaim 3228, further comprising inhibiting arcing between the first, second, and third conductors and the first, second, and third conduits with a fluid disposed within the first, second, and thfrd conduits.

3241. The method of claim 3228, further comprising removing a vapor from the first, second, and third openings using at least one perforated tube disposed proxhnate to the first, second, and third conduits in the first, second, and third openings to control a pressure in the first, second, and third openings.

3242. The method ofclaim 3228, wherein the first, second, and third conduits comprise a first section and a second section, wherein a thickness of the fh-st section is greater than a thickness of the second section such that heat radiated from the first, second, and third conductors to the section along the first section of the ffrst, second, and thfrd conduits is less than heat radiated from the first, second, and thfrd conductors to the section along the second section of the first, second, and third conduits.

3243. The method of claim 3228, further comprising flowing an oxidizing fluid through an orifice in the first, second, and thfrd conduits.

3244. The method of claim 3228, further comprising heating at least the portion of the formation to substantially pyrolyze at least some hydrocarbons withhi the formation.

3245. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a first conductor disposed in a conduit, wherein the conduit is disposed within an opening in the formation; and a second conductor disposed in the conduit, wherein the second conductor is electrically coupled to the first conductor with a connector, and wherein the first and second conductors are configured to provide heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to transfer from the first and second conductors to a selected section of the formation during use.

3246. The system of claim 3245, wherein the first conductor is further configured to generate heat during application of an elecfrical cunent to the first conductor.

3247. The system ofclaim 3245, wherein the first and second conductors comprise a pipe.

3248. The system ofclaim 3245, wherein the first and second conductors comprise stainless steel.

3249. The system of clahn 3245, wherein the conduit comprises stainless steel.

3250. The system of claim 3245, further comprising a centralizer configured to maintain a location of the ffrst and second conductors within the conduit.

3251. The system of claim 3245, further comprising a cenfralizer configured to maintain a location of the first and second conductors within the conduit, wherein the cenfralizer comprises ceramic material.

3252. The system ofclaim 3245, further comprising a cenfralizer configured to maintain a location of the first and second conductors withhi the conduit, wherein the cenfralizer comprises ceramic material and stainless steel.

3253. The system of claim 3245, wherein the opening comprises a diameter of at least approximately 5 cm.

3254. The system of claim 3245, further comprising a lead-in conductor coupled to the ffrst and second conductors, wherehi the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3255. The system ofclaim 3245, further comprising a lead-in conductor coupled to the first and second conductors, wherein the lead-in conductor comprises copper.

3256. The system ofclaim 3245, wherein the conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the first conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3257. The system ofclaim 3245, further comprising a fluid disposed within the conduit, wherein the fluid is configured to maintain a pressure within the conduit to substantially inhibit deformation of the conduit during use.

3258. The system of claim 3245, further comprising a thermally conductive fluid disposed within the conduit.

3259. The system ofclaim 3245, further comprising a thermally conductive fluid disposed within the conduit, wherein the thermally conductive fluid comprises helium.

3260. The system of claim 3245, further comprising a fluid disposed within the conduit, wherein the fluid is configured to substantially inhibit arcing between the first and second conductors and the conduit during use.

3261. The system of claim 3245, further comprising a tube disposed within the opening external to the conduit, wherein the tube is configured to remove vapor produced from at least the heated portion of the foπnation such that a pressure balance is maintained between the conduit and the opening to substantially inhibit deformation of the conduit during use.

3262. The system of claim 3245, wherein the ffrst and second conductors are ftuther configured to generate radiant heat of approxhnately 650 W/m to approximately 1650 W/m during use.

3263. The system ofclaim 3245, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3264. The system ofclaim 3245, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3265. The system ofclaim 3245, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

3266. The system ofclaim 3245, further comprising an overburden casing coupled to the openhig, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3267. The system ofclaim 3245, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3268. The system of claim 3245, wherein the heated section of the formation is substantially pyrolyzed.

3269. A system configurable to heat a relatively low permeability fonnation containing heavy hydrocarbons, comprising: a first conductor configurable to be disposed in a conduit, wherein the conduit is configurable to be disposed within an opening in the formation; and a second conductor configurable to be disposed in the conduit, wherein the second conductor is configurable to be elecfrically coupled to the ffrst conductor with a connector, and wherein the first and second conductors are further configurable to provide heat to at least a portion of the foπnation during use; and wherein the system is configurable to allow heat to transfer from the first and second conductors to a selected section of the formation during use.

3270. The system ofclaim 3269, wherein the first conductor is further configurable to generate heat during application of an electrical cunent to the first conductor.

3271. The system of clahn 3269, wherein the ffrst and second conductors comprise a pipe.

3272. The system ofclaim 3269, wherein the first and second conductors comprise stainless steel.

3273. The system ofclaim 3269, whefein the conduit comprises stainless steel.

3274. The system ofclaim 3269, further comprising a cenfralizer configurable to maintain a location of the first and second conductors within the conduit.

3275. The system o claim 3269, further comprising a cenfralizer configurable to maintain a location of the first and second conductors within the conduit, wherein the cenfralizer comprises ceramic material.

3276. The "system ofclaim 3269, further comprising a centralizer configurable to maintain a location of the ffrst and second conductors within the conduit, wherein the centralizer comprises ceramic material and stainless steel.

3277. The system ofclaim 3269, wherein the opening comprises a diameter of at least approxhnately 5 cm.

3278. The system of clahn 3269, further comprising a lead-in conductor coupled to the first and second conductors, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

3279. The system ofclaim 3269, further comprising a lead-in conductor coupled to the first and second conductors, wherein the lead-in conductor comprises copper.

3280. The system ofclaim 3269, wherein the conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the first conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3281. The system of claim 3269, further comprising a fluid disposed within the conduit, wherein the fluid is configurable to maintain a pressure within the conduit to substantially inhibit deformation of the conduit during use.

3282. The system of claim 3269, further comprising a thermally conductive fluid disposed within the conduit.

3283. The system of clahn 3269, further comprising a thermally conductive fluid disposed within the conduit, wherein the thermally conductive fluid comprises helium.

3284. The system of claim 3269, further comprising a fluid disposed within the conduit, wherein the fluid is configurable to substantially inhibit arcing between the first and second conductors and the conduit during use.

3285. The system ofclaim 3269, further comprising a tube disposed within the opening external to the conduit, wherein the tube is configurable to remove vapor produced from at least the heated portion of the formation such that a pressure balance is maintained between the conduit and the opening to substantially inhibit defonnation of the conduit during use.

3286. The system ofclaim 3269, wherein the first and second conductors are further configurable to generate radiant heat of approximately 650 W/m to approximately 1650 W/m during use.

3287. The system of claim 3269, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation.

3288. The system ofclaim 3269, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing comprises steel.

3289. The system of clahn 3269, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3290. The system ofclaim 3269, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3291. The system of claim 3269, further comprising an overburden casing coupled to the openhig, wherein the overburden casing is disposed in an overburden of the formation, wherein a packhig material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3292. The system of claim 3269, wherein the heated section of the foπnation is substantially pyrolyzed.

3293. The system ofclaim 3269, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a first conductor disposed in a conduit, wherein the conduit is disposed within an opening in the fonnation; a second conductor disposed in the conduit, wherein the second conductor is elecfrically coupled to the first conductor with a connector, and wherein the first and second conductors are configured to provide heat to at least a portion of the foπnation during use; and wherein the system is configured to allow heat to fransfer from the first and second conductors to a selected section of the formation during use.

3294. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an electrical cunent to at least two conductors to provide heat to at least a portion of the formation, wherein at least the two conductors are disposed within a conduit, wherein the conduit is disposed within an opening in the formation, and wherein at least the two conductors are elecfrically coupled with a connector; and allowing heat to transfer from at least the two conductors to a selected section of the formation.

3295. The method of claim 3294, wherein at least the two conductors comprise a pipe.

3296. The method of claim 3294, wherein at least the two conductors comprise stainless steel.

3297. The method ofclaim 3294, wherein the conduit comprises stainless steel.

3298. The method ofclaim 3294, further comprishig maintaining a location of at least the two conductors in the conduit with a cenfralizer.

3299. The method ofclaim 3294, further comprising maintaining a location of at least the two conductors in the conduit with a cenfralizer, wherein the cenfralizer comprises ceramic material.

3300. The method ofclaim 3294, further comprising maintaining a location of at least the two conductors in the conduit with a cenfralizer, wherein the cenfralizer comprises ceramic material and stainless steel.

3301. The method of claim 3294, wherein the provided heat comprises approximately 650 W/m to approximately 1650 W/m.

3302. The method ofclaim 3294, further comprising determining a temperature distribution in the conduit using an electromagnetic signal provided to the conduit.

3303. The method of claim 3294, further comprising monitoring the applied electrical cunent.

3304. The method of clahn 3294, further comprising monitoring a voltage applied to at least the two conductors.

3305. The method ofclaim 3294, further comprising monitoring a temperature in the conduit with at least one thermocouple.

3306. The method of clahn 3294, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3307. The method of clahn 3294, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foimation, and wherein the overburden casing comprises steel.

3308. The method of claim 3294, further comprising coupling an overburden casing to the opening, wherein the overburden cashig is disposed in an overburden of the formation, and wherehi the overburden casing is further disposed in cement.

3309. The method ofclaim 3294, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3310. The method of claim 3294, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with a packing material.

3 11. The method ofclaim 3294, further comprismg maintaining a sufficient pressure between the conduit and the formation to substantially inhibit defonnation of the conduit.

3312. The method of claim 3294, further comprismg providing a thermally conductive fluid within the conduit.

3313. The method ofclaim 3294, further comprising providing a thermally conductive fluid within the conduit, wherein the thermally conductive fluid comprises helium.

3314. The method of claim 3294, further comprising inhibiting arcing between at least the two conductors and the conduit with a fluid disposed within the conduit.

3315. The method ofclaim 3294, further comprising removing a vapor from the opening using a perforated tube disposed proximate to the conduit in the opening to confrol a pressure in the opening.

3316. The method ofclaim 3294, further comprising flowing a conosion inhibiting fluid through a perforated tube disposed proximate to the conduit in the opening.

3317. The method of clahn 3294, wherein the conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the first conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3318. The method of claim 3294, further comprising flowing an oxidizing fluid through an orifice in the conduit.

3319. The method of claim 3294, further comprising disposing a perforated tube proximate to the conduit and flowing an oxidizing fluid through the perforated tube.

3320. The method of claim 3294, further comprising heating at least the portion of the formation to substantially pyrolyze at least some hydrocarbons within the formation.

3321. A system configured to heat a relatively low permeability foπnation containing heavy hydrocarbons, comprising: at least one conductor disposed in a conduit, wherein the conduit is disposed within an opening in the formation, and wherein at least the one conductor is configured to provide heat to at least a first portion of the formation during use; at least one sliding connector, wherein at least the one sliding connector is coupled to at least the one conductor, wherein at least the one sliding connector is configured to provide heat during use, and wherein heat provided by at least the one sliding connector is substantiaUy less than the heat provided by at least the one conductor during use; and wherein the system is configured to allow heat to fransfer from at least the one conductor to a section of the formation during use.

3322. The system ofclaim 3321, wherein at least the one conductor is further configured to generate heat during application of an elecfrical cunent to at least the one conductor.

3323. The system ofclaim 3321, wherein at least the one conductor comprises a pipe.

3324. The system ofclaim 3321, wherein at least the one conductor comprises stainless steel.

3325. The system ofclaim 3321, wherein the conduit comprises stainless steel.

3326. The system ofclaim 3321, further comprising a cenfralizer configured to maintain a location of at least the one conductor within the conduit.

3327. The system ofclaim 3321, further comprising a centralizer configured to maintain a location of at least the one conductor within the conduit, wherein the centtalizer comprises ceramic material.

3328. The system of claim 3321 , further comprising a cenfralizer configured to maintain a location of at least the one conductor within the conduit, wherein the cenfralizer comprises ceramic material and stainless steel.

3329. The system of claim 3321, wherein the opening comprises a diameter of at least approxhnately 5 cm.

3330. The system ofclaim 3321, further comprising a lead-in conductor coupled to at least the one conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3331. The system ofclaim 3321, further comprising a lead-in conductor coupled to at least the one conductor, wherein the lead-in conductor comprises copper.

3332. The system ofclaim 3321, wherein the conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the ffrst conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3333. The system ofclaim 3321, further comprising a fluid disposed within the conduit, wherein the fluid is configured to maintain a pressure within the conduit to substantially inhibit deformation of the conduit during use.

3334. The system ofclaim 3321, further comprising a thennally conductive fluid disposed within the conduit.

3335. The system ofclaim 3321, further comprising a thermally conductive fluid disposed within the conduit, wherein the thermally conductive fluid comprises helium.

3336. The system of clahn 3321, further comprising a fluid disposed within the conduit, wherein the fluid is configured to substantially inhibit arcing between at least the one conductor and the conduit during use.

3337. The system ofclaim 3321, further comprising a tube disposed within the opening external to the conduit, wherein the tube is configured to remove vapor produced from at least the heated portion of the foimation such that a pressure balance is maintained between the conduit and the opening to substantially inhibit deformation of the conduit during use.

3338. The system ofclaim 3321, wherein at least the one conductor is further configured to generate radiant heat of approximately 650 W/m to approximately 1650 W/m during use.

3339. The system ofclaim 3321, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3340. The system ofclaim 3321, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3341. The system ofclaim 3321, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherehi the overburden casing is further disposed in cement.

3342. The system ofclaim 3321, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3343. The system of claim 3321, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configured to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3344. The system ofclaim 3321, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is electrically coupled to at least the one conductor.

3345. The system o claim 3321, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is elecfrically coupled to at least the one conductor, and wherein the substantially low resistance conductor comprises carbon steel.

3346. The system ofclaim 3321, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing and a cenfralizer configured to support the substantially low resistance conductor within the overburden casing.

3347. The system ofclaim 3321, wherein the heated section of the formation is substantially pyrolyzed.

3348. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: at least one conductor configurable to be disposed in a conduit, wherein the conduit is configurable to be disposed within an opening in the formation, and wherein at least the one conductor is further configurable to provide heat to at least a first portion of the formation during use; at least one sliding connector, wherein at least the one sliding connector is configurable to be coupled to at least the one conductor, wherein at least the one sliding connector is further configurable to provide heat during use, and wherein heat provided by at least the one sliding connector is substantially less than the heat provided by at least the one conductor during use; and wherein the system is configurable to allow heat to transfer from at least the one conductor to a section of the formation during use.

3349. The system of claim 3348, wherein at least the one conductor is further configurable to generate heat durmg application of an electrical cunent to at least the one conductor.

3350. The system ofclaim 3348, wherein at least the one conductor comprises a pipe.

3351. The system of clahn 3348, wherein at least the one conductor comprises stainless steel.

3352. The system ofclaim 3348, wherehi the conduit comprises stainless steel.

3353. The system ofclaim 3348, further comprising a cenfralizer configurable to maintain a location of at least the one conductor within the conduit.

3354. The system ofclaim 3348, further comprising a centralizer configurable to maintain a location of at least the one conductor within the conduit, wherein the cenfralizer comprises ceramic material.

3355. The system ofclaim 3348, further comprising a cenfralizer configurable to maintain a location of at least the one conductor within the conduit, wherein the cenfralizer comprises ceramic material and stainless steel.

3356. The system ofclaim 3348, wherein the opening comprises a diameter of at least approximately 5 cm.

3357. The system of claim 3348, further comprising a lead-in conductor coupled to at least the one conductor, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

3358. The system of clahn 3348, further comprising a lead-in conductor coupled to at least the one conductor, wherein the lead-in conductor comprises copper.

3359. The system ofclaim 3348, wherein the conduit comprises a first section and a second section, wherein a thickness of the first section is greater than a thickness of the second section such that heat radiated from the first conductor to the section along the first section of the conduit is less than heat radiated from the first conductor to the section along the second section of the conduit.

3360. The system of claim 3348, further comprising a fluid disposed within the conduit, wherein the fluid is configurable to maintain a pressure within the conduit to substantially inhibit deformation of the conduit during use.

3361. The system of clahn 3348, further comprising a thermally conductive fluid disposed within the conduit.

3362. The system of claim 3348, further comprising a thermally conductive fluid disposed withhi the conduit, wherein the thermally conductive fluid comprises helium.

3363. The system ofclaim 3348, further comprising a fluid disposed withhi the conduit, wherein the fluid is configurable to substantially inhibit arcing between at least the one conductor and the conduit during use.

3364. The system of claim 3348, further comprising a tube disposed within the opening external to the conduit, wherein the tube is configurable to remove vapor produced from at least the heated portion of the foimation such that a pressure balance is maintained between the conduit and the opening to substantially inhibit deformation of the conduit during use.

3365. The system of clahn 3348, wherein at least the one conductor is further configurable to generate radiant heat of approximately 650 W/m to approximately 1650 W/m during use.

3366. The system ofclaim 3348, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3367. The system ofclaim 3348, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing comprises steel.

3368. The system ofclaim 3348, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing is further disposed in cement.

3369. The system of claim 3348, further comprising an overburden casing coupled to the opening, wherehi the overburden casing is disposed in an overburden of the foπnation, and wherein a packing material is disposed at a junction of the overburden casing and the openhig.

3370. The system of claim 3348, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3371. The system ofclaim 3348, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is electrically coupled to at least the one conductor.

3372. The system ofclaim 3348, further comprismg an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing, wherein the substantially low resistance conductor is elecfrically coupled to at least the one conductor, and wherein the substantially low resistance conductor comprises carbon steel.

3373. The system o claim 3348, further comprising an overburden casing coupled to the opening and a substantially low resistance conductor disposed within the overburden casing and a cenfralizer configurable to • support the substantially low resistance conductor within the overburden casing.

3374. The system ofclaim 3348, wherein the heated section of the formation is substantially pyrolyzed.

3375. The system of claim 3348, wherein the system is configured to heat a relatively low permeability foπnation containing heavy hydrocarbons, and wherein the system comprises: at least one conductor disposed in a conduit, wherein the conduit is disposed within an opening in the formation, and wherein at least the one conductor is configured to provide heat to at least a first portion of the formation during use; at least one sliding connector, wherein at least the one sliding connector is coupled to at least the one conductor, wherein at least the one sliding connector is configured to provide heat during use, and wherein heat provided by at least the one sliding connector is substantially less than the heat provided by at least the one conductor during use; and wherein the system is configured to allow heat to fransfer from at least the one conductor to a section of the formation during use.

3376. An in situ method for heating a relatively low peπneability formation containing heavy hydrocarbons, comprising: applying an elecfrical cunent to at least one conductor and at least one sliding connector to provide heat to at least a portion of the formation, wherein at least the one conductor and at least the one sliding connector are disposed within a conduit, and wherein heat provided by at least the one conductor is substantially greater than heat provided by at least the one sliding connector; and allowing the heat to transfer from at least the one conductor and at least the one sliding connector to a section of the foπnation.

3377. The method ofclaim 3376, wherein at least the one conductor comprises a pipe.

3378. The method ofclaim 3376, wherein at least the one conductor comprises stainless steel.

3379. The method of claim 3376, wherein the conduit comprises stainless steel.

3380. The method of claim 3376, further comprising maintaining a location of at least the one conductor in the conduit with a centtalizer.

3381. The method of claim 3376, further comprising maintaining a location of at least the one conductor in the conduit with a centtalizer, wherein the cenfralizer comprises ceramic material.

3382. The method of claim 3376, further comprising maintaining a location of at least the one conductor in the conduit with a centralizer, wherein the centralizer comprises ceramic material and stainless steel.

3383. The method ofclaim 3376, wherein the provided heat comprises approximately 650 W/m to approximately 1650 W/m.

3384. The method of clahn 3376, further comprishig determining a temperature disfribution in the conduit using an electromagnetic signal provided to the conduit.

3385. The method ofclaim 3376, further comprising monitoring the applied elecfrical cunent.

3386. The method ofclaim 3376, further comprising monitoring a voltage applied to at least the one conductor.

3387. The method ofclaim 3376, further comprising monitoring a temperature in the conduit with at least one thermocouple.

3388. The method ofclaim 3376, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the fonnation.

3389. The method ofclaim 3376, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing comprises steel.

3390. The method ofclaim 3376, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3391. The method of claim 3376, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherehi a packing material is disposed at a junction of the overburden casing and the opening.

3392. The method ofclaim 3376, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with a packing material.

3393. The method of claim 3376, further comprising coupling an overburden casing to the opening, wherein a substantially low resistance conductor is disposed within the overburden casing, and wherein the substantially low resistance conductor is electtically coupled to at least the one conductor.

3394. The method of clahn 3376, further comprising coupling an overburden casing to the opening, wherein a substantially low resistance conductor is disposed within the overburden casing, wherein the substantially low resistance conductor is electtically coupled to at least the one conductor, and wherein the substantially low resistance conductor comprises carbon steel.

3395. The method ofclaim 3376, further comprising coupling an overburden casing to the opening, wherein a substantially low resistance conductor is disposed within the overburden casing, wherein the substantially low resistance conductor is electtically coupled to at least the one conductor, and wherein the method further comprises maintaining a location of the substantially low resistance conductor in the overburden casing with a centtalizer support.

3396. The method of clahn 3376, further comprising electrically coupling a lead-in conductor to at least the one conductor, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3397. The method ofclaim 3376, further comprising electtically coupling a lead-in conductor to at least the one conductor, wherein the lead-in conductor comprises copper.

3398. The method ofclaim 3376, further comprising maintaining a sufficient pressure between the conduit and the foimation to substantially inhibit defonnation of the conduit.

3399. The method ofclaim 3376, further comprising providing a thermally conductive fluid within the conduit.

3400. The method of claim 3376, further comprising providing a thermally conductive fluid within the conduit, wherein the thermally conductive fluid comprises helium.

3401. The method ofclaim 3376, further comprising inhibiting arcing between the conductor and the conduit with a fluid disposed within the conduit.

3402. The method of claim 3376, further comprising removing a vapor from the opening using a perforated tube disposed proximate to the conduit in the opening to control a pressure in the openhig.

3403. The method ofclaim 3376, further comprising flowing a conosion inhibiting fluid through a perforated tube disposed proxhnate to the conduit in the opening.

3404. The method ofclaim 3376, further comprising flowing an oxidizing fluid through an orifice in the conduit.

3405. The method ofclaim 3376, further comprising disposing a perforated tube proximate to the conduit and flowing an oxidizing fluid through the perforated tube.

3406. The method of clahn 3376, further comprising heating at least the portion of the formation to substantially pyrolyze at least some hydrocarbons withhi the foπnation.

3407. A system configured to heat a relatively low peπneability formation containing heavy hydrocarbons, comprising: at least one elongated member disposed within an opening in the formation, wherein at least the one elongated member is configured to provide heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to ttansfer from at least the one elongated member to a section of the formation during use.

3408. The system of claim 3407, wherein at least the one elongated member comprises stainless steel.

3409. The system of claim 3407, wherein at least the one elongated member is further configured to generate heat during application of an electrical cunent to at least the one elongated member.

3410. The system ofclaim 3407, further comprising a support member coupled to at least the one elongated member, wherein the support member is configured to support at least the one elongated member.

3411. The system of claim 3407, furtlier comprising a support member coupled to at least the one elongated member, wherein the support member is configured to support at least the one elongated member, and wherein the support member comprises openings.

3412. The system of claim 3407, further comprising a support member coupled to at least the one elongated member, wherein the support member is configured to support at least the one elongated member, wherein the support member comprises openings, wherein the openings are configured to flow a fluid along a length of at least the one elongated member during use, and wherein the fluid is configured to substantially inhibit carbon deposition on or proxhnate to at least the one elongated member during use.

3413. The system of clahn 3407, further comprismg a tube disposed in the opening, wherein the tube comprises openings, wherein the openings are configured to flow a fluid along a length of at least the one elongated member during use, and wherein the fluid is configured to substantially inhibit carbon deposition on or proximate to at least the one elongated member during use.

3414. The system ofclaim 3407, further comprising a centtalizer coupled to at least the one elongated member, wherein the centralizer is configured to electrically isolate at least die one elongated member.

3415. The system ofclaim 3407, further comprising a cenfralizer coupled to at least the one elongated member and a support member coupled to at least the one elongated member, wherein the cenfralizer is configured to maintain a location of at least the one elongated member on the support member.

3416. The system ofclaim 3407, wherein the opening comprises a diameter of at least approxhnately 5 cm.

3417. The system ofclaim 3407, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3418. The system ofclaim 3407, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a rubber insulated conductor.

3419. The system ofclaim 3407, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises copper wire.

3420. The system ofclaim 3407, further comprising a lead-in conductor coupled to at least the one elongated member with a cold phi fransition conductor.

3421. The system ofclaim 3407, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin fransition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

3422. The system ofclaim 3407, wherein at least the one elongated member is ananged in a series electrical configuration.

3423. The system ofclaim 3407, wherein at least the one elongated member is ananged in a parallel elecfrical configuration.

3424. The system of claim 3407, wherein at least the one elongated member is configured to generate radiant heat of approxhnately 650 W/m to approximately 1650 W/m during use.

3425. The system of claim 3407, further comprising a perforated tube disposed in the opening external to at least the one elongated member, wherein the perforated tube is configured to remove vapor from the opening to control a pressure in the opening during use.

3426. The system ofclaim 3407, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3427. The system of claim 3407, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing comprises steel.

3428. The system ofclaim 3407, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3429. The system of claim 3407, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3430. The system ofclaim 3407, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

3431. The system ofclaim 3407, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherehi the packing material is further configured to substantially mhibit a flow of fluid between the opening and the overburden casing during use.

3432. The system ofclaim 3407, wherein the heated section of the formation is substantially pyrolyzed.

3433. A system configurable to heat a relatively low peπneability foπnation containing heavy hydrocarbons, comprising: at least one elongated member configurable to be disposed within an opening in the fonnation, wherein at least the one elongated member is further configurable to provide heat to at least a portion of the formation during use; and wherein the system is configurable to allow heat to transfer from at least the one elongated member to a section of the formation during use.

3434. The system of claim 3433, wherein at least the one elongated member comprises stainless steel.

3435. The system ofclaim 3433, wherein at least the one elongated member is further configurable to generate heat during application of an electrical cunent to at least the one elongated member.

3436. The system ofclaim 3433, further comprising a support member coupled to at least the one elongated member, wherein the support member is configurable to support at least the one elongated member.

3437. The system ofclaim 3433, further comprising a support member coupled to at least the one elongated member, wherein the support member is configurable to support at least the one elongated member, and wherein the support member comprises openings.

3438. The system ofclaim 3433, further comprising a support member coupled to at least the one elongated member, wherehi the support member is configurable to support at least the one elongated member, wherein the support member comprises openings, wherein the openings are configurable to flow a fluid along a length of at least the one elongated member durmg use, and wherein the fluid is configurable to substantially inhibit carbon deposition on or proximate to at least the one elongated member during use.

3439. The system ofclaim 3433, further comprising a tube disposed in the opening, wherein the tube comprises openmgs, wherein the openings are configurable to flow a fluid along a length of at least the one elongated member during use, and wherein the fluid is configurable to substantially inhibit carbon deposition on or proximate to at least the one elongated member during use.

3440. The system ofclaim 3433, further comprising a cenfralizer coupled to at least the one elongated member, wherein the centralizer is configurable to electrically isolate at least the one elongated member.

3441. The system ofclaim 3433, further comprising a centralizer coupled to at least the one elongated member and a support member coupled to at least the one elongated member, wherein the centralizer is configurable to maintain a location of at least the one elongated member on the support member.

3442. The system ofclaim 3433, wherein the opening comprises a diameter of at least approximately 5 cm.

3443. The system ofclaim 3433, furtlier comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

3444. The system ofclaim 3433, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a rubber insulated conductor.

3445. The system ofclaim 3433, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises copper wire.

3446. The system ofclaim 3433, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin transition conductor.

3447. The system ofclaim 3433, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin transition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

3448. The system of claim 3433, wherein at least the one elongated member is ananged in a series electrical configuration.

3449. The system ofclaim 3433, wherein at least the one elongated member is ananged in a parallel elecfrical configuration.

3450. The system of clahn 3433, wherein at least the one elongated member is configurable to generate radiant heat of approxhnately 650 W/m to approximately 1650 W/m during use.

3451. The system of claim 3433, further comprishig a perforated tube disposed in the opening external to at least the one elongated member, wherein the perforated tube is configurable to remove vapor from the opening to control a pressure in the opening during use.

3452. The system ofclaim 3433, further comprising an overburden casing coupled to the openhig, wherein the overburden casing is disposed in an overburden of the formation.

3453. The system ofclaim 3433, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3454. The system ofclaim 3433, further comprising an overburden casing coupled to the openmg, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing is further disposed in cement.

3455. The system ofclaim 3433, furtlier comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3456. The system ofclaim 3433, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foimation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

3457. The system ofclaim 3433, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3458. The system ofclaim 3433, wherein the heated section of the formation is substantially pyrolyzed.

3459. The system of claim 3433, wherein the system is configured to heat a relatively low permeability foπnation containing heavy hydrocarbons, and wherein the system comprises: at least one elongated member disposed within an opening in the formation, wherein at least the one elongated member is configured to provide heat to at least a portion of the foπnation during use; and wherein the system is configured to allow heat to fransfer from at least the one elongated member to a section of the formation during use.

3460. An in situ method for heating a relatively low peπneability formation containing heavy hydrocarbons, comprising: applying an electrical cunent to at least one elongated member to provide heat to at least a portion of the formation, wherein at least the one elongated member is disposed within an opening of the foπnation; and allowing heat to fransfer from at least the one elongated member to a section of the fonnation.

3461. The method ofclaim 3458, wherein at least the one elongated member comprises a metal strip.

3462. The method ofclaim 3458, wherein at least the one elongated member comprises a metal rod.

3463. The method ofclaim 3458, wherein at least the one elongated member comprises stainless steel.

3464. The method of claim 3458, further comprising supporting at least the one elongated member on a center support member.

3465. The method ofclaim 3458, further comprising supporting at least the one elongated member on a center support member, wherein the center support member comprises a tube.

3466. The method ofclaim 3458, further comprising elecfrically isolating at least the one elongated member with a centralizer.

3467. The method of claim 3458, further comprising laterally spacing at least the one elongated member with a centtalizer.

3468. The method of claim 3458, further comprising elecfrically coupling at least the one elongated member in a series configuration.

3469. The method of claim 3458, further comprising elecfrically coupling at least the one elongated member in a parallel configuration.

3470. The method ofclaim 3458, wherein the provided heat comprises approximately 650 W/m to approximately 1650 W/m.

3471. The method of claim 3458, further comprising determining a temperature disfribution in at least the one elongated member using an electromagnetic signal provided to at least the one elongated member.

3472. The method of clahn 3458, further comprising monitoring the applied elecfrical cunent.

3473. The method of claim 3458, further comprising monitoring a voltage applied to at least the one elongated member.

3474. The method ofclaim 3458, further comprising monitoring a temperature in at least the one elongated member with at least one thermocouple.

3475. The method ofclaim 3458, further comprising supporting at least the one elongated member on a center support member, wherein the center support member comprises openings, the method further comprising flowing an oxidizing fluid through the openings to substantially inhibit carbon deposition proximate to or on at least the one elongated member.

3476. The method of claim 3458, further comprising flowing an oxidizing fluid through a tube disposed proximate to at least the one elongated member to substantially inhibit carbon deposition proximate to or on at least the one elongated member.

3477. The method ofclaim 3458, further comprising flowing an oxidizing fluid through an opening in at least the one elongated member to substantially inhibit carbon deposition proximate to or on at least the one elongated member.

3478. The method ofclaim 3458, further comprising electrically coupling a lead-in conductor to at least the one elongated member, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantially no heat.

3479. The method of clahn 3458, further comprising elecfrically coupling a lead-in conductor to at least the one elongated member using a cold pin fransition conductor.

3480. The method of claim 3458, further comprising elecfrically coupling a lead-in conductor to at least the one elongated member using a cold pin fransition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

3481. The method of claim 3458, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3482. The method of claim 3458, further comprising coupling an overburden casing to the opening, wherein the overburden casing comprises steel.

3483. The method of clahn 3458, further comprising coupling an overburden cashig to the opening, wherein the overburden casing is disposed in cement.

3484. The method of clahn 3458, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

3485. The method of clahn 3458, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with the packing material.

3486. The method ofclaim 3458, further comprising heating at least the portion of the formation to substantially pyrolyze at least some hydrocarbons within the foπnation.

3487. A system configured to heat a relatively low permeability foπnation containing heavy hydrocarbons, comprising: at least one elongated member disposed within an opening in the foπnation, wherein at least the one elongated member is configured to provide heat to at least a portion of the formation during use; an oxidizing fluid source; a conduit disposed within the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to the opening during use, and wherein the oxidizing fluid is selected to substantially inhibit carbon deposition on or proximate to at least the one elongated member during use; and wherein the system is configured to allow heat to fransfer from at least the one elongated member to a section of the formation during use.

3488. The system ofclaim 3487, wherein at least the one elongated member comprises stainless steel.

3489. The system ofclaim 3487, wherein at least the one elongated member is further configured to generate heat during application of an elecfrical cunent to at least the one elongated member.

3490. The system ofclaim 3487, wherein at least the one elongated member is coupled to the conduit, wherein the conduit is further configured to support at least the one elongated member.

3491. The system ofclaim 3487, wherein at least the one elongated member is coupled to the conduit, wherein the conduit is further configured to support at least the one elongated member, and wherein the conduit comprises openings.

3492. The system ofclaim 3487, further comprising a cenfralizer coupled to at least the one elongated member and the conduit, wherein the cenfralizer is configured to electrically isolate at least the one elongated member from the conduit.

3493. The system of clahn 3487, further comprishig a centralizer coupled to at least the one elongated member and the conduit, wherein the centtalizer is configured to maintain a location of at least the one elongated member on the conduit.

3494. The system of claim 3487, wherein the opening comprises a diameter of at least approximately 5 cm.

3495. The system ofclaim 3487, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-hi conductor comprises a low resistance conductor configured to generate substantially no heat.

3496. The system of clahn 3487, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a rubber insulated conductor.

3497. The system ofclaim 3487, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises copper wire.

3498. The system ofclaim 3487, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin fransition conductor.

3499. The system ofclaim 3487, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin transition conductor, wherein the cold pin fransition conductor comprises a substantially low resistance insulated conductor.

3500. The system ofclaim 3487, wherein at least the one elongated member is ananged in a series elecfrical configuration.

3501. The system of claim 3487, wherein at least the one elongated member is ananged in a parallel electrical configuration.

3502. The system ofclaim 3487, wherein at least the one elongated member is configured to generate radiant heat of approximately 650 W/m to approximately 1650 W/m during use.

3503. The system ofclaim 3487, further comprising a perforated tube disposed in the opening external to at least the one elongated member, wherein the perforated tube is configured to remove vapor from the opening to confrol a pressure in the opening during use.

3504. The system ofclaim 3487, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3505. The system ofclaim 3487, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3506. The system of claim 3487, further comprising an overburden casing coupled to the opening, wherehi the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3507. The system ofclaim 3487, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packhig material is disposed at a junction of the overburden casing and the opening.

3508. The system of clahn 3487, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material comprises cement.

3509. The system ofclaim 3487, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configured to substantially inhibit a flow of fluid between the openhig and the overburden casing during use.

3510. The system ofclaim 3487, wherein the heated section of the formation is substantially pyrolyzed.

3511. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: at least one elongated member configurable to be disposed within an opening in the fonnation, wherein at least the one elongated member is further configurable to provide heat to at least a portion of the formation during use; a conduit configurable to be disposed within the opening, wherehi the conduit is further configurable to provide an oxidizing fluid from the oxidizing fluid source to the opening during use, and wherein the system is configurable to allow the oxidizing fluid to substantially inhibit carbon deposition on or proximate to at least the one elongated member during use; and wherein the system is further configurable to allow heat to transfer from at least the one elongated member to a section of the formation during use.

3512. The system ofclaim 3511, wherehi at least the one elongated member comprises stainless steel.

3513. The system ofclaim 3511, wherein at least the one elongated member is further configurable to generate heat during application of an electrical cunent to at least the one elongated member.

3514. The system ofclaim 3511, wherehi at least the one elongated member is coupled to the conduit, wherein the conduit is further configurable to support at least the one elongated member.

3515. The system ofclaim 3511, wherein at least the one elongated member is coupled to the conduit, wherein the conduit is further configurable to support at least the one elongated member, and wherein the conduit comprises openings.

3516. The system ofclaim 3511, further comprising a centralizer coupled to at least the one elongated member and the conduit, wherein the centralizer is configurable to electrically isolate at least the one elongated member from the conduit.

3517. The system of claim 3511, further comprising a centralizer coupled to at least the one elongated member and the conduit, wherem the centtalizer is configurable to maintain a location of at least the one elongated member on the conduit.

3518. The system ofclaim 3511, wherein the opening comprises a diameter of at least approximately 5 cm.

3519. The system of claim 3511, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a low resistance conductor configurable to generate substantially no heat.

3520. The system of claim 3511, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises a rubber insulated conductor.

3521. The system of claim 3511, further comprising a lead-in conductor coupled to at least the one elongated member, wherein the lead-in conductor comprises copper wire.

3522. The system ofclaim 3511, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin fransition conductor.

3523. The system ofclaim 3511, further comprising a lead-in conductor coupled to at least the one elongated member with a cold pin transition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

3524. The system ofclaim 3511, wherein at least the one elongated member is ananged in a series elecfrical configuration.

3525. The system ofclaim 3511, wherein at least the one elongated member is ananged in a parallel elecfrical configuration.

3526. The system ofclaim 3511, wherein at least the one elongated member is configurable to generate radiant heat' of approximately 650 W/m to approximately 1650 W/m during use.

3527. The system of claim 3511, further comprising a perforated tube disposed in the opening external to at least the one elongated member, wherein the perforated tube is configurable to remove vapor from the opening to confrol a pressure in the openmg during use.

3528. The system of claim 3511, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3529. The system of clahn 3511, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein the overburden casing comprises steel.

3530. The system ofclaim 3511, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3531. The system ofclaim 3511, furtlier comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the foπnation, and wherein a packing material is disposed at a junction of the overburden casing and the opening.

3532. The system ofclaim 3511, further comprising an overburden casing coupled to the opening, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the openhig, and wherein the packing material comprises cement.

3533. The system ofclaim 3511, further comprising an overburden casing coupled to the opening, wherehi the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at a junction of the overburden casing and the opening, and wherein the packing material is further configurable to substantially inhibit a flow of fluid between the opening and the overburden casing during use.

3534. The system of claim 3511, wherein the heated section of the formation is substantially pyrolyzed.

3535. The system ofclaim 3511, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: at least one elongated member disposed within an opening in the formation, wherein at least the one elongated member is configured to provide heat to at least a portion of the fonnation during use; an oxidizing fluid source; a conduit disposed within the opening, wherein the conduit is configured to provide an oxidizing fluid from the oxidizing fluid source to the opening during use, and wherein the oxidizing fluid is selected to substantially inhibit carbon deposition on or proxhnate to at least the one elongated member during use; and wherein the system is configured to allow heat to transfer from at least the one elongated member to a section of the fonnation during use.

3536. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an elecfrical cunent to at least one elongated member to provide heat to at least a portion of the formation, wherein at least the one elongated member is disposed within an opening in the formation; providing an oxidizing fluid to at least the one elongated member to substantially inhibit carbon deposition on or proximate to at least the one elongated member; and allowing heat to transfer from at least the one elongated member to a section of the foπnation.

3537. The method ofclaim 3536, wherein at least the one elongated member comprises a metal strip.

3538. The method ofclaim 3536, wherein at least the one elongated member comprises a metal rod.

3539. The method ofclaim 3536, wherein at least the one elongated member comprises stainless steel.

3540. The method ofclaim 3536, further comprising supporting at least the one elongated member on a center support member.

3541. The method of claim 3536, further comprising supporting at least the one elongated member on a center support member, wherein the center support member comprises a tube.

3542. The method ofclaim 3536, further comprising elecfrically isolating at least the one elongated member with a centtalizer.

3543. The method of claim 3536, further comprising laterally spacing at least the one elongated member with a cenfralizer.

3544. The method of claim 3536, further comprising electtically coupling at least the one elongated member in a series configuration.

3545. The method of claim 3536, further comprising electrically coupling at least the one elongated member in a parallel configuration.

3546. The method of clahn 3536, wherein the provided heat comprises approximately 650 W/m to approximately 1650 W/m.

3547. The method of clahn 3536, further comprising deteπnining a temperature distribution in at least the one elongated member using an electromagnetic signal provided to at least the one elongated member.

3548. The method of clahn 3536, further comprising monitoring the applied electrical cunent.

3549. The method ofclaim 3536, further comprising monitoring a voltage applied to at least the one elongated member.

3550. The method ofclaim 3536, further comprising monitoring a temperature in at least the one elongated member with at least one thermocouple.

3551. The method of clahn 3536, further comprising supporting at least the one elongated member on a center support member, wherein the center support member comprises openings, wherein providing the oxidizing fluid to at least the one elongated member comprises flowing the oxidizing fluid through the openings in the center support member.

3552. The method ofclaim 3536, wherein providing the oxidizing fluid to at least the one elongated member comprises flowing the oxidizing fluid through orifices in a tube disposed in the opening proximate to at least the one elongated member.

3553. The method ofclaim 3536, further comprising elecfrically coupling a lead-in conductor to at least the one elongated member, wherein the lead-in conductor comprises a low resistance conductor configured to generate substantiaUy no heat.

3554. The method ofclaim 3536, further comprising electrically coupling a lead-in conductor to at least the one elongated member using a cold pin transition conductor.

3555. The method ofclaim 3536, further comprising electrically coupling a lead-in conductor to at least the one elongated member using a cold pin transition conductor, wherein the cold pin transition conductor comprises a substantially low resistance insulated conductor.

3556. The method of claim 3536, further comprising coupling an overburden casing to the opening, wherein the overburden casing is disposed in an overburden of the formation.

3557. The method ofclaim 3536, further comprising coupling an overburden casing to the opening, wherein the overburden casing comprises steel.

3558. The method of claim 3536, further comprising couplhig an overburden casing to the opening, wherein the overburden cashig is disposed in cement.

3559. The method ofclaim 3536, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening.

3560. The method of clahn 3536, further comprising coupling an overburden casing to the opening, wherein a packing material is disposed at ajunction of the overburden casing and the opening, and wherein the method further comprises inhibiting a flow of fluid between the opening and the overburden casing with the packing material.

3561. The method ofclaim 3536, further comprising heating at least the portion of the formation to substantially pyrolyze at least some hydrocarbons within the formation.

3562. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: oxidizing a fuel fluid in a heater; providing at least a portion of the oxidized fuel fluid into a conduit disposed in an opening of the formation; allowing heat to ttansfer from the oxidized fuel fluid to a section of the formation; and allowing additional heat to transfer from an elecfric heater disposed in the opening to the section of the formation, wherein heat is allowed to fransfer substantially uniformly along a length of the opening.

3563. The method ofclaim 3562, wherein providing at least the portion of the oxidized fuel fluid into the opening comprises flowing the oxidized fuel fluid through a perforated conduit disposed in the opening.

3564. The method ofclaim 3562, wherein providing at least the portion of the oxidized fuel fluid into the opening comprises flowing the oxidized fuel fluid through a perforated conduit disposed in the opening, the method further comprising removing an exhaust fluid through the opening.

3565. The method ofclaim 3562, further comprising initiating oxidation of the fuel fluid in the heater with a flame.

3566. The method ofclaim 3562, further comprising removing the oxidized fuel fluid through the conduit.

3567. The method of claim 3562, further comprising removing the oxidized fuel fluid through the conduit and providing the removed oxidized fuel fluid to at least one additional heater disposed in the foπnation.

3568. The method of claim 3562, wherein the conduit comprises an insulator disposed on a surface of the conduit, the method further comprising tapering a thickness of the insulator such that heat is allowed to fransfer substantially uniformly along a length of the conduit.

3569. The method ofclaim 3562, wherein the elecfric heater is an insulated conductor.

3570. The method ofclaim 3562, wherein the electric heater is a conductor disposed in the conduit.

3571. The method ofclaim 3562, wherein the electric heater is an elongated conductive member.

3572. A system configured to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: one or more heat sources disposed within one or more open wellbores in the formation, wherehi the one or more heat sources are configured to provide heat to at least a portion of the formation during use; and wherein the system is configured to allow heat to fransfer from the one or more heat sources to a selected section of the formation during use.

3573. The system ofclaim 3572, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

3574. The system of claim 3572, wherein the one or more heat sources comprise elecfrical heaters.

3575. The system ofclaim 3572, wherein the one or more heat sources comprise surface burners.

3576. The system ofclaim 3572, wherein the one or more heat sources comprise flameless distributed combustors.

3577. The system ofclaim 3572, wherein the one or more heat sources comprise natural disfributed combustors.

3578. The system ofclaim 3572, wherein the one or more open wellbores comprise a diameter of at least approximately 5 cm.

3579. The system ofclaim 3572, further comprising an overburden casing coupled to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation.

3580. The system ofclaim 3572, further comprising an overburden casing coupled to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing comprises steel.

3581. The system ofclaim 3572, further comprising an overburden casing coupled to at least one of the one or more open wellbores, wherein the overburden cashig is disposed in an overburden of the formation, and wherein the overburden casing is fuither disposed in cement.

3582. The system ofclaim 3572, further comprising an overburden casing coupled to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation, and wherein a packing material is disposed at ajunction of the overburden cashig and the at least one of the one or more open wellbores.

3583. The system ofclaim 3572, further comprising an overburden casing coupled to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation, wherein a packhig material is disposed at ajunction of the overburden casing and the at least one of the one or more open wellbores, and wherein the packing material is configured to substantially inhibit a flow of fluid between at least one of the one or more open wellbores and the overburden casing during use.

3584. The system ofclaim 3572, further comprising an overburden casing coupled to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation, wherein a packing material is disposed at ajunction of the overburden casing and the at least one of the one or more open wellbores, and wherein the packing material comprises cement.

3585. The system ofclaim 3572, wherein the system is further configured to fransfer heat such that the fransfened heat can pyrolyze at least some hydrocarbons in the selected section.

3586. The system ofclaim 3572, further comprising a valve coupled to at least one of the one or more heat sources configured to control pressure within at least a majority of the selected section of the foπnation.

3587. The system ofclaim 3572, further comprising a valve coupled to aproduction well configured to confrol a pressure within at least a majority of the selected section of the formation.

3588. A method of treating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the foπnation, wherein the one or more heat sources are disposed within one or more open wellbores in the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; and producing a mixture from the formation.

3589. The method ofclaim 3588, wherehi the one or more heat sources comprise at least two heat sources, and wherehi supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

3590. The method ofclaim 3588, wherein controlling formation conditions comprises maintaining a temperature within the selected section within a pyrolysis temperature range with a lower pyrolysis temperature of about 250 °C and an upper pyrolysis temperature of about 400 °C.

3591. The method ofclaim 3588, wherein the one or more heat sources comprise electrical heaters.

3592. The method ofclaim 3588, wherein the one or more heat sources comprise surface burners.

3593. The method ofclaim 3588, wherein the one or more heat sources comprise flameless distributed combustors.

3594. The method of clahn 3588, wherein the one or more heat sources comprise natural disfributed combustors.

3595. The method ofclaim 3588, wherein the one or more heat sources are suspended within the one or more open wellbores.

3596. The method of claim 3588, wherein a tube is disposed in at least one of the one or more open wellbores proximate to the heat source, the method further comprising flowing a substantially constant amount of fluid into at least one of the one or more open wellbores through critical flow orifices in the tube.

3597. The method ofclaim 3588, wherein a perforated tube is disposed in at least one of the one or more open wellbores proximate to the heat source, the method further comprising flowing a conosion inhibiting fluid into at least one of the open wellbores through the perforated tube.

3598. The method ofclaim 3588, further comprising coupling an overburden casing to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the foπnation.

3599. The method ofclaim 3588, further comprising coupling an overburden casing to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the fonnation, and wherein the overburden casing comprises steel.

3600. The method ofclaim 3588, further comprising coupling an overburden casing to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation, and wherein the overburden casing is further disposed in cement.

3601. The method of claim 3588, further comprising coupling an overburden casing to at least one of the one or more open wellbores, wherein the overburden casing is disposed in an overburden of the formation, and wherehi a packing material is disposed at ajunction of the overburden casing and the at least one of the one or more open wellbores.

3602. The method ofclaim 3588, further comprising coupling an overburden casing to at least one of the one or more open wellbores, wherehi the overburden casing is disposed in an overburden of the foπnation, and wherein the method further comprises inhibiting a flow of fluid between the at least one of the one or more open wellbores and the overburden casing with a packing material.

3603. The method of clahn 3588, further comprising heating at least the portion of the fonnation to substantially pyrolyze at least some hydrocarbons within the fonnation.

3604. The method of claim 3588, further comprising confrolling a pressure and a temperature within at least a majority of the selected section of the foπnation, wherein the pressure is controlled as a function of temperature, or the temperature is confrolled as a function of pressure.

3605. The method ofclaim 3588, furtlier comprising controlling a pressure with the wellbore.

3606. The method ofclaim 3588, further comprising confrolling a pressure within at least a majority of the selected section of the formation with a valve coupled to at least one of the one or more heat sources.

3607. The method of claim 3588, further comprising confrolling a pressure within at least a majority of the selected section of the foπnation with a valve coupled to a production well located in the foπnation.

3608. The method of claim 3588, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1 °C per day during pyrolysis.

3609. The method of claim 3588, wherein providing heat from the one or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from the one or more heat sources, wherein the formation has an average heat capacity(C_v), and wherein the heating pyrolyzes at least some hydrocarbons withhi the selected volmne of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C_v*p_B wherein Pwr is the heating energy/day, h is an average heating rate of the formation, p_B is formation bulk density, and wherein the heating rate is less than about 10 °C/day.

3610. The method ofclaim 3588, wherein allowing the heat to transfer from the one or more heat sources to the selected section comprises fransfening heat substantially by conduction.

3611. The method of claim 3588, wherein the produced mixture comprises condensable hydrocarbons having an API gravity of at least about 25°.

3612. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3613. The method of clahn 3588, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3614. The method of clahn 3588, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein about 0.1 % by weight to about 15 % by weight of the non-condensable hydrocarbons are olefins.

3615. The method of clahn 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

3616. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3617. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3618. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3619. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3620. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherehi less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3621. The method ofclaim 3588, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3622. The method ofclaim 3588, wherein the produced mixture comprises a non-condensable component, wherehi the non-condensable component comprises hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable component and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

3623. The method of claim 3588, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3624. The method ofclaim 3588, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

3625. The method ofclaim 3588, further comprising controlling a pressure within at least a majority of the selected section of the foimation.

3626. The method ofclaim 3588, further comprising controlling a pressure within at least a majority of the selected section of the formation, wherein the controlled pressure is at least about 2.0 bars absolute.

3627. The method of claim 3588, further comprising controlling foimation conditions such that the produced mixture comprises a partial pressure of H₂ within the mixture greater than about 0.5 bars.

3628. The method ofclaim 3627, wherein the partial pressure of H₂ is measured when the mixture is at a production well.

3629. The method ofclaim 3588, wherein controlling formation conditions comprises recfrculating a portion of hydrogen from the mixture into the foπnation.

3630. The method of claim 3588, further comprising altering a pressure within the formation to inhibit production of hydrocarbons from the formation having carbon numbers greater than about 25.

3631. The method ofclaim 3588, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

3632. The method ofclaim 3588, wherein the produced mixture comprises hydrogen and condensable hydrocarbons, the method further comprising hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

3633. The method ofclaim 3588, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for the production well.

3634. The method ofclaim 3633, wherein at least about 20 heat sources are disposed in the formation for each production well.

3635. The method ofclaim 3588, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

3636. The method of claim 3588, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattem of units.

3637. The method ofclaim 3588, fuither comprising separating the produced mixture into a gas stream and a liquid sfream.

3638. The method ofclaim 3588, further comprising separating the produced mixture into a gas stream and a liquid sfream and separating the liquid sfream into an aqueous stream and a non-aqueous stream.

3639. The method ofclaim 3588, wherein the produced mixture comprises H₂S, the method further comprising separating a portion of the H₂S from non-condensable hydrocarbons.

3640. The method of claim 3588, wherein the produced mixture comprises C0₂, the method further comprising separating a portion of the C0₂ from non-condensable hydrocarbons.

3641. The method ofclaim 3588, wherein the mixture is produced from a production well, wherein the heating is controlled such that the mixture can be produced from the formation as a vapor.

3642. The method ofclaim 3588, wherein the mixture is produced from a production well, the method further comprising heating a wellbore of the production well to inhibit condensation of the mixture within the wellbore.

3643. The method of claim 3588, wherein the mixture is produced from a production well, wherein a wellbore of the production well comprises a heater element configured to heat the formation adjacent to the wellbore, and further comprising heating the formation with the heater element to produce the mixture, wherein the mixture comprises a large non-condensable hydrocarbon gas component and H₂.

3644. The method ofclaim 3588, wherein the selected section is heated to a minimum pyrolysis temperature of about 270 °C.

3645. The method ofclaim 3588, further comprising maintaining the pressure within the formation above about 2.0 bars absolute to inhibit production of fluids having carbon numbers above 25.

3646. The method ofclaim 3588, further comprising controlling pressure within the foimation in a range from about atmospheric pressure to about 100 bars, as measured at a wellhead of a production well, to control an amount of condensable hydrocarbons within the produced mixture, wherein the pressure is reduced to increase production of condensable hydrocarbons, and wherein the pressure is increased to increase production of non-condensable hydrocarbons.

3647. The method ofclaim 3588, further comprising confrolling pressure within the formation in a range from about atmospheric pressure to about 100 bars, as measured at a wellhead of a production well, to control an API gravity of condensable hydrocarbons within the produced mixture, wherein the pressure is reduced to decrease the API gravity, and wherein the pressure is increased to reduce the API gravity.

3648. A mixture produced from a portion of a relatively low permeability fonnation containing heavy hydrocarbons, the mixture, comprising: non-condensable hydrocarbons comprising hydrocarbons having carbon numbers of less than 5; and wherehi a weight ratio of the hydrocarbons having carbon numbers from 2 through 4, to methane, in the mixture is greater than approximately 1.

3649. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3650. The mixture ofclaim 3648, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3651. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3652. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3653. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3654. The mixture of claim 3648, further comprising condensable hydrocarbons, wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3655. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3656. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3657. The mixture of claim 3648, further comprising condensable hydrocarbons, wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons comprise cycloalkanes.

3658. The mixture of claim 3648, wherein the non-condensable hydrocarbons further comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable hydrocarbons, and wherein the hydrogen is less than about 80 % by volume of the non-condensable hydrocarbons.

3659. The mixture ofclaim 3648, further comprising ammonia, wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3660. The mixture ofclaim 3648, further comprising ammonia, wherein the ammonia is used to produce fertilizer.

3661. The mixture of claim 3648, further comprising condensable hydrocarbons, wherein less than about 15 weight % of the condensable hydrocarbons have a carbon number greater than approximately 25.

3662. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein the condensable hydrocarbons comprise olefins, and wherein about 0.1 % to about 5 % by weight of the condensable hydrocarbons comprises olefins.

3663. The mixture ofclaim 3648, further comprising condensable hydrocarbons, wherein the condensable hydrocarbons comprises olefins, and wherein about 0.1 % to about 2.5 % by weight of the condensable hydrocarbons comprises olefins.

3664. The mixture of claim 3648, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3665. The mixture of claim 3648, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H , and wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂.

3666. The mixture of claim 3648, wherein a weight ratio of hydrocarbons having greater than about 2 carbon atoms, to methane, is greater than about 0.3.

3667. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, the mixture comprising: non-condensable hydrocarbons comprising hydrocarbons having carbon numbers of less than 5, wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1; condensable hydrocarbons; wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons comprises nitrogen; wherehi less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons comprises oxygen; and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons comprises sulfur.

3668. The mixture ofclaim 3667, further comprising ammonia, wherehi greater than about 0.05 % by weight of the produced mixture is ammonia.

3669. The mixture ofclaim 3667, wherein less than about 5 weight % of the condensable hydrocarbons have a carbon number greater than approximately 25.

3670. The mixture of claim 3667, wherein the condensable hydrocarbons comprise olefins, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3671. The mixture ofclaim 3667, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3672. The mixture ofclaim 3667, wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3673. The mixture of clahn 3667, wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3674. The mixture ofclaim 3667, wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3675. The mixture of claim 3667, wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3676. The mixture of clahn 3667, wherein the non-condensable hydrocarbons comprises hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable hydrocarbons and wherein the hydrogen is less than about 80 % by volume of the non-condensable hydrocarbons.

3677. The mixture ofclaim 3667, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3678. The mixture of claim 3667, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3679. The mixture of claim 3667, wherein the non-condensable hydrocarbons comprise H₂, and wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3680. The mixture ofclaim 3667, wherein the non-condensable hydrocarbons comprise H₂, and wherein greater than about 15 % by weight of the mixture comprises H₂.

3681. The mixture ofclaim 3667, wherein a weight ratio of hydrocarbons having greater than about 2 carbon atoms, to methane, is greater, than about 0.3.

3682. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, the mixture comprising: non-condensable hydrocarbons comprising hydrocarbons having carbon numbers of less than 5, wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1; and ammonia, wherein greater than about 0.5 % by weight of the mixture comprises ammonia.

3683. The mixture ofclaim 3682, wherein the condensable hydrocarbons further comprise olefins, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3684. The mixture ofclaim 3682, wherein the non-condensable hydrocarbons further comprise ethene and ethane, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3685. The mixture of claim 3682, wherein the condensable hydrocarbons further comprise nifrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3686. The mixture ofclaim 3682, wherein the condensable hydrocarbons further comprise oxygen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3687. The mixttire of claim 3682, wherein the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3688. The mixture ofclaim 3682, wherein the condensable hydrocarbons further comprise aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3689. The mixture ofclaim 3682, wherein the condensable hydrocarbons further comprise multi-aromatic rings, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3690. The mixture of claim 3682, wherein the condensable hydrocarbons further comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3691. The mixture of claim 3682, wherein the condensable hydrocarbons fiirther comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3692. The mixture ofclaim 3682, wherein the non-condensable hydrocarbons further comprise hydrogen, wherehi the hydrogen is greater than about 10 % by volume of the non-condensable hydrocarbons, and wherein the hydrogen is less than about 80 % by volume of the non-condensable hydrocarbons.

3693. The mixture of claim 3682, wherein the produced mixture further comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3694. The mixture ofclaim 3682, wherein the produced mixture further comprises ammonia, and wherein the ammonia is used to produce fertilizer.

3695. The mixture ofclaim 3682, wherein the condensable hydrocarbons comprise hydrocarbons having a carbon number of greater than approximately 25, and wherein less than about 15 weight % of the hydrocarbons in the mixture have a carbon number greater than approximately 25.

3696. The mixture ofclaim 3682, wherehi the non-condensable hydrocarbons further comprise H₂, and wherein greater than about 5 % by weight of the mixture comprises H₂.

3697. The mixture ofclaim 3682, wherein the non-condensable hydrocarbons further comprise H₂, and wherein greater than about 15 % by weight of the mixture comprises H₂.

3698. The mixture ofclaim 3682, wherein the non-condensable hydrocarbons further comprise hydrocarbons having carbon numbers of greater than 2, wherein a weight ratio of hydrocarbons having carbon numbers greater than 2, to methane, is greater than about 0.3.

3699. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, the mixture comprising: non-condensable hydrocarbons comprising hydrocarbons having carbon numbers of less than 5, wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1 ; and condensable hydrocarbons comprising olefins, wherein less than about 10 % by weight of the condensable hydrocarbons comprises olefins.

3700. The mixture ofclaim 3699, wherein the non-condensable hydrocarbons further comprise ethene and ethane, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3701. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise nifrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3702. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise oxygen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3703. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3704. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3705. The mixture of claim 3699, wherein the condensable hydrocarbons further comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3706. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3707. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3708. The mixture of claim 3699, wherein the non-condensable hydrocarbons further comprise hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable hydrocarbons and wherein the hydrogen is less than about 80 % by volume of the non-condensable hydrocarbons.

3709. The mixture ofclaim 3699, wherein the produced mixture further comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3710. The mixture ofclaim 3699, wherein the produced mixture further comprises ammonia, and wherein the ammonia is used to produce fertilizer.

3711. The mixture ofclaim 3699, wherein the condensable hydrocarbons further comprise hydrocarbons having a carbon number of greater than approxhnately 25, and wherein less than about 15 % by weight of the hydrocarbons have a carbon number greater than approximately 25.

3712. The mixttire ofclaim 3699, wherein about 0.1 % to about 5 % by weight of the condensable component comprises olefins.

3713. The mixture ofclaim 3699, wherein about 0.1% to about 2 % by weight of the condensable component comprises olefins.

3714. The mixture ofclaim 3699, wherehi the non-condensable hydrocarbons further comprise H₂, and wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3715. The mixture ofclaim 3699, wherein the non-condensable hydrocarbons further comprise H₂, and wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂.

3716. The mixture ofclaim 3699, wherein a weight ratio of hydrocarbons having greater than about 2 carbon atoms, to methane, is greater than about 0.3.

3717. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, comprising: condensable hydrocarbons, wherein less than about 15 weight % of the condensable hydrocarbons have a carbon number greater than 25.

3718. The mixture ofclaim 3717, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1.

3719. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise olefins, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3720. The mixture ofclaim 3717, further comprising non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3721. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise nifrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3722. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise oxygen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3723. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3724. The mixture of claim 3717, wherein the condensable hydrocarbons further comprise aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3725. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3726. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3727. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3728. The mixture of claim 3717, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable hydrocarbons and wherein the hydrogen is less than about 80 % by volume of the non- condensable hydrocarbons.

3729. The mixture ofclaim 3717, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3730. The mixture ofclaim 3717, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3731. The mixture of claim 3717, wherein the condensable hydrocarbons further comprises olefins, and wherein less than about 10 % by weight of the condensable hydrocarbons comprises olefins.

3732. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprises olefins, and wherehi about 0.1 % to about 5 % by weight of the condensable hydrocarbons comprises olefins.

3733. The mixture ofclaim 3717, wherein the condensable hydrocarbons further comprises olefins, and wherein about 0.1 % to about 2 % by weight of the condensable hydrocarbons comprises olefins.

3734. The mixture ofclaim 3717, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3735. The mixture of claim 3717, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂.

3736. The mixture ofclaim 3717, wherein a weight ratio of hydrocarbons having greater than about 2 carbon atoms, to methane, is greater than about 0.3.

3737. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, comprising: condensable hydrocarbons, wherein less than about 15 % by weight of the condensable hydrocarbons have a carbon number greater than about 25; wherein less than about 1 % by weight of the condensable hydrocarbons, when calculated on an atomic basis, is nifrogen; wherehi less than about 1 % by weight of the condensable hydrocarbons, when calculated on an atomic basis, is oxygen; and wherein less than about 1 % by weight of the condensable hydrocarbons, when calculated on an atomic basis, is sulfur.

3738. The mixture ofclaim 3737, further comprising non-condensable hydrocarbons, wherein the non- condensable component comprises hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1.

3739. The mixture ofclaim 3737, wherein the condensable hydrocarbons further comprise olefins, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3740. The mixture ofclaim 3737, further comprising non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3741. The mixture ofclaim 3737, wherein the condensable hydrocarbons further comprise aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3742. The mixture of claim 3737, wherein the condensable hydrocarbons further comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3743. The mixture of claim 3737, wherein the condensable hydrocarbons further comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3744. The mixture ofclaim 3737, wherein the condensable hydrocarbons further comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3745. The mixture ofclaim 3737, further comprising non-condensable hydrocarbons, and wherein the non- condensable hydrocarbons comprise hydrogen, and wherein greater than about 10 % by volmne and less than about 80 % by volume of the non-condensable component comprises hydrogen.

3746. The mixture of claim 3737, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3747. The mixture ofclaim 3737, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3748. The mixture ofclaim 3737, wherein the condensable component further comprises olefins, and wherein about 0.1 % to about 5 % by weight of the condensable component comprises olefins.

3749. The mixture ofclaim 3737, wherein the condensable component further comprises olefins, and wherein about 0.1 % to about 2.5 % by weight of the condensable component comprises olefins.

3750. The mixture of claim 3737, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3751. The mixture ofclaim 3737, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂.

3752. The mixture ofclaim 3737, further comprising non-condensable hydrocarbons, wherein a weight ratio of compounds within the non-condensable hydrocarbons having greater than about 2 carbon atoms, to methane, is greater than about 0.3.

3753. A mixture produced from a portion of a relatively low permeability fonnation containing heavy hydrocarbons, comprising: condensable hydrocarbons, wherein less than about 15 % by weight of the condensable hydrocarbons have a carbon number greater than 20; and wherein the condensable hydrocarbons comprise olefins, wherein an olefin content of the condensable component is less than about 10 % by weight of the condensable component.

3754. The mixture ofclaim 3753, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1.

3755. The mixture ofclaim 3753, wherein the condensable hydrocarbons further comprise olefins, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3756. The mixture ofclaim 3753, further comprising non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0,15.

3757. The mixture ofclaim 3753, wherein the condensable hydrocarbons further comprise nitrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

3758. The mixture ofclaim 3753, wherein the condensable hydrocarbons further comprise oxygen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3759. The mixture ofclaim 3753, wherehi the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3760. The mixture of claim 3753, wherein the condensable hydrocarbons further comprise aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3761. The mixture ofclaim 3753, wherein the condensable hydrocarbons further comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3762. The mixture of claim 3753, wherein the condensable hydrocarbons further comprise asphaltenes, and wherehi less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3763. The mixture ofclaim 3753, wherein the condensable hydrocarbons further comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3764. The mixture of claim 3753, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprises hydrogen, and wherein the hydrogen is about 10 % by volume to about 80 % by volume of the non-condensable hydrocarbons.

3765. The mixture ofclaim 3753, further comprising ammonia, wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3766. The mixture ofclaim 3753, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3767. The mixture ofclaim 3753, wherein about 0.1 % to about 5 % by weight of the condensable component comprises olefins.

3768. The mixture ofclaim 3753, wherein about 0.1 % to about 2 % by weight of the condensable component comprises olefins.

3769. The mixture of claim 3753, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3770. The mixture ofclaim 3753, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂.

3771. The mixture ofclaim 3753, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 0.3.

3772. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, comprising: condensable hydrocarbons, wherein less than about 5 % by weight of the condensable hydrocarbons comprises hydrocarbons having a carbon number greater than about 25; and wherein the condensable hydrocarbons further comprise aromatic compounds, wherein more than about 20 % by weight of the condensable hydrocarbons comprises aromatic compounds.

3773. The mixture of claim 3772, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 1.

3774. The mixture ofclaim 3772, wherein the condensable hydrocarbons further comprise olefins, and wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons are olefins.

3775. The mixture ofclaim 3772, further comprising non-condensable hydrocarbons, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3776. The mixture of claim 3772, wherein the condensable hydrocarbons further comprise nitrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3777. The mixture of claim 3772, wherein the condensable hydrocarbons further comprise oxygen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3778. The mixture ofclaim 3772, wherein the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3779. The mixture of claim 3772, wherein the condensable hydrocarbons further comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3780. The mixture ofclaim 3772, wherein the condensable hydrocarbons further comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3781. The mixture ofclaim 3772, wherein the condensable hydrocarbons comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3782. The mixture of claim 3772, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise hydrogen, and wherein the hydrogen is greater than about 10 % by volume and less than about 80 % by volume of the non-condensable hydrocarbons.

3783. The mixture of claim 3772, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3784. The mixture ofclaim 3772, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3785. The mixture of clahn 3772, wherein the condensable hydrocarbons further comprise olefins, and wherein about 0.1 % to about 5 % by weight of the condensable hydrocarbons comprises olefins.

3786. The mixture ofclaim 3772, wherein the condensable hydrocarbons further comprises olefins, and wherein about 0.1 % to about 2 % by weight of the condensable hydrocarbons comprises olefins.

3787. The mixture of clahn 3772, wherein the condensable hydrocarbons further comprises multi-ring aromatic compounds, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatic compounds.

3788. The mixture ofclaim 3772, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 5 % by weight of the non-condensable hydrocarbons comprises H₂.

3789. The mixture of claim 3772, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprise H₂, and wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂.

3790. The mixture ofclaim 3772, further comprising non-condensable hydrocarbons, wherein the non- condensable hydrocarbons comprises hydrocarbons having carbon numbers of less than 5, and wherehi a weight ratio of hydrocarbons having carbon numbers from 2 through 4, to methane, is greater than approximately 0.3.

3791. A mixture produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, comprising: non-condensable hydrocarbons comprising hydrocarbons having carbon numbers of less than about 5, wherein a weight ratio of the hydrocarbons having carbon number from 2 through 4, to methane, in the mixture is greater than approximately 1; wherein the non-condensable hydrocarbons further comprise H₂, wherein greater than about 15 % by weight of the non-condensable hydrocarbons comprises H₂; and condensable hydrocarbons, comprising: olefins, wherein less than about 10 % by weight of the condensable hydrocarbons comprises olefins; and aromatic compounds, wherein greater than about 20 % by weight of the condensable hydrocarbons comprises aromatic compounds.

3792. The mixture ofclaim 3791, wherein the non-condensable hydrocarbons further comprise ethene and ethane, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3793. The mixture of clahn 3791, wherein the condensable hydrocarbons further comprise nifrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3794. The mixture ofclaim 3791, wherein the condensable hydrocarbons further comprise oxygen containing compounds, and wherehi less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3795. The mixture ofclaim 3791, wherein the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3796. The mixture ofclaim 3791, wherein the condensable hydrocarbons comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3797. The mixture ofclaim 3791, wherein the condensable hydrocarbons comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3798. The mixture ofclaim 3791, wherein the condensable hydrocarbons comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3799. The mixture ofclaim 3791, wherein the non-condensable hydrocarbons further comprises hydrogen, and wherein greater than about 10 % by volume and less than about 80 % by volume of the non-condensable hydrocarbons.

3800. The mixture of clahn 3791, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3801. The mixture ofclaim 3791, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3802. The mixture ofclaim 3791, wherein the condensable hydrocarbons further comprise hydrocarbons having a carbon number of greater than approximately 25, wherein less than about 15 % by weight of the hydrocarbons have a carbon number greater than approximately 25.

3803. The mixture ofclaim 3791, wherein about 0.1 % to about 5 % by weight of the condensable hydrocarbons comprises olefins.

3804. The mixture ofclaim 3791, wherein about 0.1 % to about 2 % by weight of the condensable hydrocarbons comprises olefins.

3805. The mixture ofclaim 3791, wherein the mixture comprises hydrocarbons having greater than about 2 carbon atoms, and wherein the weight ratio of hydrocarbons having greater than about 2 carbon atoms to methane is greater than about 0.3.

3806. A mixture produced from a portion of a relatively low permeability foπnation containing heavy hydrocarbons, comprising: condensable hydrocarbons, wherein less than about 5 % by weight of the condensable hydrocarbons comprises hydrocarbons having a carbon number greater than about 25; wherein the condensable hydrocarbons further comprise: olefins, wherein less than about 10 % by weight of the condensable hydrocarbons comprises olefins; and aromatic compounds, wherein greater than about 30 % by weight of the condensable hydrocarbons comprises aromatic compounds; and non-condensable hydrocarbons comprising H₂, wherein greater than about 15 % by weight of the non- condensable hydrocarbons comprises H₂.

3807. The mixture ofclaim 3806, wherein the non-condensable hydrocarbons further comprises hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of hydrocarbons having carbon nmnbers from 2 through 4, to methane, is greater than approximately 1.

3808. The mixture ofclaim 3806, wherein the non-condensable hydrocarbons comprise ethene and ethane, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3809. The mixture ofclaim 3806, wherein the condensable hydrocarbons further comprise nitrogen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3810. The mixture ofclaim 3806, wherehi the condensable hydrocarbons further comprise oxygen containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3811. The mixture ofclaim 3806, wherein the condensable hydrocarbons further comprise sulfur containing compounds, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3812. The mixture of claim 3806, wherein the condensable hydrocarbons further comprise multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3813. The mixture of clahn 3806, wherein the condensable hydrocarbons further comprise asphaltenes, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3814. The mixture ofclaim 3806, wherein the condensable hydrocarbons comprise cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3815. The mixture of claim 3806, wherein greater than about 10 % by volume and less than about 80 % by volume of the non-condensable hydrocarbons is hydrogen.

3816. The mixture ofclaim 3806, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3817. The mixture ofclaim 3806, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3818. The mixture of clahn 3806, wherein about 0.1 % to about 5 % by weight of the condensable hydrocarbons comprises olefins.

3819. The mixture ofclaim 3806, wherein about 0.1 % to about 2 % by weight of the condensable hydrocarbons comprises olefins.

3820. The mixture ofclaim 3806, wherein the mixture comprises hydrocarbons having greater than about 2 carbon atoms, and wherehi the weight ratio of hydrocarbons having greater than about 2 carbon atoms to methane is greater than about 0.3.

3821. A mixture of condensable hydrocarbons produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, comprising: olefins, wherein about 0.1 % by weight to about 15 % by weight of the condensable hydrocarbons comprises olefins; and asphaltenes, wherein less than about 0.1 % by weight of the condensable hydrocarbons comprises asphaltenes.

3822. The mixture ofclaim 3821, wherein the condensable hydrocarbons further comprises hydrocarbons having a carbon number of greater than approximately 25, and wherein less than about 15 weight % of the hydrocarbons in the mixture have a carbon number greater than approximately 25.

3823. The mixture of claim 3821 , wherein about 0.1 % by weight to about 5 % by weight of the condensable hydrocarbons comprises olefins.

3824. The mixture of claim 3821 , wherein the condensable hydrocarbons further comprises non-condensable hydrocarbons, wherein the non-condensable hydrocarbons comprise ethene and ethane, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3825. The mixture of claim 3821 , wherein the condensable hydrocarbons further comprises nitrogen, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3826. The mixture ofclaim 3821, wherein the condensable hydrocarbons further comprises oxygen, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3827. The mixture ofclaim 3821, wherein the condensable hydrocarbons further comprises sulfur, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3828. The mixture of clahn 3821, wherein the condensable hydrocarbons further comprises aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3829. The mixture ofclaim 3821, wherein the condensable hydrocarbons further comprises multi-ring aromatics, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3830. The mixture ofclaim 3821, wherein the condensable hydrocarbons further comprises cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3831. The mixture of claim 3821, wherein the condensable hydrocarbons comprises non-condensable hydrocarbons, and wherein the non-condensable hydrocarbons comprise hydrogen, and wherein the hydrogen is greater than about 10 % by volume of the non-condensable hydrocarbons and wherein the hydrogen is less than about 80 % by volume of the non-condensable hydrocarbons.

3832. The mixture ofclaim 3821, further comprising ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3833. The mixture ofclaim 3821, further comprising ammonia, and wherein the ammonia is used to produce fertilizer.

3834. The mixture of claim 3821 , wherein about 0.1 % by weight to about 2 % by weight of the condensable hydrocarbons comprises olefins.

3835. A mixture of condensable hydrocarbons produced from a portion of a relatively low permeability formation containing heavy hydrocarbons, comprising: olefins, wherein about 0.1 % by weight to about 2 % by weight of the condensable hydrocarbons comprises olefins; multi-ring aromatics, wherein less than about 4 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings

3836. The mixture ofclaim 3835, further comprising hydrocarbons having a carbon number of greater than approximately 25, wherein less than about 5 weight % of the hydrocarbons in the mixture have a carbon number greater than approximately 25.

3837. The mixture ofclaim 3835, wherein the condensable hydrocarbons further comprises nitrogen, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

3838. The mixture ofclaim 3835, wherein the condensable hydrocarbons further comprises oxygen, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3839. The mixture o claim 3835, wherein the condensable hydrocarbons further comprises sulfur, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3840. The mixture ofclaim 3835, wherein the condensable hydrocarbons further comprises aromatic compounds, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3841. The mixture ofclaim 3835, wherein the condensable hydrocarbons further comprises condensable hydrocarbons, and wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3842. The mixture ofclaim 3835, wherein the condensable hydrocarbons further comprises cycloalkanes, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3843. The mixture ofclaim 3835, further comprising ammonia, wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3844. The mixture of claim 3835, further comprising ammonia, wherein the ammonia is used to produce fertilizer.

3845. A mixture produced from a portion of a relatively low permeability foimation containing heavy hydrocarbons, comprising: non-condensable hydrocarbons and H₂, wherein greater than about 10% by volume of the non-condensable hydrocarbons and H₂ comprises H₂; ammonia and water, wherein greater than about 0.5 % by weight of the mixture comprises ammonia; and condensable hydrocarbons.

3846. The mixture of claim 3845, wherein the non-condensable hydrocarbons further comprise hydrocarbons having carbon numbers of less than 5, and wherein a weight ratio of the hydrocarbons having carbon numbers from 2 through 4 to methane, in the mixture is greater than approximately 1.

3847. The mixture ofclaim 3845, wherein greater than about 0.1 % by weight of the condensable hydrocarbons are olefins, and wherein less than about 15 % by weight of the condensable hydrocarbons are olefins.

3848. The mixture ofclaim 3845, wherein the non-condensable hydrocarbons further comprise ethene and ethane, wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is greater than about 0.001, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons is less than about 0.15.

3849. The mixture ofclaim 3845, wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nifrogen.

3850. The mixture of claim 3845, wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3851. The mixture ofclaim 3845, wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3852. The mixture ofclaim 3845, wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3853. The mixture ofclaim 3845, wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3854. The mixture ofclaim 3845, wherein less than about 0.3 % by weight of the condensable hydrocarbons are asphaltenes.

3855. The mixture ofclaim 3845, wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3856. The mixture ofclaim 3845, wherein the H₂ is less than about 80 % by volume of the non-condensable hydrocarbons and H₂.

3857. The mixture ofclaim 3845, wherein the condensable hydrocarbons further comprise sulfur containing compounds.

3858. The mixture ofclaim 3845, wherein the ammonia is used to produce fertilizer.

3859. The mixture ofclaim 3845, wherein less than about 5% of the condensable hydrocarbons have carbon numbers greater than 25.

3860. The mixture ofclaim 3845, wherein the condensable hydrocarbons comprise olefins, wherein greater than about about 0.001 % by weight of the condensable hydrocarbons comprise olefins, and wherein less than about 15% by weight of the condensable hydrocarbons comprise olefins.

3861. The mixture of claim 3845, wherein the condensable hydrocarbons comprise olefins, wherein greater than about about 0.001 % by weight of the condensable hydrocarbons comprise olefins, and wherein less than about 10% by weight of the condensable hydrocarbons comprise olefins.

3862. The mixture ofclaim 3845, wherein the condensable hydrocarbons further comprise nitrogen containing compounds.

3863. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

3864. The method ofclaim 3863, wherein three or more of the heat sources are located in the foπnation in a plurality of the units, and wherein the plurality of units are repeated over an area of the foπnation to form a repetitive pattern of units.

3865. The method ofclaim 3863, wherein three or more of the heat sources are located in the foπnation in a plurality of the units, wherein the plurality of units are repeated over an area of the formation to form a repetitive pattern of units, and wherein a ratio of heat sources in the repetitive pattern of units to production wells in the repetitive pattern is greater than approximately 5.

3866. The method ofclaim 3863, wherein three or more of the heat sources are located in the formation in a plurality of the units, wherein the plurality of units are repeated over an area of the formation to form a repetitive pattern of units, wherein three or more production wells are located within an area defined by the plurality of units, wherein the three or more production wells are located in the formation in a unit of production wells, and wherein the unit of production wells comprises a friangular pattern.

3867. The method ofclaim 3863, wherein three or more of the heat sources are located in the formation in a plurality of the units, wherein the plurality of units are repeated over an area of the formation to form a repetitive pattern of units, wherehi three or more injection wells are located within an area defined by the plurality of units, wherein the three or more injection wells are located in the formation in a unit of injection wells, and wherein the unit of injection wells comprises a friangular pattern.

3868. The method ofclaim 3863, wherein three or more of the heat sources are located in the formation in a plurality of the units, wherein the plurality of units are repeated over an area of the formation to form a repetitive pattern of units, wherein three or more production wells and three or more injection wells are located within an area defined by the plurality of units, wherein the three or more production wells are located in the formation in a unit of production wells, wherein the unit of production wells comprises a first friangular pattern, wherein the three or more injection wells are located in the fonnation in a unit of injection wells, wherein the unit of injection wells comprises a second triangular pattern, and wherein the first triangular pattern is substantiaUy different than the second triangular pattern.

3869. The method ofclaim 3863, wherein three or more of the heat sources are located in the formation in a plurality of the units, wherein the plurality of units are repeated over an area of the formation to form a repetitive pattern of units, wherein three or more monitoring wells are located within an area defined by the plurality of units, wherein the three or more monitoring wells are located in the formation in a unit of monitoring wells, and wherein the unit of monitoring wells comprises a ttiangular pattern.

3870. The method ofclaim 3863, wherein a production well is located in an area defined by the unit of heat sources.

3871. The method ofclaim 3863, wherein three or more of the heat sources are located in the formation in a first unit and a second unit, wherein the first unit is adjacent to the second unit, and wherein the first unit is inverted with respect to the second unit.

3872. The method ofclaim 3863, wherein a distance between each of the heat sources in the unit of heat sources varies by less than about 20 %.

3873. The method ofclaim 3863, wherein a distance between each of the heat sources in the unit of heat sources is approximately equal.

3874. The method ofclaim 3863, wherein providing heat from three or more heat sources comprises substantially uniformly providing heat to at least the portion of the formation.

3875. The method ofclaim 3863, wherein the heated portion comprises a substantially uniform temperature disttibution.

3876. The method of claim 3863, wherein the heated portion comprises a substantially uniform temperature disttibution, and wherein a difference between a highest temperature in the heated portion and a lowest temperature in the heated portion comprises less than about 200 °C.

3877. The method ofclaim 3863, wherein a temperature at an outer lateral boundary of the triangular pattern and a temperature at a center of the friangular pattern are approximately equal.

3878. The method ofclaim 3863, wherein a temperature at an outer lateral boundary of the friangular pattern and a temperature at a center of the triangular pattern increase substantially linearly after an initial period of time, and wherein the initial period of time comprises less than approximately 3 months.

3879. The method ofclaim 3863, wherein a time required to increase an average temperature of the heated portion to a selected temperature with the friangular pattern of heat sources is substantially less than a time requfred to increase the average temperature of the heated portion to the selected temperature with a hexagonal pattern of heat sources, and wherein a space between each of the heat sources in the friangular pattern is approximately equal to a space between each of the heat sources in the hexagonal pattern.

3880. The method ofclaim 3863, wherein a time requfred to increase a temperature at a coldest point within the heated portion to a selected temperature with the friangular pattern of heat sources is substantially less than a time required to increase a temperature at the coldest point within the heated portion to the selected temperature with a hexagonal pattern of heat sources, and wherein a space between each of the heat sources in the triangular pattern is approximately equal to a space between each of the heat sources in the hexagonal pattern.

3881. The method ofclaim 3863, wherein a time requfred to increase a temperature at a coldest point withhi the heated portion to a selected temperature with the triangular pattern of heat sources is substantially less than a time required to increase a temperature at the coldest point within the heated portion to the selected temperature with a hexagonal pattern of heat sources, and wherehi a number of heat sources per unit area in the ttiangular pattern is equal to the number of heat sources per unit are in the hexagonal pattern of heat sources.

3882. The method ofclaim 3863, wherein a time required to increase a temperature at a coldest point within the heated portion to a selected temperature with the ttiangular pattern of heat sources is substantially equal to a time requfred to increase a temperature at the coldest point within the heated portion to the selected temperature with a hexagonal pattern of heat sources, and wherein a space between each of the heat sources in the friangular pattern is approximately 5 m greater than a space between each of the heat sources in the hexagonal pattern.

3883. The method ofclaim 3863, wherein providing heat from three or more heat sources to at least the portion of formation comprises: heating a selected volume (V) of the relatively low permeability formation containing heavy hydrocarbons from three or more of the heat sources, wherein the formation has an average heat capacity (C_v), and wherein heat from three or more of the heat sources pyrolyzes at least some hydrocarbons within the selected volume of the formation; and wherein heating energy/day provided to the volume is equal to or less than Pwr, wherein Pwr is calculated by the equation:

Pwr = h*V*C *p_B wherein Pwr is the heating energy/day, h is an average heating rate of the foπnation, p_B is formation bulk density, and wherein the heating rate is less than about 10°C/day.

3884. The method ofclaim 3863, wherein three or more of the heat sources comprise elecfrical heaters.

3885. The method ofclaim 3863, wherein three or more of the heat sources comprise surface burners.

3886. The method ofclaim 3863, wherein three or more of the heat sources comprise flameless disfributed combustors.

3887. The method ofclaim 3863, wherein three or more of the heat sources comprise natural disfributed combustors.

3888. The method ofclaim 3863, further comprising: allowing the heat to fransfer from three or more of the heat sources to a selected section of the formation such that heat from three or more of the heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation; and producing a mixture of fluids from the formation.

3889. The method ofclaim 3888, further comprising controlling a temperature withhi at least a majority of the selected section of the foπnation, wherein the pressure is controlled as a function of temperature, or the temperature is controlled as a function of pressure.

3890. The method ofclaim 3888, further comprising confrolling the heat such that an average heating rate of the selected section is less than about 1.0° C per day during pyrolysis.

3891. The method ofclaim 3888, wherein allowing the heat to fransfer from three or more of the heat sources to the selected section comprises transferring heat substantially by conduction.

3892. The method ofclaim 3888, wherein the produced mixture comprises an API gravity of at least 25°.

3893. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 0.1% by weight to about 15% by weight of the condensable hydrocarbons are olefins.

3894. The method ofclaim 3888, wherein the produced mixture comprises non-condensable hydrocarbons, and wherein a molar ratio of ethene to ethane in the non-condensable hydrocarbons ranges from about 0.001 to about 0.15.

3895. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is nitrogen.

3896. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is oxygen.

3897. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 1 % by weight, when calculated on an atomic basis, of the condensable hydrocarbons is sulfur.

3898. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein greater than about 20 % by weight of the condensable hydrocarbons are aromatic compounds.

3899. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 5 % by weight of the condensable hydrocarbons comprises multi-ring aromatics with more than two rings.

3900. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein less than about 0.1% by weight of the condensable hydrocarbons are asphaltenes.

3901. The method ofclaim 3888, wherein the produced mixture comprises condensable hydrocarbons, and wherein about 5 % by weight to about 30 % by weight of the condensable hydrocarbons are cycloalkanes.

3902. The method ofclaim 3888, wherein the produced mixture comprises a non-condensable component, wherein the non-condensable component comprises hydrogen, wherein the hydrogen is greater than about 10 % by volume of the non-condensable component, and wherein the hydrogen is less than about 80 % by volume of the non-condensable component.

3903. The method of claim 3888, wherein the produced mixture comprises ammonia, and wherein greater than about 0.05 % by weight of the produced mixture is ammonia.

3904. The method ofclaim 3888, wherein the produced mixture comprises ammonia, and wherein the ammonia is used to produce fertilizer.

3905. The method ofclaim 3888, further comprising controlling foπnation conditions to produce a mixture of hydrocarbon fluids and H₂, wherein a partial pressure of H₂ within the mixture is greater than about 2.0 bars absolute.

3906. The method ofclaim 3888, further comprishig altering a pressure within the formation to inhibit production of hydrocarbons from the foπnation having carbon numbers greater than about 25.

3907. The method ofclaim 3888, further comprising controlling formation conditions by recirculating a portion ofhydrogen from the mixture into the foπnation.

3908. The method of claim 3888, further comprising: providing hydrogen (H₂) to the heated section to hydrogenate hydrocarbons within the section; and heating a portion of the section with heat from hydrogenation.

3909. The method ofclaim 3888, further comprising: producing hydrogen from the formation; and hydrogenating a portion of the produced condensable hydrocarbons with at least a portion of the produced hydrogen.

3910. The method ofclaim 3888, wherein producing the mixture comprises producing the mixture in a production well, and wherein at least about 7 heat sources are disposed in the formation for each production well.

3911. The method of claim 3910, wherein at least about 20 heat sources are disposed in the formation for each production well.

3912. The method of clahn 3888, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

3913. The method ofclaim 3888, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherehi a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

3914. A method for in situ production of synthesis gas from a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a section of the foπnation to a temperature sufficient to allow synthesis gas generation, wherein a permeability of the section is substantially uniform; providing a synthesis gas generating fluid to the section to generate synthesis gas; and removing synthesis gas from the foimation.

3915. The method of clahn 3914, wherein the temperature sufficient to allow synthesis gas generation ranges from approximately 400 °C to approxhnately 1200 °C.

3916. The method ofclaim 3914, further comprismg heating the section when providing the synthesis gas generating fluid to inhibit temperature decrease in the section due to synthesis gas generation.

3917. The method of clahn 3914, wherehi heating the section comprises converting an oxidizing fluid into a portion of the section, wherein the temperature within the section is above a temperature sufficient to support oxidation of carbon within the section with the oxidizing fluid, and reacting the oxidizhig fluid with carbon in the section to generate heat within the section.

3918. The method of clahn 3917, wherein the oxidizing fluid comprises air.

3919. The method ofclaim 3918, wherein an amount of the oxidizing fluid convected into the section is configured to inhibit foπnation of oxides of nifrogen by maintaining a reaction temperature below a temperature sufficient to produce oxides of nitrogen compounds.

3920. The method ofclaim 3914, wherein heating the section comprises diffusing an oxidizing fluid to reaction zones adjacent to wellbores within the foimation, oxidizing carbon within the reaction zone to generate heat, and transfening the heat to the section.

3921. The method ofclaim 3914, wherein heating the section comprises heating the section by transfer of heat from one or more of electrical heaters.

3922. The method ofclaim 3914, wherein heating the section to a temperature sufficient to allow synthesis gas generation and providing a synthesis gas generating fluid to the section comprises introducing steam into the section to heat the foimation and to generate synthesis gas.

3923. The method of claim 3914, further comprising controlling the heating of the section and provision of the synthesis gas generating fluid to maintain a temperature within the section above the temperature sufficient to generate synthesis gas.

3924. The method ofclaim 3914, further comprising: monitoring a composition of the produced synthesis gas; and confrolling heating of the section and provision of the synthesis gas generating fluid to maintain the composition of the produced synthesis gas within a selected range.

3925. The method of claim 3924, wherein the selected range comprises a ratio of H₂ to CO of about 2:1.

3926. The method of claim 3914, wherein the synthesis gas generating fluid comprises liquid water.

3927. The method of clahn 3914, wherein the synthesis gas generating fluid comprises steam.

3928. The method of claim 3914, wherein the synthesis gas generating fluid comprises water and carbon dioxide, and wherein the carbon dioxide inhibits production of carbon dioxide from hydrocarbon containing material within the section.

3929. The method ofclaim 3928, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the fonnation.

3930. The method ofclaim 3914, wherein the synthesis gas generathig fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

3931. The method of claim 3930, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

3932. The method ofclaim 3914, wherein providing the synthesis gas generating fluid to the section comprises raising a water table of the formation to allow water to flow into the section.

3933. The method ofclaim 3914, wherein the synthesis gas is removed from a producer well equipped with a heating source, and wherein a portion of the heating source adjacent to a synthesis gas producing zone operates at a substantially constant temperature to promote production of the synthesis gas wherein the synthesis gas has a selected composition.

3934. The method ofclaim 3933, wherein the substantially constant temperature is about 700 °C, and wherein the selected composition has a H₂ to CO ratio of about 2 : 1.

3935. The method ofclaim 3914, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within the section to increase a H₂ concenfration of the generated synthesis gas.

3936. The method of claim 3914, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within the section to increase an energy content of the synthesis gas removed from the formation.

3937. The method ofclaim 3914, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate electricity.

3938. The method ofclaim 3914, further comprising generating electricity from the synthesis gas using a fuel cell.

3939. The method ofclaim 3914, further comprising generating electricity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent section of the fonnation.

3940. The method ofclaim 3914, further comprising using a portion of the synthesis gas as a combustion fuel to heat the formation.

3941. The method ofclaim 3914, further comprising converting at least a portion of the produced synthesis gas to condensable hydrocarbons using a Fischer-Tropsch synthesis process.

3942. The method ofclaim 3914, further comprising converting at least a portion of the produced synthesis gas to methanol.

3943. The method ofclaim 3914, further comprising converting at least a portion of the produced synthesis gas to gasoline.

3944. The method ofclaim 3914, further comprising converting at least a portion of the synthesis gas to methane using a catalytic methanation process.

3945. The method ofclaim 3914, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a ttiangular pattern.

3946. The method of claim 3914, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

3947. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to increase a temperature of the portion to a temperature sufficient to allow synthesis gas generation; providing a synthesis gas generating fluid to at least the portion of the selected section, wherein the synthesis gas generating fluid comprises carbon dioxide; obtaining a portion of the carbon dioxide of the synthesis gas generating fluid from the formation; and producing synthesis gas from the foimation.

3948. The method ofclaim 3947, wherein the temperature sufficient to allow synthesis gas generation is within a range from about 400 °C to about 1200 °C.

3949. The method ofclaim 3947, further comprising using a second portion of the separated carbon dioxide as a flooding agent to produce hydrocarbon bed methane from a relatively low permeability formation containing heavy hydrocarbons.

3950. The method ofclaim 3949, wherein the relatively low peπneability foπnation containing heavy hydrocarbons is a deep relatively low permeability formation containing heavy hydrocarbons over 760 m below ground surface.

3951. The method of claim 3949, wherein the relatively low permeability fonnation containing heavy hydrocarbons adsorbs some of the carbon dioxide to sequester the carbon dioxide.

3952. The method of claim 3947, further comprising using a second portion of the separated carbon dioxide as a flooding agent for enhanced oil recovery.

3953. The method ofclaim 3947, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons undergo a reaction within the selected section to increase a H₂ concenfration within the produced synthesis gas.

3954. The method of clahn 3947, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within the selected section to increase an energy content of the produced synthesis gas.

3955. The method of claim 3947, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate electricity.

3956. The method of claim 3947, further comprising generating electricity from the synthesis gas using a fuel cell.

3957. The method of claim 3947, further comprising generating elecfricity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent portion of the formation.

3958. The method of claim 3947, further comprising using a portion of the synthesis gas as a combustion fuel for heating the fonnation.

3959. The method of claim 3947, further comprising converting at least a portion of the produced synthesis gas to condensable hydrocarbons using a Fischer-Tropsch synthesis process.

3960. The method of claim 3947, further comprising converting at least a portion of the produced synthesis gas to methanol.

3961. The method ofclaim 3947, further comprising converting at least a portion of the produced synthesis gas to gasoline.

3962. The method ofclaim 3947, further comprising converting at least a portion of the synthesis gas to methane using a catalytic methanation process.

3963. The method ofclaim 3947, wherein a temperature of the one or more heat sources is maintained at a temperature of less than approximately 700 °C to produce a synthesis gas having a ratio of H₂ to carbon monoxide of greater than about 2.

3964. The method ofclaim 3947, wherein a temperature of the one or more heat sources is maintained at a temperature of greater than approximately 700 °C to produce a synthesis gas having a ratio of H₂ to carbon monoxide of less than about 2.

3965. The method ofclaim 3947, wherein a temperature of the one or more heat sources is maintained at a temperature of approximately 700 °C to produce a synthesis gas having a ratio of H₂ to carbon monoxide of approximately 2.

3966. The method ofclaim 3947, wherein a heat source of the one or more of heat sources comprises an electrical heater.

3967. The method of clahn 3947, wherein a heat source of the one or more heat sources comprises a natural distributed heater.

3968. The method ofclaim 3947, wherein a heat source of the one or more heat sources comprises a flameless distributed combustor (FDC) heater, and wherein fluids are produced from the wellbore of the FDC heater through a conduit positioned within the wellbore.

3969. The method of claim 3947, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

3970. The method of claim 3947, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

3971. A method of in situ synthesis gas production, comprising: providing heat from one or more flameless distributed combustor heaters to at least a first portion of a relatively low permeability foimation containing heavy hydrocarbons; allowing the heat to transfer from the one or more heaters to a selected section of the formation to raise a temperature of the selected section to a temperature sufficient to generate synthesis gas; infroducing a synthesis gas producing fluid into the selected section to generate synthesis gas; and removing synthesis gas from the formation.

3972. The method ofclaim 3971, wherein the one or more heaters comprise at least two heaters, and wherein supeφosition of heat from at least the two heaters raises a temperature of the selected section to a temperature sufficient to generate synthesis gas.

3973. The method of claim 3971, further comprising producing the synthesis gas from the formation under pressure, and generating elecfricity from the produced synthesis gas by passing the produced synthesis gas through a turbine.

3974. The method ofclaim 3971, further comprising producing pyrolyzation products from the foimation when raising the temperature of the selected section to the temperature sufficient to generate synthesis gas.

3975. The method ofclaim 3971, further comprising separating a portion of carbon dioxide from the removed synthesis gas, and storing the carbon dioxide within a spent portion of the formation.

3976. The method ofclaim 3971, further comprising storing carbon dioxide within a spent portion of the formation, wherein an amount of carbon dioxide stored within the spent portion of the formation is equal to or greater than an amount of carbon dioxide within the removed synthesis gas.

3977. The method ofclaim 3971, further comprising separating a portion of H₂ from the removed synthesis gas; and using a portion of the separated H₂ as fuel for the one or more heaters.

3978. The method ofclaim 3971, further comprising using a portion of exhaust products from the one or more heaters as a portion of the synthesis gas producing fluid.

3979. The method ofclaim 3971, further comprising using a portion of the removed synthesis gas with a fuel cell to generate electricity.

3980. The method ofclaim 3979, wherein the fuel cell produces steam, and wherein a portion of the steam is used as a portion of the synthesis gas producing fluid.

3981. The method ofclaim 3979, wherein the fuel cell produces carbon dioxide, and wherein a portion of the carbon dioxide is infroduced into the formation to react with carbon within the formation to produce carbon monoxide.

3982. The method ofclaim 3979, wherein the fuel cell produces carbon dioxide, and further comprising storing an amount of carbon dioxide within a spent portion of the foimation equal or greater to an amount of the carbon dioxide produced by the fuel cell.

3983. The method of clahn 3971, further comprising using a portion of the removed synthesis gas as a feed product for foimation of hydrocarbons.

3984. The method of claim 3971 , wherein the synthesis gas producing fluid comprises hydrocarbons having carbon numbers less than 5, and wherehi the hydrocarbons crack within the formation to increase an amount of H₂ within the generated synthesis gas.

3985. The method ofclaim 3971, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

3986. The method ofclaim 3971, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

3987. A method of treating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the formation with one or more electrical heaters to a temperature sufficient to pyrolyze hydrocarbons within the portion; producing pyrolyzation fluid from the formation; separating a fuel cell feed stteam from the pyrolyzation fluid; and directing the fuel cell feed sfream to a fuel cell to produce elecfricity.

3988. The method ofclaim 3987, wherein the fuel cell is a molten carbonate fuel cell.

3989. The method of claim 3987, wherein the fuel cell is a solid oxide fuel cell.

3990. The method of claim 3987, further comprising using a portion of the produced electticity to power the elecfrical heaters.

3991. The method ofclaim 3987, wherein the fuel cell feed sfream comprises H₂ and hydrocarbons having a carbon number of less than 5.

3992. The method of claim 3987, wherein the fuel cell feed stteam comprises H₂ and hydrocarbons having a carbon number of less than 3.

3993. The method ofclaim 3987, further comprising hydrogenating the pyrolyzation fluid with aportion of H₂ from the pyrolyzation fluid.

3994. The method of claim 3987, wherein the hydrogenation is done in situ by directing the H₂ into the foimation.

3995. The method ofclaim 3987, wherein the hydrogenation is done in a surface unit.

3996. The method of claim 3987, further comprising directing hydrocarbon fluid having carbon numbers less than 5 adjacent to at least one of the electrical heaters, cracking a portion of the hydrocarbons to produce H₂, and producing a portion of the hydrogen from the formation.

3997. The method of claim 3996, further comprising directing an oxidizhig fluid adjacent to at least the one of the elecfrical heaters, oxidizing coke deposited on or near the at least one of the elecfrical heaters with the oxidizing fluid.

3998. The method of claim 3987, further comprising storing C0₂ from the fuel cell within the formation.

3999. The method of claim 3998, wherein the C0₂ is adsorbed to carbon material within a spent portion of the formation.

4000. The method ofclaim 3987, further comprising cooling the portion to form a spent portion of formation. .

4001. The method of claim 4000, wherein cooling the portion comprises introducing water into the portion to produce steam, and removing steam from the formation.

4002. The method ofclaim 4001, further comprising using a portion of the removed steam to heat a second portion of the formation.

4003. The method ofclaim 4001, further comprising using a portion of the removed steam as a synthesis gas producing fluid in a second portion of the formation.

4004. The method ofclaim 3987, further comprising: heating the portion to a temperature sufficient to support generation of synthesis gas after production of the pyrolyzation fluids; infroducing a synthesis gas producing fluid into the portion to generate synthesis gas; and removing a portion of the synthesis gas from the formation.

4005. The method ofclaim 4004, further comprising producing the synthesis gas from the formation under pressure, and generating electricity from the produced synthesis gas by passing the produced synthesis gas through a turbine.

4006. The method ofclaim 4004, further comprising using a first portion of the removed synthesis gas as fuel cell feed.

4007. The method ofclaim 4004, further comprising producing steam from operation of the fuel cell, and using the steam as part of the synthesis gas producing fluid.

4008. The method of claim 4004, further comprising using carbon dioxide from the fuel cell as a part of the synthesis gas producing fluid.

4009. The method of claim 4004, further comprising using a portion of the synthesis gas to produce hydrocarbon product.

4010. The method ofclaim 4004, further comprising cooling the portion to form a spent portion of formation.

4011. The method of claim 4010, wherein cooling the portion comprises introducing water into the portion to produce steam, and removing steam from the formation.

4012. The method ofclaim 4011, further comprising using a portion of the removed steam to heat a second portion of the formation.

4013. The method ofclaim 4011, further comprising using a portion of the removed steam as a synthesis gas producing fluid in a second portion of the formation.

4014. The method ofclaim 3987, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

4015. The method ofclaim 3987, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a friangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

4016. A method for in situ production of synthesis gas from a relatively low permeability foπnation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least some of the hydrocarbons within the selected section of the formation; producing pyrolysis products from the formation; heating at least a portion of the selected section to a temperature sufficient to generate synthesis gas; providing a synthesis gas generating fluid to at least the portion of the selected section to generate synthesis gas; and producing a portion of the synthesis gas from the foimation.

4017. The method ofclaim 4016, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4018. The method of claim 4016, further comprising heating at least the portion of the selected section when providing the synthesis gas generating fluid to inhibit temperature decrease within the selected section during synthesis gas generation.

4019. The method ofclaim 4016, wherein the temperature sufficient to allow synthesis gas generation is within a range from approximately 400 °C to approximately 1200 °C.

4020. The method ofclaim 4016, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with an oxidizing fluid; introducing the oxidizing fluid to the zones substantially by diffusion; allowing the oxidizing fluid to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and fransfening heat from the zones to the selected section.

4021. The method of claim 4016, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: infroducing an oxidizing fluid into the formation through a wellbore; transporting the oxidizing fluid substantially by convection into the portion of the selected section, wherein the portion of the selected section is at a temperature sufficient to support an oxidation reaction with the oxidizing fluid; and reacting the oxidizing fluid within the portion of the selected section to generate heat and raise the temperature of the portion.

4022. The method of claim 4016, wherein the one or more heat sources comprise one or more electrical heaters disposed in the foπnation.

4023. The method of claim 4016, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the foπnation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4024. The method of claim 4016, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation and providing a synthesis gas generating fluid to at least the portion of the selected section comprises infroducing steam into the portion.

4025. The method of claim 4016, further comprising controlling the heating of at least the portion of selected section and provision of the synthesis gas generathig fluid to maintain a temperature within at least the portion of the selected section above the temperature sufficient to generate synthesis gas.

4026. The method ofclaim 4016, further comprising: monitoring a composition of the produced synthesis gas; and controlling heating of at least the portion of selected section and provision of the synthesis gas generating fluid to maintain the composition of the produced synthesis gas within a desired range.

4027. The method of claim 4016, wherein the synthesis gas generathig fluid comprises liquid water.

4028. The method ofclaim 4016, wherein the synthesis gas generating fluid comprises steam.

4029. The method ofclaim 4016, wherein the synthesis gas generathig fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4030. The method of claim 4029, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4031. The method of claim 4016, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4032. The method ofclaim 4031, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the foimation.

4033. The method ofclaim 4016, wherein providing the synthesis gas generating fluid to at least the portion of the selected section comprises raising a water table of the formation to allow water to flow into the at least the portion of the selected section.

4034. The method ofclaim 4016, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within at least the portion of the selected section to increase a H₂ concenfration within the produced synthesis gas.

4035. The method of clahn 4016, wherein the synthesis gas generathig fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within at least the portion of the selected section to increase an energy content of the produced synthesis gas.

4036. The method of claim 4016, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate elecfricity.

4037. The method of claim 4016, further comprising generating elecfricity from the synthesis gas using a fuel cell.

4038. The method of claim 4016, further comprising generating electricity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent section of the formation.

4039. The method of claim 4016, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4040. The method ofclaim 4016, further comprising converting at least a portion of the produced synthesis gas to condensable hydrocarbons using a Fischer-Tropsch synthesis process.

4041. The method of claim 4016, further comprising converting at least a portion of the produced synthesis gas to methanol.

4042. The method of claim 4016, further comprising converting at least a portion of the produced synthesis gas to gasoline.

4043. The method ofclaim 4016, further comprising converting at least a portion of the synthesis gas to methane using a catalytic methanation process.

4044. The method of claim 4016, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

4045. The method ofclaim 4016, further comprising providing heat from three or more heat sources to at least a portion of the foπnation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

4046. A method for in situ production of synthesis gas from a relatively low permeability foimation containing heavy hydrocarbons, comprising: heating a first portion of the formation to pyrolyze some hydrocarbons within the first portion; allowing the heat to fransfer from one or more heat sources to a selected section of the formation, pyrolyzing hydrocarbons within the selected section; producing fluid from the ffrst portion, wherein the fluid comprises an aqueous fluid and a hydrocarbon fluid; heating a second portion of the formation to a temperature sufficient to allow synthesis gas generation; introducing at least a portion of the aqueous fluid to the second section after the section reaches the temperature sufficient to allow synthesis gas generation; and producing synthesis gas from the foπnation.

4047. The method of claim 4046, wherein the temperature sufficient to allow synthesis gas generation ranges from approximately 400 °C to approximately 1200 °C.

4048. The method ofclaim 4046, further comprising separating ammonia within the aqueous phase from the aqueous phase prior to introduction of at least the portion of the aqueous fluid to the second section.

4049. The method ofclaim 4046, further comprising heating the second portion of the formation during introduction of at least the portion of the aqueous fluid to the second section to inhibit temperature decrease in the second section due to synthesis gas generation.

4050. The method of claim 4046, wherein heating the second portion of the formation comprises converting an oxidizing fluid into a portion of the second portion that is above a temperature sufficient to support oxidation of carbon within the portion with the oxidizing fluid, and reacting the oxidizing fluid with carbon in the portion to generate heat within the portion.

4051. The method of claim 4046, wherein heating the second portion of the foimation comprises diffusing an oxidizing fluid to reaction zones adjacent to wellbores within the formation, oxidizing carbon within the reaction zones to generate heat, and fransfening the heat to the second portion.

4052. The method of claim 4046, wherein heating the second portion of the formation comprises heating the second section by transfer of heat from one or more electrical heaters.

4053. The method ofclaim 4046, wherein heating the second portion of the formation comprises heating the second section with a flameless disfributed combustor.

4054. The method of claim 4046, wherein heating the second portion of the formation comprises injecting steam into at least the portion of the formation.

4055. The method ofclaim 4046, wherein at least the portion of the aqueous fluid comprises a liquid phase.

4056. The method of clahn 4046, wherein at least a portion of the aqueous fluid comprises a vapor phase.

4057. The method of claim 4046, further comprising adding carbon dioxide to at least the portion of aqueous fluid to inhibit production of carbon dioxide from carbon within the formation.

4058. The method ofclaim 4057, wherein a portion of the carbon dioxide comprises carbon dioxide removed from the formation.

4059. The method of claim 4046, further comprising adding hydrocarbons with carbon numbers less than 5 to at least the portion of the aqueous fluid to increase a H₂ concentration within the produced synthesis gas.

4060. The method of claim 4046, further comprising adding hydrocarbons with carbon numbers less than 5 to at least the portion of the aqueous fluid to increase a H₂ concenfration within the produced synthesis gas, wherein the hydrocarbons are obtained from the produced fluid.

4061. The method of claim 4046, further comprising adding hydrocarbons with carbon numbers greater than 4 to at least the portion of the aqueous fluid to increase energy content of the produced synthesis gas.

4062. The method of claim 4046, further comprising adding hydrocarbons with carbon numbers greater than 4 to at least the portion of the aqueous fluid to increase energy content of the produced synthesis gas, wherein the hydrocarbons are obtained from the produced fluid.

4063. The method of claim 4046, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate electricity.

4064. The method of claim 4046, further comprising generating elecfricity from the synthesis gas using a fuel cell.

4065. The method of claim 4046, further comprising generating elecfricity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent portion of the foπnation.

4066. The method of claim 4046, further comprishig using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4067. The method ofclaim 4046, further comprising converting at least a portion of the produced synthesis gas to condensable hydrocarbons using a Fischer-Tropsch synthesis process.

4068. The method ofclaim 4046, further comprising converting at least a portion of the produced synthesis gas to methanol.

4069. The method of claim 4046, further comprising converting at least a portion of the produced synthesis gas to gasoline.

4070. The method of claim 4046, further comprising converting at least a portion of the synthesis gas to methane using a catalytic methanation process.

4071. The method ofclaim 4046, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

4072. The method of claim 4046, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

4073. A method for in situ production of synthesis gas from a relatively low peπneability fonnation containing heavy hydrocarbons, comprising: heating a portion of the formation with one or more heat sources to raise a temperature within the portion to a temperature sufficient to allow synthesis gas generation; providing a synthesis gas generating fluid into the portion through at least one injection wellbore to generate synthesis gas from hydrocarbons and the synthesis gas generating fluid; and producing synthesis gas from at least one heat source in which is positioned a heat source of the one or more heat sources.

4074. The method of claim 4073, wherein the temperature sufficient to allow synthesis gas generation is within a range from about 400° C to about 1200 °C.

4075. The method ofclaim 4073, wherein heating the portion comprises heating the portion to a temperature within a range sufficient to pyrolyze hydrocarbons within the portion, raising the temperature within the portion at a rate of less than about 5 °C per day during pyrolyzation and removing a portion of pyrolyzed fluid from the formation.

4076. The method ofclaim 4073, further comprising removing fluid from the formation through at least the one injection wellbore prior to heating the selected section to the temperature sufficient to allow synthesis gas generation.

4077. The method of claim 4073, wherein the injection wellbore comprises a wellbore of a heat source in which is positioned a heat source of the one or more heat sources.

4078. The method ofclaim 4073, further comprising heating the selected portion during providing the synthesis gas generating fluid to inhibit temperature decrease in at least the portion of the selected section due to synthesis gas generation.

4079. The method of clahn 4073 , further comprising providing a portion of the heat needed to raise the temperature sufficient to allow synthesis gas generation by convecting an oxidizing fluid to hydrocarbons within the selected section to oxidize a portion of the hydrocarbons and generate heat.

4080. The method ofclaim 4073, further comprising confrolling the heating of the selected section and provision of the synthesis gas generating fluid to maintain a temperature within the selected section above the temperature sufficient to generate synthesis gas.

4081. The method of claim 4073, further comprishig: monitoring a composition of the produced synthesis gas; and confrolling heating of the selected section and provision of the synthesis gas generating fluid to maintain the composition of the produced synthesis gas within a desfred range.

4082. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises liquid water.

4083. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises steam.

4084. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises steam to heat the selected section and to generate synthesis gas.

4085. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4086. The method ofclaim 4085, wherein a portion of the carbon dioxide comprises carbon dioxide removed from the fonnation.

4087. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4088. The method ofclaim 4087, wherein a portion of the carbon dioxide comprises carbon dioxide removed from the formation.

4089. The method ofclaim 4073, wherehi providing the synthesis gas generating fluid to the selected section comprises raising a water table of the formation to allow water to enter the selected section.

4090. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons undergo a reaction within the selected section to increase a H₂ concenfration within the produced synthesis gas.

4091. The method ofclaim 4073, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within the selected section to increase an energy content of the produced synthesis gas.

4092. The method of claim 4073, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate electticity.

4093. The method ofclaim 4073, further comprising generating electticity from the synthesis gas using a fuel cell.

4094. The method ofclaim 4073, further comprising generating electticity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent portion of the formation.

4095. The method ofclaim 4073, further comprising using a portion of the synthesis gas as a combustion fuel for heating the formation.

4096. The method ofclaim 4073, further comprising converting at least a portion of the produced synthesis gas to condensable hydrocarbons using a Fischer-Tropsch synthesis process.

4097. The method ofclaim 4073, further comprising converting at least a portion of the produced synthesis gas to methanol.

4098. The method ofclaim 4073, further comprising converting at least a portion of the produced synthesis gas to gasoline.

4099. The method of claim 4073, further comprising converting at least a portion of the synthesis gas to methane using a catalytic methanation process.

4100. The method ofclaim 4073, wherein a temperature of at least the one heat source is maintained at a temperature of less than approximately 700 °C to produce a synthesis gas having a ratio of H₂ to carbon monoxide of greater than about 2.

4101. The method of claim 4073 , wherehi a temperature of at least the one heat source is maintained at a temperature of greater than approximately 700 °C to produce a synthesis gas having a ratio of H₂ to carbon monoxide of less than about 2.

4102. The method of claim 4073 , wherein a temperature of at least the one heat source is maintained at a temperature of approximately 700 °C to produce a synthesis gas having a ratio of H₂ to carbon monoxide of approximately 2.

4103. The method ofclaim 4073, wherein a heat source of the one or more heat sources comprises an electrical heater.

4104. The method ofclaim 4073, wherein a heat source of the one or more heat sources comprises a natural distributed heater.

4105. The method ofclaim 4073, wherein a heat source of the one or more heat sources comprises a flameless disfributed combustor (FDC) heater, and wherein fluids are produced from the wellbore of the FDC heater through a conduit positioned within the wellbore.

4106. The method of claim 4073 , further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a friangular pattern.

4107. The method ofclaim 4073, further comprising providing heat from three or more heat sources to at least a portion of the foimation, wherein three or more of the heat sources are located in the foimation in a unit of heat sources, wherein the unit of heat sources comprises a ttiangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

4108. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least a portion of the hydrocarbon containing material within the selected section of the formation; producing pyrolysis products from the formation; heating a first portion of a formation with one or more heat sources to a temperature sufficient to allow generation of synthesis gas; providing a ffrst synthesis gas generating fluid to the first portion to generate a first synthesis gas; removing a portion of the first synthesis gas from the formation; heating a second portion of a formation with one or more heat sources to a temperature sufficient to allow generation of synthesis gas having a H₂ to CO ratio greater than a H₂ to CO ratio of the ffrst synthesis gas; providing a second synthesis gas generating component to the second portion to generate a second synthesis gas; removing a portion of the second synthesis gas from the formation; and blending a portion of the ffrst synthesis gas with a portion of the second synthesis gas to produce a blended synthesis gas having a selected H₂ to CO ratio.

4109. The method of clahn 4108, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4110. The method ofclaim 4108, wherein the first synthesis gas generating fluid and second synthesis gas generating fluid are the same component.

4111. The method of claim 4108, further comprising controlling the temperature in the first portion to confrol a composition of the first synthesis gas.

4112. The method of claim 4108, further comprising confrolling the temperature in the second portion to confrol a composition of the second synthesis gas.

4113. The method of claim 4108, wherein the selected ratio is confrolled to be approximately 2: 1 H₂ to CO.

4114. The method of clahn 4108, wherein the selected ratio is confrolled to range from approximately 1.8:1 to approximately 2.2: 1 H₂ to CO.

4115. The method ofclaim 4108, wherein the selected ratio is confrolled to be approximately 3:1 H₂to CO.

4116. The method of clahn 4108, wherein the selected ratio is confrolled to range from approximately 2.8:1 to approximately 3.2:1 H₂to CO.

4117. The method ofclaim 4108, further comprishig providing at least a portion of the produced blended synthesis gas to a condensable hydrocarbon synthesis process to produce condensable hydrocarbons.

4118. The method of claim 4117, wherein the condensable hydrocarbon synthesis process comprises a Fischer- Tropsch process.

4119. The method ofclaim 4118, further comprising cracking at least a portion of the condensable hydrocarbons to form middle distillates.

4120. The method ofclaim 4108, further comprising providing at least a portion of the produced blended synthesis gas to a catalytic methanation process to produce methane.

4121. The method of claim 4108, further comprising providing at least a portion of the produced blended synthesis gas to a methanol-synthesis process to produce methanol.

4122. The method ofclaim 4108, further comprising providing at least a portion of the produced blended synthesis gas to a gasoline-synthesis process to produce gasoline.

4123. The method of clahn 4108, wherein removing a portion of the second synthesis gas comprises withdrawing second synthesis gas through a production well, wherein a temperature of the production well adjacent to a second syntheses gas production zone is maintained at a substantially constant temperature configured to produce second synthesis gas having the H₂ to CO ratio greater the first synthesis gas.

4124. The method of claim 4108, wherein the first synthesis gas producing fluid comprises C0₂ and wherein the temperature of the ffrst portion is at a temperature that will result in conversion of C0₂ and carbon from the ffrst portion to CO to generate a CO rich first synthesis gas.

4125. The method ofclaim 4108, wherein the second synthesis gas producing fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons react within the formation to increase a H₂ concenfration within the produced second synthesis gas.

4126. The method ofclaim 4108, wherein blending a portion of the first synthesis gas with a portion of the second synthesis gas comprises producing an intermediate mixture having a H₂ to CO mixture of less than the selected ratio, and subjecting the intermediate mixture to a shift reaction to reduce an amount of CO and increase an amount of H₂ to produce the selected ratio of H₂ to CO.

4127. The method of claim 4108, further comprising removing an excess of first synthesis gas from the first portion to have an excess of CO, subjecting the ffrst synthesis gas to a shift reaction to reduce an amount of CO and increase an amount of H₂ before blending the first synthesis gas with the second synthesis gas.

4128. The method ofclaim 4108, further comprising removing the first synthesis gas from the foπnation under pressure, and passing removed first synthesis gas through a turbine to generate elecfricity.

4129. The method ofclaim 4108, further comprising removing the second synthesis gas from the formation under pressure, and passing removed second synthesis gas through a turbine to generate electticity.

4130. The method ofclaim 4108, further comprising generating electticity from the blended synthesis gas using a fuel cell.

4131. The method of claim 4108, further comprising generating elecfricity from the blended synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent portion of the formation.

4132. The method ofclaim 4108, further comprising using at least a portion of the blended synthesis gas as a combustion fuel for heating the formation.

4133. The method of clahn 4108, further comprising heating at least the portion of the selected section when providing the synthesis gas generating fluid to inhibit temperature decrease within the selected section during synthesis gas generation.

4134. The method ofclaim 4108, wherehi the temperature sufficient to allow synthesis gas generation is within a range from approxhnately 400 °C to approxhnately 1200 °C.

4135. The method ofclaim 4108, wherein heating the first a portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with an oxidizing fluid; introducing the oxidizing fluid to the zones substantially by diffusion; allowing the oxidizing fluid to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and transfening heat from the zones to the selected section.

4136. The method of claim 4108, wherehi heating the second portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with an oxidizing fluid; introducing the oxidizing fluid to the zones substantially by diffusion; allowing the oxidizing fluid to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and transfening heat from the zones to the selected section.

4137. The method ofclaim 4108, wherein heating the first portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: introducing an oxidizing fluid into the formation through a wellbore; ttansporting the oxidizing fluid substantially by convection into the first portion of the selected section, wherein the ffrst portion of the selected section is at a temperature sufficient to support an oxidation reaction with the oxidizing fluid; and reacting the oxidizing fluid within the first portion of the selected section to generate heat and raise the temperature of the first portion.

4138. The method ofclaim 4108, wherein heating the second portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: infroducing an oxidizing fluid into the foπnation through a wellbore; ttansporting the oxidizing fluid substantially by convection into the second portion of the selected section, wherein the second portion of the selected section is at a temperature sufficient to support an oxidation reaction with the oxidizing fluid; and reacting the oxidizing fluid within the second portion of the selected section to generate heat and raise the temperature of the second portion.

4139. The method ofclaim 4108, wherein the one or more heat sources comprise one or more electrical heaters disposed in the formation.

4140. The method ofclaim 4108, wherein the one or more heat sources comprises one or more natural distributed combustors.

4141. The method ofclaim 4108, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4142. The method of claim 4108, wherein heating the ffrst portion of the selected section to a temperature sufficient to allow synthesis gas generation and providing a first synthesis gas generating fluid to the first portion of the selected section comprises introducing steam into the first portion.

4143. The method of claim 4108, wherein heating the second portion of the selected section to a temperature sufficient to allow synthesis gas generation and providing a second synthesis gas generating fluid to the second portion of the selected section comprises introducing steam into the second portion.

4144. The method of clahn 4108, further comprising controlling the heating of the ffrst portion of selected section and provision of the first synthesis gas generating fluid to maintain a temperature within the ffrst portion of the selected section above the temperature sufficient to generate synthesis gas.

4145. The method of claim 4108, further comprising confrolling the heating of the second portion of selected section and provision of the second synthesis gas generating fluid to maintain a temperature within the second portion of the selected section above the temperature sufficient to generate synthesis gas.

4146. The method ofclaim 4108, wherein the ffrst synthesis gas generating fluid comprises liquid water.

4147. The method ofclaim 4108, wherein the second synthesis gas generating fluid comprises liquid water.

4148. The method ofclaim 4108, wherein the first synthesis gas generating fluid comprises steam.

4149. The method ofclaim 4108, wherein the second synthesis gas generathig fluid comprises steam.

4150. The method ofclaim 4108, wherein the first synthesis gas generating fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4151. The method of claim 4150, wherein a portion of the carbon dioxide within the ffrst synthesis gas generating fluid comprises carbon dioxide removed from the foπnation.

4152. The method ofclaim 4108, wherein the second synthesis gas generathig fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4153. The method ofclaim 4152, wherein a portion of the carbon dioxide within the second synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4154. The method ofclaim 4108, wherein the first synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4155. The method of clahn 4154, wherein a portion of the carbon dioxide within the first synthesis gas generating fluid comprises carbon dioxide removed from the foimation.

4156. The method ofclaim 4108, wherein the second synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the foimation to generate carbon monoxide.

4157. The method ofclaim 4156, wherein a portion of the carbon dioxide within the second synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4158. The method ofclaim 4108, wherein providing the first synthesis gas generating fluid to the ffrst portion of the selected section comprises raising a water table of the formation to allow water to flow into the first portion of the selected section.

4159. The method ofclaim 4108, wherein providing the second synthesis gas generating fluid to the second portion of the selected section comprises raising a water table of the formation to allow water to flow into the second portion of the selected section.

4160. The method of claim 4108, wherein the first synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within the first portion of the selected section to increase a H₂ concentration within the produced first synthesis gas.

4161. The method of clahn 4108, wherein the second synthesis gas generating fluid comprises water and hydrocarbons having carbon nmnbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within the second portion of the selected section to increase a H₂ concenfration within the produced second synthesis gas.

4162. The method ofclaim 4108, wherein the ffrst synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within the first portion of the selected section to increase an energy content of the produced first synthesis gas.

4163. The method ofclaim 4108, wherein the second synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within at least the second portion of the selected section to increase an energy content of the second produced synthesis gas.

4164. The method of claim 4108, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced blended synthesis gas through a turbine to generate electticity.

4165. The method of claim 4108, further comprising generating electricity from the blended synthesis gas using a fuel cell.

4166. The method ofclaim 4108, further comprising generating elecfricity from the blended synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent section of the foimation.

4167. The method ofclaim 4108, further comprising using a portion of the blended synthesis gas as a combustion fuel for the one or more heat sources.

4168. The method of clahn 4108, further comprising using a portion of the ffrst synthesis gas as a combustion fuel for the one or more heat sources.

4169. The method of claim 4108, further comprising using a portion of the second synthesis gas as a combustion fuel for the one or more heat sources.

4170. The method ofclaim 4108, further comprising using a portion of the blended synthesis gas as a combustion fuel for the one or more heat sources.

4171. A method of freating a relatively low permeability foimation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least some of the hydrocarbons within the selected section of the formation; producing pyrolysis products from the formation; heating at least a portion of the selected section to a temperature sufficient to generate synthesis gas; confrolling a temperature of at least a portion of the selected section to generate synthesis gas having a selected H₂ to CO ratio; providing a synthesis gas generating fluid to at least the portion of the selected section to generate synthesis gas; and producing a portion of the synthesis gas from the fonnation.

4172. The method ofclaim 4171, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4173. The method ofclaim 4171, wherein the selected ratio is confrolled to be approxhnately 2: 1 H₂ to CO.

4174. The method ofclaim 4171, wherein the selected ratio is confrolled to range from approximately 1.8: 1 to approximately 2.2:1 H₂to CO.

4175. The method ofclaim 4171, wherein the selected ratio is controlled to be approximately 3:1 H₂to CO.

4176. The method ofclaim 4171, wherein the selected ratio is confrolled to range from approximately 2.8:1 to approxhnately 3.2: 1 H₂to CO.

177. The method of claim 4171, further comprising providing at least a portion of the produced synthesis gas to a condensable hydrocarbon synthesis process to produce condensable hydrocarbons.

4178. The method ofclaim 4177, wherein the condensable hydrocarbon synthesis process comprises a Fischer- Tropsch process.

4179. The method ofclaim 4178, further comprising cracking at least a portion of the condensable hydrocarbons to form middle distillates.

4180. The method ofclaim 4171, further comprishig providing at least a portion of the produced synthesis gas to a catalytic methanation process to produce methane.

4181. The method ofclaim 4171, further comprising providing at least a portion of the produced synthesis gas to a methanol-synthesis process to produce methanol.

4182. The method ofclaim 4171, further comprising providing at least a portion of the produced synthesis gas to a gasoline-synthesis process to produce gasoline.

4183. The method ofclaim 4171, further comprising heating at least-the portion of the selected section when providing the synthesis gas generating fluid to inhibit temperature decrease within the selected section during synthesis gas generation.

4184. The method ofclaim 4171, wherein the temperature sufficient to allow synthesis gas generation is within a range from approximately 400 °C to approximately 1200 °C.

4185. The method ofclaim 4171, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with an oxidizing fluid; infroducing the oxidizing fluid to the zones substantially by diffusion; allowing the oxidizing fluid to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and transferring heat from the zones to the selected section.

4186. The method of claim 4171, wherehi heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: infroducing an oxidizing fluid into the formation through a wellbore; fransporting the oxidizing fluid substantially by convection into the portion of the selected section, wherein the portion of the selected section is at a temperature sufficient to support an oxidation reaction with the oxidizing fluid; and reacting the oxidizing fluid within the portion of the selected section to generate heat and raise the temperature of the portion.

4187. The method of claim 4171, wherein the one or more heat sources comprise one or more elecfrical heaters disposed in the formation.

4188. The method of claim 4171, wherein the one or more heat sources comprises one or more natural disfributed combustors.

4189. The method ofclaim 4171, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the foimation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4190. The method of clahn 4171, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation and providing a synthesis gas generating fluid to at least the portion of the selected section comprises infroducing steam into the portion.

4191. The method of claim 4171, further comprising confrolling the heating of at least the portion of selected section and provision of the synthesis gas generating fluid to maintain a temperature within at least the portion of the selected section above the temperature sufficient to generate synthesis gas.

4192. The method ofclaim 4171, wherein the synthesis gas generating fluid comprises liquid water.

4193. The method of claim 4171, wherein the synthesis gas generating fluid comprises steam.

4194. The method ofclaim 4171, wherein the synthesis gas generating fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4195. The method ofclaim 4194, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the foimation.

4196. The method ofclaim 4171, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4197. The method ofclaim 4196, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4198. The method of claim 4171, wherein providing the synthesis gas generating fluid to at least the portion of the selected section comprises raising a water table of the formation to allow water to flow into the at least the portion of the selected section.

4199. The method ofclaim 4171, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within at least the portion of the selected section to increase a H₂ concenfration within the produced synthesis gas.

4200. The method of clahn 4171 , wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within at least the portion of the selected section to increase an energy content of the produced synthesis gas.

4201. The method of claim 4171, further comprishig maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate electricity.

4202. The method of clahn 4171, further comprishig generating elecfricity from the synthesis gas using a fuel cell.

4203. The method ofclaim 4171, further comprismg generating electticity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent section of the formation.

4204. The method ofclaim 4171, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4205. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least some of the hydrocarbons within the selected section of the formation; producing pyrolysis products from the formation; heating at least a portion of the selected section to a temperature sufficient to generate synthesis gas; conttoUing a temperature in or proximate to a synthesis gas production well to generate synthesis gas having a selected H₂ to CO ratio; providing a synthesis gas generating fluid to at least the portion of the selected section to generate synthesis gas; and producing synthesis gas from the formation.

4206. The method of claim 4205, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4207. The method of claim 4205, wherein the selected ratio is confrolled to be approximately 2:1 H₂ to CO.

4208. The method of claim 4205, wherein the selected ratio is controlled to range from approximately 1.8: 1 to approximately 2.2:1 H₂to CO.

4209. The method of claim 4205, wherein the selected ratio is confrolled to be approximately 3 : 1 H₂ to CO.

4210. The method ofclaim 4205, wherein the selected ratio is confrolled to range from approximately 2.8:1 to approximately 3.2:1 H₂ to CO.

4211. The method of clahn 4205, further comprising providing at least a portion of the produced synthesis gas to a condensable hydrocarbon synthesis process to produce condensable hydrocarbons.

4212. The method ofclaim 4211, wherein the condensable hydrocarbon synthesis process comprises a Fischer- Tropsch process.

4213. The method ofclaim 4212, further comprising cracking at least a portion of the condensable hydrocarbons to form middle distillates.

4214. The method ofclaim 4205, further comprising providing at least a portion of the produced synthesis gas to a catalytic methanation process to produce methane.

4215. The method ofclaim 4205, further comprising providing at least a portion of the produced synthesis gas to a methanol-synthesis process to produce methanol.

4216. The method ofclaim 4205, further comprising providing at least a portion of the produced synthesis gas to a gasoline-synthesis process to produce gasoline.

4217. The method ofclaim 4205, further comprising heating at least the portion of the selected section when providing the synthesis gas generating fluid to inhibit temperature decrease within the selected section during synthesis gas generation.

4218. The method ofclaim 4205, wherein the temperature sufficient to allow synthesis gas generation is within a range from approximately 400 °C to approximately 1200 °C.

4219. The method ofclaim 4205, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with an oxidizing fluid; introducing the oxidizing fluid to the zones substantially by diffusion; allowing the oxidizing fluid to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and fransfening heat from the zones to the selected section.

4220. The method of claim 4205, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: introducing an oxidizing fluid into the formation through a wellbore; transporting the oxidizing fluid substantially by convection into the portion of the selected section, wherein the portion of the selected section is at a temperature sufficient to support an oxidation reaction with the oxidizing fluid; and reacting the oxidizing fluid within the portion of the selected section to generate heat and raise the temperature of the portion.

4221. The method of claim 4205, wherein the one or more heat sources comprise one or more electrical heaters disposed in the foπnation.

4222. The method ofclaim 4205, wherein the one or more heat sources comprises one or more natural distributed combustors.

4223. The method ofclaim 4205, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4224. The method ofclaim 4205, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation and providing a synthesis gas generating fluid to at least the portion of the selected section comprises introducing steam into the portion.

4225. The method ofclaim 4205, further comprishig confrolling the heating of at least the portion of selected section and provision of the synthesis gas generating fluid to maintain a temperature within at least the portion of the selected section above the temperature sufficient to generate synthesis gas.

4226. The method of claim 4205, wherein the synthesis gas generating fluid comprises liquid water.

4227. The method of clahn 4205, wherein the synthesis gas generating fluid comprises steam.

4228. The method ofclaim 4205, wherein the synthesis gas generating fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4229. The method of claim 4228, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4230. The method ofclaim 4205, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4231. The method of claim 4230, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4232. The method of claim 4205, wherein providing the synthesis gas generating fluid to at least the portion of the selected section comprises raising a water table of the formation to allow water to flow into the at least the portion of the selected section.

4233. The method ofclaim 4205, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within at least the portion of the selected section to increase a H₂ concentration within the produced synthesis gas.

4234. The method ofclaim 4205, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within at least the portion of the selected section to increase an energy content of the produced synthesis gas.

4235. The method ofclaim 4205, further comprising maintaining a pressure withhi the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate electricity.

4236. The method ofclaim 4205, further comprising generating elecfricity from the synthesis gas using a fuel cell.

4237. The method ofclaim 4205, further comprising generating elecfricity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent section of the formation.

4238. The method ofclaim 4205, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4239. A method of treating a relatively low permeability formation containing heavy, hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least some of the hydrocarbons within the selected section of the formation; producing pyrolysis products from the formation; heating at least a portion of the selected section to a temperature sufficient to generate synthesis gas; confrolling a temperature of at least a portion of the selected section to generate synthesis gas having a H₂ to CO ratio different than a selected H₂ to CO ratio; providing a synthesis gas generating fluid to at least the portion of the selected section to generate synthesis gas; and producing synthesis gas from the foimation; providing at least a portion of the produced synthesis gas to a shift process wherein an amount of carbon monoxide is converted to carbon dioxide; separating at least a portion of the carbon dioxide to obtain a gas having a selected H₂ to CO ratio.

4240. The method of clahn 4239, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4241. The method of claim 4239, wherein the selected ratio is confrolled to be approximately 2: 1 H₂ to CO.

4242. The method ofclaim 4239, wherein the selected ratio is controlled to range from approximately 1.8:1 to 2.2:1 H₂ to CO.

4243. The method of claim 4239, wherein the selected ratio is controlled to be approximately 3 : 1 H₂ to CO.

4244. The method ofclaim 4239, wherein the selected ratio is confrolled to range from approximately 2.8: 1 to 3.2:1 H₂ to CO.

4245. The method ofclaim 4239, further comprising providing at least a portion of the produced synthesis gas to a condensable hydrocarbon synthesis process to produce condensable hydrocarbons.

4246. The method ofclaim 4245, wherein the condensable hydrocarbon synthesis process comprises a Fischer- Tropsch process.

4247. The method of claim 4246, further comprising cracking at least a portion of the condensable hydrocarbons to form middle distillates.

4248. The method ofclaim 4239, further comprising providing at least a portion of the produced synthesis gas to a catalytic methanation process to produce methane.

4249. The method of claim 4239, further comprising providing at least a portion of the produced synthesis gas to a methanol-synthesis process to produce methanol.

4250. The method of claim 4239, further comprising providing at least a portion of the produced synthesis gas to a gasoline-synthesis process to produce gasoline.

4251. The method of claim 4239, further comprising heating at least the portion of the selected section when providing the synthesis gas generating fluid to inhibit temperature decrease within the selected section during synthesis gas generation.

4252. The method ofclaim 4239, wherein the temperature sufficient to allow synthesis gas generation is within a range from approximately 400 °C to approximately 1200 °C.

4253. The method ofclaim 4239, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with an oxidizing fluid; introducing the oxidizing fluid to the zones substantially by diffusion; allowing the oxidizing fluid to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and fransfening heat from the zones to the selected section.

4254. The method of claim 4239, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation comprises: infroducing an oxidizing fluid into the formation through a wellbore; transporting the oxidizhig fluid substantially by convection into the portion of the selected section, wherein the portion of the selected section is at a temperature sufficient to support an oxidation reaction with the oxidizing fluid; and reacting the oxidizing fluid within the portion of the selected section to generate heat and raise the temperature of the portion.

4255. The method of claim 4239, wherein the one or more heat sources comprise one or more electrical heaters disposed in the formation.

4256. The method ofclaim 4239, wherein the one or more heat sources comprises one or more natural distributed combustors.

4257. The method ofclaim 4239, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4258. The method of clahn 4239, wherein heating at least the portion of the selected section to a temperature sufficient to allow synthesis gas generation and providing a synthesis gas generating fluid to at least the portion of the selected section comprises infroducing steam into the portion.

4259. The method of claim 4239, further comprising confrolling the heating of at least the portion of selected section and provision of the synthesis gas generating fluid to maintain a temperature within at least the portion of the selected section above the temperature sufficient to generate synthesis gas.

4260. The method of claim 4239, wherein the synthesis gas generating fluid comprises liquid water.

4261. The method ofclaim 4239, wherein the synthesis gas generating fluid comprises steam.

4262. The method of claim 4239, wherein the synthesis gas generating fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4263. The method of claim 4262, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the foimation.

4264. The method ofclaim 4239, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4265. The method ofclaim 4264, wherein a portion of the carbon dioxide within the synthesis gas generathig fluid comprises carbon dioxide removed from the formation.

4266. The method of claim 4239, wherehi providing the synthesis gas generating fluid to at least the portion of the selected section comprises raising a water table of the formation to allow water to flow into the at least the portion of the selected section.

4267. The method of claim 4239, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers less than 5, and wherein at least a portion of the hydrocarbons are subjected to a reaction within at least the portion of the selected section to increase a H₂ concenfration within the produced synthesis gas.

4268. The method ofclaim 4239, wherein the synthesis gas generating fluid comprises water and hydrocarbons having carbon numbers greater than 4, and wherein at least a portion of the hydrocarbons react within at least the portion of the selected section to increase an energy content of the produced synthesis gas.

4269. The method ofclaim 4239, further comprising maintaining a pressure within the formation during synthesis gas generation, and passing produced synthesis gas through a turbine to generate elecfricity.

4270. The method ofclaim 4239, further comprising generating elecfricity from the synthesis gas using a fuel cell.

4271. The method ofclaim 4239, further comprising generating elecfricity from the synthesis gas using a fuel cell, separating carbon dioxide from a fluid exiting the fuel cell, and storing a portion of the separated carbon dioxide within a spent section of the formation.

4272. The method of clahn 4239, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4273. A method of forming a spent portion of formation within a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a first portion of the formation to pyrolyze hydrocarbons within the first portion; and cooling the first portion.

4274. The method of claim 4273, wherein heating the first portion comprises transfening heat to the ffrst portion from one or more elecfrical heaters.

4275. The method ofclaim 4273, wherein heating the first portion comprises fransfening heat to the first portion from one or more natural disfributed combustors.

4276. The method ofclaim 4273, wherein heating the first portion comprises transfening heat to the first portion from one or more flameless disfributed combustors.

4277. The method ofclaim 4273, wherein heating the first portion comprises fransfening heat to the first portion from heat ttansfer fluid flowing within one or more wellbores within the formation.

4278. The method ofclaim 4277, wherein the heat transfer fluid comprises steam.

4279. The method of claim 4277, wherein the heat fransfer fluid comprises combustion products from a burner.

4280. The method of claim 4273, wherein heating the ffrst portion comprises transfening heat to the ffrst portion from at least two heater wells positioned within the formation, wherein the at least two heater wells are placed in a substantially regular pattern, wherein the substantially regular pattern comprises repetition of a base heater unit, and wherein the base heater unit is formed of a number of heater wells.

4281. The method of claim 4280, wherein a spacing between a pair of adjacent heater wells is within a range from about 6 m to about 15 m.

4282. The method ofclaim 4280, further comprising removing fluid from the formation through one or more production wells.

4283. The method of claim 4282, wherein the one or more production wells are located in a pattern, and wherehi the one or more production wells are positioned substantially at centers of base heater units.

4284. The method ofclaim 4280, wherein the heater unit comprises three heater wells positioned substantially at apexes of an equilateral triangle.

4285. The method ofclaim 4280, wherein the heater unit comprises four heater wells positioned substantially at apexes of a rectangle.

4286. The method of claim 4280, wherein the heater unit comprises five heater wells positioned substantially at apexes of a regular pentagon.

4287. The method ofclaim 4280, wherein the heater unit comprises six heater wells positioned substantially at apexes of a regular hexagon.

4288. The method ofclaim 4273, further comprising infroducing water to the first portion to cool the formation.

4289. The method of claim 4273, further comprising removmg steam from the formation.

4290. The method ofclaim 4289, further comprising using a portion of the removed steam to heat a second portion of the formation.

4291. The method ofclaim 4273, further comprising removing pyrolyzation products from the formation.

4292. The method of claim 4273, further comprising generating synthesis gas within the portion by introducing a synthesis gas generating fluid into the portion, and removing synthesis gas from the foimation.

4293. The method of claim 4273, further comprising heating a second section of the formation to pyrolyze hydrocarbons within the second portion, removing pyrolyzation fluid from the second portion, and storing a portion of the removed pyrolyzation fluid within the first portion.

4294. The method ofclaim 4293, wherein the portion of the removed pyrolyzation fluid is stored within the first portion when surface facilities that process the removed pyrolyzation fluid are not able to process the portion of the removed pyrolyzation fluid.

4295. The method ofclaim 4293, further comprising heating the first portion to facilitate removal of the stored pyrolyzation fluid from the ffrst portion.

4296. The method of claim 4273, further comprising generating synthesis gas within a second portion of the formation, removing synthesis gas from the second portion, and storing a portion of the removed synthesis gas within the ffrst portion.

4297. The method ofclaim 4296, wherein the portion of the removed synthesis gas from the second portion is stored within the first portion when surface facilities that process the removed synthesis gas are not able to process the portion of the removed synthesis gas.

4298. The method ofclaim 4296, further comprising heating the first portion to facilitate removal of the stored synthesis gas from the first portion.

4299. The method of claim 4273, further comprising removing at least a portion of hydrocarbon containing material in the first portion and, further comprising using at least a portion of the hydrocarbon containing material removed from the foπnation in a metallurgical application.

4300. The method ofclaim 4299, wherein the metallurgical application comprises steel manufacturing.

4301. A method of sequestering carbon dioxide within a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the formation; allowing the portion to cool; and storing carbon dioxide within the portion.

4302. The method ofclaim 4301, further comprising raising a water level within the portion to inhibit migration of the carbon dioxide from the portion.

4303. The method ofclaim 4301, further comprising heathig the portion to release carbon dioxide, and removing carbon dioxide from the portion.

4304. The method ofclaim 4301, further comprising pyrolyzing hydrocarbons within the portion during heating of the portion, and removing pyrolyzation product from the formation.

4305. The method ofclaim 4301, further comprising producing synthesis gas from the portion during the heating of the portion, and removing synthesis gas from the foπnation.

4306. The method ofclaim 4301, wherehi heating the portion comprises: heating hydrocarbon containing material adjacent to one or more wellbores to a temperature sufficient to support oxidation of the hydrocarbon containing material with an oxidizing fluid; introducing the oxidizing fluid to hydrocarbon containing material adjacent to the one or more wellbores to oxidize the hydrocarbons and produce heat; and conveying produced heat to the portion.

4307. The method ofclaim 4306, wherein heating hydrocarbon containing material adjacent to the one or more wellbores comprises electtically heating the hydrocarbon containing material.

4308. The method of claim 4306, wherehi the temperature sufficient to support oxidation is in a range from approximately 200 °C to approximately 1200 °C.

4309. The method ofclaim 4301, wherehi heating the portion comprises circulating heat transfer fluid through one or more heating wells within the foπnation.

4310. The method of claim 4309, wherein the heat transfer fluid comprises combustion products from a burner.

4311. The method of claim 4309, wherein the heat fransfer fluid comprises steam.

4312. The method ofclaim 4301, further comprising removing fluid from the formation during heating of the foimation, and combusting a portion of the removed fluid to generate heat to heat the formation.

4313. The method ofclaim 4301, further comprising using at least a portion of the carbon dioxide for hydrocarbon bed demethanation prior to storing the carbon dioxide within the portion.

4314. The method ofclaim 4301, further comprising using a portion of the carbon dioxide for enhanced oil recovery prior to storing the carbon dioxide within the portion.

4315. The method of claim 4301 , wherein at least a portion of the carbon dioxide comprises carbon dioxide generated in a fuel cell.

4316. The method ofclaim 4301, wherein at least a portion of the carbon dioxide comprises carbon dioxide formed as a combustion product.

4317. The method of claim 4301, further comprising allowing the portion to cool by infroducing water to the portion; and removing the water from the foimation as steam.

4318. The method of claim 4317, further comprishig using the steam as a heat transfer fluid to heat a second portion of the formation.

4319. The method ofclaim 4301, wherein storing carbon dioxide in the portion comprises adsorbing carbon dioxide to hydrocarbon containing material within the formation.

4320. The method ofclaim 4301, wherein storing carbon dioxide comprises passing a first fluid sfream comprising the carbon dioxide and other fluid through the portion; adsorbing carbon dioxide onto hydrocarbon containing material withhi the formation; and removing a second fluid stream from the foπnation, wherein a concenfration of the other fluid in the second fluid stream is greater than concentration of other fluid in the first stteam due to the absence of the adsorbed carbon dioxide in the second stteam.

4321. The method ofclaim 4301, wherein an amount of carbon dioxide stored within the portion is equal to or greater than an amount of carbon dioxide generated within the portion and removed from the foπnation during heating of the portion.

4322. The method ofclaim 4301, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherein the unit of heat sources comprises a triangular pattern.

4323. The method ofclaim 4301, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

4324. A method of in situ sequestration of carbon dioxide within a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a first portion of the formation; allowing the heat to fransfer from one or more sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least some of the hydrocarbons within the selected section of the formation; producing pyrolyzation fluids, wherehi the pyrolyzation fluids comprise carbon dioxide; and storing an amount of carbon dioxide in the formation, wherein the amount of stored carbon dioxide is equal to or greater than an amount of carbon dioxide within the pyrolyzation fluids.

4325. The method of claim 4324, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4326. The method of claim 4324, wherein the carbon dioxide is stored within a spent portion of the foimation.

4327. The method ofclaim 4324, wherein a portion of the carbon dioxide stored within the formation is carbon dioxide separated from the pyrolyzation fluids.

4328. The method ofclaim 4324, further comprising separating a portion of carbon dioxide from the pyrolyzation fluids, and using the carbon dioxide as a flooding agent in enhanced oil recovery.

4329. The method of claim 4324, further comprising separating a portion of carbon dioxide from the pyrolyzation fluids, and using the carbon dioxide as a synthesis gas generating fluid for the generation of synthesis gas from a section of the formation that is heated to a temperature sufficient to generate synthesis gas upon introduction of the synthesis gas generating fluid.

4330. The method ofclaim 4324, further comprising separating a portion of carbon dioxide from the pyrolyzation fluids, and using the carbon dioxide to displace hydrocarbon bed methane.

4331. The method ofclaim 4330, wherein the hydrocarbon bed is a deep hydrocarbon bed located over 760 m below ground surface.

4332. The method ofclaim 4330, further comprising adsorbing a portion of the carbon dioxide within the hydrocarbon bed.

4333. The method ofclaim 4324, further comprising using at least a portion of the pyrolyzation fluids as a feed stream for a fuel cell.

4334. The method ofclaim 4333, wherein the fuel cell generates carbon dioxide, and further comprising storing an amount of carbon dioxide equal to or greater than an amount of carbon dioxide generated by the fuel cell within the formation.

4335. The method ofclaim 4324, wherein a spent portion of the formation comprises hydrocarbon containing material within a section of the formation that has been heated and from which condensable hydrocarbons have been produced, and wherein the spent portion of the formation is at a temperature at which carbon dioxide adsorbs onto the hydrocarbon containing material.

4336. The method of claim 4324, further comprising raising a water level within the spent portion to inhibit migration of the carbon dioxide from the portion.

4337. The method ofclaim 4324, wherein producing fluids from the formation comprises removing pyrolyzation products from the formation.

4338. The method ofclaim 4324, wherehi producing fluids from the formation comprises heating the selected section to a temperature sufficient to generate synthesis gas; introducing a synthesis gas generating fluid into the selected section; and removing synthesis gas from the formation.

4339. The method ofclaim 4338, wherein the temperature sufficient to generate synthesis gas ranges from about 400 °C to about 1200 °C.

4340. The method ofclaim 4338, wherein heating the selected section comprises infroducing an oxidizing fluid into the selected section, reacting the oxidizing fluid within the selected section to heat the selected section.

4341. The method ofclaim 4338, wherein heating the selected section comprises: heating hydrocarbon containing material adjacent to one or more wellbores to a temperature sufficient to support oxidation of the hydrocarbon containing material with an oxidant; infroducing the oxidant to hydrocarbon containing material adjacent to the one or more wellbores to oxidize the hydrocarbons and produce heat; and conveying produced heat to the portion.

4342. The method ofclaim 4324, wherein the one or more heat sources comprise elecfrical heaters.

4343. The method ofclaim 4324, wherein the one or more heat sources comprise flameless distributed combustors.

4344. The method ofclaim 4343, wherein a portion of fuel for the one or more flameless disfributed combustors is obtained from the foπnation.

4345. The method ofclaim 4324, wherein the one or more heat sources comprise heater wells in the formation through which heat transfer fluid is circulated.

4346. The method of claim 4345, wherein the heat fransfer fluid comprises combustion products.

4347. The method of claim 4345, wherein the heat fransfer fluid comprises steam.

4348. The method of claim 4324, wherein condensable hydrocarbons are produced under pressure, and further comprising generating elecfricity by passing a portion of the produced fluids through a turbine.

4349. The method ofclaim 4324, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, and wherehi the unit of heat sources comprises a ttiangular pattern.

4350. The method of claim 4324, further comprising providing heat from three or more heat sources to at least a portion of the formation, wherein three or more of the heat sources are located in the formation in a unit of heat sources, wherein the unit of heat sources comprises a triangular pattern, and wherein a plurality of the units are repeated over an area of the formation to form a repetitive pattern of units.

4351. A method for in situ production of energy from a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation such that the heat from the one or more heat sources pyrolyzes at least a portion of the hydrocarbons within the selected section of the formation; producing pyrolysis products from the formation; providing at least a portion of the pyrolysis products to a reformer to generate synthesis gas; producing the synthesis gas from the reformer; providing at least a portion of the produced synthesis gas to a fuel cell to produce electricity, wherein the fuel cell produces a carbon dioxide containing exit sfream; and storing at least a portion of the carbon dioxide in the carbon dioxide containing exit sfream in a subsurface formation.

4352. The method ofclaim 4351, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the fonnation.

4353. The method ofclaim 4351, wherein at least a portion of the pyrolysis products are used as fuel in the reformer.

4354. The method ofclaim 4351, wherein the synthesis gas comprises substantially H₂.

4355. The method of claim 4351, wherein the subsurface formation is a spent portion of the foimation.

4356. The method of clahn 4351, wherein the subsurface formation is an oil reservoir.

4357. The method ofclaim 4356, wherein at least a portion of the carbon dioxide is used as a drive fluid for enhanced oil recovery in the oil reservofr.

4358. The method of claim 4351, wherein the subsurface formation is a hydrocarbon formation.

4359. The method of claim 4358, wherein at least a portion of the carbon dioxide is used to produce methane from the hydrocarbon foimation.

4360. The method of claim 4358, wherein the hydrocarbon formation is located over about 760 m below ground surface.

4361. The method ofclaim 4359, further comprising sequestering at least a portion of the carbon dioxide within the hydrocarbon formation.

4362. The method ofclaim 4351, wherein the reformer produces a reformer carbon dioxide containing exit stream.

4363. The method ofclaim 4362, further comprising storing at least a portion of the carbon dioxide in the reformer carbon dioxide containing exit sfream in the hydrocarbon foπnation.

4364. The method ofclaim 4351, wherein the subsurface foimation is a spent portion of the fonnation.

4365. The method ofclaim 4351, wherein the subsurface formation is an oil reservofr.

4366. The method ofclaim 4365, wherein at least a portion of the carbon dioxide in the reformer carbon dioxide containing exit sfream is used as a drive fluid for enhanced oil recovery in the oil reservofr.

4367. The method ofclaim 4351, wherein the subsurface foπnation is a coal formation.

4368. The method ofclaim 4367, wherein at least a portion of the carbon dioxide in the reformer carbon dioxide containing exit sfream is used to produce methane from the coal formation.

4369. The method ofclaim 4367, wherein the coal formation is located over about 760 m below ground surface.

4370. The method of claim 4368, further comprising sequestering at least a portion of the carbon dioxide in the reformer carbon dioxide containing exit sfream within the coal formation.

4371. The method of claim 4351, wherein the fuel cell is a molten carbonate fuel cell.

4372. The method ofclaim 4351, wherein the fuel cell is a solid oxide fuel cell.

4373. The method ofclaim 4351, further comprising using a portion of the produced elecfricity to power electrical heaters within the formation.

4374. The method ofclaim 4351, further comprising using a portion of the produced pyrolysis products as a feed sfream for the fuel cell.

4375. The method ofclaim 4351, wherein the one or more heat sources comprise one or more electrical heaters disposed in the formation.

4376. The method ofclaim 4351, wherein the one or more heat sources comprise one or more flameless distributed combustors disposed in the foimation.

4377. The method ofclaim 4376, wherein a portion of fuel for the flameless distributed combustors is obtained from the formation.

4378. The method ofclaim 4351, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the foimation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4379. The method of claim 4351, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4380. A method for producing ammonia using a relatively low penneability formation containing heavy hydrocarbons, comprising: separating afr to produce an 0₂ rich sfream and a N₂ rich sfream; heating a selected section of the formation to a temperature sufficient to support reaction of hydrocarbon containing material in the formation to form synthesis gas; providing synthesis gas generating fluid and at least a portion of the 0₂ rich sfream to the selected section; allowing the synthesis gas generating fluid and 0₂ in the 0₂ rich sfream to react with at least a portion of the hydrocarbon containing material in the formation to generate synthesis gas; producing synthesis gas from the formation, wherein the synthesis gas comprises H₂ and CO; providing at least a portion of the H₂ in the synthesis gas to an ammonia synthesis process; providing N₂ to the ammonia synthesis process; and using the ammonia synthesis process to generate ammonia.

4381. The method of claim 4380, wherein the ratio of the H₂ to N₂ provided to the ammonia synthesis process is approximately 3:1.

4382. The method ofclaim 4380, wherein the ratio of the H₂ to N₂ provided to the ammonia synthesis process ranges from approximately 2.8:1 to approxhnately 3.2:1.

4383. The method ofclaim 4380, wherein the temperature sufficient to support reaction of hydrocarbon containing material in the formation to form synthesis gas ranges from approximately 400 °C to approximately 1200 °C.

4384. The method of claim 4380, further comprising separating at least a portion of carbon dioxide in the synthesis gas from at least a portion of the synthesis gas.

4385. The method ofclaim 4384, wherein the carbon dioxide is separated from the synthesis gas by an amine separator.

4386. The method ofclaim 4385, further comprising providing at least a portion of the carbon dioxide to a urea synthesis process to produce urea.

4387. The method ofclaim 4380, wherein at least a portion of the N₂ sfream is used to condense hydrocarbons with 4 or more carbon atoms from a pyrolyzation fluid.

4388. The method ofclaim 4380, wherein at least a portion of the N₂ rich sfream is provided to the ammonia synthesis process.

4389. The method ofclaim 4380, wherein the afr is separated by cryogenic distillation.

4390. The method ofclaim 4380, wherein the ah is separated by membrane separation.

4391. The method of clahn 4380, wherein fluids produced during pyrolysis of a relatively low peπneability formation containing heavy hydrocarbons comprise aimnonia and, further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4392. The method ofclaim 4380, wherein fluids produced during pyrolysis of a hydrocarbon formation are hydrofreated and at least some ammonia is produced during hydrofreating, and, further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4393. The method of claim 4380, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea.

4394. The method of claim 4380, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and, further comprising providing carbon dioxide from the foπnation to the urea synthesis process.

4395. The method ofclaim 4380, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and, further comprising shifting at least a portion of the carbon monoxide to carbon dioxide in a shift process, and further comprising providing at least a portion of the carbon dioxide from the shift process to the urea synthesis process.

4396. The method of claim 4380, wherein heating the selected section of the formation to a temperature to support reaction of hydrocarbon containing material in the formation to form synthesis gas comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material within the zones with 0₂ in the 0₂rich sfream; infroducing the 0₂to the zones substantially by diffusion; allowing 0₂ in the 0₂ rich sfream to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and fransfening heat from the zones to the selected section.

4397. The method of claim 4396, wherein temperatures sufficient to support reaction of hydrocarbon containing material within the zones with 0₂ range from approximately 200 °C to approximately 1200 °C.

4398. The method ofclaim 4396, wherein the one or more heat sources comprises one or more electrical heaters disposed in the formation.

4399. The method ofclaim 4396, wherein the one or more heat sources comprises one or more natural disfributed combustors.

4400. The method ofclaim 4396, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and ftuther comprising heating the conduit by flowing a hot fluid through the conduit.

4401. The method ofclaim 4396, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4402. The method ofclaim 4380, wherein heating the selected section of the formation to a temperature to support reaction of hydrocarbon containing material in the formation to form synthesis gas comprises: infroducing the 0₂ rich stream into the foimation through a weUbore; fransporting 0₂ in the 0₂ rich stteam substantially by convection into the portion of the selected section, wherein the portion of the selected section is at a temperature sufficient to support an oxidation reaction with 0₂ in the 0₂ rich stream; and reacting the 0₂ within the portion of the selected section to generate heat and raise the temperature of the portion.

4403. The method of claim 4403 , wherein the temperature sufficient to support an oxidation reaction with 0₂ ranges from approximately 200 °C to approximately 1200 °C.

4404. The method of clahn 4403, wherein the one or more heat sources comprises one or more electrical heaters disposed in the foimation.

4405. The method ofclaim 4403, wherein the one or more heat sources comprises one or more natural distributed combustors.

4406. The method of claim 4403, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4407. The method ofclaim 4403, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4408. The method ofclaim 4380, further comprising controlling the heating of at least the portion of the selected section and provision of the synthesis gas generating fluid to maintain a temperature within at least the portion of the selected section above the temperature sufficient to generate synthesis gas.

4409. The method of claim 4380, wherein the synthesis gas generating fluid comprises liquid water.

4410. The method ofclaim 4380, wherein the synthesis gas generating fluid comprises steam.

4411. The method of claim 4380, wherein the synthesis gas generating fluid comprises water and carbon dioxide wherehi the carbon dioxide inhibits production of carbon dioxide from the selected section.

4412. The method ofclaim 4411, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the foimation.

4413. The method ofclaim 4380, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4414. The method ofclaim 4413, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4415. The method of claim 4380, wherein providing the synthesis gas generating fluid to at least the portion of the selected section comprises raising a water table of the formation to allow water to flow into the at least the portion of the selected section.

4416. A method for producing ammonia using a relatively low permeability formation containing heavy hydrocarbons, comprising: generating a ffrst ammonia feed stteam from a first portion of the formation; generating a second ammonia feed sfream from a second portion of the formation, wherein the second ammonia feed sfream has a H₂ to N₂ ratio greater than a H₂ to N₂ ratio of the first ammonia feed sfream; blending at least a portion of the first ammonia feed sfream with at least a portion of the second ammonia feed sfream to produce a blended ammonia feed stream having a selected H₂ to N₂ ratio; providing the blended ammonia feed stteam to an ammonia synthesis process; and using the ammonia synthesis process to generate ammonia.

4417. The method of claim 4416, wherein the selected ratio is approximately 3:1.

4418. The method ofclaim 4416, wherein the selected ratio ranges from approximately 2.8:1 to approximately 3.2:1.

4419. The method ofclaim 4416, further comprising separating at least a portion of carbon dioxide in the first ammonia feed stream from at least a portion of the ffrst ammonia feed sfream.

4420. The method ofclaim 4419, wherein the carbon dioxide is separated from the ffrst ammonia feed sfream by an amine separator.

4421. The method of clahn 4420, further comprising providing at least a portion of the carbon dioxide to a urea synthesis process.

4422. The method ofclaim 4416, further comprising separating at least a portion of carbon dioxide in the blended ammonia feed sfream from at least a portion of the blended ammonia feed stteam.

4423. The method ofclaim 4422, wherein the carbon dioxide is separated from the blended ammonia feed stream by an amine separator.

4424. The method of claim 4423 , further comprising providing at least a portion of the carbon dioxide to a urea synthesis process

4425. The method ofclaim 4416, further comprising separating at least a portion of carbon dioxide in the second ammonia feed sfream from at least a portion of the second ammonia feed stream.

4426. The method of claim 4425, wherehi the carbon dioxide is separated from the second ammonia feed sfream by an amine separator.

4427. The method ofclaim 4426, further comprising providing at least a portion of the carbon dioxide to a urea synthesis process.

4428. The method of claim 4416, wherein fluids produced during pyrolysis of a relatively low permeability foimation containing heavy hydrocarbons comprise ammonia and, further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4429. The method of claim 4416, wherein fluids produced during pyrolysis of a hydrocarbon foimation are hydrofreated and at least some ammonia is produced during hydrotreating, and further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4430. The method ofclaim 4416, further comprising providing at least a portion of the aimnonia to a urea synthesis process to produce urea.

4431. The method of claim 4416, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and, further comprising providing carbon dioxide from the formation to the urea synthesis process.

4432. The method ofclaim 4416, further comprishig providing at least a portion of the ammonia to a urea synthesis process to produce urea and further comprising shifting at least a portion of carbon monoxide in the blended ammonia feed stream to carbon dioxide in a shift process, and further comprising providing at least a portion of the carbon dioxide from the shift process to the urea synthesis process.

4433. A method for producing ammonia using a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a selected section of the formation to a temperature sufficient to support reaction of hydrocarbon containing material in the formation to form synthesis gas; providing a synthesis gas generating fluid and an 0₂ rich stream to the selected section, wherein the amount of N₂ in the 0₂ rich sfream is sufficient to generate synthesis gas having a selected ratio of H₂ to N₂; allowing the synthesis gas generating fluid and 0₂ in the 0₂ rich sfream to react with at least a portion of the hydrocarbon containing material in the foπnation to generate synthesis gas having a selected ratio of H₂ to N₂; producing the synthesis gas from the fonnation; providing at least a portion of the H₂ and N₂ in the synthesis gas to an ammonia synthesis process; using the ammonia synthesis process to generate ammonia.

4434. The method ofclaim 4433, further comprising confrolling a temperature of at least a portion of the selected section to generate synthesis gas having the selected H₂ to N₂ ratio.

4435. The method of clahn 4433, wherein the selected ratio is approximately 3:1.

4436. The method ofclaim 4433, wherein the selected ratio ranges from approximately 2.8:1 to 3.2:1.

4437. The method ofclaim 4433, wherein the temperature sufficient to support reaction of hydrocarbon containing material in the formation to form synthesis gas ranges from approxhnately 400 °C to approximately 1200 °C.

4438. The method ofclaim 4433, wherein the 0₂ stream and N₂ sfream are obtained by cryogenic separation of afr.

4439. The method ofclaim 4433, wherein the 0₂ stream and N₂ stream are obtained by membrane separation of afr.

4440. The method ofclaim 4433, further comprising separating at least a portion of carbon dioxide in the synthesis gas from at least a portion of the synthesis gas.

4441. The method ofclaim 4440, wherein the carbon dioxide is separated from the synthesis gas by an amine separator.

4442. The method of clahn 4441, further comprising providing at least a portion of the carbon dioxide to a urea synthesis process.

4443. The method of clahn 4433 , wherein fluids produced during pyrolysis of a relatively low permeability foπnation containing heavy hydrocarbons comprise ammonia and, further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4444. The method of claim 4433 , wherein fluids produced during pyrolysis of a hydrocarbon formation are hydrofreated and at least some ammonia is produced during hydrotreating, and further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4445. The method of claim 4433, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea.

4446. The method ofclaim 4433, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and, further comprising providing carbon dioxide from the formation to the urea synthesis process.

4447. The method ofclaim 4433, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and further comprising shifting at least a portion of carbon monoxide in the synthesis gas to carbon dioxide in a shift process, and further comprising providing at least a portion of the carbon dioxide from the shift process to the urea synthesis process.

4448. The method ofclaim 4433, wherein heating a selected section of the formation to a temperature to support reaction of hydrocarbon containing material in the formation to form synthesis gas comprises: heating zones adjacent to wellbores of one or more heat sources with heaters disposed in the wellbores, wherein the heaters are configured to raise temperatures of the zones to temperatures sufficient to support reaction of hydrocarbon containing material withhi the zones with 0₂ in the 0₂ rich sfream; introducing the 0₂to the zones substantially by diffusion; allowing 0₂ in the 0₂ rich sfream to react with at least a portion of the hydrocarbon containing material within the zones to produce heat in the zones; and transfening heat from the zones to the selected section.

4449. The method ofclaim 4448, wherein temperatures sufficient to support reaction of hydrocarbon containing material within the zones with 0₂ range from approximately 200 °C to approximately 1200 °C.

4450. The method of claim 4448, wherein the one or more heat sources comprises one or more elecfrical heaters disposed in the foimation.

4451. The method ofclaim 4448, wherein the one or more heat sources comprises one or more natural distributed combustors.

4452. The method of claim 4448, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4453. The method of claim 4448, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4454. The method ofclaim 4433, wherein heating the selected section of the formation to a temperature to support reaction of hydrocarbon containing material in the formation to foπn synthesis gas comprises: infroducing the 0₂ rich sfream into the formation through a wellbore; fransporting 0₂ in the 0₂ rich sfream substantially by convection into the portion of the selected section, wherein the portion of the selected section is at a temperature sufficient to support an oxidation reaction with 0₂ in the 0₂ rich sfream; and reacting the 0₂ within the portion of the selected section to generate heat and raise the temperature of the portion.

4455. The method of claim 4454, wherein the temperature sufficient to support an oxidation reaction with 0₂ ranges from approximately 200 °C to approximately 1200 °C.

4456. The method ofclaim 4454, wherein the one or more heat sources comprises one or more elecfrical heaters disposed in the formation.

4457. The method ofclaim 4454, wherein the one or more heat sources comprises one or more natural distributed combustors.

4458. The method of clahn 4454, wherein the one or more heat sources comprise one or more heater wells, wherein at least one heater well comprises a conduit disposed within the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4459. The method of claim 4454, further comprising using a portion of the synthesis gas as a combustion fuel for the one or more heat sources.

4460. The method ofclaim 4433, further comprising confrolling the heating of at least the portion of the selected section and provision of the synthesis gas generating fluid to maintain a temperature within at least the portion of the selected section above the temperature sufficient to generate synthesis gas.

4461. The method of claim 4433 , wherein the synthesis gas generating fluid comprises liquid water.

4462. The method of claim 4433, wherein the synthesis gas generating fluid comprises steam.

4463. The method ofclaim 4433, wherein the synthesis gas generating fluid comprises water and carbon dioxide, wherein the carbon dioxide inhibits production of carbon dioxide from the selected section.

4464. The method of claim 4463, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4465. The method ofclaim 4433, wherein the synthesis gas generating fluid comprises carbon dioxide, and wherein a portion of the carbon dioxide reacts with carbon in the formation to generate carbon monoxide.

4466. The method ofclaim 4465, wherein a portion of the carbon dioxide within the synthesis gas generating fluid comprises carbon dioxide removed from the formation.

4467. The method ofclaim 4433, wherein providing the synthesis gas generating fluid to at least the portion of the selected section comprises raising a water table of the formation to allow water to flow into the at least the portion of the selected section.

4468. A method for producing ammonia using a relatively low permeability formation containing heavy hydrocarbons, comprising: providing a first sfream comprising N₂ and carbon dioxide to the formation; allowing at least a portion of the carbon dioxide in the ffrst sfream to adsorb in the foimation; producing a second stream from the formation, wherein the second sfream comprises a lower percentage of carbon dioxide than the first stream; providing at least a portion of the N₂ in the second stream to an ammonia synthesis process.

4469. The method of claim 4468, wherein the second stteam comprises H₂ from the formation.

4470. The method of claim 4468, wherein the first stteam is produced from a relatively low permeability formation containing heavy hydrocarbons.

4471. The method of claim 4470, wherein the first sfream is generated by reacting a oxidizing fluid with hydrocarbon containing material in the formation.

4472. The method ofclaim 4468, wherein the second sfream comprises H₂ from the formation and, further comprising providing such H₂ to the ammonia synthesis process.

4473. The method of claim 4468, further comprising using the ammonia synthesis process to generate ammonia.

4474. The method ofclaim 4473, wherein fluids produced during pyrolysis of a relatively low permeability foimation containing heavy hydrocarbons comprise ammonia and, further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4475. The method of claim 4473 , wherein fluids produced during pyrolysis of a hydrocarbon formation are hydrofreated and at least some ammonia is produced during hydrofreating, and further comprising adding at least a portion of such ammonia to the ammonia generated from the ammonia synthesis process.

4476. The method of claim 4473, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea.

4477. The method of claim 4473, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and, further comprising providing carbon dioxide from the formation to the urea synthesis process.

4478. The method of claim 4473, further comprising providing at least a portion of the ammonia to a urea synthesis process to produce urea and further comprising shifting at least a portion of carbon monoxide in the synthesis gas to carbon dioxide in a shift process, and further comprising providing at least a portion of the carbon dioxide from the shift process to the urea synthesis process.

4479. A method for freating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to the formation; allowing the heat to fransfer from one or more of the heat sources to a selected section of the formation such that heat from the heat sources pyrolyzes at least some hydrocarbons within the selected section, and wherein heat from the heat sources increases the permeability of at least a portion of the selected section; and producing a mixture comprising hydrocarbons from the formation.

4480. The method of clahn 4479, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the foimation, and wherein supeφosition of heat from at least the two heat sources increases the permeability of at least the portion of the selected section.

4481. The method of claim 4479, further comprising allowing heat to fransfer from at least one of the heat sources to the selected section to create thermal fractures in the formation wherein the thermal fractures substantially increase the permeability of the selected section.

4482. The method of claim 4479, wherein the heat is provided such that an average temperature in the selected section ranges from approximately about 270 °C to about 375 °C.

4483. The method ofclaim 4479, wherehi at least one of the heat sources comprises an electrical heater located in the foimation.

4484. The method of clahn 4479, wherein at least one of the heat sources is located in a heater well, and wherein at least one of the heater wells comprises a conduit located in the foπnation, and further comprising heathig the conduit by flowing a hot fluid through the conduit.

4485. The method ofclaim 4479, wherein at least some of the heat sources are ananged in a ttiangular pattern.

4486. The method of claim 4479, further comprising: monitoring a composition of the produced mixture; and controlling a pressure in at least a portion of the foimation to control the composition of the produced mixture.

4487. The method of claim 4486, wherein the pressure is confrolled by a valve proximate to a location where the mixture is produced.

4488. The method ofclaim 4486, wherein the pressure is confrolled such that pressure proximate to one or more of the heat sources is greater than a pressure proximate to a location where the fluid is produced.

4489. The method ofclaim 4479, wherein an average distance between heat sources is between about 2 m and about 8 m.

4490. A method for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to the formation; allowing the heat to ttansfer from one or more of the heat sources to a selected section of the formation such that heat from the heat sources pyrolyzes at least some hydrocarbons within the selected section, and wherehi heat from the heat sources vaporizes at least a portion of the hydrocarbons in the selected section; and producing a mixture comprising hydrocarbons from the foπnation.

4491. The method of claim 4490, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation, and wherein supeφosition of heat from at least the two heat sources vaporizes at least the portion of the hydrocarbons in the selected section.

4492. The method ofclaim 4490, further comprising allowing heat to fransfer from at least one of the heat sources to the selected section to create thermal fractures in the formation, wherein the thermal fractures substantially increase the peπneability of the selected section.

4493. The method of claim 4490, wherein the heat is provided such that an average temperature in the selected section ranges from approximately about 270 °C to about 375 °C.

4494. The method of claim 4490, wherein at least one of the heat sources comprises an electrical heater located in the formation.

4495. The method ofclaim 4490, wherein at least one of the heat sources is located in a heater well, and wherein at least one of the heater wells comprises a conduit located in the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4496. The method of claim 4490, wherein at least some of the heat sources are ananged in a triangular pattern.

4497. The method ofclaim 4490, further comprising: monitoring a composition of the produced mixture; and controlling a pressure in at least a portion of the formation to confrol the composition of the produced mixture.

4498. The method of claim 4497, wherein the pressure is controlled by a valve proximate to a location where the mixture is produced.

4499. The method of claim 4497, wherein the pressure is controlled such that pressure proxhnate to one or more of the heat sources is greater than a pressure proximate to a location where the mixture is produced.

4500. The method of claim 4490, wherein an average distance between heat sources is between about 2 m and about 8 m.

4501. A method for treating a relatively low peπneability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to the formation, wherein at least one of the heat sources is located in a heater well; allowing the heat to transfer from one or more of the heat sources to a selected section of the formation such that heat from the heat sources pyrolyzes at least some hydrocarbons within the selected section, and wherein heat from the heat sources pressurizes at least a portion of the selected section; and producing a mixture comprising hydrocarbons from the foimation, wherein the mixture is produced from one or more heater wells.

4502. The method ofclaim 4501, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4503. The method of claim 4501 , further comprising producing fluid from at least one heater well in which is positioned the heat source of the one or more heat sources.

4504. The method of claim 4501 , further comprising allowing heat to transfer from at least one of the heat sources to the selected section to create thermal fractures in the formation, wherein the thermal fractures substantially increase the permeability of the selected section.

4505. The method of claim 4501 , wherein the heat is provided such that an average temperature in the selected section ranges from approximately about 270 °C to about 375 °C.

4506. The method ofclaim 4501, wherein at least one of the heat sources comprises an electtical heater located in the formation.

4507. The method ofclaim 4501, wherein at least one of the heat sources is located in a heater well, and wherein at least one of the heater wells comprises a conduit located in the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4508. The method ofclaim 4501, wherein at least some of the heat sources are ananged in a triangular pattern.

4509. The method of clahn 4501, further comprising: monitoring a composition of the produced mixture; and confrolling a pressure in at least a portion of the formation to confrol the composition of the produced mixture.

4510. The method ofclaim 4509, wherein the pressure is confrolled by a valve proximate to a location where the mixture is produced.

4511. The method of claim 4509, wherein the pressure is confrolled such that pressure proximate to one or more of the heat sources is greater than a pressure proximate to a location where the mixture is produced.

4512. The method of claim 4501 wherein an average distance between heat sources is between about 2 m and about 8 m.

4513. A method for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to the formation; allowing the heat to ttansfer from one or more of the heat sources to a selected ffrst section of the formation such that heat from the heat sources creates a pyrolysis zone wherein at least some hydrocarbons are pyrolyzed within the first selected section, and allowing the heat to fransfer from one or more of the heat sources to a selected second section of the formation such that heat from the heat sources heats at least some hydrocarbons within the selected second section to a temperature less than the average temperature within the pyrolysis zone; and producing a mixture comprising hydrocarbons from the formation.

4514. The method of claim 4513, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from the at least two heat sources pyrolyzes at least some hydrocarbons within the selected first section of the foimation, and wherein supeφosition of heat from the at least two heat sources heats at least some hydrocarbons within the selected second section to a temperature less than the average temperature within the pyrolysis zone.

4515. The method ofclaim 4513, wherein at least some heated hydrocarbons within the selected second section flow into the pyrolysis zone.

4516. The method ofclaim 4513, wherein the heat decreases the viscosity of at least some of the hydrocarbons in the selected second section.

4517. The method of claim 4513, further comprising allowing heat to ttansfer from at least one of the heat sources to the selected first section to create thermal fractures in the foimation, wherein the thermal fractures substantially increase the permeability of the selected first section.

4518. The method ofclaim 4513, further comprising allowing heat to transfer from at least one of the heat sources to the selected second section to create thermal fractures in the formation, wherein the thermal fractures substantially increase the permeability of the selected second section.

4519. The method of claim 4513, wherein the heat is provided such that an average temperature in the selected first section ranges from approximately about 270 °C to about 375 °C.

4520. The method of claim 4513, wherein the heat is provided such that an average temperature in the selected second section ranges from approxhnately about 180 °C to about 250 °C.

4521. The method ofclaim 4513, wherein a viscosity of at least some of the hydrocarbons in the selected second section ranges from approxhnately about 20 centipoise to about 1000 centipoise.

4522. The method ofclaim 4513, wherein at least one of the heat sources comprises an electrical heater located in the formation.

4523. The method of claim 4513, wherein at least one of the heat sources is located in a heater well, and wherein at least one of the heater wells comprises a conduit located in the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4524. The method of claim 4513 , further comprising: monitoring a composition of the produced mixture; and controlling a pressure in at least a portion of the foimation to confrol the composition of the produced mixture.

4525. The method ofclaim 4524, wherein the pressure is controlled by a valve proximate to a location where the mixture is produced.

4526. The method of claim 4524, wherein the pressure is confrolled such that pressure proximate to one or more of the heat sources is greater than a pressure proximate to a location where the fluid is produced.

4527. The method of clahn 4513, wherein the pressure in the selected second section is substantially greater than the pressure in the selected first section.

4528. The method of claim 4513, wherein at least some of the heat sources are ananged in a triangular pattern.

4529. The method of claim 4513, wherein an average distance between heat sources in the selected first section is less than an average distance between heat sources in the selected second section.

4530. The method ofclaim 4513, wherein the heat is provided to the selected ffrst section before heat is provided to the selected second section.

4531. The method of clahn 4513, wherein the selected first section comprises at least one production well.

4532. The method ofclaim 4513, wherehi an average distance between heat sources in the selected first section is between about 2 m and about 10 m.

4533. The method ofclaim 4513, wherein an average distance between heat sources in the selected second section is between about 5 m and about 20 m.

4534. The method of claim 4513, wherein the selected first section comprises a planar region.

4535. The method ofclaim 4513, wherein at least one row of the heat sources provides heat to the planar region.

4536. The method ofclaim 4535 wherein a length of a row is between about 75 m and about 125 m.

4537. The method of claim 4534, wherein the planar region comprises a vertical hydraulic fracture.

4538. The method ofclaim 4537, wherein a width of the vertical hydraulic fracture is between about 0.3 cm and about 2.5 cm.

4539. The method ofclaim 4537, wherein a length of the vertical hydraulic fracture is between about 75 m and about 125 m.

4540. The method ofclaim 4513, wherein at least one ring comprising the heat sources provides heat to the selected ffrst section.

4541. The method of claim 4540, wherein at least one ring comprishig the heat sources provides heat to the selected second section.

4542. The method of claim 4540, wherein the ring comprises a polygon.

4543. The method ofclaim 4540, wherein the ring comprises a regular polygon.

4544. The method ofclaim 4540, wherein the ring comprises a hexagon.

4545. The method of clahn 4540, wherein the ring comprises a triangle.

4546. A method for freating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from three or more heat sources to the formation; allowing the heat to fransfer from three or more of the heat sources to a selected section of the foπnation such that heat from the heat sources pyrolyzes at least some hydrocarbons within the selected section, and at least three of the heat sources are ananged in a substantially triangular pattern; and producing a mixture comprising hydrocarbons from the formation.

4547. The method ofclaim 4546, wherein supeφosition of heat from at least the three heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4548. The method of claim 4546, wherein the mixture is produced from a production well located in a friangular region created by at least three heat sources.

4549. The method ofclaim 4546, further comprising allowing heat to fransfer from at least one of the heat sources to the selected section to create thermal fractures in the formation, wherein the thermal fractures substantially increase the permeability of the selected section.

4550. The method ofclaim 4546, wherein the heat is provided such that an average temperature in the selected section ranges from approximately about 270 °C to about 375 °C.

4551. The method ofclaim 4546, wherein at least one of the heat sources comprises an elecfrical heater located in the formation.

4552. The method ofclaim 4546, wherein at least one of the heat sources is located in a heater well, and wherein at least one of the heater wells comprises a conduit located in the formation, and further comprising heating the conduit by flowing a hot fluid through the conduit.

4553. The method ofclaim 4546, wherein at least some of the heat sources are ananged in a friangular pattern.

4554. The method ofclaim 4546, further comprising: monitoring a composition of the produced mixture; and controlling a pressure in at least a portion of the foπnation to control the composition of the produced mixture.

4555. The method of claim 4554, wherein the pressure is controlled by a valve proximate to a location where the mixture is produced.

4556. The method of clahn 4554, wherein the pressure is controlled such that pressure proximate to one or more of the heat sources is greater than a pressure proximate to a location where the fluid is produced.

4557. The method ofclaim 4546, wherein an average distance between heat sources is between about 2 m and about 8 m.

4558. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit configurable to be placed within an opening in the formation; a conductor configurable to be placed within the conduit, wherein the conductor is further configurable to provide heat to at least a portion of the formation during use; at least one centralizer configurable to be coupled to the conductor, wherein at least one cenfralizer inhibits movement of the conductor within the conduit during use; and wherein the system is configurable to allow heat to fransfer from the conductor to a section of the formation during use.

4559. The system ofclaim 4558, wherein at least one cenfralizer comprises elecfrically insulating material.

4560. The system ofclaim 4558, wherein at least one centralizer is configurable to inhibit arcing between the conductor and the conduit.

4561. The system ofclaim 4558, wherein at least one centralizer comprises ceramic material.

4562. The system ofclaim 4558, wherein at least one cenfralizer comprises at least one recess, wherein at least one recess is placed at ajunction of at least one cenfralizer and the first conductor, wherein at least one protrusion is formed on the first conductor at the junction to maintain a location of at least one cenfralizer on the first conductor, and wherein at least one protrusion resides substantially within at least one recess.

4563. The system of clahn 4562, wherein at least one protrusion comprises a weld.

4564. The system ofclaim 4562, wherein an elecfrically insulating material substantially covers at least one recess.

4565. The system ofclaim 4562, wherein a thermal plasma applied coating substantially covers at least one recess.

4566. The system ofclaim 4562, wherein a thermal plasma applied coating comprises alumina.

4567. The system ofclaim 4558, wherein the system is further configurable to allow at least some hydrocarbons to pyrolyze in the heated section of the foimation during use.

4568. The system ofclaim 4558, further comprising an insulation layer configurable to be coupled to at least a portion of the conductor or at least one centralizer.

4569. The system ofclaim 4558, wherein at least one cenfralizer comprises a neck portion.

4570. The system ofclaim 4558, wherein at least one cenfralizer comprises one or more grooves.

4571. The system of claim 4558, wherein at least one centralizer comprises at least two portions, and wherein the portions are configurable to be coupled to the conductor to form at least one centralizer placed on the conductor.

4572. The system of claim 4558, wherein a thickness of the conductor is greater adjacent to a lean zone in the formation than a thickness of the conductor adjacent to a rich zone in the foimation such that more heat is provided to the rich zone.

4573. The system of claim 4558, wherein the system is configured to heat a relatively low permeability fonnation containing heavy hydrocarbons, and wherein the system comprises: a conduit configured to be placed within an opening in the formation; a conductor configured to be placed within the conduit, wherein the conductor is further configured to provide heat to at least a portion of the formation during use; at least one centtalizer configured to be coupled to the conductor, wherein at least one centralizer inhibits movement of the conductor within the conduit during use; and wherein the system is configured to allow heat to fransfer from the conductor to a section of the formation during use.

4574. The system of claim 4558, wherein the system heats a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit placed within an opening in the formation; a conductor placed within the conduit, wherein the conductor provides heat to at least a portion of the foimation; at least one centtalizer coupled to the conductor, wherein at least one centralizer inhibits movement of the conductor within the conduit; and wherein the system allows heat to transfer from the conductor to a section of the formation.

4575. The system ofclaim 4558, wherein the system is configurable to be removed from the opening in the formation.

4576. The system ofclaim 4558, further comprising a moveable thermocouple.

4577. The system ofclaim 4558, further comprising an isolation block.

4578. A system configurable to heat a relatively low peπneability formation containing heavy hydrocarbons, comprising: a conduit configurable to be placed withhi an opening in the formation; a conductor configurable to be placed within the conduit, wherein the conductor is further configurable to provide heat to at least a portion of the formation during use; at least one centralizer configurable to be coupled to the conductor, wherein at least one cenfralizer inhibits movement of the conductor within the conduit during use wherein the system is configurable to allow heat to ttansfer from the conductor to a section of the formation during use; and wherein the system is configurable to be removed from the opening in the formation.

4579. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an elecfrical cunent to a conductor to provide heat to at least a portion of the formation, wherein the conductor is placed within a conduit, wherein at least one centralizer is coupled to the conductor to inhibit movement of the conductor within the conduit, and wherein the conduit is placed within an opening in the formation; and allowing the heat to fransfer from the first conductor to a section of the formation.

4580. The method ofclaim 4579, further comprising pyrolyzing at least some hydrocarbons in the section of the formation.

4581. The method of claim 4579, further comprising inhibiting arcing between the conductor and the conduit.

4582. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit configurable to be placed within an opening in the foimation; a conductor configurable to be placed within a conduit, wherein the conductor is further configurable to provide heat to at least a portion of the formation during use; an insulation layer coupled to at least a portion of the conductor, wherein the insulation layer elecfrically insulates at least a portion of the conductor from the conduit during use; and wherein the system is configurable to allow heat to fransfer from the conductor to a section of the formation during use

4583. The system of claim 4582, wherein the insulation layer comprises a spiral insulation layer.

4584. The system of claim 4582, wherein the insulation layer comprises at least one metal oxide.

4585. The system ofclaim 4582, wherein the insulation layer comprises at least one alumina oxide.

4586. The system ofclaim 4582, wherein the insulation layer is configurable to be fastened to the conductor with a high temperature glue.

4587. The system ofclaim 4582, wherein the system is further configurable to allow at least some hydrocarbons to pyrolyze in the heated section of the formation during use.

4588. The system ofclaim 4582, wherein the system is configured to heat a relatively low peπneability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit configured to be placed within an opening in the foπnation; a conductor configured to be placed within a conduit, wherein the conductor is further configured to provide heat to at least a portion of the formation during use; an insulation layer coupled to at least a portion of the conductor, wherein the insulation layer electrically insulates at least a portion of the conductor from the conduit during use; and wherein the system is configured to allow heat to transfer from the conductor to a section of the foimation during use.

4589. The system ofclaim 4582, wherein the system heats a relatively low permeability foπnation containing heavy hydrocarbons, and wherein the system comprises: a conduit placed within an opening in the formation; a conductor placed within a conduit, wherein the conductor provides heat to at least a portion of the foπnation; an insulation layer coupled to at least a portion of the conductor, wherein the insulation layer electtically insulates at least a portion of the conductor from the conduit; and wherein the system allows heat to fransfer from the conductor to a section of the formation.

4590. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an electrical cunent to a conductor to provide heat to at least a portion of the fonnation, wherein the conductor is placed within a conduit, wherein an insulation layer is coupled to at least a portion of the conductor to electrically insulate at least a portion of the conductor from the conduit, and wherein the conduit is placed within an opening in the foπnation; and allowing the heat to transfer from the first conductor to a section of the formation.

4591. The method of claim 4590, further comprising pyrolyzing at least some hydrocarbons in the section of the formation.

4592. The method ofclaim 4590, further comprising inhibiting arcing between the conductor and the conduit.

4593. A method for making a conductor-in-conduit heat source for a relatively low permeability formation containing heavy hydrocarbons, comprising: placing at least one protrusion on a conductor; placing at least one cenfralizer on the conductor; and placing the conductor within a conduit to form a conductor-in-conduit heat source, wherein at least one cenfralizer maintains a location of the conductor within the conduit.

4594. The method of claim 4593, wherein at least one cenfralizer comprises at least two portions, and wherein the portions are coupled to the conductor to form at least one centtalizer placed on the conductor.

4595. The method of clahn 4593, further comprising placing the conductor-in-conduit heat source in an opening in a relatively low permeability formation containing heavy hydrocarbons.

4596. The method ofclaim 4593, further comprising coupling an insulation layer on the conductor, wherein the insulation layer is configured to electrically insulate at least a portion of the conductor from the conduit.

4597. The method of clahn 4593, further comprising providing heat from the conductor-in-conduit heat source to at least a portion of the formation.

4598. The method ofclaim 4593, further comprising pyrolyzing at least some hydrocarbons in a selected section of the formation.

4599. The method of claim 4593, further comprising producing a mixture from a selected section of the formation.

4600. The method of claim 4593, wherein the conductor-in-conduit heat source is configurable to provide heat to the relatively low permeability formation containing heavy hydrocarbons.

4601. The method of claim 4593, wherein at least one cenfralizer comprises at least one recess placed at a junction of at least one centralizer on the conductor, and wherein at least one protrasion resides substantially within at least one recess.

4602. The method ofclaim 4601, further comprising at least partially covering at least one recess with an electrically insulating material.

4603. The method of claim 4601 , further comprising spraying an elecfrically insulating material to at least partially cover at least one recess.

4604. The method of claim 4593 , wherein placing at least one protrusion on the conductor comprises welding at least one protrusion on the conductor.

4605. The method ofclaim 4593, further comprising coiling the conductor-in-conduit heat source on a spool after forming the heat source.

4606. The method of claim 4593, further comprising uncoiling the heat source from the spool while placing the heat source in an opening in the formation.

4607. The method ofclaim 4593, wherein placing the conductor within a conduit comprises placing the conductor within a conduit that has been placed in an opening in the formation.

4608. The method of claim 4593, further comprising couplhig the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source.

4609. The method ofclaim 4593, wherein the conductor-in-conduit heat source is configurable to be installed into an opening in a relatively low permeability formation containing heavy hydrocarbons.

4610. The method of claim 4593, wherein the conductor-in-conduit heat source is configurable to be removed from an opening in a relatively low permeability formation containing heavy hydrocarbons.

4611. The method of claim 4593 , wherein the conductor-in-conduit heat source is configurable to heat to a section of the relatively low permeability formation containing heavy hydrocarbons, and wherein the heat pyrolyzes at least some hydrocarbons in the section of the formation during use.

4612. The method ofclaim 4593, wherein a thickness of the conductor configurable to be placed adjacent to a lean zone in the formation is greater than a thickness of the conductor configurable to be placed adjacent to a rich zone in the formation such that more heat is provided to the rich zone during use.

4613. A method for forming an opening in a relatively low permeability foπnation containing heavy hydrocarbons, comprising: forming a first opening in the formation; providing a series of magnetic fields from a plurality of magnets positioned along a portion of the first opening; and forming a second opening in the formation using magnetic tracking such that the second opening is positioned a selected distance from the first opening.

4614. The method of claim 4613, further comprising providing a magnetic sfring to a portion of the ffrst opening.

4615. The method ofclaim 4613, wherein the plurality of magnets is positioned within a casing.

4616. The method ofclaim 4613, wherein the plurality of magnets is positioned within a heater casing.

4617. The method ofclaim 4613, wherein the plurality of magnets is positioned within a perforated casing.

4618. The method ofclaim 4613, further comprising providing a magnetic string to a portion of the ffrst opening, wherein the magnetic string comprises two or more magnetic segments, and wherein the two or more segments are positioned such that the polarity of adjacent segments is reversed.

4619. The method of claim 4613, further comprising moving the magnetic fields within the first opening.

4620. The method ofclaim 4613, further comprishig moving the magnetic fields within the first opening such that the magnetic fields vary with time.

4621. The method ofclaim 4613, further comprising adjusting a position of the magnetic fields within the ffrst opening to increase a length of the second opening.

4622. The method ofclaim 4613, further comprising forming a plurality of openings adjacent to the ffrst opening.

4623. The method of claim 4613 , wherein the first opening comprises a non-metallic casing.

4624. The method ofclaim 4613, wherein the series of the magnetic fields comprises a first magnetic field and a second magnetic field and wherein a sfrength of the first magnetic differs from a sfrength of the second magnetic field.

4625. The method of clahn 4613, wherein the series of the magnetic fields comprises a first magnetic field and a second magnetic field and wherein a strength of the ffrst magnetic is about a sfrength of the second magnetic field.

4626. The method ofclaim 4613, wherein the ffrst opening comprises a center opening in a pattern of openings, and further comprishig forming a plurality of openings adjacent to the first opening.

4627. The method of claim 4613 , wherein the ffrst opening comprises a center opening in a pattern of openings, and further comprising forming a plurality of openings adjacent to the first opening, wherein each of the plurality of openings is positioned at the selected distance from the first opening.

4628. The method ofclaim 4613, further comprising providing at least one heat source within the first opening and at least one heat source within the second opening such that the heat sources can provide heat to at least a portion of the formation.

4629. A method for forming an opening in a relatively low permeability foπnation containing heavy hydrocarbons, comprising: forming a ffrst opening in the formation; providing a magnetic sfring to the first opening, wherein the magnetic sfring comprises two or more magnetic segments, and wherein the magnetic segments are positioned such that the polarities of the segments are reversed; and forming a second opening in the formation using magnetic tracking such that the second opening is positioned a selected distance from the ffrst opening.

4630. The method of claim 4629, further comprising providing at least one heat source within the first opening and at least one heat source within the second opening such that the heat sources can provide heat to at least a portion of the formation.

4631. The method of claim 4629, wherein the two or more segments comprise a plurality of magnets.

4632. The method of claim 4629, further comprising providing a series of magnetic fields along a portion of the ffrst opening.

4633. The method ofclaim 4629, wherein a length of a segment conesponds to a distance between the first opening and the second opening.

4634. The method of claim 4629, further comprising moving the magnetic fields within the first opening.

4635. The method of claim 4629, further comprising moving the magnetic fields within the first opening such that the magnetic fields vary with time.

4636. The method ofclaim 4629, further comprising adjusting a position of the magnetic fields within the first opening to increase a length of the second opening.

4637. The method of claim 4629, further comprising forming a plurality of openings adjacent to the ffrst openhig.

4638. The method ofclaim 4629, wherein the first opening comprises a non-metallic casing.

4639. The method of claim 4629, wherein the series of the magnetic fields comprises a first magnetic field and a second magnetic field and wherehi a strength of the ffrst magnetic field differs from a sfrength of the second magnetic field.

4640. The method of claim 4629, wherein the series of the magnetic fields comprises a first magnetic field and a second magnetic field and wherein a sfrength of the first magnetic field is about a sfrength of the second magnetic field.

4641. The method of claim 4629, wherein the first opening comprises a center opening in a pattern of openings, and further comprising forming a plurality of openings adjacent to the first opening.

4642. The method ofclaim 4629, wherein the first opening comprises a center opening in a pattern of openings, and further comprising forming a plurality of openings adjacent to the first opening, wherein each of the plurality of openings is positioned at the selected distance from the first opening.

4643. The method ofclaim 4629, further comprising providing at least one heat source within the ffrst opening and at least one heat source within the second opening such that the heat sources can provide heat to at least a portion of the formation.

4644. The method of claim 4629, wherein the magnetic string is positioned within a casing.

4645. The method of claim 4629, wherein the magnetic sfring is positioned within a heater casing.

4646. A system for drilling openings in a relatively low permeability foimation containing heavy hydrocarbons, comprising: a drilling apparatus; a magnetic sfring, comprising: a conduit; and two or more magnetic segments positionable in the conduit, wherein the magnetic segments comprise a plurality of magnets ; and a sensor configurable to detect a magnetic field within the formation.

4647. The system ofclaim 4646, wherein the magnetic string further comprises one or more members configurable to inhibit movement of the magnetic segments relative to the conduit.

4648. The system of claim 4646, wherein the one or more magnetic segments are positioned such that a polarity of adjacent segments is reversed.

4649. The system ofclaim 4646, wherehi the magnetic string is positionable within a first opening in the formation.

4650. The system ofclaim 4646, wherein the magnetic string is positionable within a ffrst opening in the formation and wherein the magnetic string induces a magnetic field in a portion of the first opening.

4651. The system of clahn 4646, further comprising at least one heat source within a ffrst opening.

4652. The system ofclaim 4646, further comprising at least one heat source within a first opening and at least one heat source within a second opening such that the heat sources can provide heat to at least a portion of the formation.

4653. The system ofclaim 4646, further comprising providing a series of magnetic fields along a portion of a first opening.

4654. The system ofclaim 4646, wherein a length of a segment conesponds to a distance between the first opening and the second opening.

4655. The system ofclaim 4646, wherein the magnetic sfring is movable in a first opening.

4656. The system ofclaim 4646, wherein a position of the magnetic sfring in the first openhig can be adjusted to increase a length of a second opening.

4657. The system of clahn 4646, further comprising a first opening positioned in the formation and wherein the magnetic string is positionable in the ffrst opening.

4658. The system ofclaim 4646, further comprising a non-metallic casing.

4659. The system of claim 4646, wherein the magnetic segments comprises a first magnetic segment and a second magnetic segment and wherehi a length of the first magnetic segment differs from a length of the second magnetic segment.

4660. The system of clahn 4646, wherein the magnetic segments comprises a first magnetic segment and a second magnetic segment and wherein a length of the first magnetic segment is about the same as a length of the second magnetic segment.

4661. The system ofclaim 4646, further comprising a casing and wherein the magnetic string is positioned within the casing.

4662. A method of installing a conductor-in-conduit heat source of a desfred length in a relatively low permeability foπnation containing heavy hydrocarbons, comprising: assembling a conductor-in-conduit heat source of a desired length, comprising: placing a conductor within a conduit to form a conductor-in-conduit heat source; and coupling the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source to foπn a conductor-in-conduit heat source of the desired length, wherein the conductor is electrically coupled to the conductor of at least one additional conductor-in-conduit heat source and the conduit is electtically coupled to the conduit of at least one additional conductor-in-conduit heat source; coiling the conductor-in-conduit heat source of the desired length after forming the heat source; and placing the conductor-in-conduit heat source of the desired length in an opening in a relatively low permeability formation containing heavy hydrocarbons.

4663. The method of clahn 4662, wherein the conductor-in-conduit heat source is configurable to provide heat to the relatively low permeability formation containing heavy hydrocarbons.

4664. The method of clahn 4662, wherein the conductor-in-conduit heat source of the desired length is removable from the opening in the relatively low permeability formation containing heavy hydrocarbons.

4665. The method ofclaim 4662, further comprising uncoiling the conductor-in-conduit heat source of the desfred length while placing the heat source in the opening.

4666. The method ofclaim 4662, further comprising placing at least one centralizer on the conductor.

4667. The method ofclaim 4662, further comprising placing at least one centtalizer on the conductor, wherein at least one cenfralizer inhibits movement of the conductor within the conduit.

4668. The method of claim 4662, further comprising placing an insulation layer on at least a portion of the conductor.

4669. The method ofclaim 4662, further comprising coiling the conductor-in-conduit heat source.

4670. The method of claim 4662, further comprising testing the conductor-in-conduit heat source and coiling the heat source.

4671. The method of claim 4662, wherein coupling the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source comprises welding the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source.

4672. The method ofclaim 4662, wherehi coupling the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source comprises shielded active gas welding the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source.

4673. The method of claim 4662, wherehi coupling the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source comprises shielded active gas welding the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source, and wherein using shielded active gas welding inhibits changes in the grain structure of the conductor or conduit during coupling.

4674. The method ofclaim 4662, wherein the assembling of the conductor-in-conduit heat source of the desired length is performed at a location proximate the relatively low permeability formation containing heavy hydrocarbons.

4675. The method ofclaim 4662, wherein the assembling of the conductor-in-conduit heat source of the desired length takes place sufficiently proximate the relatively low permeability foimation containing heavy hydrocarbons such that the conductor-in-conduit heat source can be placed directly in an opening of the formation after the heat source is assembled.

4676. The method of claim 4662, further comprising coupling at least one substantially low resistance conductor to the conductor-in-conduit heat source of the desfred length, wherein at least one substantially low resistance conductor is configured to be placed in an overburden of the formation.

4677. The method of claim 4676, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor.

4678. The method ofclaim 4676, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor, wherein coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor comprises coupling a threaded end of at least one additional substantially low resistance conductor to a threaded end of at least one substantially low resistance conductor.

4679. The method ofclaim 4676, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor, wherein coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor comprises welding at least one additional substantially low resistance conductor to at least one substantially low resistance conductor.

4680. The method ofclaim 4676, wherein at least one substantially low resistance conductor is coupled to the conductor-in-conduit heat source of the desired length during assembling of the heat source of the desfred length.

4681. The method of claim 4676, wherein at least one substantially low resistance conductor is coupled to the conductor-in-conduit heat source of the desired length after assembling of the heat source of the desfred length.

4682. The method of clahn 4662, further comprising ttansporting the coiled conductor-in-conduit heat source of the desfred length on a cart or train from an assembly location to the opening in the relatively low permeability foimation containing heavy hydrocarbons.

4683. The method of claim 4682, wherein the cart or train can be further used to transport more than one conductor-in-conduit heat source of the desired length to more than one opening in the relatively low permeability formation containing heavy hydrocarbons.

4684. The method ofclaim 4662, wherein the desfred length comprises a length determined for using the conductor-in-conduit heat source in a selected openmg in the relatively low permeability foπnation containing heavy hydrocarbons.

4685. The method of claim 4662, further comprising freating the conductor to increase an emissivity of the conductor.

4686. The method of claim 4685, wherein treating the conductor comprises roughening the surface of the conductor.

4687. The method of claim 4685, wherein treating the conductor comprises heathig the conductor to a temperature above about 750 °C in an oxidizing fluid atmosphere.

4688. The method ofclaim 4662, further comprising treating the conduit to increase an emissivity of the conduit.

4689. The method of claim 4662, further comprising coating at least a portion of the conductor or at least a portion of the conduit during assembly of the conductor-in-conduit heat source.

4690. The method ofclaim 4662, further comprising placing an insulation layer on at least a portion of the conductor-in-conduit heat source prior to placing the heat source in the opening in the relatively low peπneability foπnation containing heavy hydrocarbons.

4691. The method ofclaim 4690, wherein the insulation layer comprises a spiral insulation layer.

4692. The method of claim 4690, wherein the insulation layer comprises at least one metal oxide.

4693. The method of claim 4690, further comprising fastening at least a portion of the insulation layer to at least a portion of the conductor-in-conduit heat source with a high temperature glue.

4694. The method of claim 4662, further comprising providing heat from the conductor-in-conduit heat source of the desired length to at least a portion of the foimation.

4695. The method of claim 4662, wherein a thickness of the conductor configurable to be placed adjacent to a lean zone in the formation is greater than a thickness of the conductor configurable to be placed adjacent to a rich zone in the formation such that more heat is provided to the rich zone during use

4696. The method of claim 4662, further comprising pyrolyzing at least some hydrocarbons in a selected section of the formation.

4697. The method of claim 4662, further comprising producing a mixture from a selected section of the formation.

4698. A method for making a conductor-in-conduit heat source configurable to be used to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: placing a conductor within a conduit to form a conductor-in-conduit heat source; and shielded active gas welding the conductor-in-conduit heat source to at least one additional conductor-in- conduit heat source to form a conductor-in-conduit heat source of a desfred length, wherein the conductor is elecfrically coupled to the conductor of at least one additional conductor-in-conduit heat source and the conduit is elecfrically coupled to the conduit of at least one additional conductor-in-conduit heat source; and wherein the conductor-in-conduit heat source is configurable to be placed in an opening in the relatively low permeability foπnation containing heavy hydrocarbons, and wherein the conductor-in-conduit heat source is further configurable to heat a section of the relatively low permeability formation containing heavy hydrocarbons during use.

4699. The method ofclaim 4698, further comprising providing heat from the conductor-in-conduit heat source of the desfred length to at least a portion of the foimation.

4700. The method of claim 4698, further comprising pyrolyzing at least some hydrocarbons in a selected section of the foimation.

4701. The method of clahn 4698, further comprising producing a mixture from a selected section of the formation.

4702. The method of claim 4698, wherein the conductor and the conduit comprise stainless steel.

4703. The method of claim 4698, wherein the conduit comprises stainless steel.

4704. The method ofclaim 4698, wherehi the heat source is configurable to be removed from the formation.

4705. The method ofclaim 4698, further comprising providing a reducing gas during welding.

4706. The method of claim 4698, wherein the reducing gas comprises molecular hydrogen.

4707. The method ofclaim 4698, further comprising providing a reducing gas during welding such that welding occurs in an environment comprising less than about 25 % reducing gas by volume.

4708. The method ofclaim 4698, further comprising providing a reducing gas during welding such that welding occurs in an environment comprising about 10 % reducing gas by volume.

4709. A system configurable to heat a relatively low peπneability foπnation containing heavy hydrocarbons, comprising: a conduit configurable to be placed within an opening in the formation; a conductor configurable to be placed within the conduit, wherein the conductor is further configurable to provide heat to at least a portion of the fonnation during use, and wherein the conductor comprises at least two conductor sections coupled by shielded active gas welding; and wherein the system is configurable to allow heat to ttansfer from the conductor to a section of the foimation during use.

4710. The system ofclaim 4709, wherein the conduit comprises at least two conduit sections coupled by shielded active gas welding.

4711. The system of claim 4709, wherein the system is further configurable to allow at least some hydrocarbons to pyrolyze in the heated section of the foimation during use.

4712. The system ofclaim 4709, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit configured to be placed within an opening in the formation; a conductor configured to be placed within the conduit, wherein the conductor is further configured to provide heat to at least a portion of the formation during use, and wherein the conductor comprises at least two conductor sections coupled by shielded active gas welding; and wherein the system is configured to allow heat to transfer from the conductor to a section of the formation during use.

4713. The system ofclaim 4709, wherein the system heats a relatively low permeability foπnation containing heavy hydrocarbons, and wherein the system comprises: a conduit placed within an opening in the formation; a conductor placed within the conduit, wherein the conductor provides heat to at least a portion of the foπnation during use, and wherein the conductor comprises at least two conductor sections coupled by shielded active gas welding; and wherein the system allows heat to transfer from the conductor to a section of the formation during use.

4714. The system ofclaim 4709, wherein the conductor-in-conduit heat source is configurable to be removed from the formation.

4715. A method for installing a heat source of a desfred length in a relatively low permeability formation containing heavy hydrocarbons, comprising: assembling a heat source of a desfred length, wherein the assembling of the heat source of the desfred length is performed at a location proximate the relatively low permeability formation containing heavy hydrocarbons; coiling the heat source of the desired length after forming the heat source; and placing the heat source of the desfred length in an opening in a relatively low permeability formation containing heavy hydrocarbons, wherein placing the heat source in the opening comprises uncoiling the heat source while placing the heat source in the opening.

4716. The method ofclaim 4715, wherein the heat source is configurable to heat a section of the relatively low permeability formation containing heavy hydrocarbons.

4717. The method of claim 4716, wherein the heat pyrolyzes at least some hydrocarbons in the section of the formation during use.

4718. The method ofclaim 4715, further comprising coupling at least one substantially low resistance conductor to the heat source of the desired length, wherein at least one substantially low resistance conductor is configured to be placed in an overburden of the formation.

4719. The method of claim 4718, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor.

4720. The method ofclaim 4718, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor, wherein coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor comprises coupling a threaded end of at least one additional substantially low resistance conductor to a threaded end of at least one substantially low resistance conductor.

4721. The method of claim 4718, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor, wherein coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor comprises welding at least one additional substantially low resistance conductor to at least one substantially low resistance conductor.

4722. The method ofclaim 4715, further comprising transporting the heat source of the deshed length on a cart or train from an assembly location to the opening in the relatively low permeability formation containing heavy hydrocarbons.

4723. The method of clahn 4722, wherein the cart or train can be further used to fransport more than one heat source to more than one opening in the relatively low permeability formation containing heavy hydrocarbons.

4724. The method of claim 4722, wherein the heat source is configurable to removable from the opening.

4725. A method for installing a heat source of a desfred length in a relatively low permeability formation containing heavy hydrocarbons, comprising: assembling a heat source of a deshed length, wherein the assembling of the heat source of the desfred length is performed at a location proximate the relatively low peπneability formation containing heavy hydrocarbons; coiling the heat source of the desired length after forming the heat source; placing the heat source of the desired length in an opening in a relatively low permeability formation containing heavy hydrocarbons, wherein placing the heat source in the opening comprises uncoiling the heat source while placing the heat source in the opening; and wherein the heat source is configurable to be removed from the opening.

4726. The method ofclaim 4725, wherein the heat source is configurable to heat a section of the relatively low peπneability foπnation containing heavy hydrocarbons.

4727. The method ofclaim 4726, wherein the heat pyrolyzes at least some hydrocarbons in the section of the formation during use.

4728. The method ofclaim 4725, further comprising coupling at least one substantially low resistance conductor to the heat source of the desired length, wherein at least one substantially low resistance conductor is configured to be placed in an overburden of the formation.

4729. The method of claim 4728, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor.

4730. The method ofclaim 4728, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor, wherein coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor comprises coupling a threaded end of at least one additional substantially low resistance conductor to a threaded end of at least one substantially low resistance conductor.

4731. The method ofclaim 4728, further comprising coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor, wherein coupling at least one additional substantially low resistance conductor to at least one substantially low resistance conductor comprises welding at least one additional substantially low resistance conductor to at least one substantially low resistance conductor.

4732. The method of clahn 4725, further comprising transporting the heat source of the deshed length on a cart or train from an assembly location to the opening in the relatively low permeability formation containing heavy hydrocarbons.

4733. The method ofclaim 4725, wherein removing the heat source comprises recoiling the heat source.

4734. The method of claim 4725, wherein the heat source can be removed from the opening and installed in an alternate opening in the formation.

4735. A system configurable to heat a relatively low permeability foπnation containing heavy hydrocarbons, comprising: a conduit configurable to be placed withhi an opening in the formation; a conductor configurable to be placed within a conduit, wherein the conductor is further configurable to provide heat to at least a portion of the formation during use; an electrically conductive material configurable to be coupled to at least a portion of the conductor, wherein the electrically conductive material is configurable to lower an elecfrical resistance of the conductor in the overburden during use; and wherein the system is configurable to allow heat to fransfer from the conductor to a section of the formation during use.

4736. The system ofclaim 4735, further comprising an elecfrically conductive material configurable to be coupled to at least a portion of an inside surface of the conduit.

4737. The system ofclaim 4735, further comprising a substantially low resistance conductor configurable to be electtically coupled to the conductor and the elecfrically conductive material during use, wherein the substantially low resistance conductor is further configurable to be placed within an overburden of the formation.

4738. The system ofclaim 4737, wherein the low resistance conductor comprises carbon steel.

4739. The system of clahn 4735, wherein the elecfrically conductive material comprises metal tubing configurable to be clad to the conductor.

4740. The system ofclaim 4735, wherein the electrically conductive material comprises an electtically conductive coating configurable to be applied to the conductor.

4741. The system of claim 4735, wherein the electrically conductive material comprises a thermal plasma applied coating.

4742. The system of claim 4735, wherein the elecfrically conductive material is configurable to be sprayed on the conductor.

4743. The system ofclaim 4735, wherein the elecfrically conductive material comprises aluminum.

4744. The system ofclaim 4735, wherein the elecfrically conductive material comprises copper.

4745. The system of claim 4735, wherein the elecfrically conductive material is configurable to reduce the elecfrical resistance of the conductor in the overburden by a factor of greater than about 3.

4746. The system ofclaim 4735, wherein the elecfrically conductive material is configurable to reduce the electtical resistance of the conductor in the overburden by a factor of greater than about 15.

4747. The system ofclaim 4735, wherein the system is further configurable to allow at least some hydrocarbons to pyrolyze in the heated section of the formation during use.

4748. The system of claim 4735, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit configured to be placed within an opening in the formation; a conductor configured to be placed within a conduit, wherein the conductor is further configured to provide heat to at least a portion of the foimation during use; an elecfrically conductive material configured to be coupled to the conductor, wherein the electrically conductive material is further configured to lower an electrical resistance of the conductor in the overburden during use; and wherein the system is configured to allow heat to transfer from the conductor to a section of the foπnation during use.

4749. The system of claim 4735, wherein the system heats a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit placed withhi an opening in the foπnation; a conductor placed within a conduit, wherein the conductor is provides heat to at least a portion of the formation during use; an electrically conductive material coupled to the conductor, wherein the electrically conductive material lowers an electtical resistance of the conductor in the overburden during use; and wherein the system allows heat to ttansfer from the conductor to a section of the formation during use.

4750. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: applying an electrical cunent to a conductor to provide heat to at least a portion of the formation, wherein the conductor is placed in a conduit, and wherein the conduit is placed in an opening in the foπnation, and wherein the conductor is coupled to an elecfrically conductive material; and allowing the heat to fransfer from the conductor to a section of the formation.

4751. The method of claim 4750, wherein the elecfrically conductive material comprises copper.

4752. The method ofclaim 4750, further comprising coupling an elecfrically conductive material to an inside surface of the conduit.

4753. The method of claim 4750, wherein the elecfrically conductive material comprises metal tubing clad to the substantially low resistance conductor.

4754. The method of clahn 4750, wherein the elecfrically conductive material reduces an electrical resistance of the substantially low resistance conductor in the overburden.

4755. The method ofclaim 4750, further comprising pyrolyzing at least some hydrocarbons within the formation.

4756. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit configurable to be placed within an opening in the foπnation; a conductor configurable to be placed within a conduit, wherein the conductor is further configurable to provide heat to at least a portion of the formation during use, and wherein the conductor has been treated to increase an emissivity of at least a portion of a surface of the conductor; and wherein the system is configurable to allow heat to transfer from the conductor to a section of the formation during use.

4757. The system of claim 4756, wherein at least a portion of the surface of the conductor has been roughened to increase the emissivity of the conductor.

4758. The system ofclaim 4756, wherein the conductor has been heated to a temperature above about 750 °C in an oxidizing fluid atmosphere to increase the emissivity of at least a portion of the surface of the conductor.

4759. The system of claim 4756, wherein the conduit has been freated to increase an emissivity of at least a portion of the surface of the conduit.

4760. The system ofclaim 4756, further comprising an electrically insulative, thermally conductive coating coupled to the conductor.

4761. The system ofclaim 4760, wherein the electtically insulative, thermally conductive coating is configurable to electtically insulate the conductor from the conduit.

4762. The system ofclaim 4760, wherein the elecfrically insulative, thermally conductive coating inhibits emissivity of the conductor from decreasing.

4763. The system of claim 4760, wherein the elecfrically insulative, thennally conductive coating substantially increases an emissivity of the conductor.

4764. The system ofclaim 4760, wherein the elecfrically insulative, thennally conductive coating comprises silicon oxide.

4765. The system ofclaim 4760, wherein the elecfrically insulative, thermally conductive coating comprises aluminum oxide.

4766. The system of claim 4760, wherein the electrically insulative, thermally conductive coating comprises refractive cement.

4767. The system ofclaim 4760, wherein the electrically insulative, thermally conductive coating is sprayed on the conductor.

4768. The system ofclaim 4756, wherein the system is fiuther configurable to allow at least some hydrocarbons to pyrolyze in the heated section of the formation during use.

4769. The system ofclaim 4756, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit configured to be placed within an opening in the formation; a conductor configured to be placed within a conduit, wherein the conductor is further configured to provide heat to at least a portion of the formation during use, and wherein the conductor has been freated to increase an emissivity of at least a portion of a surface of the conductor; and wherein the system is configured to allow heat to fransfer from the conductor to a section of the formation during use.

4770. The system of clahn 4756, wherein the system heats a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit placed within an opening in the formation; a conductor placed within a conduit, wherein the conductor provides heat to at least a portion of the formation during use, and wherein the conductor has been treated to increase an emissivity of at least a portion of a surface of the conductor; and wherein the system allows heat to fransfer from the conductor to a section of the formation during use.

4771. A heat source configurable to heat a relatively low permeability foπnation containing heavy hydrocarbons, comprising: a conduit configurable to be placed within an opening in the formation; and a conductor configurable to be placed within a conduit, wherein the conductor is further configurable to provide heat to at least a portion of the formation during use, and wherein the conductor has been freated to increase an emissivity of at least a portion of a surface of the conductor.

4772. The heat source of claim 4771 , wherein at least a portion of the surface of the conductor has been roughened to increase the emissivity the conductor.

4773. The heat source ofclaim 4771, wherein the conductor has been heated to a temperature above about 750 °C in an oxidizing fluid atmosphere to increase the emissivity of at least at least a portion of the surface of the conductor.

4774. The heat source ofclaim 4771, wherein the conduit has been freated to increase an emissivity of at least a portion of the surface of the conduit.

4775. The heat source of claim 4771 , further comprising an elecfrically insulative, thermally conductive coating placed on the conductor.

4776. The heat source ofclaim 4775, wherein the electtically insulative, thermally conductive coating is configurable to electrically insulate the conductor from the conduit.

4777. The heat source ofclaim 4775, wherein the electrically insulative, thermally conductive coating substantially maintains an emissivity of the conductor.

4778. The heat source ofclaim 4775, wherein the electrically insulative, thennally conductive coating substantially increases an emissivity of the conductor.

4779. The heat source ofclaim 4775, wherein the electtically insulative, thermally conductive coating comprises silicon oxide.

4780. The heat source of claim 4775, wherein the elecfrically insulative, thermally conductive coating comprises aluminum oxide.

4781. The heat source of claim 4775, wherein the elecfrically insulative, thermally conductive coating comprises refractive cement.

4782. The heat source ofclaim 4775, wherein the elecfrically insulative, thermally conductive coating is sprayed on the conductor.

4783. The heat source ofclaim 4771, wherein the conductor is further configurable to provide heat to at least a portion of the foimation during use such that at least some hydrocarbons pyrolyze in the heated section of the formation during use.

4784. The heat source ofclaim 4771, wherein the heat source is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit configured to be placed within an opening in the formation; a conductor configured to be placed within a conduit, wherein the conductor is further configured to provide heat to at least a portion of the foimation during use, and wherein the conductor has been freated to increase an emissivity of at least a portion of a surface of the conductor.

4785. The heat source ofclaim 4771, wherein the heat source heats a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a conduit placed within an opening in the formation; a conductor placed within a conduit, wherein the conductor provides heat to at least a portion of the formation, and wherein the conductor has been treated to increase an emissivity of at least a portion of a surface of the conductor.

4786. A method for forming an increased emissivity conductor-in-conduit heat source, comprising: treating a surface of a conductor to increase an emissivity of at least the surface of the conductor; placing the conductor within a conduit to form a conductor-in-conduit heat source; and wherein the conductor-in-conduit heat source is configurable to heat a relatively low permeability formation containing heavy hydrocarbons.

4787. The method of claim 4786, wherein treating the surface of the conductor comprises roughening at least a portion of the surface of the conductor.

4788. The method ofclaim 4786, wherein freating the surface of the conductor comprises heating the conductor to a temperature above about 750 °C in an oxidizing fluid atmosphere.

4789. The method ofclaim 4786, further comprising treating a surface of the conduit to increase an emissivity of at least a portion of the surface of the conduit.

4790. The method ofclaim 4786, further comprising placing the conductor-in-conduit heat source of the desfred length in an opening in a relatively low permeability formation containing heavy hydrocarbons.

4791. The method ofclaim 4786, further comprising assembling a conductor-in-conduit heat source of a desfred length, the assembling comprising: coupling the conductor-in-conduit heat source to at least one additional conductor-in-conduit heat source to form a conductor-in-conduit heat source of a desfred length, wherein the conductor is electrically coupled to the conductor of at least one additional conductor-in-conduit heat source and the conduit is electtically coupled to the conduit of at least one additional conductor-in-conduit heat source; coiling the conductor-in-conduit heat source of the desired length after forming the heat source; and placing the conductor-in-conduit heat source of the desired length in an opening in a relatively low permeability formation containing heavy hydrocarbons.

4792. The method of claim 4786, wherein the conductor-in-conduit heat source is configurable to heat to a section of the relatively low permeability foπnation containing heavy hydrocarbons, and wherein the heat pyrolyzes at least some hydrocarbons in the section of the formation during use.

4793. A system configurable to heat a relatively low permeability formation containing heavy hydrocarbons, comprising: a heat source configurable to be placed in an opening in the formation, wherein the heat source is further configurable to provide heat to at least a portion of the formation during use; an expansion mechanism configurable to be coupled to the heat source, wherein the expansion mechanism is configurable to allow for movement of the heat source during use; and wherein the system is configurable to allow heat to transfer to a section of the formation during use.

4794. The system of claim 4793, wherein the expansion mechanism is configurable to allow for expansion of the heat source during use.

4795. The system ofclaim 4793, wherein the expansion mechanism is configurable to allow for confraction of the heat source during use.

4796. The system of claim 4793, wherein the expansion mechanism is configurable to allow for expansion of at least one component of the heat source during use.

4797. The system ofclaim 4793, wherein the expansion mechanism is configurable to allow for expansion and contraction of the heat source within a wellbore during use.

4798. The system ofclaim 4793, wherein the expansion mechanism comprises spring loading.

4799. The system ofclaim 4793, wherein the expansion mechanism comprises an accordion mechanism.

4800. The system of claim 4793, wherein the expansion mechanism is configurable to be coupled to a bottom of the heat source.

4801. The system of claim 4793, wherein the heat source is configurable to allow at least some hydrocarbons to pyrolyze in the heated section of the formation during use.

4802. The system of clahn 4793, wherein the system is configured to heat a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a heat source configured to be placed in an opening in the foπnation, wherein the heat source is further configured to provide heat to at least a portion of the formation during use; an expansion mechanism configured to be coupled to the heat source, wherein the expansion mechanism is configured to allow for movement of the heat source during use; and wherein the system is configured to allow heat to ttansfer to a section of the formation during use.

4803. The system ofclaim 4793, wherein the system heats a relatively low permeability formation containing heavy hydrocarbons, and wherein the system comprises: a heat source placed in an opening in the formation, wherein the heat source provides heat to at least a portion of the formation during use; an expansion mechanism coupled to the heat source, wherein the expansion mechanism allows for movement of the heat source during use; and wherein the system allows heat to fransfer to a section of the formation during use.

4804. The system of claim 4793, wherein the heat source is removable.

4805. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit positionable in at least a portion of an opening in the formation, wherein a first end of the opening contacts an earth surface at a first location, and wherein a second end of the opening contacts the earth surface at a second location; and an oxidizer configurable to provide heat to a selected section of the formation by transferring heat through the conduit.

4806. The system ofclaim 4805, wherein heat from the oxidizer pyrolyzes at least some hydrocarbons in the selected section.

4807. The system ofclaim 4805, wherein the conduit is positioned in the opening.

4808. The system of clahn 4805, wherein the oxidizer is positionable in the conduit.

4809. The system ofclaim 4805, wherein the oxidizer is positioned in the conduit, and wherein the oxidizer is configured to heat the selected section.

4810. The system ofclaim 4805, wherein the oxidizer comprises a ring burner.

481 1. The system ofclaim 4805, wherein the oxidizer comprises an inline burner.

4812. The system ofclaim 4805, wherein the oxidizer is configurable to provide heat in the conduit.

4813. The system of claim 4805, further comprising an annulus foπned between a wall of the conduit and a wall of the opening.

4814. The system o claim 4805, wherein the oxidizer comprises a first oxidizer and a second oxidizer, and further comprising an annulus formed between a wall of the conduit and a wall of the openhig, wherein the second oxidizer is positionable in the annulus.

4815. The system ofclaim 4814, wherein the first oxidizer is configurable to provide heat in the conduit, and wherehi the second oxidizer is configurable to provide heat outside of the conduit.

4816. The system of claim 4814, wherehi heat provided by the ffrst oxidizer fransfers in the first conduit in a direction opposite of heat provided by the second oxidizer.

4817. The system of claim 4814, wherehi heat provided by the first oxidizer fransfers in the first conduit in a same direction as heat provided by the second oxidizer.

4818. The system ofclaim 4805, wherein the oxidizer is configurable to oxidize fuel to generate heat, and further comprising a recycle conduit configurable to recycle at least some of the fuel in the conduit to a fuel source.

4819. The system of claim 4805, wherein the oxidizer comprises a first oxidizer positioned in the conduit and a second oxidizer positioned in an annulus formed between a wall of the conduit and a wall of the opening, wherein the oxidizers are configurable to oxidize fuel to generate heat, and further comprising: a first recycle conduit configurable to recycle at least some of the fuel in the conduit to the second oxidizer; and a second recycle conduit configurable to recycle at least some of the fuel in the annulus to the first oxidizer.

4820. The system of claim 4805, further comprising insulation positionable proximate the oxidizer.

4821. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat to a conduit positioned in an opening in the formation, wherein a ffrst end of the opening contacts an earth surface at a first location, and wherein a second end of the openhig contacts the earth surface at a second location; and allowing the heat in the conduit to fransfer through the opening and to a sunounding portion of the formation.

4822. The method of claim 4821, further comprishig: providing fuel to an oxidizer; oxidizing at least some of the fuel; and allowing oxidation products to migrate through the opening, wherein the oxidation products comprise heat.

4823. The method of claim 4822, wherein the fuel is provided to the oxidizer proximate the first location, and wherein the oxidation products migrate towards the second location.

4824. The method of claim 4821 , wherein the oxidizer comprises a ring burner.

4825. The method ofclaim 4821, wherein the oxidizer comprises an inline burner.

4826. The method ofclaim 4821, further comprising recycling at least some fuel in the conduit.

4827. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit positionable in an opening in the foimation, wherein a ffrst end of the opening contacts an earth surface at a ffrst location, wherein a second end of the opening contacts the earth surface at a second location; an annulus foπned between a wall of the conduit and a wall of the opening; and a oxidizer configurable to provide heat to a selected section of the formation by transferring heat through the annulus.

4828. The system of claim 4827, wherein heat from the oxidizer pyrolyzes at least some hydrocarbons in the selected section.

4829. The system ofclaim 4827, wherein the conduit is positioned in the opening.

4830. The system ofclaim 4827, wherein the oxidizer comprises a first oxidizer and a second oxidizer, wherein the second oxidizer is positioned in the conduit, and wherein the second oxidizer is configured to heat the selected section.

4831. The system of claim 4827, wherein the oxidizer comprises a ring burner.

4832. The system of claim 4827, wherein the oxidizer comprises an inline burner.

4833. The system of claim 4830, wherein heat provided by the ffrst oxidizer fransfers in the first conduit in a direction opposite of heat provided by the second oxidizer.

4834. The system ofclaim 4827, wherein the oxidizer is configurable to oxidize fuel to generate heat, and further comprising a recycle conduit configurable to recycle at least some of the fuel in the conduit to a fuel source.

4835. The system ofclaim 4827, further comprising insulation positionable proximate the oxidizer.

4836. The system ofclaim 4827, wherein the conduit is positioned in the opening.

4837. The system ofclaim 4827, wherein the oxidizer is positioned in the annulus, and wherein the oxidizer is configured to heat the selected section.

4838. The system of clahn 4827, wherein the oxidizer comprises a first oxidizer and a second oxidizer.

4839. The system ofclaim 4838, wherein heat provided by the ffrst oxidizer fransfers through the opening in a direction opposite of heat provided by the second oxidizer.

4840. The system ofclaim 4827, wherein the oxidizer is configurable to oxidize fuel to generate heat, and further comprising a recycle conduit configurable to recycle at least some of the fuel in the annulus to a fuel source.

4841. The system ofclaim 4827, further comprising insulation positionable proxhnate the oxidizer.

4842. The system ofclaim 4838, wherein the first oxidizer and the second oxidizer comprise oxidizers, and wherein a first mixture of oxidation products generated by the first oxidizer flows countercurrent to a second mixture of oxidation products generated by the second heater.

4843. The system ofclaim 4838, wherein the first heater and the second heater comprise oxidizers, wherein fuel is oxidized by the oxidizers to generate heat, and further comprising a first recycle conduit to recycle fuel in the first conduit proximate the second location to the second conduit.

4844. The system ofclaim 4838, wherein the first oxidizer and the second oxidizer comprise oxidizers, wherein fuel is oxidized by the oxidizers to generate heat, and further comprising a second recycle conduit to recycle fuel in the second conduit proximate the first location to the first conduit.

4845. The system of claim 4827, further comprising a casing, wherein the conduit is positionable in the casing.

4846. The system ofclaim 4827, wherein the oxidizer comprises a first oxidizer positioned in the annulus and a second oxidizer positioned in the conduit, wherein the oxidizers are configurable to oxidize fuel to generate heat, and further comprising: a first recycle conduit configurable to recycle at least some of the fuel in the annulus to the second oxidizer; and a second recycle conduit configurable to recycle at least some of the fuel in the conduit to the first oxidizer.

4847. An in situ method for heating a relatively low permeability fonnation containing heavy hydrocarbons, comprising: providing heat to an annulus formed between a wall of an opening in the formation and a wall of a conduit in the opening, wherein a first end of the opening contacts an earth surface at a ffrst location, and wherein a second end of the opening contacts the earth surface at a second location; and allowing the heat in the annulus to fransfer through the openhig and to a sunounding portion of the foimation.

4848. The method ofclaim 4847, further comprising: providing fuel to an oxidizer; oxidizing at least some of the fuel; and allowing oxidation products to migrate through the opening, wherehi the oxidation products comprise heat.

4849. The method of claim 4848, wherein the fuel is provided the oxidizer proxhnate the first location, and wherein the oxidation products migrate towards the second location.

4850. The method ofclaim 4847, wherein the oxidizer comprises a ring burner.

4851. The method ofclaim 4847, wherein the oxidizer comprises an inline burner.

4852. The method ofclaim 4847, further comprising recycling at least some fuel in the conduit.

4853. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a first conduit positionable in an opening in the formation, wherein a first end of the opening contacts an earth surface at a ffrst location, wherehi a second end of the opening contacts the earth surface at a second location; a second conduit positionable in the opening; a first oxidizer configurable to provide heat to a selected section of the foπnation by transferring heat through the first conduit; and a second oxidizer configurable to provide heat to the selected section of the foπnation by fransfening heat through the second conduit..

4854. The system ofclaim 4853, wherein the first oxidizer is positionable in the first conduit.

4855. The system ofclaim 4853, wherehi the second oxidizer is positionable in the second conduit.

4856. The system ofclaim 4853, further comprising a casing positionable in the opening.

4857. The system ofclaim 4853, wherein at least a portion of the second conduit is positionable in the first conduit, and further comprising an annulus formed between a wall of the first conduit and a wall of the second conduit.

4858. The system of clahn 4853, wherein a portion of the second conduit is positionable proximate a portion of the first conduit.

4859. The system of claim 4853, wherein the ffrst oxidizer or the second oxidizer provide heat to at least a portion of the formation.

4860. The system ofclaim 4853, wherein the ffrst oxidizer and the second oxidizer provide heat to at least a portion of the formation concunently.

4861. The system ofclaim 4853, wherein the first oxidizer is positioned in the first conduit, wherein the second oxidizer is positioned in the second conduit, wherein the first oxidizer and the second oxidizer comprise oxidizers, and wherein a first flow of oxidation products from the first oxidizer flows in a direction opposite of a second flow of oxidation products from the second oxidizer.

4862. The system ofclaim 4853, further comprising: a first recycle conduit configurable to recycle at least some of the fuel in the first conduit to the second oxidizer; and a second recycle conduit configurable to recycle at least some of the fuel in the second conduit to the first oxidizer.

4863. An in situ method for heating a relatively low permeability foπnation containing heavy hydrocarbons, comprising: providing heat to a first conduit positioned in an opening in the formation, wherein a first end of the opening contacts an earth surface at a ffrst location, and wherein a second end of the opening contacts the earth surface at a second location; providing heat to a second conduit positioned in the opening in the formation; allowing the heat in the first conduit to fransfer through the opening and to a sunounding portion of the formation; and allowing the heat in the second conduit to transfer through the opening and to a sunounding portion of the formation;

4864. The method of claim 4863, wherein providing heat to the first conduit comprises providing fuel to an oxidizer.

4865. The method of claim 4863, wherein providing heat to the second conduit comprises providing fuel to an oxidizer.

4866. The method of claim 4863, wherein the ffrst fuel is provided to the ffrst conduit proximate the first location, and wherein the second fuel is provided to the second conduit proximate the second location.

4867. The method ofclaim 4863, wherem the first oxidizer or the second oxidizer comprises a ring burner.

4868. The method ofclaim 4863, wherein the first oxidizer or the second oxidizer an inline burner.

4869. The method ofclaim 4863, further comprising:

transfening heat through the first conduit in a first direction; and transfening heat in the second conduit in a second direction.

4870. The method of claim 4863, further comprising recycling at least some fuel in the first conduit to the second conduit; and recycling at least some fuel in the second conduit to the first conduit.

4871. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a first conduit positionable in an openmg in the formation, wherein a first end of the opening contacts an earth surface at a ffrst location, wherehi a second end of the opening contacts the earth surface at a second location; a second conduit positionable in the first conduit; and at least one surface unit configurable to provide heat to the first conduit.

4872. The system ofclaim 4871, wherein the surface unit comprises a furnace.

4873. The system of claim 4871, wherein the surface unit comprises a burner.

4874. The system ofclaim 4871, wherein at least one surface unit is configurable to provide heat to the second conduit.

4875. The system ofclaim 4874, wherein the first conduit and the second conduit provide heat to at least a portion of the foimation.

4876. The system of claim 4874, wherein the first conduit provides heat to at least a portion of the formation.

4877. The system ofclaim 4874, wherein the second conduit provides heat to at least a portion of the formation.

4878. The system ofclaim 4871, further comprising a casing positionable in the opening.

4879. The method of claim 4871, wherein the first conduit and the second conduit are concentric.

4880. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a fluid using at least one surface unit; providing the heated fluid to a ffrst conduit wherein a portion of the ffrst conduit is positioned in an opening in the formation, wherem a first end of the opening contacts an earth surface at a ffrst location, and wherein a second end of the opening contacts the earth surface at a second location; allowing the heated fluid to flow into a second conduit, wherein the first conduit is positioned within the second conduit; and allowing heat from the ffrst and second conduit to ttansfer to a portion of the foπnation.

4881. The method of claim 4880, further comprising providing additional heat to the heated fluid using at least one surface unit proximate the second location.

4882. The method of claim 4880, wherein the fluid comprises an oxidizing fluid.

4883. The method of claim 4880, wherein the fluid comprises air.

4884. The method of claim 4880, wherein the fluid comprises flue gas.

4885. The method ofclaim 4880, wherein the fluid comprises steam.

4886. The method ofclaim 4880, wherein the fluid comprises fuel.

4887. The method ofclaim 4880, further comprising compressing the fluid prior to heating.

4888. The method of clahn 4880, wherein the surface unit comprises a furnace.

4889. The method of claim 4880, wherein the surface unit comprises an indirect furnace.

4890. The method of claim 4880, wherein the surface unit comprises a burner.

4891. The method of claim 4880, wherein the first conduit and the second conduit are concentric.

4892. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit positionable in at least a portion of an opening in the formation, wherein a first end of the opening contacts an earth surface at a ffrst location, and wherein a second end of the opening contacts the earth surface at a second location; and at least two oxidizers configurable to provide heat to a portion of the foπnation.

4893. The system ofclaim 4892, wherein heat from the oxidizers pyrolyzes at least some hydrocarbons in the selected section.

4894. The system of clahn 4892, wherein the conduit comprises a fuel conduit.

4895. The system ofclaim 4892, wherein at least one oxidizer is positionable proximate the conduit.

4896. The system of claim 4892, wherein at least one oxidizer comprises a ring burner.

4897. The system of claim 4892, wherein at least one oxidizer comprises an inline burner.

4898. The system ofclaim 4892, further comprising insulation positionable proximate at least one oxidizer.

4899. The system ofclaim 4892, further comprising a casing comprising insulation proximate at least one oxidizer.

4900. An in situ method for heating a relatively low permeability foπnation containing heavy hydrocarbons, comprising: providing fuel to a conduit positioned in an openhig in the foπnation, wherein a ffrst end of the opening contacts an earth surface at a first location, and wherein a second end of the openhig contacts the earth surface at a second location; providing an oxidizmg fluid to the opening; oxidizing fuel in at least one oxidizer positioned proximate the conduit; and allowing heat to transfer to a portion of the formation.

4901. The method of claim 4900, further comprising providing steam to the conduit.

4902. The method ofclaim 4900, further comprising inhibiting coking within the conduit.

4903. The method ofclaim 4900, wherein the oxidizing fluid comprises afr.

4904. The method of claim 4900, wherein the oxidizing fluid comprises oxygen.

4905. The method of claim 4900, further comprising allowing oxidation products to exit the opening proxhnate the second location.

4906. The method ofclaim 4900, wherein the fuel is provided to proximate the first location, and wherein the oxidation products migrate towards the second location.

4907. The method ofclaim 4900, wherein the oxidizer comprises a ring burner.

4908. The method ofclaim 4900, wherein the oxidizer comprises an inline burner.

4909. The method ofclaim 4900, further comprising recycling at least some fuel in the conduit.

4910. The system ofclaim 4900, wherein the opening comprises a casing and further comprising insulating a portion of the casing proximate at least one oxidizer.

4911. The system ofclaim 4900, further comprising at least two oxidizers, wherein the oxidizers are positioned about 30 m apart.

4912. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a conduit positionable in at least a portion of an opening in the formation, wherein a first end of the opening contacts an earth surface at a first location, and wherein a second end of the opening contacts the earth surface at a second location; and an oxidizing fluid source configurable to provide an oxidizing fluid to a reaction zone of the formation.

4913. The system of claim 4912, wherein the conduit comprises a conductor and wherein the conductor is configured to generate heat during application of an electtical cunent to the conduit.

4914. The system of claim 4912, wherehi the conduit comprises a low resistance conductor and wherein at least some of the low resistance conductor is positionable in an overburden.

4915. The system of claim 4912, wherein the oxidizing fluid source is configurable to provide at least some oxidizing fluid to the conduit at the first location and at the second location.

4916. The system of claim 4912, wherein the opening is configurable to allow products of oxidation to be produced from the formation.

4917. The system ofclaim 4912, wherein the oxidizing fluid reacts with at least some hydrocarbons and wherein the oxidizing fluid source is configurable to provide at least some oxidizing fluid to the first location and to the second location.

4918. The system ofclaim 4912, wherein the heat source is configurable to heat a reaction zone of the selected section to a temperature sufficient to support reaction of hydrocarbons in the selected section with an oxidizing fluid.

4919. The system ofclaim 4918, wherein the heat source is configurable to provide an oxidizing fluid to the selected section of the formation to generate heat during use.

4920. The system ofclaim 4918, wherein the generated heat transfers to a pyrolysis zone of the foimation.

4921. The system of claim 4912, further comprising an oxidizing fluid source configurable to provide an oxidizing fluid to the heat source, and wherein the conduit is configurable to provide the oxidizing fluid to the selected section of the foimation during use.

4922. The system of claim 4912, wherein the conduit comprises a low resistance conductor and a conductor, and wherein the conductor is further configured to generate heat during application of an elecfrical cunent to the conduit.

4923. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing an elecfrical cunent to a conduit positioned in an openmg in the formation; allowing heat to fransfer from the conduit to a reaction zone of the formation; providing at least some oxidizing fluid to the conduit; allowing the oxidizhig fluid to fransfer from the conduit to the reaction zone in the formation; allowing the oxidizing fluid to oxidize at least some hydrocarbons in the reaction zone to generate heat; and allowing at least some of the generated heat to transfer to a pyrolysis zone in the formation.

4924. The method ofclaim 4923, wherein at least a portion of the conduit is configured to generate heat during application of the electrical cunent to the conduit.

4925. The method of claim 4923 , further comprising: providing at least some oxidizing fluid to the conduit proximate a first end of the conduit; providing at least some oxidizing fluid to the conduit proximate a second end of the conduit; and wherein the first end of the conduit is positioned at a first location on a surface of the formation and wherein the second end of the conduit is positioned at a second location on the surface.

4926. The method of claim 4923, further comprising allowing the oxidizing fluid to move out of the conduit through orifices positioned on the conduit.

4927. The method ofclaim 4923, further comprishig removing products of oxidation through the opening during use.

4928. The method of claim 4923, wherein a first end of the opening is positioned at a first location on a surface of the formation and wherein a second end of the opening is positioned at a second location on the surface.

4929. The method of claim 4923, further comprising heating the reaction zone to a temperature sufficient to support reaction of hydrocarbons with an oxidizing fluid.

4930. The method ofclaim 4923, further comprising controlling a flow rate of the oxidizing fluid into the formation.

4931. The method of claim 4923, further comprising controlling a temperature in the pyrolysis zone.

4932. The method of claim 4923, further comprising removing products from oxidation through an opening in the formation during use.

4933. A method of using a computer system for modeling an in situ process for freating a relatively low permeability fonnation containing heavy hydrocarbons, comprising: providing at least one property of the formation to the computer system; providing at least one operating condition of the process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation; and assessing at least one process characteristic of the in situ process using a simulation method on the computer system, and using at least one property of the formation and at least one operating condition.

4934. The method ofclaim 4933, wherein at least one process characteristic is assessed as function of time.

4935. The method ofclaim 4933, wherein the simulation method is a body-fitted finite difference simulation method.

4936. The method of claim 4933, wherein the simulation method is a space-fitted finite difference simulation method.

4937. The method ofclaim 4933, wherein the simulation method is a reservoir simulation method.

4938. The method of clahn 4933, wherein the simulation method simulates heat fransfer by conduction.

4939. The method ofclaim 4933, wherein the shnulation method simulates heat fransfer by convection.

4940. The method ofclaim 4933, wherein the simulation method simulates heat fransfer by radiation.

4941. The method ofclaim 4933, wherein the simulation method simulates heat fransfer in a near wellbore region.

4942. The method ofclaim 4933, wherein the simulation method assesses a temperature disfribution in the foπnation.

4943. The method ofclaim 4933, wherein at least one property of the formation comprises one or more materials from the formation.

4944. The method ofclaim 4943, wherein one material comprises mineral matter.

4945. The method of claim 4943, wherein one material comprises organic matter.

4946. The method of claim 4933, wherehi at least one property of the foπnation comprises one or more phases.

4947. The method of claim 4946, wherein one phase comprises a water phase.

4948. The method ofclaim 4946, wherein one phase comprises an oil phase.

4949. The method of claim 4948, wherein the oil phase comprises one or more components.

4950. The method of claim 4946, wherein one phase comprises a gas phase.

4951. The method of claim 4950, wherein the gas phase comprises one or more components.

4952. The method of claim 4933, wherein at least one property of the foπnation comprises a porosity of the fonnation.

4953. The method ofclaim 4933, wherein at least one property of the formation comprises a peπneability of the formation.

4954. The method of clahn 4953, wherein the permeability depends on the composition of the foπnation.

4955. The method of clahn 4933, wherein at least one property of the formation comprises a saturation of the formation.

4956. The method ofclaim 4933, wherein at least one property of the fonnation comprises a density of the formation.

4957. The method ofclaim 4933, wherein at least one property of the foπnation comprises a thermal conductivity of the formation.

4958. The method ofclaim 4933, wherein at least one property of the foimation comprises a volumetric heat capacity of the formation.

4959. The method ofclaim 4933, wherein at least one property of the formation comprises a compressibility of the formation.

4960. The method ofclaim 4933, wherein at least one property of the formation comprises a composition of the foπnation.

4961. The method ofclaim 4933, wherein at least one property of the formation comprises a thickness of the foimation.

4962. The method of clahn 4933, wherein at least one property of the formation comprises a depth of the formation.

4963. The method ofclaim 4933, wherein at least one property comprises one or more chemical components.

4964. The method of claim 4963, wherein one component comprises a pseudo-component.

4965. The method of clahn 4933, wherein at least property comprises one or more kinetic parameters.

4966. The method of claim 4933, wherein at least one property comprises one or more chemical reactions.

4967. The method of claim 4966, wherein a rate of at least one chemical reaction depends on a pressure of the fonnation.

4968. The method of claim 4966, wherein a rate of at least one chemical reaction depends on a temperature of the formation.

4969. The method ofclaim 4966, wherein at least one chemical reaction comprises a pre-pyrolysis water generation reaction.

4970. The method of claim 4966, wherein at least one chemical reaction comprises a hydrocarbon generating reaction.

4971. The method of claim 4966, wherein at least one chemical reaction comprises a coking reaction.

4972. The method ofclaim 4966, wherein at least one chemical reaction comprise a cracking reaction.

4973. The method of claim 4966, wherein at least one chemical reaction comprises a synthesis gas reaction.

4974. The method of claim 4933, wherein at least one process characteristic comprises an API gravity of produced fluids.

4975. The method of claim 4933, wherein at least one process characteristic comprises an olefin content of produced fluids.

4976. The method ofclaim 4933, wherein at least one process characteristic comprises a carbon number distribution of produced fluids.

4977. The method ofclaim 4933, wherein at least one process characteristic comprises an ethene to ethane ratio of produced fluids.

4978. The method ofclaim 4933, wherein at least one process characteristic comprises an atomic carbon to hydrogen ratio of produced fluids.

4979. The method ofclaim 4933, wherein at least one process characteristic comprises a ratio of non- condensable hydrocarbons to condensable hydrocarbons of produced fluids.

4980. The method of claim 4933, wherein at least one process characteristic comprises a pressure in the formation

4981. The method ofclaim 4933, wherein at least one process characteristic comprises total mass recovery from the formation.

4982. The method ofclaim 4933, wherein at least one process characteristic comprises a production rate of fluid produced from the formation.

4983. The method of claim 4933, wherein at least one operating condition comprises a pressure.

4984. The method of clahn 4933, wherein at least one operating condition comprises a temperature.

4985. The method of claim 4933 , wherein at least one operating condition comprises a heating rate.

4986. The method ofclaim 4933, wherein at least one operating condition comprises a process time.

4987. The method ofclaim 4933, wherein at least one operating condition comprises a location of producer wells.

4988. The method of clahn 4933, wherein at least one operating condition comprises an orientation of producer wells.

4989. The method ofclaim 4933, wherein at least one operating condition comprises a ratio of producer wells to heater wells.

4990. The method of claim 4933, wherein at least one operating condition comprises a spacing between heater wells.

4991. The method ofclaim 4933, wherein at least one operating condition comprises a distance between an overburden and horizontal heater wells.

4992. The method ofclaim 4933, wherein at least one operating condition comprises a pattern of heater wells.

4993. The method ofclaim 4933, wherein at least one operating condition comprises an orientation of heater wells.

4994. A method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: simulating a heat input rate to the formation from two or more heat sources on the computer system, wherein heat is allowed to fransfer from the heat sources to a selected section of the formation; providing at least one desired parameter of the in situ process to the computer system; and controlling the heat input rate from the heat sources to achieve at least one desired parameter.

4995. The method ofclaim 4994, wherein the heat is allowed to fransfer from the heat sources substantially by conduction.

4996. The method of claim 4994, wherein the heat input rate is simulated with a body-fitted finite difference simulation method.

4997. The method of claim 4994, wherein simulating the heat input rate from two or more heat sources comprises simulating a model of one or more heat sources with symmetry boundary conditions.

4998. The method ofclaim 4994, wherein supeφosition of heat from the two or more heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation.

4999. The method of claim 4994, wherein at least one desfred parameter comprises a selected process characteristic.

5000. The method of claim 4994, wherein at least one desfred parameter comprises a selected temperature.

5001. The method ofclaim 4994, wherein at least one desired parameter comprises a selected heating rate.

5002. The method of claim 4994, wherein at least one desired parameter comprises a desired product mixture produced from the formation.

5003. The method of claim 4994, wherein at least one desfred parameter comprises a desfred product mixture produced from the foπnation, and wherein the desfred product mixture comprises a selected composition.

5004. The method ofclaim 4994, wherein at least one desfred parameter comprises a selected pressure.

5005. The method of claim 4994, wherein at least one desired parameter comprises a selected heating time.

5006. The method of claim 4994, wherein at least one desired parameter comprises a market parameter.

5007. The method ofclaim 4994, wherein at least one desfred parameter comprises a price of crude oil.

5008. The method of claim 4994, wherein at least one desired parameter comprises an energy cost.

5009. The method of claim 4994, wherein at least one desired parameter comprises a selected molecular hydrogen to carbon monoxide volume ratio.

5010. A method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing at least one heat input property to the computer system; assessing heat injection rate data for the formation using a first simulation method on the computer system; providing at least one property of the foπnation to the computer system; assessing at least one process characteristic of the in situ process from the heat injection rate data and at least one property of the formation using a second shnulation method; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation

501 1. The method ofclaim 5010, wherein at least one process characteristic is assessed as a function of time.

5012. The method ofclaim 5010, wherein assessing heat injection rate data comprises simulating heating of the formation.

5013. The method of claim 5010, wherein the heating is confrolled to obtain a desfred parameter.

5014. The method of clahn 5010, wherein determining at least one process characteristic comprises simulating heating of the foπnation.

5015. The method ofclaim 5014, wherein the heating is confrolled to obtain a desired parameter.

5016. The method of claim 5010, wherein the first simulation method is a body-fitted finite difference simulation method.

5017. The method ofclaim 5010, wherein the second simulation method is a space-fitted finite difference simulation method.

5018. The method ofclaim 5010, wherein the second simulation method is a reservoir simulation method.

5019. The method ofclaim 5010, wherein the first simulation method simulates heat transfer by conduction.

5020. The method of clahn 5010, wherehi the first simulation method simulates heat transfer by convection.

5021. The method ofclaim 5010, wherein the first simulation method simulates heat transfer by radiation.

5022. The method ofclaim 5010, wherein the second simulation method shnulates heat ttansfer by conduction.

5023. The method ofclaim 5010, wherein the second simulation method simulates heat ttansfer by convection.

5024. The method of claim 5010, wherein the first simulation method simulates heat fransfer in a near wellbore region.

5025. The method ofclaim 5010, wherein the first shnulation method determines a temperature disttibution in the fonnation.

5026. The method ofclaim 5010, wherein at least one heat input property comprises a property of the fonnation.

5027. The method ofclaim 5010, wherein at least one heat input property comprises a heat fransfer property. '

5028. The method ofclaim 5010, wherein at least one heat input property comprises an initial property of the formation.

5029. The method ofclaim 5010, wherein at least one heat input property comprises a heat capacity.

5030. The method ofclaim 5010, wherein at least one heat input property comprises a thermal conductivity.

5031. The method ofclaim 5010, wherein the heat injection rate data comprises a temperature disfribution within the formation.

5032. The method ofclaim 5010, wherein the heat injection rate data comprises a heat input rate.

5033. The method of clahn 5032, wherein the heat input rate is confrolled to maintain a specified maximum temperature at a point in the foπnation.

5034. The method ofclaim 5010, wherein the heat injection rate data comprises heat flux data.

5035. The method ofclaim 5010, wherein at least one property of the foπnation comprises one or more materials in the formation.

5036. The method ofclaim 5035, wherein one material comprises mineral matter.

5037. The method of claim 5035, wherein one material comprises organic matter.

5038. The method ofclaim 5010, wherein at least one property of the formation comprises one or more phases.

5039. The method of claim 5038, wherein one phase comprises a water phase.

5040. The method of claim 5038, wherein one phase comprises an oil phase.

5041. The method of claim 5040, wherein the oil phase comprises one or more components.

5042. The method ofclaim 5038, wherein one phase comprises a gas phase.

5043. The method of claim 5042, wherein the gas phase comprises one or more components.

5044. The method ofclaim 5010, wherein at least one property of the foπnation comprises a porosity of the formation.

5045. The method ofclaim 5010, wherein at least one property of the formation comprises apermeability of the formation.

5046. The method ofclaim 5045, wherein the permeability depends on the composition of the formation.

5047. The method ofclaim 5010, wherein at least one property of the formation comprises a saturation of the formation.

5048. The method ofclaim 5010, wherein at least one property of the formation comprises a density of the formation.

5049. The method ofclaim 5010, wherein at least one property of the formation comprises a theπnal conductivity of the foπnation.

5050. The method ofclaim 5010, wherein at least one property of the foπnation comprises a volumetric heat capacity of the formation.

5051. The method ofclaim 5010, wherein at least one property of the formation comprises a compressibility of the formation.

5052. The method of claim 5010, wherein at least one property of the foπnation comprises a composition of the foπnation.

5053. The method of clahn 5010, wherein at least one property of the formation comprises a thickness of the formation.

5054. The method of claim 5010, wherein at least one property of the formation comprises a depth of the foπnation.

5055. The method of claim 5010, wherein at least one property of the formation comprises one or more chemical components.

5056. The method of clahn 5055, wherein at least one chemical component comprises a pseudo-component.

5057. The method ofclaim 5010, wherein at least one property of the fonnation comprises one or more kinetic parameters.

5058. The method ofclaim 5010, wherein at least one property of the fonnation comprises one or more chemical reactions.

5059. The method ofclaim 5058, wherein a rate of at least one chemical reaction depends on a pressure of the formation.

5060. The method ofclaim 5058, wherehi a rate of at least one chemical reaction depends on a temperature of the formation.

5061. The method ofclaim 5058, wherein at least one chemical reaction comprises a pre-pyrolysis water generation reaction.

5062. The method ofclaim 5058, wherein at least one chemical reaction comprises a hydrocarbon generating reaction.

5063. The method of clahn 5058, wherein at least one chemical reaction comprises a coking reaction.

5064. The method ofclaim 5058, wherehi at least one chemical reaction comprises a cracking reaction.

5065. The method of claim 5058, wherein at least one chemical reaction comprises a synthesis gas reaction.

5066. The method ofclaim 5010, wherein at least one process characteristic comprises an API gravity of produced fluids.

5067. The method ofclaim 5010, wherein at least one process characteristic comprises an olefin content of produced fluids.

5068. The method ofclaim 5010, wherein at least one process characteristic comprises a carbon number disttibution of produced fluids.

5069. The method ofclaim 5010, wherein at least one process characteristic comprises an ethene to ethane ratio of produced fluids.

5070. The method of clahn 5010, wherein at least one process characteristic comprises an atomic carbon to hydrogen ratio of produced fluids.

5071. The method of clahn 5010, wherein at least one process characteristic comprises a ratio of non- condensable hydrocarbons to condensable hydrocarbons of produced fluids.

5072. The method ofclaim 5010, wherein at least one process characteristic comprises a pressure in the formation.

5073. The method ofclaim 5010, wherem at least one process characteristic comprises a total mass recovery from the formation.

5074. The method ofclaim 5010, wherein at least one process characteristic comprises a production rate of fluid produced from the formation.

5075. The method ofclaim 5010, further comprising: assessing modified heat injection rate data using the first simulation method at a specified time of the second simulation method based on at least one heat input property of the formation at the specified time; assessing at least one process characteristic of the in situ process as a function of time from the modified heat injection rate data and at least one property of the formation at the specified time using the second shnulation method.

5076. A method of using a computer system for modeling an in situ process for freating a relatively low peπneability foπnation containing heavy hydrocarbons, comprising: providing one or more model parameters for the in situ process to the computer system; assessing one or more simulated process characteristics based on one or more model parameters using a simulation method; modifying one or more model parameters such that at least one simulated process characteristic matches or approximates at least one real process characteristic; assessing one or more modified simulated process characteristics based on the modified model parameters; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation.

5077. The method of claim 5076, further comprising using the simulation method with the modified model parameters to determine at least one operating condition of the in situ process to achieve a desfred parameter.

5078. The method ofclaim 5076, wherein the simulation method comprises a body-fitted finite difference shnulation method.

5079. The method ofclaim 5076, wherein the simulation method comprises a space-fitted finite difference simulation method.

5080. The method of claim 5076, wherehi the simulation method comprises a reservofr simulation method.

5081. The method of claim 5076, wherein the real process characteristics comprise process characteristics obtained from laboratory experhnents of the in situ process.

5082. The method of claim 5076, wherein the real process characteristics comprise process characteristics . obtained from field test experiments of the in situ process.

5083. The method ofclaim 5076, further comprising comparing the simulated process characteristics to the real process characteristics as a function of time.

5084. The method of claim 5076, further comprising associating differences between the simulated process characteristics and the real process characteristics with one or more model parameters.

5085. The method of claim 5076, wherein at least one model parameter comprises a chemical component.

5086. The method of claim 5076, wherein at least one model parameter comprises a kinetic parameter.

5087. The method of claim 5086, wherein the kinetic parameter comprises an order of a reaction.

5088. The method ofclaim 5086, wherein the kinetic parameter comprises an activation energy.

5089. The method ofclaim 5086, wherein the kinetic parameter comprises a reaction enthalpy.

5090. The method of claim 5086, wherehi the kinetic parameter comprises a frequency factor.

5091. The method ofclaim 5076, wherein at least one model parameter comprises a chemical reaction.

5092. The method of claim 5091 , wherein at least one chemical reaction comprises a pre-pyrolysis water generation reaction.

5093. The method ofclaim 5091, wherein at least one chemical reaction comprises a hydrocarbon generating reaction.

5094. The method of claim 5091, wherein at least one chemical reaction comprises a coking reaction.

5095. The method ofclaim 5091, wherein at least one chemical reaction comprises a cracking reaction.

5096. The method of clahn 5091, wherein at least one chemical reaction comprises a synthesis gas reaction.

5097. The method ofclaim 5076, wherein one or more model parameters comprise one or more properties.

5098. The method ofclaim 5076, wherein at least one model parameter comprises a relationship for the dependence of a property on a change in conditions in the formation.

5099. The method ofclaim 5076, wherein at least one .model parameter comprises an expression for the dependence of porosity on pressure in the formation.

5100. The method of claim 5076, wherein at least one model parameter comprises an expression for the dependence of permeability on porosity.

5101. The method of claim 5076, wherein at least one model parameter comprises an expression for the dependence of thermal conductivity on composition of the formation.

5102. A method of using a computer system for modeling an in situ process for freating a relatively low permeability fonnation containing heavy hydrocarbons, comprising: assessing at least one operating condition of the in situ process using a simulation method based on one or more model parameter; modifying at least one model parameter such that at least one simulated process characteristic of the in situ process matches or approximates at least one real process characteristic of the in situ process; assessing one or more modified simulated process characteristics based on the modified model parameters; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the fonnation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the foπnation

5103. The method of claim 5102, wherein at least one operating condition is assessed to achieve at least one desfred parameter.

5104. The method of claim 5102, wherein the real process characteristic comprises a process characteristic from a field test of the in situ process.

5105. The method of claim 5102, wherein the simulation method comprises a body-fitted finite difference simulation method.

5106. The method of clahn 5102, wherein the simulation method comprises a space-fitted finite difference simulation method.

5107. The method of claim 5102, wherein the shnulation method comprises a reservoir simulation method.

5108. A method of modeling a process of treating a relatively low permeability fonnation containing heavy hydrocarbons in situ using a computer system, comprising: providing one or more model parameters to the computer system; assessing one or more ffrst process characteristics based on the one or more model parameters using a first simulation method on the computer system; assessing one or more second process characteristics based on one or more model parameters using a second shnulation method on the computer system; modifying one or more model parameters such that at least one first process characteristic matches or approximates at least one second process characteristic; and wherein the in situ process comprises providmg heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation.

5109. The method of claim 5108, further comprising assessing one or more third process characteristics based on the one or more modified model parameters using the second simulation method.

5110. The method of claim 5108, wherehi modifying one or more model parameters such that at least one first process characteristic matches or approximates at least one second process characteristic further comprises: assessing at least one set of first process characteristics based on at least one set of modified model parameters using the first simulation method; and assessing the set of modified model parameters that results in at least one first process characteristic that matches or approximates at least one second process characteristic.

51 11. The method of claim 5108, wherein the first simulation method comprises a body-fitted finite difference simulation method.

51 12. The method of claim 5108, wherein the second simulation method comprises a space-fitted finite difference simulation method.

5113. The method of claim 5108, wherehi at least one first process characteristic comprises a process characteristic at a shaφ interface in the foπnation.

5114. The method of claim 5108, wherein at least one first process characteristic comprises a process characteristic at a combustion front in the foimation.

5115. The method ofclaim 5108, wherein modifying the one or more model parameters comprises changing the order of a chemical reaction.

5116. The method of claim 5108, wherein modifying the one or more model parameters comprises adding one or more chemical reactions.

5117. The method ofclaim 5108, wherein modifying the one or more model parameters comprises changing an activation energy.

5118. The method of claim 5108, wherein modifying the one or more model parameters comprises changing a frequency factor.

5119. A method of using a computer system for modeling an in situ process for treating a relatively low peπneability formation containing heavy hydrocarbons, comprising: providing to the computer system one or more values of at least one operating condition of the in situ process, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; assessing one or more values of at least one process characteristic conesponding to one or more values of at least one operating condition using a simulation method; providing a desfred value of at least one process characteristic for the in situ process to the computer system; and assessing a desfred value of at least one operating condition to achieve the desfred value of at least one process characteristic from the assessed values of at least one process characteristic and the provided values of at least one operating condition.

5120. The method of clahn 5119, further comprising operating the in situ system using the desired value of at least one operating condition.

5121. The method of claim 5119, wherein the process comprises providing heat from one or more heat sources to at least one portion of the fonnation.

5122. The method of claim 5119, wherein the process comprises allowing heat to ttansfer from one or more heat sources to a selected section of the foπnation.

5123. The method of claim 5119, wherein a value of at least one process characteristic comprises the process characteristic as a function of time.

5124. The method of claim 5119, further comprising determining a value of at least one process characteristic based on the desired value of at least one operating condition using the simulation method.

5125. The method of clahn 5119, wherein determining the desfred value of at least one operating condition comprises inteφolating the desired value from the determined values of at least one process characteristic and the provided values of at least one operating condition.

5126. A method of using a computer system for modeling an in situ process for freating a relatively low permeability foimation containing heavy hydrocarbons, comprising: providing a desired value of at least one process characteristic for the in situ process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the foπnation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and assessing a value of at least one operating condition to achieve the desfred value of at least one process characteristic, wherein such assessing comprises using a relationship between at least one process characteristic and at least one operating condition for the in situ process, wherein such relationship is stored on a database accessible by the computer system.

5127. The method ofclaim 5126, further comprising operating the in situ system using the desired value of at least one operating condition.

5128. The method of claim 5126, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation.

5129. The method of claim 5126, wherein the process comprises providing heat to ttansfer from one or more heat sources to a selected section of the formation.

5130. The method ofclaim 5126, wherein the relationship is determined from one or more simulations of the in situ process using a simulation method.

5131. The method of claim 5126, wherein the relationship comprises one or more values of at least one process characteristic and conesponding values of at least one operating condition.

5132. The method ofclaim 5126, wherein the relationship comprises an analytical function.

5133. The method of claim 5126, wherein determining the value of at least one operating condition comprises inteφolating the value of at least one operating condition from the relationship.

5134. The method ofclaim 5126, wherein at least one process characteristic comprises a selected composition of produced fluids.

5135. The method of clahn 5126, wherein at least one operating condition comprises a pressure.

5136. The method ofclaim 5126, wherein at least one operating condition comprises a heat input rate.

5137. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modelmg an in situ process for treating a relatively low penneability formation containing heavy hydrocarbons, the method comprising: providing at least one property of the foπnation to the computer system; providmg at least one operating condition of the process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the foimation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the foimation; and assessing at least one process characteristic of the in situ process using a simulation method on the computer system, and using at least one property of the foπnation and at least one operating condition.

5138. A canier medium comprising program instructions, wherein the program instractions are computer- executable to implement a method comprishig: providing at least one property of the foπnation to the computer system; providing at least one operating condition of the process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; and assessing at least one process characteristic of the in situ process using a simulation method on the computer system, and using at least one property of the fonnation and at least one operating condition.

5139. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons, the method comprising: simulating a heat input rate to the formation from two or more heat sources on the computer system, wherein heat is allowed to fransfer from the heat sources to a selected section of the formation; providing at least one desired parameter of the in situ process to the computer system; and controlling the heat input rate from the heat sources to achieve at least one desfred parameter.

5140. A canier medium comprising program instructions, wherein the program instructions are computer- executable to implement a method comprising: simulating a heat input rate to the formation from two or more heat sources on the computer system, wherein heat is allowed to transfer from the heat sources to a selected section of the formation; providing at least one deshed parameter of the in situ process to the computer system; and controlling the heat input rate from the heat sources to achieve at least one desired parameter.

5141. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons, the method comprising: providing at least one heat input property to the computer system; assessing heat injection rate data for the formation using a first simulation method on the computer system; providing at least one property of the foimation to the computer system; assessing at least one process characteristic of the in situ process from the heat injection rate data and at least one property of the foimation using a second simulation method; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation

5142. A canier medium comprising program instructions, wherein the program instractions are computer- executable to implement a method comprising: providing at least one heat input property to the computer system; assessing heat injection rate data for the formation using a first simulation method on the computer system; providing at least one property of the foimation to the computer system; assessing at least one process characteristic of the in situ process from the heat injection rate data and at least one property of the foπnation using a second shnulation method; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the foπnation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the fonnation

5143. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons, the method comprising: providing one or more model parameters for the in situ process to the computer system; assessing one or more simulated process characteristics based on one or more model parameters using a simulation method; modifying one or more model parameters such that at least one simulated process characteristic matches or approximates at least one real process characteristic; assessing one or more modified simulated process characteristics based on the modified model parameters; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the foπnation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the foπnation.

5144. A canier medium comprising program instractions, wherein the program instructions are computer- executable to implement a method comprising: providing one or more model parameters for the in situ process to the computer system; assessing one or more simulated process characteristics based on one or more model parameters using a simulation method; modifying one or more model parameters such that at least one simulated process characteristic matches or approximates at least one real process characteristic; assessing one or more modified simulated process characteristics based on the modified model parameters; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation.

5145. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for freating a relatively low permeability foimation containing heavy hydrocarbons, the method comprishig: assessing at least one operating condition of the in situ process using a simulation method based on one or more model parameter; modifying at least one model parameter such that at least one simulated process characteristic of the in situ process matches or approximates at least one real process characteristic of the in situ process; assessing one or more modified simulated process characteristics based on the modified model parameters; and wherehi the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation simulated process characteristics based on the modified model parameters.

5146. A canier medium comprising program instructions, wherein the program insfructions are computer- executable to implement a method comprising: assessing at least one operating condition of the in situ process using a simulation method based on one or more model parameter; modifying at least one model parameter such that at least one simulated process characteristic of the in situ process matches or. approximates at least one real process characteristic of the in situ process; assessing one or more modified simulated process characteristics based on the modified model parameters; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation

5147. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement , a method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, the method comprising: providing one or more model parameters to the computer system; assessing one or more ffrst process characteristics based on one or more model parameters using a first simulation method on the computer system; assessing one or more second process characteristics based on one or more model parameters using a second simulation method on the computer system; modifying one or more model parameters such that at least one ffrst process characteristic matches or approximates at least one second process characteristic; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation

5148. A canier medium comprising program instructions, wherein the program insfructions are computer- executable to implement a method comprising: providing one or more model parameters to the computer system; assessing one or more first process characteristics based on one or more model parameters using a first simulation method on the computer system; assessing one or more second process characteristics based on one or more model parameters using a second simulation method on the computer system; modifying one or more model parameters such that at least one first process characteristic matches at least one second process characteristic; and wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation.

5149. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherehi the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for treating a relatively low permeability foπnation containing heavy hydrocarbons, the method comprising: providing to the computer system one or more values of at least one operating condition of the in situ process, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the foimation; assessing one or more values of at least one process characteristic conesponding to one or more values of at least one operating condition using a simulation method; providing a desfred value of at least one process characteristic for the in situ process to the computer system; and assessing a desfred value of at least one operating condition to achieve the desfred value of at least one process characteristic from the assessed values of at least one process characteristic and the provided values of at least one operating condition.

5150. A canier medium comprising program instructions, wherein the program insfructions are computer- executable to implement a method comprising: providing to the computer system one or more values of at least one operating condition of the in situ process, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; assessing one or more values of at least one process characteristic conesponding to one or more values of at least one operating condition using a shnulation method; providing a desired value of at least one process characteristic for the in situ process to the computer system; and assessing a desired value of at least one operating condition to achieve the desfred value of at least one process characteristic from the assessed values of at least one process characteristic and the provided values of at least one operating condition.

5151. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for treating a relatively low permeability foimation containing heavy hydrocarbons, the method comprising: providing a desfred value of at least one process characteristic for the in situ process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation; and assessing a value of at least one operating condition to achieve the desired value of at least one process characteristic, wherein such assessing comprises using a relationship between at least one process characteristic and at least one operating condition for the in situ process, wherein such relationship is stored on a database accessible by the computer system.

5152. A canier medium comprising program instractions, wherein the program instructions are computer- executable to hnplement a method comprising: providing a desired value of at least one process characteristic for the in situ process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and assessing a value of at least one operating condition to achieve the desired value of at least one process characteristic, wherein such assessing comprises using a relationship between at least one process characteristic and at least one operating condition for the in situ process, wherein such relationship is stored on a database accessible by the computer system.

5153. A method of ushig a computer system for operating an in situ process for freathig a relatively low permeability formation containing heavy hydrocarbons, comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; providing at least one operating parameter of the in situ process to the computer system; and using at least one parameter with a simulation method and the computer system to provide assessed infoπnation about the in situ process.

5154. The method of clahn 5153, wherein one or more of the operating parameters comprise a thickness of a treated portion of the foπnation.

5155. The method of claim 5153, wherein one or more of the operating parameters comprise an area of a treated portion of the foπnation.

5156. The method of claim 5153, wherein one or more of the operating parameters comprise a volume of a freated portion of the foπnation.

5157. The method ofclaim 5153, wherein one or more of the operating parameters comprise a property of the formation.

5158. The method of claim 5153, wherein one or more of the operating parameters comprise a heat capacity of the formation.

5159. The method of claim 5153, wherein one or more of the operating parameters comprise a permeability of the formation.

5160. The method ofclaim 5153, wherein one or more of the operating parameters comprise a density of the formation.

5161. The method of clahn 5153, wherein one or more of the operating parameters comprise a thennal conductivity of the foπnation.

5162. The method ofclaim 5153, wherein one or more of the operating parameters comprise a porosity of the formation.

5163. The method ofclaim 5153, wherehi one or more of the operating parameters comprise a pressure.

5164. The method ofclaim 5153, wherein one or more of the operating parameters comprise a temperature.

5165. The method of claim 5153, wherein one or more of the operating parameters comprise a heating rate.

5166. The method of claim 5153, wherein one or more of the operating parameters comprise a process time.

5167. The ethod of claim 5153, wherein one or more of the operating parameters comprises a location of producer wells.

5168. The method of claim 5153, wherein one or more of the operating parameters comprise an orientation of producer wells.

5169. The method ofclaim 5153, wherein one or more of the operating parameters comprise a ratio of producer wells to heater wells.

5170. The method ofclaim 5153, wherein one or more of the operating parameters comprise a spacing between heater wells.

5171. The method ofclaim 5153, wherein one or more of the operating parameters comprise a distance between an overburden and horizontal heater wells.

5172. The method ofclaim 5153, wherein one or more of the operating parameters comprise atype of pattern of heater wells.

5173. The method ofclaim 5153, wherein one or more of the operating parameters comprise an orientation of heater wells.

5174. The method of claim 5153, wherein one or more of the operating parameters comprise a mechanical property.

5175. The method ofclaim 5153, wherein one or more of the operating parameters comprise subsidence of the formation.

5176. The method ofclaim 5153, wherein one or more of the operating parameters comprise fracture progression in the formation.

5177. The method ofclaim 5153, wherein one or more of the operating parameters comprise heave of the formation.

5178. The method of clahn 5153, wherein one or more of the operating parameters comprise compaction of the formation.

5179. The method of claim 5153, wherein one or more of the operating parameters comprise shear deformation of the formation.

5180. The method ofclaim 5153, wherein the assessed infoπnation comprises information relating to properties of the foπnation.

5181. The method ofclaim 5153, wherein the assessed information comprises a relationship between one or more operating parameters and at least one other operating parameter.

5182. The method of claim 5153, wherein the computer system is remote from the in situ process.

5183. The method ofclaim 5153, wherein the computer system is located at or near the in situ process.

5184. The method ofclaim 5153, wherein at least one parameter is provided to the computer system using hardwire communication.

5185. The method ofclaim 5153, wherein at least one parameter is provided to the computer system using internet communication.

5186. The method of claim 5153, wherein at least one parameter is provided to the computer system using wireless communication.

5187. The method ofclaim 5153, wherein the one or more parameters are monitored using sensors in the foπnation.

5188. The method of clahn 5153 , wherein at least one parameter is provided automatically to the computer system.

5189. The method ofclaim 5153, wherein using at least one parameter with a simulation method comprises performing a simulation and obtaining properties of the formation.

5190. A method of using a computer system for operating an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; providing at least one operating parameter of the in situ process to the computer system; using at least one parameter with a simulation method and the computer system to provide assessed information about the in situ process; and using the assessed infonnation to operate the in situ process.

5191. The method of claim 5190, further comprising providing the assessed infonnation to a computer system used for controlling the in situ process.

5192. The method of claim 5190, wherein the computer system is remote from the in situ process.

5193. The method of claim 5190, wherein the computer system is located at or near the in situ process.

5194. The method of claim 5190, wherein using the assessed information to operate the in situ process comprises: modifying at least one operating parameter; and operating the in situ process with at least one modified operating parameter.

5195. A method of using a computer system for operating an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation; providing at least one operating parameter of the in situ process to the computer system; using at least one parameter with a first simulation method and the computer system to provide assessed information about the in situ process; and obtaining information from a second simulation method and the computer system using the assessed infonnation and a desfred parameter.

5196. The method of claim 5195, further comprising using the obtained information to operate the in situ process.

5197. The method of claim 5195, wherein the first simulation method is the same as the second simulation method.

5198. The method of claim 5195, further comprising providing the obtained infoπnation to a computer system used for controlling the in situ process.

5199. The method ofclaim 5195, wherein using the obtained information to operate the in situ process comprises: modifying at least one operating parameter; and operating the in situ process with at least one modified operating parameter.

5200. The method of claim 5195, wherein the obtained information comprises at least one operating parameter for use in the in situ process that achieves the desired parameter.

5201. The method of clahn 5195, wherein the computer system is remote from the in situ process.

5202. The method of claim 5195, wherein the computer system is located at or near the in situ process.

5203. The method of claim 5195, wherein the desired parameter comprises a selected gas to oil ratio.

5204. The method ofclaim 5195, wherein the desired parameter comprises a selected production rate of fluid produced from the formation.

5205. The method ofclaim 5195, wherein the desfred parameter comprises a selected production rate of fluid at a selected time produced from the foπnation.

5206. The method of claim 5195, wherein the desired parameter comprises a selected olefin content of produced fluids.

5207. The method ofclaim 5195, wherein the desfred parameter comprises a selected carbon number disfribution of produced fluids.

5208. The method of claim 5195, wherein the deshed parameter comprises a selected ethene to ethane ratio of produced fluids.

5209. The method of claim 5195, wherein the desfred parameter comprises a desfred atomic carbon to hydrogen ratio of produced fluids.

5210. The method ofclaim 5195, wherein the desfred parameter comprises a selected gas to oil ratio of produced fluids.

5211. The method ofclaim 5195, wherein the desfred parameter comprises a selected pressure in the formation.

5212. The method ofclaim 5195, wherein the desired parameter comprises a selected total mass recovery from the formation.

5213. The method of claim 5195, wherein the desfred parameter comprises a selected production rate of fluid produced from the foimation.

5214. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for operating an in situ process for treating a relatively low peπneability formation containing heavy hydrocarbons, comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the foπnation; providing at least one operating parameter of the in situ process to the computer system; and using at least one parameter with a simulation method and the computer system to provide assessed information about the in situ process.

5215. A canier medium comprising program instructions, wherein the program instructions are computer- executable to implement a method comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the foimation; providing at least one operating parameter of the in situ process to the computer system; and using at least one parameter with a simulation method and the computer system to provide assessed information about the in situ process.

5216. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for operating an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; providing at least one operating parameter of the in situ process to the computer system; using at least one parameter with a simulation method and the computer system to provide assessed information about the in situ process; and using the assessed information to operate the in situ process.

5217. A canier medium comprising program instructions, wherein the program instructions are computer- executable to hnplement a method comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the foimation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; providing at least one operating parameter of the in situ process to the computer system; using at least one parameter with a shnulation method and the computer system to provide assessed information about the in situ process; and using the assessed information to operate the in situ process.

5218. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for operating an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons, comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the fonnation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; providing at least one operating parameter of the in situ process to the computer system; using at least one parameter with a first simulation method and the computer system to provide assessed information about the in situ process; and obtaining information from a second simulation method and the computer system using the assessed information and a desired parameter.

5219. A canier medium comprising program instructions, wherein the program instructions are computer- executable to implement a method comprising: operating the in situ process using one or more operating parameters, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; providing at least one operating parameter of the in situ process to the computer system; using at least one parameter with a first simulation method and the computer system to provide assessed information about the in situ process; and obtaining infonnation from a second simulation method and the computer system using the assessed information and a desired parameter.

5220. A method of modeling one or more stages of a process for freating a relatively low permeability foimation containing heavy hydrocarbons in situ with a simulation method using a computer system, comprising: providing at least one property of the formation to the computer system; providing at least one operating condition for the one or more stages of the in situ process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation; assessing at least one process characteristic of the one or more stages using the shnulation method.

5221. The method ofclaim 5220, wherein the simulation method is a body-fitted finite difference simulation method.

5222. The method ofclaim 5220, wherein the simulation method is a reservoir simulation method.

5223. The method of claim 5220, wherein the simulation method is a space-fitted finite difference simulation method.

5224. The method of claim 5220, wherein the simulation method simulates heating of the fonnation.

5225. The method ofclaim 5220, wherein the simulation method simulates fluid flow in the foπnation.

5226. The method of claim 5220, wherein the simulation method simulates mass ttansfer in the foπnation.

5227. The method of claim 5220, wherein the simulation method simulates heat ttansfer in the formation.

5228. The method of clahn 5220, wherein the simulation method simulates chemical reactions in the one or more stages of the process in the foπnation.

5229. The method ofclaim 5220, wherein the simulation method simulates removal of contaminants from the formation.

5230. The method ofclaim 5220, wherehi the simulation method shnulates recovery of heat from the formation.

5231. The method of claim 5220, wherein the simulation method shnulates injection of fluids into the formation.

5232. The method ofclaim 5220, wherein the one or more stages comprise heating of the foimation.

5233. The method ofclaim 5220, wherein the one or more stages comprise generation of pyrolyzation fluids.

5234. The method ofclaim 5220, wherein the one or more stages comprise remediation of the formation.

5235. The method of clahn 5220, wherehi the one or more stages comprise shut-in of the formation.

5236. The method of claim 5220, wherein at least one operating condition of a remediation stage is the flow rate of ground water into the foπnation.

5237. The method of claim 5220, wherein at least one operating condition of a remediation stage is the flow rate of injected fluids into the fonnation.

5238. The method of claim 5220, wherein at least one process characteristic of a remediation stage is the concenfration of contaminants in the formation.

5239. The method of claim 5220, further comprising: providing to the computer system at least one set of operating conditions for at least one of the stages of the in situ process, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the foπnation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; providing to the computer system at least one desired process characteristic for at least one of the stages of the in situ process; and assessing at least one additional operating condition for at least one of the stages that achieves at least one desired process characteristic for at least one of the stages.

5240. A method of using a computer system for modeling an in situ process for freating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing at least one property of the formation to a computer system; providing at least one operating condition to the computer system; assessing at least one process characteristic of the in situ process, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and assessing at least one deformation characteristic of the foπnation using a simulation method from at least one property, at least one operating condition, and at least one process characteristic.

5241. The method of claim 5240, wherein the in situ process comprises two or more heat sources.

5242. The method of claim 5240, wherein the in situ process provides heat from one or more heat sources to at least one portion of the fonnation.

5243. The method of claim 5240, wherein the simulation method comprises a finite element simulation method.

5244. The method of claim 5240, wherein the formation comprises a freated portion and an untreated portion.

5245. The method of clahn 5240, wherein at least one deformation characteristic comprises subsidence.

5246. The method of claim 5240, wherein at least one deformation characteristic comprises heave.

5247. The method ofclaim 5240, wherein at least one defonnation characteristic comprises compaction.

5248. The method ofclaim 5240, wherein at least one defonnation characteristic comprises shear deformation.

5249. The method of claim 5240, wherein at least one operating condition comprises a pressure.

5250. The method of claim 5240, wherein at least one operating condition comprises a temperature.

5251. The method of claim 5240, wherein at least one operating condition comprises a process time.

5252. The method of claim 5240, wherein at least one operating condition comprises a rate of pressure increase.

5253. The method ofclaim 5240, wherein at least one operating condition comprises a heating rate.

5254. The method of claim 5240, wherein at least one operatmg condition comprises a width of a freated portion of the formation.

5255. The method ofclaim 5240, wherein at least one operating condition comprises a thickness of a treated portion of the formation.

5256. The method ofclaim 5240, wherein at least one operating condition comprises a thickness of an overburden of the formation.

5257. The method ofclaim 5240, wherein at least one process characteristic comprises a pore pressure disfribution in the formation.

5258. The method ofclaim 5240, wherein at least one process characteristic comprises a temperature disttibution in the formation.

5259. The method of claim 5240, wherein at least one process characteristic comprises a heat input rate.

5260. The method ofclaim 5240, wherehi at least one property comprises a physical property of the foπnation.

5261. The method of claim 5240, wherein at least one property comprises richness of the foπnation.

5262. The method of claim 5240, wherein at least one property comprises a heat capacity.

5263. The method of claim 5240, wherein at least one property comprises a thermal conductivity.

5264. The method ofclaim 5240, wherein at least one property comprises a coefficient of thermal expansion.

5265. The method of claim 5240, wherein at least one property comprises a mechanical property.

5266. The method of claim 5240, wherein at least one property comprises an elastic modulus.

5267. The method ofclaim 5240, wherein at least one property comprises a Poisson's ratio.

5268. The method of claim 5240, wherein at least one property comprises cohesion sfress.

5269. The method of claim 5240, wherein at least one property comprises a friction angle.

5270. The method of claim 5240, wherein at least one property comprises a cap eccentricity.

5271. The method of claim 5240, wherein at least one property comprises a cap yield stress.

5272. The method of claim 5240, wherein at least one property comprises a cohesion creep multiplier.

5273. The method of claim 5240, wherein at least one property comprises a thermal expansion coefficient.

5274. A method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing to the computer system at least one set of operating conditions for the in situ process, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; providing to the computer system at least one desfred defonnation characteristic for the in situ process; and assessing at least one additional operating condition of the foπnation that achieves at least one desired deformation characteristic.

5275. The method of clahn 5274, further comprising operating the in situ system using at least one additional operating condition.

5276. The method ofclaim 5274, wherein the in situ process comprises two or more heat sources.

5277. The method ofclaim 5274, wherein the in situ process provides heat from one or more heat sources to at least one portion of the formation.

5278. The method ofclaim 5274, wherein the in situ process allows heat to fransfer from one or more heat sources to a selected section of the fonnation.

5279. The method ofclaim 5274, wherein at least one set of operating conditions comprises at least one set of pressures.

5280. The method ofclaim 5274, wherein at least one set of operating conditions comprises at least one set of temperatures.

5281. The method of claim 5274, wherein at least one set of operating conditions comprises at least one set of heating rates.

5282. The method ofclaim 5274, wherein at least one set of operating conditions comprises at least one set of overburden thicknesses.

5283. The method of claim 5274, wherein at least one set of operating conditions comprises at least one set of thicknesses of a treated portion of the formation.

5284. The method ofclaim 5274, wherein at least one set of operating conditions comprises at least one set of widths of a treated portion of the formation.

5285. The method ofclaim 5274, wherein at least one set of operating conditions comprises at least one set of radii of a freated portion of the foπnation.

5286. The method ofclaim 5274, wherein at least one desfred deformation characteristic comprises a selected subsidence.

5287. The method ofclaim 5274, wherein at least one desfred defonnation characteristic comprises a selected heave.

5288. The method ofclaim 5274, wherein at least one desired deformation characteristic comprises a selected compaction.

5289. The method of clahn 5274, wherein at least one desfred deformation characteristic comprises a selected shear deformation.

5290. A method of using a computer system for modeling an in situ process for treating a relatively low permeability fonnation containing heavy hydrocarbons, comprising: providing one or more values of at least one operating condition; assessing one or more values of at least one defonnation characteristic using a simulation method based on the one or more values of at least one operating condition; providing a desired value of at least one deformation characteristic for the in situ process to the computer system, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and assessing a desired value of at least one operating condition that achieves the desired value of at least one deformation characteristic from the deteπnined values of at least one deformation characteristic and the provided values of at least one operating condition.

5291. The method ofclaim 5290, further comprising operating the in situ process using the desired value of at least one operating condition.

5292. The method ofclaim 5290, wherein the in situ process comprises two or more heat sources.

5293. The method of claim 5290, wherein at least one operating condition comprises a pressure.

5294. The method of claim 5290, wherein at least one operating condition comprises a heat input rate.

5295. The method of claim 5290, wherehi at least one operating condition comprises a temperature.

5296. The method ofclaim 5290, wherein at least one operating condition comprises a heating rate.

5297. The method ofclaim 5290, wherein at least one operating condition comprises an overburden thickness.

5298. The method ofclaim 5290, wherehi at least one operating condition comprises a thickness of a treated portion of the formation.

5299. The method ofclaim 5290, wherein at least one operating condition comprises a width of a treated portion of the foπnation.

5300. The method ofclaim 5290, wherein at least one operating condition comprises a radius of a treated portion of the formation.

5301. The method of claim 5290, wherein at least one deformation characteristic comprises subsidence.

5302. The method ofclaim 5290, wherein at least one deformation characteristic comprises heave.

5303. The method ofclaim 5290, wherein at least one deformation characteristic comprises compaction.

5304. The method ofclaim 5290, wherein at least one defonnation characteristic comprises shear defonnation.

5305. The method ofclaim 5290, wherein a value of at least one foimation characteristic comprises the formation characteristic as a function of time.

5306. The method of clahn 5290, further comprising deteπninhig a value of at least one defonnation characteristic based on the desfred value of at least one operating condition using the simulation method.

5307. The method ofclaim 5290, wherein deteπnining the desired value of at least one operating condition comprises inteφolating the desired value from the detennined values of at least one foimation characteristic and the provided values of at least one operating condition.

5308. A method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing a deshed value of at least one deformation characteristic for the in situ process to the computer system, wherein the in situ process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the in situ process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the foimation; and assessing a value of at least one operating condition to achieve the desired value of at least one deformation characteristic from a database in memory on the computer system comprising a relationship between at least one deformation characteristic and at least one operating condition for the in situ process.

5309. The method ofclaim 5308, further comprising operating the in situ system using the desired value of at least one operating condition.

5310. The method ofclaim 5308, wherein the in situ system comprises two or more heat sources.

5311. The method ofclaim 5308, wherein the relationship is determined from one or more simulations of the in situ process using a simulation method.

5312. The method ofclaim 5308, wherein the relationship comprises one or more values of at least one deformation characteristic and conesponding values of at least one operating condition.

5313. The method of claim 5308, wherein the relationship comprises an analytical function.

5314. The method ofclaim 5308, wherein determining a value of at least one operating condition comprises inteφolating a value of at least one operating condition from the relationship.

5315. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for treating a relatively low permeability foπnation containing heavy hydrocarbons, the method comprising: providing at least one property of the formation to a computer system; providing at least one operating condition to the computer system; determining at least one process characteristic of the in situ process, wherein the process comprises providing heat from one or more heat sources to at least one portion of the foimation, and wherehi the process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and determining at least one deformation characteristic of the formation using a simulation method from at least one property, at least one operating condition, and at least one process characteristic.

5316. A canier medium comprising program instructions, wherein the program instructions are computer- executable to implement a method comprishig: providing at least one property of the formation to a computer system; providing at least one operating condition to the computer system; determining at least one process characteristic of the in situ process, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises allowing the heat to transfer from the one or more heat sources to a selected section of the formation; and determining at least one deformation characteristic of the formation using a simulation method from at least one property, at least one operating condition, and at least one process characteristic.

5317. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, the method comprising: providing to the computer system at least one set of operating conditions for the in situ process, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises aUowing the heat to fransfer from the one or more heat sources to a selected section of the formation; providing to the computer system at least one desired deformation characteristic for the in situ process; and determining at least one additional operating condition of the formation that achieves at least one desired deformation characteristic.

5318. A canier medium comprising program instructions, wherein the program instractions are computer- executable to implement a method comprising: providing to the computer system at least one set of operating conditions for the in situ process, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; providing to the computer system at least one desired deformation characteristic for the in situ process; and determhiing at least one additional operating condition of the foimation that achieves at least one desfred deformation characteristic.

5319. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherein the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for treating a relatively low permeability foimation containing heavy hydrocarbons, the method comprising: providing one or more values of at least one operating condition; deteπnining one or more values of at least one defonnation characteristic using a shnulation method based on the one or more values of at least one operating condition; providing a desfred value of at least one defonnation characteristic for the in situ process to the computer system,' wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises aUowing the heat to transfer from the one or more heat sources to a selected section of the formation; and determining a desired value of at least one operating condition that achieves the desired value of at least one defonnation characteristic from the determined values of at least one defonnation characteristic and the provided values of at least one operating condition.

5320. A canier medium comprising program instructions, wherein the program instructions are computer- executable to implement a method comprising: providing one or more values of at least one operating condition; deteπnining one or more values of at least one defonnation characteristic using a simulation method based on the one or more values of at least one operating condition; providing a desired value of at least one defonnation characteristic for the in situ process to the computer system, wherein the process comprises providing heat from one or more heat sources to at least one portion of the foimation, and wherein the process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and determining a desired value of at least one operating condition that achieves the desired value of at least one defonnation characteristic from the determined values of at least one defonnation characteristic and the provided values of at least one operating condition.

5321. A system, comprising: a CPU; a data memory coupled to the CPU; and a system memory coupled to the CPU, wherehi the system memory is configured to store one or more computer programs executable by the CPU, and wherein the computer programs are executable to implement a method of using a computer system for modeling an in situ process for treating a relatively low permeability formation containing heavy hydrocarbons, the method comprising: providing a desfred value of at least one deformation characteristic for the in situ process to the computer system, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and determining a value of at least one operating condition to achieve the desired value of at least one deformation characteristic from a database in memory on the computer system comprising a relationship between at least one formation characteristic and at least one operating condition for the in situ process.

5322. A canier medium comprising program instractions, wherein the program instructions are computer- executable to implement a method comprising: providing a desfred value of at least one deformation characteristic for the in situ process to the computer system, wherein the process comprises providing heat from one or more heat sources to at least one portion of the formation, and wherein the process comprises allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; and determining a value of at least one operating condition to achieve the desired value of at least one deformation characteristic from a database in memory on the computer system comprising a relationship between at least one formation characteristic and at least one operating condition for the in situ process.

5323. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a first oxidizer configurable to be placed in an opening in the foπnation, wherein the first oxidizer is configurable to oxidize a first fuel during use; a second oxidizer configurable to be placed in the opening, wherein the second oxidizer is configurable to oxidize a second fuel during use; and wherein the system is configurable to allow heat from oxidation of the first fuel or the second fuel to fransfer to the foπnation during use.

5324. The system ofclaim 5323, wherein the system is configured to provide heat to the relatively low permeability formation containing heavy hydrocarbons.

5325. The system ofclaim 5323, wherein the first oxidizer is configured to be placed in an opening in the formation and wherein the ffrst oxidizer is configured to oxidize the first fuel during use.

5326. The system ofclaim 5323, wherein the second oxidizer is configured to be placed in the opening and wherein the second oxidizer is configured to oxidize the second fuel during use.

5327. The system of claim 5323, wherein the system is configured to allow the heat from the oxidation to ttansfer to the formation during use.

5328. The system of claim 5323, wherein the first oxidizer comprises a burner.

5329. The system of claim 5323, wherein the first oxidizer comprises an inline burner.

5330. The system ofclaim 5323, wherein the second oxidizer comprises a burner.

5331. The system ofclaim 5323, wherein the second oxidizer comprises a ring burner.

5332. The system ofclaim 5323, wherein a distance between the first oxidizer and the second oxidizer is less than about 250 meters.

5333. The system ofclaim 5323, further comprising a conduit configurable to be placed in the opening.

5334. The system ofclaim 5323, further comprising a conduit configurable to be placed in the opening, wherein the conduit is configurable to provide an oxidizing fluid to the first oxidizer during use.

5335. The system ofclaim 5323, further comprising a conduit configurable to be placed in the opening, wherein the conduit is configurable to provide the first fuel to the first oxidizer during use.

5336. The system ofclaim 5323, further comprising a conduit configurable to be placed in the opening, wherein the conduit is configurable to provide an oxidizhig fluid to the second oxidizer during use.

5337. The system ofclaim 5323, further comprising a conduit configurable to be placed in the opening, wherein the conduit is configurable to provide the second fuel to the second oxidizer during use.

5338. The system ofclaim 5323, further comprising a thfrd oxidizer configurable to be placed in the opening, wherein the thfrd oxidizer is configurable to oxidize a third fuel during use.

5339. The system ofclaim 5323, further comprising a fuel source, wherein the fuel source is configurable to provide the ffrst fuel to the first oxidizer or the second fuel to the second oxidizer during use.

5340. The system ofclaim 5323, wherein the first fuel is different from the second fuel.

5341. The system ofclaim 5323, wherein the ffrst fuel is different from the second fuel, wherein the second fuel comprises hydrogen.

5342. The system ofclaim 5323, wherein a flow of the first fuel is separately confrolled from a flow of the second fuel.

5343. The system of claim 5323, wherein the first oxidizer is configurable to be placed proximate an upper portion of the opening.

5344. The system ofclaim 5323, wherein the second oxidizer is configurable to be placed proximate a lower portion of the opening.

5345. The system ofclaim 5323, further comprising insulation configurable to be placed proximate the first oxidizer.

5346. The system ofclaim 5323, further comprising insulation configurable to be placed proxhnate the second oxidizer.

5347. The system ofclaim 5323, wherehi products from oxidation of the first fuel or the second fuel are removed from the formation through the opening during use.

5348. The system ofclaim 5323, further comprising an exhaust conduit configurable to be coupled to the opening to allow exhaust fluid to flow from the formation through the exhaust conduit during use.

5349. The system ofclaim 5323, wherein the system is configured to allow the heat from the oxidation of the first fuel or the second fuel to fransfer to the foimation during use.

5350. The system of claim 5323, wherein the system is configured to allow the heat from the oxidation to fransfer to a pyrolysis zone in the formation during use.

5351. The system ofclaim 5323, wherehi the system is configured to allow the heat from the oxidation to fransfer to a pyrolysis zone in the foπnation during use, and wherein the fransfened heat causes pyrolysis of at least some hydrocarbons in the pyrolysis zone during use.

5352. The system ofclaim 5323, wherein at least some of the heat from the oxidation is generated at the ffrst oxidizer.

5353. The system ofclaim 5323, wherein at least some of the heat from the oxidation is generated at the second oxidizer

5354. The system ofclaim 5323, wherein a combination of heat from the first oxidizer and heat from the second oxidizer substantially uniformly heats a portion of the foimation during use.

5355. The system ofclaim 5323, further comprising a first conduit configurable to be placed in the opening of the formation, wherein the first conduit is configurable to provide a first oxidizing fluid to the first oxidizer in the opening during use, and wherein the first conduit is further configurable to provide a second oxidizing fluid to the second oxidizer in the opening during use.

5356. The system ofclaim 5355, further comprising a fuel conduit configurable to be placed in the opening, wherein the fuel conduit is further configurable to provide the ffrst fuel to the first oxidizer during use.

5357. The system ofclaim 5356, wherein the fuel conduit is further configurable to be placed in the first conduit.

5358. The system ofclaim 5356, wherein the first conduit is further configurable to be placed in the fuel conduit.

5359. The system ofclaim 5355, further comprising a fuel conduit configurable to be placed in the openhig, wherein the fuel conduit is further configurable to provide the second fuel to the second oxidizer during use.

5360. The system ofclaim 5355, wherein the first conduit is further configurable to provide the first fuel to the first oxidizer during use.

5361. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing a ffrst oxidizing fluid to a first oxidizer placed in an opening in the foπnation; providing a first fuel to the first oxidizer; oxidizing at least some of the ffrst fuel in the first oxidizer; providing a second oxidizing fluid to a second oxidizer placed in the opening in the formation; providing a second fuel to the second oxidizer; oxidizing at least some of the second fuel in the second oxidizer; and allowing heat from oxidation of the first fuel and the second fuel to fransfer to a portion of the formation.

5362. The method ofclaim 5361, wherein the ffrst oxidizing fluid is provided to the first oxidizer through a conduit placed in the openhig.

5363. The method ofclaim 5361, wherein the second oxidizing fluid is provided to the second oxidizer through a conduit placed in the opening.

5364. The method of claim 5361, wherein the ffrst fuel is provided to the first oxidizer through a conduit placed in the opening.

5365. The method of clahn 5361, wherein the first fuel is provided to the second oxidizer through a conduit placed in the opening.

5366. The method ofclaim 5361, wherein the first oxidizing fluid and the first fuel are provided to the first oxidizer through a conduit placed in the opening.

5367. The method ofclaim 5361, further comprising using exhaust fluid from the first oxidizer as a portion of the second fuel used in the second oxidizer.

5368. The method ofclaim 5361, further comprising allowing the heat to fransfer substantially by conduction from the portion of the formation to a pyrolysis zone of the formation.

5369. The method ofclaim 5361, further comprising initiating oxidation of the second fuel in the second oxidizer with an ignition source.

5370. The method of claim 5361, further comprising removing exhaust fluids through the opening.

5371. The method of claim 5361, further comprismg removing exhaust fluids through the opening, wherein the exhaust fluids comprise heat and allowing at least some heat in the exhaust fluids to ttansfer from the exhaust fluids to the ffrst oxidizing fluid prior to oxidation in the first oxidizer.

5372. The method ofclaim 5361, further comprising removing exhaust fluids comprising heat through the opening, allowing at least some heat in the exhaust fluids to transfer from the exhaust fluids to the ffrst oxidizing fluid prior to oxidation, and increasing a thermal efficiency of heathig the relatively low permeability formation containing heavy hydrocarbons.

5373. The method ofclaim 5361, further comprising removing exhaust fluids through an exhaust conduit coupled to the opening.

5374. The method of claim 5361, further comprising removing exhaust fluids tiirough an exhaust conduit coupled to the opening and providing at least a portion of the exhaust fluids to a fourth oxidizer to be used as a fourth fuel in a fourth oxidizer, wherein the fourth oxidizer is located in a separate opening in the formation.

5375. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: an opening placed in the fonnation, wherein the opening comprises a first elongated portion, a second elongated portion, and a third elongated portion, wherein the second elongated portion diverges from the first elongated portion in a first direction, wherein the thfrd elongated portion diverges from the first elongated portion in a second dfrection, and wherein the first direction is substantially different than the second direction; a ffrst heater configurable to be placed in the second elongated portion, wherein the first heater is configurable to heat at least a portion of the formation during use; a second heater configurable to be placed in the third elongated portion, wherein the second heater is configurable to heat to at least a portion of the formation during use; and wherein the system is configurable to allow heat to ttansfer to the formation during use.

5376. The system ofclaim 5375, wherein the first heater and the second heater are configurable to heat to at least a portion of the foimation during use.

5377. The system ofclaim 5375, wherein the second and the third elongated portions are oriented substantially horizontally within the formation.

5378. The system ofclaim 5375, wherein the first dfrection is about 180° opposite the second dfrection.

5379. The system ofclaim 5375, wherein the first elongated portion is placed substantially within an overburden of the formation.

5380. The system of claim 5375, wherein the fransfened heat substantially uniformly heats a portion of the fonnation during use.

5381. The system of claim 5375, wherein the first heater or the second heater comprises a downhole combustor.

5382. The system of claim 5375, wherein the first heater or the second heater comprises an insulated conductor heater.

5383. The system ofclaim 5375, wherein the first heater or the second heater comprises a conductor-in-conduit heater.

5384. The system ofclaim 5375, wherein the first heater or the second heater comprises an elongated member heater.

5385. The system ofclaim 5375, wherein the first heater or the second heater comprises a natural disfributed combustor heater.

5386. The system ofclaim 5375, wherein the first heater or the second heater comprises a flameless disfributed combustor heater.

5387. The system of claim 5375, wherein the first heater comprises a first oxidizer and the second heater comprises a second oxidizer.

5388. The system ofclaim 5387, wherein the second elongated portion has a length of less than about 175 meters.

5389. The system ofclaim 5387, wherein the third elongated portion has a length of less than about 175 meters.

5390. The system of clahn 5387, further comprising a fuel conduit configurable to be placed in the opening, wherein the fuel conduit is further configurable to provide fuel to the first oxidizer during use.

5391. The system of claim 5387, further comprising a fuel conduit configurable to be placed in the opening, wherein the fuel conduit is further configurable to provide fuel to the second oxidizer during use.

5392. The system ofclaim 5387, further comprising a fuel source, wherein the fuel source is configurable to provide fuel to the first oxidizer or the second oxidizer during use.

5393. The system of claim 5387, further comprising a thfrd oxidizer placed within the first elongated portion of the opening.

5394. The system ofclaim 5393, further comprising a fuel conduit configurable to be placed in the opening, wherein the fuel conduit is further configurable to provide fuel to the third oxidizer during use.

5395. The system ofclaim 5393, further comprising a first fuel source configurable to provide a first fuel to the first fuel conduit, a second fuel source configurable to provide a second fuel to a second fuel conduit, and a third fuel source configurable to provide a thfrd fuel to a third fuel conduit.

5396. The system ofclaim 5395, wherein the first fuel has a composition substantiaUy different from the second fuel or the third fuel.

5397. The system ofclaim 5375, further comprising insulation configurable to be placed proximate the first heater.

5398. The system ofclaim 5375, further comprising insulation configurable to be placed proximate the second heater.

5399. The system of clahn 5375, wherein a fuel is oxidized in the first heater or the second heater to generate heat and wherein products from oxidation are removed from the foimation through the opening during use.

5400. The system ofclaim 5375, wherein a fuel is oxidized in the ffrst heater and the second heater and wherein products from oxidation are removed from the formation through the opening during use.

5401. The system ofclaim 5375, further comprising an exhaust conduit configurable to be coupled to the opening to allow exhaust fluid to flow from the formation through the exhaust conduit during use.

5402. The system ofclaim 5387, wherein the system is configured to allow the heat from oxidation of fuel to fransfer to the foimation during use.

5403. The system of claim 5375, wherein the system is configured to allow heat to fransfer to a pyrolysis zone in the formation during use.

5404. The system ofclaim 5375, wherein the system is configured to allow heat to fransfer to a pyrolysis zone in the formation during use, and wherein the transfened heat causes pyrolysis of at least some hydrocarbons within the pyrolysis zone during use.

5405. The system of claim 5375, wherehi a combination of the heat generated from the first heater and the heat generated from the second heater substantially uniformly heats a portion of the foimation during use.

5406. The system ofclaim 5375, further comprising a thfrd heater placed in the second elongated portion.

5407. The system ofclaim 5406, wherein the third heater comprises a downhole combustor.

5408. The system of claim 5406, further comprising a fourth heater placed in the third elongated portion.

5409. The system ofclaim 5408, wherein the fourth heater comprises a downhole combustor.

5410. The system ofclaim 5375, wherein the first heater is configured to be placed in the second elongated portion, wherein the first heater is configured to provide heat to at least a portion of the formation during use, wherein the second heater is configured to be placed in the thfrd elongated portion, wherehi the second heater is configured to provide heat to at least a portion of the formation during use, and wherein the system is configured to allow heat to fransfer to the formation during use.

5411. The system ofclaim 5375, wherein the second and the thfrd elongated portions are located in a substantially similar plane.

5412. The system ofclaim 5411, wherein the opening comprises a fourth elongated portion and a fifth elongated portion, wherein the fourth elongated portion diverges from the first elongated portion in a thhd dfrection, wherein the fifth elongated portion diverges from the first elongated portion in a fourth direction, and wherein the third direction is substantially different than the fourth direction.

5413. The system ofclaim 5412, wherein the fourth and fifth elongated portions are located in a plane substantially different than the second and the thfrd elongated portions.

5414. The system ofclaim 5412, wherein a third heater is configurable to be placed in the fourth elongated portion, and wherein a fourth heater is configurable to be placed in the fifth elongated portion.

5415. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from two or more heaters placed in an opening in the formation, wherehi the opening comprises a ffrst elongated portion, a second elongated portion, and a third elongated portion, wherein the second elongated portion diverges from the first elongated portion in a first direction, wherein the third elongated portion diverges from the first elongated portion in a second direction, and wherein the first dfrection is substantially different than the second direction; allowing heat from the two or more heaters to transfer to a portion of the formation; and wherein the two or more heaters comprise a first heater placed in the second elongated portion and a second heater placed in the thfrd elongated portion.

5416. The method of claim 5415, wherein the second and the third elongated portions are oriented substantially horizontally within the formation.

5417. The method of clahn 5415, wherein the first elongated portion is located substantially within an overburden of the formation.

5418. The method ofclaim 5415, further comprising substantially uniformly heating a portion of the formation.

5419. The method of claim 5415, wherein the first heater or the second heater comprises a downhole combustor.

5420. The method ofclaim 5415, wherein the first heater or the second heater comprises an insulated conductor heater.

5421. The method of claim 5415, wherein the ffrst heater or the second heater comprises a conductor-in-conduit heater.

5422. The method ofclaim 5415, wherein the ffrst heater or the second heater comprises an elongated member heater.

5423. The method of claim 5415, wherein the ffrst heater or the second heater comprises a natural disfributed combustor heater.

5424. The method ofclaim 5415, wherein the first heater or the second heater comprises a flameless distributed combustor heater.

5425. The method ofclaim 5415, wherein the first heater comprises a first oxidizer and the second heater comprises a second oxidizer.

5426. The method ofclaim 5415, wherein the first heater comprises a ffrst oxidizer and the second heater comprises a second oxidizer and further comprising providing fuel to the ffrst oxidizer through a fuel conduit placed in the opening.

5427. The method ofclaim 5415, wherein the ffrst heater comprises a first oxidizer and the second heater comprises a second oxidizer and further comprising providing fuel to the second oxidizer through a fuel conduit placed in the opening.

5428. The method ofclaim 5415, wherein the two or more heaters comprise oxidizers and further comprising providing fuel to the oxidizers from a fuel source.

5429. The method of claim 5425, further comprising providing heat to a portion of the formation using a third oxidizer placed within the ffrst elongated portion of the opening.

5430. The method ofclaim 5415, wherein the ffrst heater comprises a first oxidizer and the second heater comprises a second oxidizer further comprising: providing heat to a portion of the formation using a third oxidizer placed within the ffrst elongated portion of the opening; and providing fuel to the third oxidizer through a fuel conduit placed in the opening.

5431. The method of claim 5415, wherein the two or more heaters comprise oxidizers, and further comprising providing heat by oxidizing a fuel within the oxidizers and removing products of oxidation of fuel through the opening.

5432. The method ofclaim 5415, wherein the two or more heaters comprise oxidizers, and further comprising removing products from oxidation of fuel through an exhaust conduit coupled to the opening.

5433. The method ofclaim 5415, further comprising allowing the heat to ttansfer from the portion to a pyrolysis zone in the formation.

5434. The method of claim 5415, further comprising allowing the heat to ttansfer from the portion to a pyrolysis zone in the formation and pyrolyzing at least some hydrocarbons within the pyrolysis zone with the fransfened heat.

5435. The method ofclaim 5415, further comprising allowing the heat to ttansfer to from the portion to a pyrolysis zone in the formation, pyrolyzing at least some hydrocarbons within the pyrolysis zone with the transfened heat, and producing a portion of the pyrolyzed hydrocarbons through a conduit placed in the first elongated portion.

5436. The method ofclaim 5415, further comprising providing heat to a portion of the formation using a thfrd heater placed in the second elongated portion.

5437. The method of claim 5436, wherein the third heater comprises a downhole combustor.

5438. The method of claim 5436, further comprising providing heat to a portion of the formation using a fourth heater placed in the thfrd elongated portion.

5439. The method ofclaim 5438, wherein the fourth heater comprises a downhole combustor.

5440. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: an oxidizer configurable to be placed in an opening in the formation, wherein the oxidizer is configurable to oxidize fuel to generate heat during use; a first conduit configurable to be placed in the opening of the foπnation, wherein the first conduit is configurable to provide oxidizing fluid to the oxidizer in the opening during use; a heater configurable to be placed in the opening and configurable to provide additional heat; and wherein the system is configurable to allow the generated heat and the additional heat to ttansfer to the foπnation during use.

5441. The system of claim 5440, wherein the heater comprises an insulated conductor.

5442. The system of claim 5440, wherein the heater comprises a conductor-in-conduit heater.

5443. The system ofclaim 5440, wherein the heater comprises an elongated member heater.

5444. The system ofclaim 5440, wherein the heater comprises a flameless disfributed combustor.

5445. The system ofclaim 5440, wherein the oxidizer is configurable to be placed proximate an upper portion of the opening.

5446. The system ofclaim 5440, further comprising insulation configurable to be placed proximate the oxidizer.

5447. The system of claim 5440, wherein the heater is configurable to be coupled" to the first conduit.

5448. The system ofclaim 5440, wherein products from the oxidation of the fuel are removed from the formation through the opening during use.

5449. The system of claim 5440, further comprising an exhaust conduit configurable to be coupled to the opening to allow exhaust fluid to flow from the formation through the exhaust conduit during use.

5450. The system ofclaim 5440, wherein the system is configured to allow the generated heat and the additional heat to fransfer to the foimation during use.

5451. The system of claim 5440, wherein the system is configured to allow the generated heat and the additional heat to transfer to a pyrolysis zone in the formation during use.

5452. The system of claim 5440, wherein the system is configured to allow the generated heat and the additional heat to ttansfer to a pyrolysis zone in the formation during use, and wherein the fransfened heat pyrolyzes of at least some hydrocarbons within the pyrolysis zone during use.

5453. The system ofclaim 5440, wherehi a combination of the generate heat and the additional heat substantially uniformly heats a portion of the formation during use.

5454. The system of claim 5440, wherein the oxidizer is configured to be placed in the opening in the formation and wherein the oxidizer is configured to oxidize at least some fuel during use.

5455. The system ofclaim 5440, wherein the first conduit is configured to be placed in the opening of the formation and wherein the ffrst conduit is configured to provide oxidizing fluid to the oxidizer in the opening during use.

5456. The system of claim 5440, wherein the heater is configured to be placed in the opening and wherein the heater is configurable to provide heat to a portion of the foπnation during use

5457. The system ofclaim 5440, wherein the system is configured to allow the heat from the oxidation of at least some fuel and from the heater to fransfer to the formation during use.

5458. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: allowing heat to fransfer from a heater placed in an opening to a portion of the formation. providing oxidizing fluid to an oxidizer placed in the opening in the formation; providing fuel to the oxidizer; oxidizing at least some fuel in the oxidizer; and allowing additional heat from oxidation of at least some fuel to fransfer to the portion of the foimation.

5459. The method ofclaim 5458, wherein the heater comprises an insulated conductor.

5460. The method of claim 5458, wherein the heater comprises a conductor-in-conduit heater.

5461. The method ofclaim 5458, wherein the heater comprises an elongated member heater.

5462. The method ofclaim 5458, wherein the heater comprises a flameless disfributed combustor.

5463. The method of claim 5458, wherein the oxidizer is placed proximate an upper portion of the opening.

5464. The method ofclaim 5458, further comprising allowing the additional heat to transfer from the portion to a pyrolysis zone in the formation.

5465. The method of clahn 5458, further comprising allowing the additional heat to fransfer from the portion to a pyrolysis zone in the foπnation and pyrolyzing at least some hydrocarbons within the pyrolysis zone.

5466. The method ofclaim 5458, further comprising substantially uniformly heating the portion of the formation.

5467. The method ofclaim 5458, further comprising removing exhaust fluids through the opening.

5468. The method ofclaim 5458, further comprising removing exhaust fluids through an exhaust annulus in the formation.

5469. The method ofclaim 5458, further comprising removing exhaust fluids through an exhaust conduit coupled to the opening.

5470. A system configurable to provide heat to a relatively low peπneability foπnation containing heavy hydrocarbons, comprising: a heater conflgurable to be placed in an opening in the formation, wherein the heater is configurable to heat a portion of the formation to a temperature sufficient to sustain oxidation of hydrocarbons during use; an oxidizing fluid source configurable to provide an oxidizing fluid to a reaction zone of the formation to oxidize at least some hydrocarbons in the reaction zone during use such that heat is generated in the reaction zone, and wherein at least some of the reaction zone has been previously heated by the heater; a ffrst conduit configurable to be placed in the opening, wherein the first conduit is configurable to provide the oxidizing fluid from the oxidizing fluid source to the reaction zone in the formation during use, wherein the flow of oxidizing fluid can be controlled along at least a segment of the first conduit; and wherein the system is configurable to allow the generated heat to transfer from the reaction zone to the formation during use.

5471. The system of claim 5470, wherein the system is configurable to provide hydrogen to the reaction zone during use.

5472. The system ofclaim 5470, wherein the oxidizing fluid is transported through the reaction zone substantiaUy by diffusion.

5473. The system of claim 5470, wherein the system is configurable to allow the generated heat to ttansfer from the reaction zone to a pyrolysis zone in the foπnation during use.

5474. The system of claim 5470, wherein the system is conflgurable to allow the generated heat to transfer substantially by conduction from the reaction zone to the formation during use.

5475. The system ofclaim 5470, wherein a temperature within the reaction zone can be controlled along at least a segment of the first conduit during use.

5476. The system of claim 5470, wherein a heating rate in at least a section of the formation proximate at least a segment of the first conduit be confrolled.

5477. The system of claim 5470, wherein the oxidizing fluid is configurable to be transported through the reaction zone substantially by diffusion, and wherein a rate of diffusion of the oxidizing fluid can controlled by a temperature within the reaction zone.

5478. The system ofclaim 5470, wherein the first conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening during use.

5479. The system of claim 5470, wherehi the ffrst conduit comprises critical flow orifices, and wherein the critical flow orifices are positioned on the first conduit such that a flow rate of the oxidizing fluid is confrolled at a selected rate during use.

5480. The system ofclaim 5470, further comprising a second conduit configurable to remove an oxidation product during use.

5481. The system of claim 5480, wherein the second conduit is further configurable to allow heat within the oxidation product to ttansfer to the oxidizing fluid in the first conduit during use.

5482. The system ofclaim 5480, wherein a pressure of the oxidizing fluid in the first conduit and a pressure of the oxidation product in the second conduit are controlled during use such that a concentration of the oxidizing fluid along the length of the first conduit is substantiaUy uniform.

5483. The system ofclaim 5480, wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone during use.

5484. The system ofclaim 5470, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the foimation beyond the reaction zone during use.

5485. The system ofclaim 5470, wherein the portion of the formation extends radially from the opening a distance of less than approxhnately 3 m.

5486. The system ofclaim 5470, wherein the reaction zone extends radially from the opening a distance of less than approximately 3 m.

5487. The system ofclaim 5470, wherehi the system is configurable to pyrolyze at least some hydrocarbons in a pyrolysis zone of the formation.

5488. The system ofclaim 5470, wherein the heater is configured to be placed in an opening in the formation and wherein the heater is configured to provide the heat to at least the portion of the formation during use.

5489. The system ofclaim 5470, wherein a first conduit is configured to be placed in the opening and wherein the first conduit is configured to provide the oxidizing fluid from the oxidizing fluid source to the reaction zone in the formation during use.

5490. The system ofclaim 5470, wherein the flow of oxidizing fluid is confrolled along at least a segment of the length of the ffrst conduit and wherein the system is configured to allow the additional heat to fransfer from the reaction zone to the formation during use.

5491. An in situ method for providing heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons with an oxidizing fluid within the portion of the foimation; providing the oxidizing fluid to a reaction zone in the foπnation; confrolling a flow of the oxidizing fluid along at least a length of the reaction zone; generating heat within the reaction zone; and allowing the generated heat to transfer to the formation.

5492. The method ofclaim 5491, further comprising allowing the oxidizing fluid to react with at least some of the hydrocarbons in the reaction zone to generate the heat in the reaction zone.

5493. The method ofclaim 5491, wherein at least a section of the reaction zone is proximate an opening in the formation.

5494. The method ofclaim 5491, further comprising fransporting the oxidizing fluid through the reaction zone substantially by diffusion.

5495. The method of claim 5491 , further comprising transporting the oxidizing fluid through the reaction zone substantially by diffusion, and confrolling a rate of diffusions of the oxidizing fluid by controlling a temperature within the reaction zone.

5496. The method ofclaim 5491, wherein the generated heat fransfers from the reaction zone to a pyrolysis zone in the formation.

5497. The method of claim 5491 , wherein the generated heat transfers from the reaction zone to the foimation substantially by conduction.

5498. The method ofclaim 5491, further comprismg controlling a temperature along at least a length of the reaction zone.

5499. The method ofclaim 5491, further comprising controlling a flow of the oxidizing fluid along at least a length of the reaction zone, and controlling a temperature along at least a length of the reaction zone.

5500. The method ofclaim 5491, further comprising controlling a heating rate along at least a length of the reaction zone.

5501. The method of claim 5491, wherein the oxidizing fluid is provided through a conduit placed within an opening in the formation, wherein the conduit comprises orifices.

5502. The method of claim 5491, further comprising confrolling a rate of oxidation by providing the oxidizing fluid to the reaction zone from a conduit having critical flow orifices.

5503. The method ofclaim 5491, wherein the oxidizing fluid is provided to the reaction zone through a conduit placed within the foimation, and further comprising positioning critical flow orifices on the conduit such that the flow rate of the oxidizhig fluid to at least a length of the reaction zone is controlled at a selected flow rate.

5504. The method ofclaim 5491, wherein the oxidizing fluid is provided to the reaction zone from a conduit placed within an opening in the foimation, and further comprising sizing critical flow orifices on the conduit such that the flow rate of the oxidizing fluid to at least a length of the reaction zone is controlled at a selected flow rate.

5505. The method of claim 5491 , further comprising increasing a volume of the reaction zone, and increasing the flow of the oxidizing fluid to the reaction zone such that a rate of oxidation within the reaction zone is substantially constant over time.

5506. The method ofclaim 5491, further comprismg maintaining a substantially constant rate of oxidation within the reaction zone over time.

5507. The method ofclaim 5491, wherein a conduit is placed in an opening in the formation, and further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

5508. The method ofclaim 5491, further comprising removing an oxidation product from the formation through a conduit placed in an opening in the formation.

5509. The method ofclaim 5491, further comprising removing an oxidation product from the formation through a conduit placed in an opening in the formation and substantially inhibiting the oxidation product from flowing into a sunounding portion of the foimation.

5510. The method of claim 5491 , ftirther comprising inhibiting the oxidizing fluid from flowing into a sunounding portion of the formation.

5511. The method of claim 5491 , further comprising removing at least some water from the formation prior to heating the portion.

5512. The method of claim 5491, further comprising providing additional heat to the formation from an elecfric heater placed in the opening.

5513. The method of claim 5491 , further comprising providing additional heat to the formation from an electric heater placed in an opening in the formation such that the oxidizing fluid continuously oxidizes at least a portion of the hydrocarbons in the reaction zone.

5514. The method of claim 5491 , further comprising providing additional heat to the formation from an elecfric heater placed in the opening to maintain a constant heat rate in the formation.

5515. The method of claim 5514, further comprising providing elecfricity to the elecfric heater using a wind powered device.

5516. The method of claim 5514, further comprising providing electticity to the elecfric heater using a solar powered device.

5517. The method of claim 5491 , further comprising maintaining a temperature within the portion above about the temperature sufficient to support the reaction of hydrocarbons with the oxidizing fluid.

5518. The method ofclaim 5491, further comprising providing additional heat to the formation from an electric heater placed in the opening and controlling the additional heat such that a temperature of the portion is greater than about the temperature sufficient to support the reaction of hydrocarbons with the oxidizing fluid.

5519. The method of claim 5491 , further comprising removing oxidation products from the formation, and generating electticity using oxidation products removed from the formation.

5520. The method ofclaim 5491, further comprising removing oxidation products from the formation, and using at least some of the removed oxidation products in an afr compressor.

5521. The method ofclaim 5491, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone over time.

5522. The method ofclaim 5491, further comprising assessing a temperature in or proximate an opening in the foπnation, wherein the flow of oxidizing fluid along at least a section of the reaction zone is confrolled as a function of the assessed temperature.

5523. The method ofclaim 5491, further comprising assessing a temperature in or proximate an opening in the formation, and increasing the flow of oxidizing fluid as the assessed temperature decreases.

5524. The method ofclaim 5491, further comprising controlling the flow of oxidizing fluid to maintain a temperature in or proximate an opening in the formation at a temperature less than a pre-selected temperature.

5525. A system configurable to provide heat to a relatively low permeability formation containing heavy hydrocarbons, comprising: a heater configurable to be placed in an opening in the formation, wherein the heater is configurable to provide heat to at least a portion of the formation during use; an oxidizing fluid source conflgurable to provide an oxidizing fluid to a reaction zone of the foimation to generate heat in the reaction zone during use, wherein at least a portion of the reaction zone has been previously heated by the heater during use; a conduit configurable to be placed in the opening, wherein the conduit is configurable to provide the oxidizing fluid from the oxidizing fluid source to the reaction zone in the formation during use; wherein the system is configurable to provide molecular hydrogen to the reaction zone during use; and wherein the system is configurable to allow the generated heat to transfer from the reaction zone to the formation during use.

5526. The system ofclaim 5525, wherein the system is configurable to allow the oxidizing fluid to be transported through the reaction zone substantially by diffusion during use.

5527. The system of claim 5525, wherein the system is configurable to allow the generated heat to ttansfer from the reaction zone to a pyrolysis zone in the foimation during use.

5528. The system ofclaim 5525, wherein the system is configurable to allow the generated heat to fransfer substantially by conduction from the reaction zone to the formation during use.

5529. The system ofclaim 5525, wherein the flow of oxidizing fluid can be controlled along at least a segment of the conduit such that a temperature can be confrolled along at least a segment of the conduit during use.

5530. The system ofclaim 5525, wherein a flow of oxidizing fluid can be confrolled along at least a segment of the conduit such that a heating rate in at least a section of the foπnation can be controlled.

5531. The system ofclaim 5525, wherein the oxidizhig fluid is configurable to move through the reaction zone substantiaUy by diffusion during use, wherein a rate of diffusion can confrolled by a temperature of the reaction zone.

5532. The system of claim 5525, wherein the conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening during use.

5533. The system ofclaim 5525, wherein the conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is controlled during use.

5534. The system of claim 5525, wherein the conduit comprises a ffrst conduit and a second conduit, wherein the second conduit is configurable to remove an oxidation product during use.

5535. The system ofclaim 5525, wherein the oxidizing fluid is substantially inhibited from flowing from the reaction zone into a sunounding portion of the formation.

5536. The system ofclaim 5525, wherein at least the portion of the foimation extends radially from the opening a distance of less than approximately 3 m.

5537. The system ofclaim 5525, wherein the reaction zone extends radially from the opening a distance of less than approximately 3 m.

5538. The system of clahn 5525, wherein the system is conflgurable to allow transfened heat to pyrolyze at least some hydrocarbons in a pyrolysis zone of the foimation.

5539. The system ofclaim 5525, wherein the heater is configured to be placed in an opening in the foimation and wherein the heater is configured to provide heat to at least a portion of the foπnation during use.

5540. The system ofclaim 5525, wherein the conduit is configured to be placed in the openhig to provide at least some of the oxidizing fluid from the oxidizing fluid source to the reaction zone in the foimation during use, and wherein the flow of at least some of the oxidizing fluid can be controlled along at least a segment of the ffrst conduit.

5541. The system ofclaim 5525, wherein the system is configured to allow heat to fransfer from the reaction zone to the formation during use.

5542. The system ofclaim 5525, wherein the heater is configured to be placed in an opening in the formation and wherein the heater is configured to provide heat to at least a portion of the formation during use.

5543. The system of claim 5525, wherein the conduit is configured to be placed in the opening and wherein the conduit is configured to provide the oxidizing fluid from the oxidizing fluid source to the reaction zone in the formation during use.

5544. The system of claim 5525, wherein the flow of oxidizing fluid can be controlled along at least a segment of the conduit.

5545. The system ofclaim 5525, wherein the system is configured to allow heat to transfer from the reaction zone to the fonnation during use.

5546. The system ofclaim 5525, wherein at least some of the provided hydrogen is produced in the pyrolysis zone during use.

5547. The system ofclaim 5525, wherein at least some of the provided hydrogen is produced in the reaction zone during use.

5548. The system of clahn 5525, wherein at least some of the provided hydrogen is produced in at least the heated portion of the formation during use.

5549. The system ofclaim 5525, wherein the system is configurable to provide hydrogen to the reaction zone during use such that production of carbon dioxide in the reaction zone is inhibited.

5550. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the formation to a temperature sufficient to support reaction of hydrocarbons within the portion of the fonnation with an oxidizing fluid; providing the oxidizing fluid to a reaction zone in the fonnation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons in the reaction zone to generate heat in the reaction zone; providing molecular hydrogen to the reaction zone; and transfening the generated heat from the reaction zone to a pyrolysis zone in the formation.

5551. The method ofclaim 5550, further comprising producing the molecular hydrogen in the pyrolysis zone.

5552. The method ofclaim 5550, further comprising producing the molecular hydrogen in the reaction zone.

5553. The method ofclaim 5550, .further comprising producing the molecular hydrogen in at least the heated portion of the formation.

5554. The method of claim 5550, further comprising inhibiting production of carbon dioxide in the reaction zone.

5555. The method ofclaim 5550, further comprising allowing the oxidizing fluid to fransfer through the reaction zone substantially by diffusion.

5556. The method of claim 5550, further comprising allowing the oxidizing fluid to fransfer through the reaction zone by diffusion, wherein a rate of diffusion is confrolled by a temperature of the reaction zone.

5557. The method ofclaim 5550, wherein at least some of the generated heat transfers to the pyrolysis zone substantially by conduction.

5558. The method ofclaim 5550, further comprising confrolling a flow of the oxidizing fluid along at least a segment reaction zone such that a temperature is controlled along at least a segment of the reaction zone.

5559. The method ofclaim 5550, further comprising controlling a flow of the oxidizing fluid along at least a segment of the reaction zone such that a heating rate is controlled along at least a segment of the reaction zone.

5560. The method of claim 5550, further comprising allowing at least some oxidizing fluid to flow into the formation through orifices in a conduit placed in an opening in the formation.

5561. The method ofclaim 5550, further comprising controlling a flow of the oxidizing fluid into the formation using critical flow orifices on a conduit placed in the opening such that a rate of oxidation is controlled.

5562. The method ofclaim 5550, further comprising controlling a flow of the oxidizing fluid into the formation with a spacing of critical flow orifices on a conduit placed in an opening in the formation.

5563. The method of clahn 5550, further comprising controlling a flow of the oxidizing fluid with a diameter of critical flow orifices in a conduit placed in an opening in the formation.

5564. The method of claim 5550, further comprising increasing a volume of the reaction zone, and increasing the flow of the oxidizing fluid to the reaction zone such that a rate of oxidation within the reaction zone is substantially constant over time

5565. The method of claim 5550, wherein a conduit is placed in an openhig in the foπnation, and further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

5566. The method of claim 5550, further comprising removing an oxidation product from the foimation through a conduit placed in an opening in the formation.

5567. The method of claim 5550, further comprising removing an oxidation product from the foimation through a conduit placed in an opening in the formation and inhibiting the oxidation product from flowing into a sunounding portion of the formation beyond the reaction zone.

5568. The method ofclaim 5550, further comprising inhibiting the oxidizing fluid from flowing into a sunounding portion of the formation beyond the reaction zone.

5569. The method ofclaim 5550, further comprising removing at least some water from the formation prior to heating the portion.

5570. The method ofclaim 5550, further comprising providing additional heat to the foimation from an elecfric heater placed in the opening.

5571. The method ofclaim 5550, further comprising providing additional heat to the formation from an electric heater placed in the opening and continuously oxidizing at least a portion of the hydrocarbons in the reaction zone.

5572. The method ofclaim 5550, further comprising providing additional heat to the formation from an elecfric heater placed in an opening in the formation and maintaining a constant heat rate within the pyrolysis zone.

5573. The method of claim 5550, further comprising providing additional heat to the formation from an elecfric heater placed in the opening such that the oxidation of at least a portion of the hydrocarbons does not burn out.

5574. The method ofclaim 5550, further comprising removing oxidation products from the formation and generating elecfricity using at least some oxidation products removed from the formation.

5575. The method ofclaim 5550, further comprising removing oxidation products from the formation and using at least some oxidation products removed from the formation in an ah compressor.

5576. The method ofclaim 5550, further comprising increasing a flow of the oxidizing fluid in the reaction zone to accommodate an increase in a volume of the reaction zone over time.

5577. The method ofclaim 5550, further comprising increasing a volume of the reaction zone such that an amount of heat provided to the formation increases.

5578. The method ofclaim 5550, further comprising assessing a temperature in or proximate the opening, and controlling the flow of oxidizing fluid as a function of the assessed temperature.

5579. The method ofclaim 5550, further comprising assessing a temperature in or proximate the opening, and increasing the flow of oxidizing fluid as the assessed temperature decreases.

5580. The method ofclaim 5550, further comprising controlling the flow of oxidizing fluid to maintain a temperature in or proximate the opening at a temperature less than a pre-selected temperature.

5581. A system configurable to heat a relatively low permeability foimation containing heavy hydrocarbons, comprising: a heater configurable to be placed in an opening in the formation, wherein the heater is configurable to provide heat to at least a portion of the formation during use; an oxidizing fluid source, wherein an oxidizing fluid is selected to oxidize at least some hydrocarbons at a reaction zone during use such that heat is generated in the reaction zone; a first conduit configurable to be placed in the opening, wherein the first conduit is configurable to provide the oxidizing fluid from the oxidizing fluid source to the reaction zone in the formation during use; and; a second conduit configurable to be placed in the opening, wherein the second conduit is configurable to remove a product of oxidation from the opening during use; and wherein the system is configurable to allow the generated heat to fransfer from the reaction zone to the formation during use.

5582. The system ofclaim 5581, wherein the second conduit is conflgurable to control the concentration of oxygen in the opening during use such that the concenfration of oxygen in the opening is substantially constant in the opening.

5583. The system of claim 5581, wherein the second conduit comprises orifices, and wherein the second conduit comprises a greater concenfration of orifices towards an upper end of the second conduit.

5584. The system ofclaim 5581, wherein the first conduit comprises orifices that direct oxidizing fluid in a direction substantially opposite the second conduit.

5585. The system ofclaim 5581, wherein the second conduit comprises orifices that remove the oxidation product from a direction substantially opposite the first conduit.

5586. The system ofclaim 5581, wherein the second conduit is configurable to remove a product of oxidation from the opening during use such that the reaction zone comprises a substantially uniform temperature profile.

5587. The system ofclaim 5581, wherein a flow of the oxidizing fluid can be varied along a portion of a length of the ffrst conduit,

5588. The system of claim 5581 , wherein the oxidizing fluid is configurable to generate heat in the reaction zone such that the oxidizing fluid is transported through the reaction zone substantially by diffusion.

5589. The system ofclaim 5581, wherein the system is configurable to allow heat to transfer from the reaction zone to a pyrolysis zone in the formation during use.

5590. The system ofclaim 5581, wherein the system is configurable to allow heat to fransfer substantially by conduction from the reaction zone to the formation during use.

5591. The system of clahn 5581, wherein a flow of oxidizing fluid can be confrolled along at least a portion of a length of the first conduit such that a temperature can be controlled along at least a portion of the length of the first conduit during use.

5592. The system ofclaim 5581, wherein a flow of oxidizing fluid can be confrolled along at least a portion of the length of the first conduit such that a heating rate in at least a portion of the formation can be confrolled.

5593. The system ofclaim 5581, wherein the oxidizing fluid is configurable to generate heat in the reaction zone during use such that the oxidizing fluid is transported through the reaction zone during use substantially by diffusion, wherein a rate of diffusion can controlled by a temperature of the reaction zone.

5594. The system ofclaim 5581, wherein the first conduit comprises orifices, and wherein the orifices are configurable to provide the oxidizing fluid into the opening during use.

5595. The system ofclaim 5581, wherein the first conduit comprises critical flow orifices, and wherein the critical flow orifices are configurable to control a flow of the oxidizing fluid such that a rate of oxidation in the formation is confrolled during use.

5596. The system ofclaim 5581, wherein the second conduit is further configurable to remove an oxidation product such that the oxidation product fransfers heat to the oxidizing fluid in the first conduit during use.

5597. The system ofclaim 5581, wherein a pressure of the oxidizing fluid in the first conduit and a pressure of the oxidation product in the second conduit are controlled during use such that a concentration of the oxidizing fluid in along the length of the conduit is substantially uniform.

5598. The system ofclaim 5581, wherein the oxidation product is substantially inhibited from flowing into portions of the formation beyond the reaction zone during use.

5599. The system ofclaim 5581, wherein the oxidizing fluid is substantially inhibited from flowing into portions of the formation beyond the reaction zone during use.

5600. The system ofclaim 5581 , wherein the portion of the formation extends radially from the opening a distance of less than approximately 3 m.

5601. The system ofclaim 5581, wherein the reaction zone extends radially from the opening a distance of less than approximately 3 m.

5602. The system ofclaim 5581, wherein the system is further conflgurable such that fransfened heat can pyrolyze at least some hydrocarbons in the pyrolysis zone.

5603. The system ofclaim 5581, wherein the heater is configured to be placed in an opening in the formation and wherein the heater is configured to provide heat to at least a portion of the formation during use.

5604. The system ofclaim 5581, wherein the first conduit is configured to be placed in the opening, and wherein the first conduit is configured to provide the oxidizing fluid from the oxidizing fluid source to the reaction zone in the formation during use.

5605. The system ofclaim 5581, wherein the flow of oxidizing fluid can be controlled along at least a segment of the ffrst conduit.

5606. The system ofclaim 5581, wherein the second conduit is configured to be placed in the opening, and wherein the second conduit is configured to remove a product of oxidation from the opening during use.

5607. The system ofclaim 5581, wherein the system is configured to allow heat to fransfer from the reaction zone to the foπnation during use.

5608. An in situ method for heating a relatively low permeability formation containing heavy hydrocarbons, comprising: heating a portion of the foπnation to a temperature sufficient to support reaction of hydrocarbons within the portion of the formation with an oxidizhig fluid; providing the oxidizing fluid to a reaction zone in the foimation; allowing the oxidizing fluid to react with at least a portion of the hydrocarbons in the reaction zone to generate heat in the reaction zone; removing an oxidation product from the opening; and fransfening the generated heat from the reaction zone to the formation.

5609. The method ofclaim 5608, further comprising removing the oxidation product such that a concenfration of oxygen in the openhig is substantially constant in the opening.

5610. The method ofclaim 5608, further comprising removing the oxidation product from the opening and maintaining a substantially uniform temperature profile within the reaction zone.

5611. The method of claim 5608, further comprising transporting the oxidizing fluid through the reaction zone substantially by diffusion.

5612. The method of claim 5608, further comprising ttansporting the oxidizing fluid through the reaction zone by diffusion, wherein a rate of diffusion is controlled by a temperature of the reaction zone.

5613. The method of claim 5608, further comprising allowing heat to ttansfer from the reaction zone to a pyrolysis zone in the formation.

5614. The method ofclaim 5608, further comprising allowing heat to fransfer from the reaction zone to the formation substantially by conduction.

5615. The method ofclaim 5608, further comprising controlling a flow of the oxidizing fluid along at least a portion of the length of the reaction zone such that a temperature is controlled along at least a portion of the length of the reaction zone.

5616. The method of claim 5608, ftirther comprising confrolling a flow of the oxidizing fluid along at least a portion of the length of the reaction zone such that a heating rate is confrolled along at least a portion of the length of the reaction zone.

5617. The method of claim 5608, further comprising allowing at least a portion of the oxidizing fluid into the opening through orifices of a conduit placed in the openhig.

5618. The method ofclaim 5608, further comprising confrolling a flow of the oxidizing fluid with critical flow orifices in a conduit placed in the opening such that a rate of oxidation is controlled.

5619. The method of claim 5608, further comprising controlling a flow of the oxidizing fluid with a spacing of critical flow orifices in a conduit placed in the opening.

5620. The method ofclaim 5608, further comprising confrolling a flow of the oxidizhig fluid with a diameter of critical flow orifices in a conduit placed in the openhig.

5621. The method ofclaim 5608, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volume of the reaction zone such that a rate of oxidation is substantially constant over time within the reaction zone.

5622. The method of claim 5608, wherein a conduit is placed in the opening, and further comprising cooling the conduit with the oxidizing fluid to reduce heating of the conduit by oxidation.

5623. The method o claim 5608, further comprising removing an oxidation product from the formation through a conduit placed in the opening.

5624. The method ofclaim 5608, further comprising removing an oxidation product from the formation through a conduit placed in the opening and substantially inhibiting the oxidation product from flowing into portions of the formation beyond the reaction zone.

5625. The method ofclaim 5608, further comprising substantially inhibiting the oxidizing fluid from flowing into portions of the formation beyond the reaction zone.

5626. The method of claim 5608, further comprising removing water from the formation prior to heating the portion.

5627. The method ofclaim 5608, further comprising providing additional heat to the formation from an electric heater placed in the opening.

5628. The method ofclaim 5608, further comprising providing additional heat to the fonnation from an electric heater placed in the opening such that the oxidizing fluid continuously oxidizes at least a portion of the hydrocarbons in the reaction zone.

5629. The method of clahn 5608, further comprising providing additional heat to the formation from an elecfric heater placed in the opening such that a constant heat rate in the foimation is maintained.

5630. The method ofclaim 5608, further comprising providing additional heat to the formation from an elecfric heater placed in the opening such that the oxidation of at least a portion of the hydrocarbons does not bum out.

5631. The method ofclaim 5608, further comprising generating elecfricity using oxidation products removed from the foπnation.

5632. The method ofclaim 5608, further comprising using oxidation products removed from the formation in an afr compressor.

5633. The method of claim 5608, further comprising increasing a flow of the oxidizing fluid in the opening to accommodate an increase in a volmne of the reaction zone over time.

5634. The method ofclaim 5608, further comprishig increasing the amount of heat provided to the foπnation by increasing the reaction zone.

5635. The method ofclaim 5608, further comprising assessing a temperature in or proximate the opening, and confrolling the flow of oxidizing fluid as a function of the assessed temperature.

5636. The method ofclaim 5608, further comprising assessing a temperature in or proximate the opening, and increasing the flow of oxidizing fluid as the assessed temperature decreases.

5637. The method ofclaim 5608, further comprising controlling the flow of oxidizing fluid to maintain a temperature in or proximate the opening at a temperature less than a pre-selected temperature.

5638. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprishig: providing heat from one or more heat sources to at least one portion of the fonnation; allowing the heat to transfer from the one or more heat sources to a selected section of the formation; controlling the heat from the one or more heat sources such that an average temperature within at least a selected section of the formation is less than about 375 °C; producing a mixture from the formation from a production well; and confrolling heating in or proximate the production well to produce a selected yield of non-condensable hydrocarbons in the produced mixture.

5639. The method ofclaim 5638, further comprising controlling heating in or proximate the production well to produce a selected yield of condensable hydrocarbons in the produced mixture.

5640. The method ofclaim 5638, wherein the mixture comprises more than about 50 weight percent non- condensable hydrocarbons.

5641. The method ofclaim 5638, wherein the mixture comprises more than about 50 weight percent condensable hydrocarbons.

5642. The method ofclaim 5638, wherein the average temperature and a pressure within the formation are controlled such that production of carbon dioxide is substantially inhibited.

5643. The method of claim 5638, heating in or proximate the production well is controlled such that production of carbon dioxide is substantially inhibited.

5644. The method ofclaim 5638, wherein at least a portion of the mixture produced from a first portion of the formation at a lower temperature is recycled into a second portion of the formation at a higher temperature such that production of carbon dioxide is substantially inhibited.

5645. The method ofclaim 5638, wherein the mixture comprises a volume ratio of molecular hydrogen to carbon monoxide of about 2 to 1, and wherein producing the mixture is controlled such that the volume ratio is maintained between about 1.8 to 1 and about 2.2 to 1.

5646. The method ofclaim 5638, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5647. The method ofclaim 5638, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the foπnation is at least about 0.5 bars absolute.

5648. The method ofclaim 5638, wherein at least one heat source comprises a heater.

5649. A method of freating a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; confrolling the heat from the one or more heat sources such that an average temperature within at least a selected section of the formation is less than about 375 °C; and producing a mixture from the formation.

5650. The method of claim 5649, removing a fluid from the formation through a production well.

5651. The method of claim 5649, further comprising removing a liquid through a production well.

5652. The method of claim 5649, further comprising removing water through a production well.

5653. The method of clahn 5649, further comprising removing a fluid through a production well prior to providing heat to the foimation.

5654. The method ofclaim 5649, fuither comprising removing water from the formation through a production well prior to providing heat to the foimation.

5655. The method ofclaim 5649, further comprising removing the fluid through a production well using a pump.

5656. The method of claim 5649, further comprising removing a fluid through a conduit.

5657. The method of claim 5649, wherein the heat provided from at least one heat source is transfened to the foπnation substantially by conduction.

5658. The method ofclaim 5649, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5659. The method of claim 5649, wherein at least one heat source comprises a heater.

5660. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to transfer from the one or more heat sources to a selected section of the foimation; confrolling the heat from the one or more heat sources such that an average temperature within at least a selected section of the formation is less than about 375 °C; measuring a temperature within a wellbore placed in the foπnation; and producing a mixture from the formation.

5661. The method of claim 5660, further comprising measuring the temperature using a moveable thermocouple.

5662. The method ofclaim 5660, further comprishig measuring the temperature using an optical fiber assembly.

5663. The method ofclaim 5660, further comprising measuring the temperature within a production well.

5664. The method of claim 5660, further comprising measuring the temperature within a heater well.

5665. The method ofclaim 5660, further comprising measuring the temperature within a monitoring well.

5666. The method ofclaim 5660, further comprising providing a pressure wave from a pressure wave source into the wellbore, wherehi the wellbore comprises a plurality of discontinuities along a length of the wellbore, measuring a reflection signal of the pressure wave, and using the reflection signal to assess at least one temperature between at least two discontinuities.

5667. The method of claim 5660, ftuther comprising assessing an average temperature in the formation using one or more temperatures measured within at least one wellbore.

5668. The method ofclaim 5660, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5669. The method ofclaim 5660, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5670. The method ofclaim 5660, wherein at least one heat source comprises a heater.

5671. An in situ method of measuring assessing a temperature within a wellbore in a relatively low peπneability foπnation containing heavy hydrocarbons, comprising: providing a pressure wave from a pressure wave source into the wellbore, wherein the wellbore comprises a plurality of discontinuities along a length of the wellbore; measuring a reflection signal of the pressure wave; and using the reflection signal to assess at least one temperature between at least two discontinuities.

5672. The method ofclaim 5671, wherein the plurality of discontinuities are placed along a length of a conduit placed in the wellbore.

5673. The method of claim 5672, wherein the pressure wave is propagated through a wall of the conduit.

5674. The method of claim 5672, wherein the plurality of discontinuities comprises collars placed within the conduit.

5675. The method of claim 5672, wherein the plurality of discontinuities comprises welds placed within the conduit.

5676. The method ofclaim 5671, wherein determining the at least one temperature between at least the two discontinuities comprises relating a velocity of the pressure wave between discontinuities to the at least one temperature.

5677. The method ofclaim 5671, further comprising measuring a reference signal of the pressure wave within the wellbore at an ambient temperature.

5678. The method of clahn 5671, further comprising measuring a reference signal of the pressure wave within the wellbore at an ambient temperature, and then determining the at least one temperature between at least the two discontinuities by comparing the measured signal to the reference signal.

5679. The method of claim 5671 , wherein the at least one temperature is a temperature of a gas between at least the two discontinuities.

5680. The method of claim 5671 , wherein the wellbore comprises a production well.

5681. The method ofclaim 5671, wherein the wellbore comprises a heater well.

5682. The method ofclaim 5671, wherein the wellbore comprises a monitoring well.

5683. The method ofclaim 5671, wherein the pressure wave source comprises a solenoid valve.

5684. The method of claim 5671, wherein the pressure wave source comprises an explosive device.

5685. The method of clahn 5671, wherein the pressure wave source comprises a sound device.

5686. The method of claim 5671, wherein the pressure wave is propagated through the wellbore.

5687. The method ofclaim 5671, wherein the plurality of discontinuities have a spacing between each discontinuity of about 5 m.

5688. The method ofclaim 5671, further comprising repeatedly providing the pressure wave into the wellbore at a selected frequency and continuously measuring the reflected signal to increase a signal-to-noise ratio of the reflected signal.

5689. The method ofclaim 5671, further comprising providing heat from one or more heat sources to a portion of the formation.

5690. The method ofclaim 5671, further comprising pyrolyzing at least some hydrocarbons within a portion of the foπnation.

5691. The method ofclaim 5671, further comprising generating synthesis gas in at least a portion of the foπnation.

5692. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; controlling the heat from the one or more heat sources such that an average temperature within at least a majority of the selected section of the formation is less than about 375 °C; and producing a mixture from the foimation through a heater well.

5693. The method ofclaim 5692, wherein producing the mixture through the heater well increases a production rate of the mixture from the formation.

5694. The method ofclaim 5692, further comprising providing heat using at least 2 heat sources.

5695. The method ofclaim 5692, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons with the selected section of the foπnation.

5696. The method ofclaim 5692, wherein the one or more heat sources comprise a pattern of heat sources in a formation, and wherein supeφosition of heat from the pattern of heat sources pyrolyzes at least some hydrocarbons with the selected section of the formation.

5697. The method of claim 5692, wherein heating of a majority of selected section is controlled such that a temperature of the majority of the selected section is less than about 375 °C.

5698. The method of claim 5692, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5699. The method of clahn 5692, wherein the mixture is produced from the foπnation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5700. The method ofclaim 5692, wherein at least one heat source comprises a heater.

5701. A method of freating a relatively low permeability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; wherein heating is provided from at least a ffrst heat source and at least a second heat source, wherein the first heat source has a first heating cost and the second heat source has a second heating cost; controlling a heating rate of at least a portion of the selected section to preferentially use the first heat source when the first heating cost is less than the second heating cost; and confrolling the heat from the one or more heat sources to pyrolyze at least some hydrocarbon in the selected section of the foimation.

5702. The method of clahn 5701, further comprising confrolling the heating rate such that a temperature within at least a majority of the selected section of the formation is less than about 375 °C.

5703. The method ofclaim 5701, further comprising providing heat using at least 2 heat sources.

5704. The method ofclaim 5701, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons with the selected section of the formation.

5705. The method ofclaim 5701, wherein the one or more heat sources comprise a pattern of heat sources in a fonnation, and wherein supeφosition of heat from the pattern of heat sources pyrolyzes at least some hydrocarbons with the selected section of the foπnation.

5706. The method of clahn 5701, further comprising controlling the heating to preferentiaUy use the second heat source when the second heating cost is less than the first heating cost.

5707. The method ofclaim 5701, further comprising producing a mixture from the formation.

5708. The method ofclaim 5701, wherein heating of a majority of selected section is controlled such that a temperature of the majority of the selected section is less than about 375 °C.

5709. The method ofclaim 5701, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

5710. The method ofclaim 5701, wherein at least one heat source comprises aheater.

5711. The method of claim 5701, further comprising producing a mixture from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5712. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to ttansfer from the one or more heat sources to a selected section of the formation; wherein heating is provided from at least a first heat source and at least a second heat source, wherein the first heat source has a first heathig cost and the second heat source has a second heating cost; controlling a heating rate of at least a portion of the selected section such that a cost associated with heating the selected section is minimized; and controlling the heat from the one or more heat sources to pyrolyze at least some hydrocarbon in at least a portion of the selected section of the formation.

5713. The method ofclaim 5712, wherein the heating rate is varied within a day depending on a cost associated with heating at various times in the day.

5714. The method ofclaim 5712, further comprising confrolling the heating rate such that a temperature within at least a majority of the selected section of the formation is less than about 375 °C.

5715. The method ofclaim 5712, further comprising providing heat using at least 2 heat sources.

5716. The method ofclaim 5712, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons with the selected section of the foimation.

5717. The method of claim 5712, wherein the one or more heat sources comprise a pattern of heat sources in a formation, and wherein supeφosition of heat from the pattern of heat sources pyrolyzes at least some hydrocarbons with the selected section of the formation.

5718. The method of clahn 5712, further comprising producing a mixture from the formation.

5719. The method ofclaim 5712, wherein heating of a majority of selected section is controlled such that a temperature of the majority of the selected section is less than about 375 °C.

5720. The method ofclaim 5712, wherein the heat provided from at least one heat source is transfened to the fonnation substantially by conduction.

5721. The method ofclaim 5712, wherein at least one heat source comprises a heater.

5722. The method ofclaim 5712, further comprising producing a mixture from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5723. A method for controlling an in situ system of treating a relatively low penneability formation containing heavy hydrocarbons, comprising: monitoring at least one acoustic event within the foimation using at least one acoustic detector placed within a wellbore in the formation; recording at least one acoustic event with an acoustic monitoring system; analyzing at least one acoustic event to determine at least one property of the formation; and controlling the in situ system based on the analysis of the at least one acoustic event.

5724. The method of clahn 5723, wherein the at least one acoustic event comprises a seismic event.

5725. The method ofclaim 5723, wherein the method is continuously operated.

5726. The method ofclaim 5723, wherein the acoustic monitoring system comprises a seismic monitoring system.

5727. The method of claim 5723, further comprishig recording the at least one acoustic event with the acoustic monitoring system.

5728. The method ofclaim 5723, further comprising monitoring more than one acoustic event simultaneously with the acoustic monitoring system.

5729. The method of clahn 5723, further comprising monitoring the at least one acoustic event at a sampling rate of about at least once every 0.25 milliseconds.

5730. The method ofclaim 5723, wherein analyzing the at least one acoustic event comprises inteφreting the at least one acoustic event.

5731. The method ofclaim 5723, wherein the at least one property of the formation comprises a location of at least one fracture in the fonnation.

5732. The method ofclaim 5723, wherein the at least one property of the formation comprises an extent of at least one fracture in the formation.

5733. The method ofclaim 5723, wherein the at least one property of the foπnation comprises an orientation of at least one fracture in the formation.

5734. The method ofclaim 5723, wherein the at least one property of the foimation comprises a location and an extent of at least one fracture in the formation.

5735. The method of claim 5723, wherein confrolling the in situ system comprises modifying a temperature of the in situ system.

5736. The method ofclaim 5723, wherein confrolling the in situ system comprises modifying a pressure of the in situ system.

5737. The method of claim 5723, wherein the at least one acoustic detector comprises a geophone.

5738. The method ofclaim 5723, wherein the at least one acoustic detector comprises a hydrophone.

5739. The method ofclaim 5723, further comprising providing heat to at least a portion of the formation.

5740. The method of claim 5723, further comprising pyrolyzing hydrocarbons within at least a portion of the formation.

5741. The method ofclaim 5723, further comprising providing heat from one or more heat sources to a portion of the formation.

5742. The method ofclaim 5723, further comprising pyrolyzing at least some hydrocarbons within a portion of the formation.

5743. The method of clahn 5723, further comprising generating synthesis gas in at least a portion of the formation.

5744. A method of predicting characteristics of a fonnation fluid produced from an in situ process, wherein the in situ process is used for freating a relatively low permeability formation containing heavy hydrocarbons, comprising: determining an isothermal experimental temperature that can be used when treating a sample of the formation, wherein the isothermal experimental temperature is conelated to a selected in situ heating rate for the formation; and treating a sample of the formation at the determined isothermal experimental temperature, wherein the experiment is used to assess at least one product characteristic of the foimation fluid produced from the foimation for the selected heating rate.

5745. The method ofclaim 5744, further comprising determining the at least one product characteristic at a selected pressure.

5746. The method ofclaim 5744, further comprising modifying the selected heating rate so that at least one desfred product characteristic of the formation fluid is obtained.

5747. The method of claim 5744, further comprising using a selected well spacing in the formation to deteπnine the selected heating rate.

5748. The method ofclaim 5744, further comprising using a selected heat input into the formation to determine the selected heating rate.

5749. The method ofclaim 5744, further comprising using at least one property of the formation to deteπnine the selected heating rate.

5750. The method of claim 5744, further comprising selecting a deshed heating rate such that at least one desired product characteristic of the foπnation fluid is obtained.

5751. The method of claim 5744, further comprising determining the isothermal temperature using an equation that estimates a temperature in which a selected amount of hydrocarbons in the formation are converted.

5752. The method ofclaim 5744, wherein the selected heating rate is less than about 1 °C per day.

5753. The method ofclaim 5744, wherein the sample is treated in an insulated vessel.

5754. The method ofclaim 5744, wherein at least one assessed produced characteristic is used to design at least one surface processing system, wherein the surface processing system is used to treat produced fluids on the surface.

5755. The method ofclaim 5744, wherein the formation is treated using a heating rate of about the selected heathig rate.

5756. The method ofclaim 5744, further comprising using at least one product characteristic to assess a pressure to be maintained in the formation during freatment.

5757. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the foπnation; adding hydrogen to the selected section after a temperature of the selected section is at least about 270 °C; and producing a mixture from the formation.

5758. The method ofclaim 5757, wherein the temperature of the selected section is at least about 290 °C.

5759. The method of claim 5757, wherein the temperature of the selected section is at least about 320 °C.

5760. The method ofclaim 5757, wherehi the temperature of the selected section is less than about 375 °C.

5761. The method of claim 5757, wherein the temperature of the selected section is less than about 400 °C.

5762. The method of claim 5757, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

5763. The method of claim 5757, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5764. The method of claim 5757, wherein at least one heat source comprises a heater.

5765. A method of freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion of the formation; allowing the heat to fransfer from the one or more heat sources to a selected section of the formation; and confrolling a temperature of a majority of the selected section by selectively adding hydrogen to the formation.

5766. The method of clahn 5765, further comprising controlling the temperature such that the temperature is less than about 375 °C.

5767. The method of claim 5765, further comprising controlling the temperature such that the temperature is less than about 400 °C.

5768. The method ofclaim 5765, further comprising controlling a heating rate such that the temperature is less than about 375 °C.

5769. The method ofclaim 5765, wherein the one or more heat sources comprise a pattern of heat sources in a formation, and wherein supeφosition of heat from the pattern of heat sources pyrolyzes at least some hydrocarbons with the selected section of the formation.

5770. The method ofclaim 5765, further comprising producing a mixture from the formation.

5771. The method of claim 5765, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

5772. The method of claim 5765, further comprising producing a mixture from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5773. The method of claim 5765, wherein at least one heat source comprises a heater.

5774. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from at least the portion to a selected section of the formation; and producing fluids from the formation wherein at least a portion of the produced fluids have been heated by the heat provided by one or more of the heat sources, and wherein at least a portion of the produced fluids are produced at a temperature greater than about 200 °C.

5775. The method ofclaim 5774 wherein at least a portion of the produced fluids are produced at a temperature greater than about 250 °C.

5776. The method ofclaim 5774 wherein at least a portion of the produced fluids are produced at a temperature greater than about 300 °C.

5777. The method of clahn 5774, further comprising varying the heat provided to the one or more heat sources to vary heat in at least a portion of the produced fluids.

5778. The method of clahn 5774 wherein the produced fluids are produced from a well comprising at least one of the heat sources, and further comprising varying the heat provided to the one or more heat sources to vary heat in at least a portion of the produced fluids.

5779. The method of claim 5774, further comprising providing at least a portion of the produced fluids to a hydrofreating unit.

5780. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a hydrofreating unit, and further comprising varying the heat provided to the one or more heat sources to vary heat in at least a portion of the produced fluids provided to the hydrofreating unit.

5781. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a hydrofreating unit, and using heat in the produced fluids when hydrotreating at least a portion of the produced fluids.

5782. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a hydrotreating unit, and hydrofreating at least a portion of the produced fluids without using a surface heater to heat produced fluids.

5783. The method of clahn 5774, further comprising: providing at least a portion of the produced fluids to a hydrofreating unit; and hydrotreating at least a portion of the produced fluids; wherein at least 50% of heat used for hydrotreating is provided by heat in the produced fluids.

5784. The method of claim 5774, further comprising providing at least a portion of the produced fluids to a hydrotreating unit, wherein at least a portion of the produced fluids are provided to the hydrotreating unit via an insulated conduit, and wherein the insulated conduit is insulated to inhibit heat loss from the produced fluids.

5785. The method of claim 5774, further comprising providing at least a portion of the produced fluids to a hydrofreating unit, wherein at least a portion of the produced fluids are provided to the hydrotreating unit via a heated conduit.

5786. The method of claim 5774, further comprishig providing at least a portion of the produced fluids to a hydrotreating unit wherein the produced fluids are produced at a wellhead, and wherein at least a portion of the produced fluids are provided to the hydrotreating unit at a temperature that is within about 50 °C of the temperature of the produced fluids at the wellhead.

5787. The method ofclaim 5774, further comprising hydrofreating at least a portion of the produced fluids such that the volume of hydrofreated produced fluids is about 4% greater than a volume of the produced fluids.

5788. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a hydrofreating unit wherein the produced fluids comprise molecular hydrogen, and using the molecular hydrogen in the produced fluids to hydrotreat at least a portion of the produced fluids.

5789. The method of claim 5774, further comprising providing at least a portion of the produced fluids to a hydrotreating unit wherein the produced fluids comprise molecular hydrogen, hydrotreating at least a portion of the produced fluids, and wherein at least 50% of molecular hydrogen used for hydrofreating is provided by the molecular hydrogen in the produced fluids.

5790. The method of claim 5774 wherein the produced fluids comprise molecular hydrogen, separating at least a portion of the molecular hydrogen from the produced fluids, and providing at least a portion of the separated molecular hydrogen to a surface treatment unit.

5791. The method ofclaim 5774 wherein the produced fluids comprise molecular hydrogen, separating at least a portion of the molecular hydrogen from the produced fluids, and providing at least a portion of the separated molecular hydrogen to an in situ treatment area.

5792. The method of claim 5774 further comprising providing a portion of the produced fluids to an olefin generating unit.

5793. The method of clahn 5774 further comprising providing a portion of the produced fluids to a steam cracking unit.

5794. The method of claim 5774, fuither comprising providing at least a portion of the produced fluids to an olefin generating unit, and further comprising varying heat provided to the one or more heat sources to vary the heat in at least a portion of the produced fluids provided to the olefin generating unit.

5795. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and using heat in the produced fluids when generating olefins from at least a portion of the produced fluids.

5796. The method of claim 5774, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and generating olefins from at least a portion of the produced fluids without using a surface heater to heat produced fluids.

5797. The method ofclaim 5774, further comprismg providmg at least a portion of the produced fluids to an olefin generating unit, and generating olefins from at least a portion of the produced fluids, and wherein at least 50% of the heat used for generating olefins is provided by heat in the produced fluids.

5798. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via an insulated conduit, and wherein the insulated conduit is insulated to inhibit heat loss from the produced fluids.

5799. The method of claim 5774, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via a heated conduit.

5800. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein the produced fluids are produced at a wellhead, and wherein at least a portion of the produced fluids are provided to the olefin generating unit at a temperature that is within about 50 °C of the temperature of the produced fluids at the wellhead.

5801. The method ofclaim 5774 further comprising removing heat from the produced fluids in a heat exchanger.

5802. The method ofclaim 5774 further comprising separating the produced fluids into two or more streams comprising at least a synthetic condensate sfream, and a non-condensable fluid sfream.

5803. The method of claim 5774 further comprising providing at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids into two or more sfreams.

5804. The method ofclaim 5774 furtlier comprising providing at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids into two or more streams, and further comprising separating at least one of such sfreams into two or more subsfreams.

5805. The method ofclaim 5774 further comprising providing at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids into three or more sfreams, and wherein such sfreams comprise at least a top stream, a bottom stteam, and a middle stream.

5806. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a separating unit, and further comprising varying heat provided to the one or more heat sources to vary the heat in at least a portion of the produced fluids provided to the separating unit.

5807. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a separating unit, and using heat in the produced fluids when separating at least a portion of the produced fluids.

5808. The method of claim 5774, further comprising providmg at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids without using a surface heater to heat produced fluids.

5809. The method of claim 5774, further comprising providing at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids, and wherein at least 50% of the heat used for separating is provided by heat in the produced fluids.

5810. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a separating unit wherein at least a portion of the produced fluids are provided to the separating unit via an insulated conduit, and wherein the insulated conduit is insulated to inhibit heat loss from the produced fluids.

5811. The method of claim 5774, further comprising providing at least a portion of the produced fluids to a separating unit wherein at least a portion of the produced fluids are provided to the separating unit via a heated conduit.

5812. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a separating unit wherein the produced fluids are produced at a wellhead, and wherein at least a portion of the produced fluids are provided to the separating unit at a temperature that is within about 50 °C of the temperature of the produced fluids at the wellhead.

5813. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids into four or more sfreams, and wherein such streams comprise at least a top sfream, a bottoms stream, and at least two middle sfreams wherein one of the middle sfreams is heavier than the other middle sfream.

5814. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a separating unit, and separating at least a portion of the produced fluids into five or more sfreams, and wherein such streams comprise at least a top stream, a bottoms stream, a naphtha sfream, diesel stteam, and a jet fuel sfream.

5815. The method ofclaim 5774, further comprising providing at least a portion of the produced fluids to a distillation column, and using heat in the produced fluids when distilling at least a portion of the produced fluids.

5816. The method of claim 5774 wherein the produced fluids comprise pyrolyzation fluids.

5817. The method of claim 5774 wherein the produced fluids comprise carbon dioxide, and further comprising separating at least a portion of the carbon dioxide from the produced fluids.

5818. The method of claim 5774 wherein the produced fluids comprise carbon dioxide, and further comprising separating at least a portion of the carbon dioxide from the produced fluids, and utilizing at least some carbon dioxide in one or more treatment processes.

5819. The method of claim 5774 wherein the produced fluids comprise molecular hydrogen and wherein the molecular hydrogen is used when treating the produced fluids.

5820. The method ofclaim 5774 wherein the produced fluids comprise steam and wherein the steam is used when treating the produced fluids.

5821. The method of claim 5774, wherein the heat provided from at least one heat source is transfened to the fonnation substantially by conduction.

5822. The method ofclaim 5774, wherein the fluids are produced from the foπnation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5823. The method of claim 5774, wherein at least one heat source comprises a heater.

5824. A method of converting fonnation fluids into olefins, comprising: converting formation fluids into olefins, wherein the foimation fluids are obtained by: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to fransfer from one or more heat sources to a selected section of the formation such that at least some hydrocarbons in the formation are pyrolyzed; and producing fonnation fluids from the foπnation.

5825. The method of claim 5824 wherein the produced fluids comprise steam.

5826. The method ofclaim 5824 wherein the produced fluids comprise steam and wherein the steam in the produced fluids comprises at least a portion of steam used in the olefin generating unit.

5827. The method of claim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit.

5828. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to a steam cracking unit.

5829. The method of claim 5824 wherein olefins comprise ethylene.

5830. The method ofclaim 5824 wherein olefins comprise propylene.

5831. The method ofclaim 5824, further comprising separating liquids from the produced fluids, and then separating olefin generating compounds from the produced fluids, and then providing at least a portion of the olefin generathig compounds to an olefin generating unit.

5832. The method ofclaim 5824 wherein the produced fluids comprise molecular hydrogen, and further comprising removing at least a portion of the molecular hydrogen from the produced fluids prior to using the produced fluids to produce olefins.

5833. The method ofclaim 5824 wherein the produced fluids comprise molecular hydrogen, and further comprising separating at least a portion of the molecular hydrogen from the produced fluids, and utilizing at least a portion of the separated molecular hydrogen in one or more treatment processes.

5834. The method ofclaim 5824 wherein the produced fluids comprise molecular hydrogen, and further comprising removing at least a portion of the molecular hydrogen from the produced fluids using a hydrogen removal unit prior to using the produced fluids to produce olefins.

5835. The method of claim 5824 wherein the produced fluids comprises molecular hydrogen, and further comprising removing at least a portion of the molecular hydrogen from the produced fluids using a membrane prior to using the produced fluids to produce olefins.

5836. The method of claim 5824, further comprising generathig molecular hydrogen during production of olefins, and providing at least a portion of the generated molecular hydrogen to one or more hydrofreating units.

5837. The method of clahn 5824, further comprising generating molecular hydrogen during production of olefins, and providing at least a portion of the generated molecular hydrogen to an in situ treatment area.

5838. The method ofclaim 5824, further comprising generating molecular hydrogen during production of olefins, and providing at least a portion of the generated molecular hydrogen to one or more fuel cells.

5839. The method of claim 5824, further comprising generating molecular hydrogen during production of olefins, and using at least a portion of the generated molecular hydrogen to hydrotteat pyrolysis liquids generated in the olefin generation plant.

5840. The method ofclaim 5824 wherein the produced fluids are at least 200 °C, and further comprising using heat in the produced fluids to produce olefins.

5841. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to a hydrotreating unit wherein the produced fluids are produced at a wellhead, and wherein at least a portion of the produced fluids are provided to the olefins generating unit at a temperature that is within about 50 °C of the temperature of the produced fluids at the wellhead.

5842. The method of clahn 5824 wherein the produced fluids can be used to make olefins without substantial hydrofreating of the produced fluids.

5843. The method ofclaim 5824, further comprising separating liquids from the produced fluids, and then using at least a portion of the produced fluids to produce olefins.

5844. The method ofclaim 5824, further comprising controlling a fluid pressure within at least a portion of the formation to enhance production of olefin generating compounds in the produced fluids.

5845. The method ofclaim 5824, further comprising controlling a temperature within at least a portion of the formation to enhance production of olefin generating compounds in the produced fluids.

5846. The method ofclaim 5824, further comprising controlling a temperature profile within at least a portion of the formation to enhance production of olefin generating compounds in the produced fluids.

5847. The method ofclaim 5824, further comprising controlling a heating rate within at least a portion of the formation to enhance production of olefin generating compounds in the produced fluids.

5848. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and further comprising varying heat provided to the one or more heat sources to vary the heat in at least a portion of the produced fluids provided to the olefin generating unit.

5849. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and using heat in the produced fluids when generating olefins from at least a portion of the produced fluids.

5850. The method of claim 5824 wherein the produced fluids comprise steam, and further comprising providing at least a portion of the produced fluids to an olefin generathig unit, and using steam in the produced fluids when generating olefins from at least a portion of the produced fluids.

5851. The method ofclaim 5824 wherein the produced fluids comprise steam, and further comprising providing at least a portion of the produced fluids to an olefin generating unit, generating olefins from at least a portion of the produced fluids, and wherein at least some steam used for generating olefins is provided by the steam in the produced fluids.

5852. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via an insulated conduit, and wherein the insulated conduit is insulated to inhibit heat loss from the produced fluids.

5853. The method of claim 5824, further comprising providing at least a portion of the produced fluids to an olefm generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via a heated conduit.

5854. The method ofclaim 5824, further comprising separating at least a portion of the produced fluids into one or more fractions wherein the one or more fractions comprise a naphtha fraction, and further comprising providing the naphtha fraction to an olefin generating unit.

5855. The method ofclaim 5824, further comprising separating at least a portion of the produced fluids into one or more fractions wherein the one or more fractions comprise a olefin generating fraction wherein the olefin generating fraction comprises hydrocarbons having a carbon number greater than about 1 and a carbon nmnber less than about 8, and further comprising providing the olefin generating fraction to a olefin generating unit.

5856. The method ofclaim 5824, further comprising separating at least a portion of the produced fluids into one or more fractions wherein the one or more fractions comprise an olefin generating fraction wherein the olefin generating fraction comprises hydrocarbons having a carbon number greater than about 1 and a carbon number less than about 6, and further comprising providing the olefin generating fraction to a olefin generating unit.

5857. The method of clahn 5824, further comprising providing at least the portion of the produced fluids to a component removal unit such that at least one component stream and a reduced component fluid stream are formed, and then providing the reduced component fluid stream to an olefin generating unit.

5858. The method of clahn 5857, wherein the component comprises a metal.

5859. The method of claim 5857, wherein the component comprises arsenic.

5860. The method ofclaim 5857, wherein the component comprises mercury.

5861. The method of claim 5857, wherein the component comprises lead.

5862. The method ofclaim 5824, further comprising providing at least the portion of the produced fluids to a component removal unit such that at least one component stteam and a reduced component fluid stteam are formed, then providing the reduced component fluid sfream to a molecular hydrogen separating unit such that a molecular hydrogen sfream and a reduced hydrogen fluid sfream are formed, then providing the molecular hydrogen sfream to a hydrotreating unit, and then providing the reduced hydrogen produced fluid stream to an olefin generating unit.

5863. The method of clahn 5824 wherein the produced fluids comprise molecular hydrogen and wherein the molecular hydrogen is used when freating the produced fluids.

5864. The method ofclaim 5824 wherein the produced fluids comprise steam and wherein the steam is used when freating the produced fluids.

5865. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and using heat in the produced fluids when generating olefins from at least a portion of the produced fluids.

5866. The method ofclaim 5824 wherein the produced fluids comprise steam, and further comprising providing at least a portion of the produced fluids to an olefin generating unit, and using steam in the produced fluids when generating olefins from at least a portion of the produced fluids.

5867. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via an insulated conduit, and wherein the insulated conduit is insulated to inhibit heat loss from the produced fluids.

5868. The method ofclaim 5824, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via a heated conduit.

5869. The method ofclaim 5824, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5870. The method ofclaim 5824, wherein the formation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5871. The method ofclaim 5824, wherein at least one heat source comprises aheater.

5872. A method of separating olefins from fluids produced from a relatively low permeability formation containing heavy hydrocarbons, comprising: separating olefins from the produced fluids, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion of the foπnation; allowing the heat to transfer from at least one or more heat sources to a selected section of the fonnation; and producing fluids from the formation wherein the produced fluids comprise olefins.

5873. The method ofclaim 5872 wherein olefins comprise ethylene.

5874. The method ofclaim 5872 wherein olefins comprise propylene.

5875. The method ofclaim 5872, further comprising separating liquids from the produced fluids.

5876. The method ofclaim 5872 wherein the produced fluids comprise molecular hydrogen, and further comprising separating at least a portion of the molecular hydrogen from the produced fluids, and utilizing at least a portion of the separated molecular hydrogen in one or more freatment processes.

5877. The method ofclaim 5872 wherein the produced fluids comprise molecular hydrogen, and further comprising removing at least a portion of the molecular hydrogen from the produced fluids using a hydrogen removal unit.

5878. The method ofclaim 5872 wherein the produced fluids comprises molecular hydrogen, and further comprising removing at least a portion of the molecular hydrogen from the produced fluids using a membrane.

5879. The method of claim 5872, further comprising confrolling a fluid pressure within at least a portion of the formation to enhance production of olefins in the produced fluids.

5880. The method ofclaim 5872, further comprising controlling a temperature within at least a portion of the formation to enhance production of olefins in the produced fluids.

5881. The method of claim 5872, fuither comprising confrolling a temperature profile within at least a portion of the formation to enhance production of olefins in the produced fluids.

5882. The method ofclaim 5872, ftirther comprising confrolling a heating rate within at least a portion of the formation to enhance production of olefins in the produced fluids.

5883. The method ofclaim 5872, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and further comprising varying heat provided to the one or more heat sources to vary the heat in at least a portion of the produced fluids provided to the olefin generating unit.

5884. The method ofclaim 5872, further comprising providing at least a portion of the produced fluids to an olefin generating unit, and using heat in the produced fluids when generating olefins from at least a portion of the produced fluids.

5885. The method of claim 5872 wherein the produced fluids comprise steam, and further comprising providing at least a portion of the produced fluids to an olefin generating unit, and using steam in the produced fluids when generating olefins from at least a portion of the produced fluids.

5886. The method of claim 5872, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via an insulated conduit, and wherein the insulated conduit is insulated to inhibit heat loss from the produced fluids.

5887. The method ofclaim 5872, further comprising providing at least a portion of the produced fluids to an olefin generating unit wherein at least a portion of the produced fluids are provided to the olefin generating unit via a heated conduit.

5888. The method ofclaim 5872, further comprising separating at least a portion of the produced fluids into one or more fractions wherein the one or more fractions comprise a naphtha fraction, and further comprising providing the naphtha fraction to an olefin generating unit.

5889. The method of claim 5872, further comprising separating at least a portion of the produced fluids into one or more fractions wherein the one or more fractions comprise a olefin generating fraction wherein the olefin generating fraction comprises hydrocarbons having a carbon number greater than about 1 and a carbon number less than about 8, and further comprising providing the olefin generathig fraction to a olefin generating unit.

5890. The method ofclaim 5872, further comprising separating at least a portion of the produced fluids into one or more fractions wherein the one or more fractions comprise an olefin generating fraction wherein the olefhi generating fraction comprises hydrocarbons having a carbon number greater than about 1 and a carbon number less than about 6, and further comprising providing the olefin generating fraction to a olefin generating unit.

5891. The method ofclaim 5872, further comprising providing at least the portion of the produced fluids to a component removal unit such that at least one component stream and a reduced component fluid sfream are formed, and then providing the reduced component fluid stteam to an olefin generating unit.

5892. The method of claim 5891 wherein the component comprises a metal.

5893. The method ofclaim 5891 wherein the component comprises arsenic.

5894. The method ofclaim 5891 wherein the component comprises mercury.

5895. The method ofclaim 5891 wherein the component comprises lead.

5896. The method of clahn 5872, further comprising providing at least the portion of the produced fluids to a component removal unit such that at least one component stream and a reduced component fluid stream are formed, then providing the reduced component fluid stream to a molecular hydrogen separating unit such that a molecular hydrogen sfream and a reduced hydrogen fluid sfream are formed, then providing the molecular hydrogen sfream to a hydrofreating unit, and then providing the reduced hydrogen produced fluid stteam to an olefin generating unit.

5897. The method ofclaim 5872, further comprising confrolling a temperature gradient within at least a portion of the fonnation to enhance production of olefins in the produced fluids.

5898. The method ofclaim 5872, further comprising confrolling a fluid pressure within at least a portion of the formation to enhance production of olefins in the produced fluids.

5899. The method ofclaim 5872, further comprising controlling a temperature within at least a portion of the formation to enhance production of olefins in the produced fluids.

5900. The method of claim 5872, further comprising controlling a heating rate within at least a portion of the formation to enhance production of olefins in the produced fluids.

5901. The method of claim 5872, further comprising separating the olefins from the produced fluids such that an amount of molecular hydrogen utilized in one or more downstream hydrofreating units decreases.

5902. The method of claim 5872, further comprising removing at least a portion of the olefins prior to hydrofreating produced fluids.

5903. A method of enhancing BTEX compounds production from a relatively low peπneability formation containing heavy hydrocarbons, comprising: confrollmg at least one condition within at least a portion of the formation to enhance production of BTEX compounds in formation fluid, wherein the formation fluid is obtained by: providing heat from one or more heat sources to at least a portion of the formation; allowing the heat to fransfer from at least one or more heat sources to a selected section of the fonnation; and producing formation fluids from the formation.

5904. The method ofclaim 5903, further comprising separating at least a portion of the BTEX compounds from the produced fluids.

5905. The method ofclaim 5903, further comprising separating at least a portion of the BTEX compounds from the produced fluids via solvent extraction.

5906. The method of clahn 5903, further comprising separating at least a portion of the BTEX compounds from the produced fluids via distillation.

5907. The method ofclaim 5903, further comprising separating at least a portion of the BTEX compounds from the produced fluids via condensation.

5908. The method ofclaim 5903, further comprising separating at least a portion of the BTEX compounds from the produced fluids such that an amount of molecular hydrogen utilized in one or more downstream hydrotreating units decreases.

5909. The method of claim 5903, wherein controlling at least one condition in the formation comprises controlling a fluid pressure within at least a portion of the foπnation.

5910. The method of claim 5903, wherein controlling at least one condition in the formation comprises controlling a temperature gradient withhi at least a portion of the formation.

5911. The method ofclaim 5903, wherein controlling at least one condition in the formation comprises controlling a temperature within at least a portion of the formation.

5912. The method ofclaim 5903, wherein controlling at least one condition in the formation comprises confrolling a heating rate within at least a portion of the formation.

5913. The method of clahn 5903, further comprising removing at least a portion of the BTEX compounds prior to hydrofreating produced fluids.

5914. The method ofclaim 5903, wherein the heat provided from at least one heat source is fransfened to the foπnation substantially by conduction.

5915. The method of claim 5903, wherein the fonnation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5916. The method ofclaim 5903, wherein at least one heat source comprises a heater.

5917. A method of separating BTEX compounds from foimation fluid from a relatively low peπneability fonnation containing heavy hydrocarbons, comprising: separating at least a portion of the BTEX compounds from the formation fluid wherein the formation fluid is obtained by: providing heat from one or more heat sources to at least a portion of the foimation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the foπnation wherein the produced fluids comprise BTEX compounds.

5918. The method of clahn 5917, further comprising hydrotreating at least a portion ofthe produced fluids after the BTEX compounds have been separated from same.

5919. The method of claim 5917 wherein separating at least a portion of the BTEX compounds from the produced fluids comprises extracting at least the portion ofthe BTEX compounds from the produced fluids via solvent exfraction.

5920. The method ofclaim 5917 wherein separating at least a portion ofthe BTEX compounds from the produced fluids comprises distilling at least the portion ofthe BTEX compounds from the produced fluids.

5921. The method of claim 5917 wherein separating at least a portion of the BTEX compounds from the produced fluids comprises condensing at least the portion ofthe BTEX compounds from the produced fluids

5922. The method ofclaim 5917 wherein separating at least a portion ofthe BTEX compounds from the produced fluids such that an amount of molecular hydrogen utilized in one or more downstream hydrotreating units decreases.

5923. The method ofclaim 5917, further comprising controlling a fluid pressure within at least a portion ofthe formation.

5924. The method of claim 5917, further comprising confrolling a temperature gradient within at least a portion ofthe foπnation.

5925. The method ofclaim 5917, fuither comprising controlling a temperature within at least a portion ofthe formation.

5926. The method ofclaim 5917, further comprising controlling a heating rate within at least a portion ofthe formation.

5927. The method ofclaim 5917 wherein separating at least the portion of BTEX compounds from the produced fluids further comprises removing a naphtha fraction from the produced fluids, and separating at least the portion of

BTEX compounds from the naphtha fraction.

5928. The method of clahn 5917, wherein separating at least the portion of BTEX compounds from the produced fluids, further comprises removing a BTEX fraction from the produced fluids, and separating at some BTEX compounds from the BTEX fraction.

5929. The method ofclaim 5917, wherein separating at least the portion of BTEX compounds from the produced fluids decreases an amount of molecular hydrogen utilized in one or more downstream hydrotreating units.

5930. A method of in situ converting at least a portion of formation fluid into BTEX compounds, comprising: in situ converting at least the portion ofthe foπnation fluid into BTEX compounds, wherein the formation fluid are obtained by: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe formation such that at least some hydrocarbons in the formation are pyrolyzed; and producing formation fluid from the formation.

5931. The method of claim 5930, further comprising providing at least a portion ofthe formation fluid to an BTEX generating unit.

5932. The method of claim 5930, further comprising providing at least a portion ofthe formation fluid to a catalytic reforming unit.

5933. The method of claim 5930, further comprising hydrotreating at least some ofthe formation fluid, and then separating the hydrofreated mixture into one more sfreams comprising a naphtha sfream, and then reforming at least a portion the naphtha stream to form a reformate comprishig BTEX compounds, and then separating at least a portion ofthe BTEX compounds from the reformate.

5934. The method of clahn 5930, further comprising hydrofreating at least some ofthe formation fluid, and then separating the hydrofreated mixture into one more sfreams comprising a naphtha stream, and then reforming at least a portion the naphtha sfream to form a molecular hydrogen stream and a reformate comprising BTEX compounds, and then separating at least a portion of the BTEX compounds from the reformate, and then utilizing the molecular hydrogen stream to hydrotreat at least some ofthe formation fluid.

5935. The method ofclaim 5930, further comprising hydrofreating the foπnation fluid, and then separating the hydrofreated formation fluid into one more sfreams comprising a naphtha stream, and then reforming at least a portion the naphtha sfream to form a reformate comprising BTEX compounds, and then separating at least a portion ofthe refoπnate into two or more streams comprising a raffinate and a BTEX stream..

5936. The method ofclaim 5930 wherein the formation fluid is at least 200 °C, and further comprising using heat in the formation fluid to hydrofreat at least a portion ofthe formation fluid.

5937. The method of claim 5930, further comprising separating at least a portion ofthe formation fluid into one or more fractions wherehi the one or more fractions comprise a naphtha fraction, and further comprising providing the naphtha fraction to a catalytic reforming unit.

5938. The method of clahn 5930, further comprising separating at least a portion ofthe foπnation fluid into one or more fractions wherein the one or more fractions comprise a BTEX compound generating fraction wherein the BTEX compound generating fraction comprises hydrocarbons, and further comprising providing the BTEX compound generating fraction to a catalytic reforming unit.

5939. The method of claim 5930, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5940. The method of claim 5930, wherein the fluids are produced from the foπnation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5941. The method ofclaim 5930, wherein at least one heat source comprises a heater.

5942. A method of enhancing naphthalene production from a relatively low permeability formation containing heavy hydrocarbons, comprising: confrolling at least one condition within at least a portion ofthe formation to enhance production of naphthalene in formation fluid, wherein the formation fluid is obtained by: providing heat from one or more heat sources to at least a portion ofthe foπnation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe foπnation; and producing formation fluids from the foimation.

5943. The method of clahn 5942, further comprising separating at least a portion ofthe naphthalene from the produced fluids.

5944. The method of claim 5942 wherein controlling at least one condition in the formation comprises confrolling a fluid pressure within at least a portion ofthe formation.

5945. The method ofclaim 5942 wherein controlling at least one condition in the foπnation comprises controlling a temperature gradient within at least a portion ofthe formation.

5946. The method of clahn 5942 wherein confrolling at least one condition in the formation comprises confrolling a temperature within at least a portion ofthe formation.

5947. The method ofclaim 5942 wherein controlling at least one condition in the formation comprises controlling a heating rate within at least a portion ofthe formation.

5948. The method ofclaim 5942, further comprising separating the produced fluids into one or more fractions using distillation.

5949. The method ofclaim 5942, further comprising separating the produced fluids into one or more fractions using condensation.

5950. The method ofclaim 5942, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and further comprising providing the heart cut to an exfraction unit, and separating at least some naphthalene from the heart cut.

5951. The method of claim 5942, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a naphthalene fraction, and further comprising providing the naphthalene fraction to an exfraction unit, and separating at least some naphthalene from the naphthalene fraction.

5952. The method ofclaim 5942, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5953. The method of claim 5942, wherein the foimation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5954. The method ofclaim 5942, wherein at least one heat source comprises a heater.

5955. A method of separating naphthalene from fluids produced from a relatively low permeability fonnation containing heavy hydrocarbons, comprising: separating naphthalene from the produced fluids, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to transfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the formation wherein the produced fluids comprise naphthalene.

5956. The method ofclaim 5955, further comprising controlling a fluid pressure within at least a portion ofthe foπnation.

5957. The method of claim 5955, further comprising controlling a temperature gradient within at least a portion ofthe formation.

5958. The method of claim 5955, further comprising controlling a temperature within at least a portion ofthe formation.

5959. The method ofclaim 5955, further comprising controlling a heating rate within at least a portion ofthe formation.

5960. The method ofclaim 5955, wherein separating at least some naphthalene from the produced fluids further comprises separating the produced fluids into one or more fractions using distillation.

5961. The method ofclaim 5955, wherein separating at least some naphthalene from the produced fluids further comprises separating the produced fluids into one or more fractions using condensation.

5962. The method ofclaim 5955, wherein separating at least some naphthalene from the produced fluids further comprises separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and extracting at least a portion ofthe naphthalene from the heart cut.

5963. The method of claim 5955, wherein separating at least some naphthalene from the produced fluids further comprises removing a naphtha fraction from the produced fluids, and separating at least a portion ofthe naphthalene from the naphtha fraction.

5964. The method ofclaim 5955, wherein separating at least some naphthalene from the produced fluids further comprises removing an naphthalene fraction from the produced fluids, and separating at least a portion ofthe naphthalene from the naphthalene fraction.

5965. The method ofclaim 5955, wherein separating the naphthalene from the produced fluids further comprises removing naphthalene using distillation.

5966. The method of claim 5955, wherein separating the naphthalene from the produced fluids further comprises removing naphthalene using crystallization.

5967. The method of claim 5955, further comprising removing at least a portion ofthe naphthalene prior to hydrotreating produced fluids.

5968. The method ofclaim 5955, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

5969. The method of claim 5955, wherein the foimation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5970. The method of claim 5955, wherein at least one heat source comprises a heater.

5971. A method of enhancing anthracene production from a relatively low permeability fonnation containing heavy hydrocarbons, comprising: controlling at least one condition within at least a portion ofthe formation to enhance production of anthracene in fonnation fluid, wherein the fonnation fluid is obtained by: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe foπnation; and producing formation fluids from the formation.

5972. The method ofclaim 5971, further comprising separating at least a portion ofthe anthracene from the produced fluids.

5973. The method ofclaim 5971 wherehi confrolling at least one condition in the fonnation comprises confrolling a fluid pressure within at least a portion ofthe foimation.

5974. The method ofclaim 5971 wherein controlling at least one condition in the formation comprises confrolling a temperature gradient within at least a portion ofthe formation.

5975. The method ofclaim 5971 wherein controlling at least one condition in the formation comprises confrolling a temperature withhi at least a portion ofthe formation.

5976. The method ofclaim 5971 wherein confrolling at least one condition in the formation comprises confrolling a heating rate within at least a portion ofthe formation.

5977. The method ofclaim 5971, further comprising separating the produced fluids into one or more fractions using distillation.

5978. The method ofclaim 5971, further comprising separating the produced fluids into one or more fractions using condensation.

5979. The method o claim 5971, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and further comprising providing the heart cut to an extraction unit, and separating at least some anthracene from the heart cut.

5980. The method ofclaim 5971 , further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a anthracene fraction, and further comprising providing the anthracene fraction to an extraction unit, and separating at least some anthracene from the anthracene fraction.

5981. The method ofclaim 5971, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5982. The method ofclaim 5971, wherein the formation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5983. The method ofclaim 5971, wherein at least one heat source comprises a heater.

5984. A method of separating anthracene from fluids produced from a relatively low permeability formation containing heavy hydrocarbons, comprising: separating anthracene from the produced fluids, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe foπnation; allowing the heat to transfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the foimation wherein the produced fluids comprise anthracene.

5985. The method ofclaim 5984, further comprising confrolling a fluid pressure within at least a portion ofthe foπnation.

5986. The method ofclaim 5984, further comprising confrolling a temperature gradient within at least a portion ofthe formation.

5987. The method of clahn 5984, further comprising confrolling a temperature within at least a portion ofthe formation.

5988. The method ofclaim 5984, further comprising controlling a heating rate within at least a portion ofthe formation

5989. The method of claim 5984, wherein separating at least some anthracene from the produced fluids fiuther comprises separating the produced fluids into one or more fractions using distillation.

5990. The method ofclaim 5984, wherein separating at least some anthracene from the produced fluids further comprises separating the produced fluids into one or more fractions using condensation.

5991. The method of claim 5984, wherein separating at least some anthracene from the produced fluids further comprises separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and extracting at least a portion ofthe anthracene from the heart cut.

5992. The method ofclaim 5984, wherein separating at least some anthracene from the produced fluids fiuther comprises removing a naphtha fraction from the produced fluids, and separathig at least a portion ofthe anthracene from the naphtha fraction.

5993. The method of clahn 5984, wherein separating at least some anthracene from the produced fluids further comprises removing an anthracene fraction from the produced fluids, and separating at least a portion ofthe anthracene from the anthracene fraction.

5994. The method of claim 5984, wherein separating the anthracene from the produced fluids further comprises removing anthracene using distillation.

5995. The method of claim 5984, wherein separating the anthracene from the produced fluids further comprises removing anthracene using crystallization.

5996. The method ofclaim 5984, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

5997. The method ofclaim 5984, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

5998. The method of claim 5984, wherein at least one heat source comprises a heater.

5999. A method of separating ammonia from fluids produced from a relatively low permeability formation containing heavy hydrocarbons, comprising: separating at least a portion ofthe ammonia from the produced fluid, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to transfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the foπnation.

6000. The method ofclaim 5999 wherein the produced fluids are pyrolyzation fluids.

6001. The method ofclaim 5999 wherein separating at least a portion ofthe ammonia from the produced fluids further comprises providing at least a portion ofthe produced fluids to a sour water stripper.

6002. The method of claim 5999 wherein separating at least a portion ofthe ammonia from the produced fluids further comprises separating the produced fluids into one or more fractions, and providing at least a portion ofthe one or more fractions to a stripping unit.

6003. The method of clahn 5999, further comprising using at least a portion ofthe separated ammonia to generate ammonium sulfate.

6004. The method ofclaim 5999, further comprising using at least a portion ofthe separated ammonia to generate urea.

6005. The method ofclaim 5999 wherein the produced fluids comprise carbon dioxide, and further comprising separating the carbon dioxide from the produced fluids, and reacting the carbon dioxide with at least some ammonia to form urea.

6006. The method ofclaim 5999 wherein the produced fluids comprise hydrogen sulfide, and ftirther comprising separating the hydrogen sulfide from the produced fluids, converting at least some hydrogen sulfide into sulfuric acid, and reacting at lest some sulfuric acid with at lease some ammonia to form ammonium sulfate.

6007. The method of claim 5999 wherein the produced fluids further comprise hydrogen sulfide, and further comprising separating at least a portion ofthe hydrogen sulfide from the produced fluids, and converting at least some hydrogen sulfide into sulfuric acid.

6008. The method of claim 5999, further comprising generating ammonium bicarbonate using separated ammonia.

6009. The method of claim 5999, further comprising providing separated ammonia to a fluid comprising carbon dioxide to generate ammonium bicarbonate.

6010. The method of claim 5999, further comprising providing separated ammonia to at least some synthesis gas to generate ammonium bicarbonate.

6011. The method of clahn 5999, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

6012. The method ofclaim 5999, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the foimation is at least about 0.5 bars absolute.

6013. The method of claim 5999, wherein at least one heat source comprises a heater.

6014. A method of generating ammonia from fluids produced from a relatively low permeability formation containing heavy hydrocarbons, comprising: hydrofreating at least a portion ofthe produced fluids to generate ammonia wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the fonnation.

6015. The method of claim 6014 wherein the produced fluids are pyrolyzation fluids.

6016. The method ofclaim 6014, ftuther comprising separating at least a portion ofthe ammonia from the hydrofreated fluids.

6017. The method ofclaim 6014, further comprising using at least a portion ofthe ammonia to generate ammonium sulfate.

6018. The method of claim 6014, further comprising using at least a portion of the ammonia to generate urea.

6019. The method ofclaim 6014 wherein the produced fluids further comprise carbon dioxide, and further comprising separating at least a portion ofthe carbon dioxide from the produced fluids, and reacting at least the portion ofthe carbon dioxide with at least a portion of ammonia to form urea.

6020. The method of claim 6014 wherein the produced fluids further comprise hydrogen sulfide, and further comprishig separating at least a portion ofthe hydrogen sulfide from the produced fluids, converting at least some hydrogen sulfide into sulfuric acid, and reacting at least some sulfuric acid with at least a portion ofthe aimnonia to form ammonium sulfate.

6021. The method ofclaim 6014 wherein the produced fluids further comprise hydrogen sulfide, and further comprising separating at least a portion ofthe hydrogen sulfide from the produced fluids, and converting at least some hydrogen sulfide into sulfuric acid.

6022. The method of claim 6014, further comprising generating ammonium bicarbonate using at least a portion ofthe ammonia.

6023. The method ofclaim 6014, further comprising providing at least a portion ofthe ammonia to a fluid comprishig carbon dioxide to generate ammonium bicarbonate.

6024. The method of claim 6014, further comprising providing at least a portion ofthe ammonia to at least some synthesis gas to generate ammonium bicarbonate

6025. The method ofclaim 6014, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

6026. The method ofclaim 6014, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6027. The method of claim 6014, wherein at least one heat source comprises a heater.

6028. A method of enhancing pyridines production from a relatively low penneability foπnation containing heavy hydrocarbons, comprising: controlling at least one condition within at least a portion ofthe formation to enhance production of pyridines in formation fluid, wherein the formation fluid is obtained by: providing heat from one or more heat sources to at least a portion ofthe fonnation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe foπnation; and producing foπnation fluids from the foπnation.

6029. The method of claim 6028, further comprising separating at least a portion ofthe pyridines from the produced fluids.

6030. The method of claim 6028 wherein controlling at least one condition in the formation comprises confrolling a fluid pressure within at least a portion ofthe formation.

6031. The method ofclaim 6028 wherein confrolling at least one condition in the formation comprises confrolling a temperature gradient within at least a portion of the formation.

6032. The method of claim 6028 wherein controlling at least one condition in the formation comprises confrolling a temperature within at least a portion ofthe formation.

6033. The method of claim 6028 wherein controlling at least one condition in the fonnation comprises controlling a heating rate within at least a portion ofthe foimation.

6034. The method ofclaim 6028, further comprising separating the produced fluids into one or more fractions using distillation.

6035. The method ofclaim 6028, further comprising separating the produced fluids into one or more fractions using condensation.

6036. The method of clahn 6028, further comprising separathig the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and further comprising providmg the heart cut to an extraction unit, and separating at least some pyridines from the heart cut.

6037. The method of clahn 6028, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a pyridines fraction, and further comprising providing the pyridines fraction to an extraction unit, and separating at least some pyridines from the pyridines fraction.

6038. The method ofclaim 6028, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

6039. The method ofclaim 6028, wherein the foπnation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6040. The method ofclaim 6028, wherehi at least one heat source comprises a heater.

6041. A method of separating pyridines from fluids produced from a relatively low permeability foπnation containing heavy hydrocarbons, comprising: separating pyridines from the produced fluids, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the formation wherein the produced fluids comprise pyridines.

6042. The method of clahn 6041, further comprising controlling a fluid pressure within at least a portion ofthe formation.

6043. The method of claim 6041 , further comprising controlling a temperature gradient within at least a portion ofthe fonnation.

6044. The method ofclaim 6041, further comprising controlling a temperature within at least a portion ofthe formation.

6045. The method of claim 6041 , further comprising confrolling a heating rate within at least a portion of the formation

6046. The method ofclaim 6041 wherein separating at least some pyridines from the produced fluids further comprises separating the produced fluids into one or more fractions using distillation.

6047. The method of clahn 6041 wherein separating at least some pyridines from the produced fluids fiuther comprises separating the produced fluids into one or more fractions using condensation.

6048. The method of clahn 6041 wherein separating at least some pyridines from the produced fluids further comprises separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and extracting at least a portion ofthe pyridines from the heart cut.

6049. The method ofclaim 6041 wherein separating at least some pyridines from the produced fluids further comprises removing a naphtha fraction from the produced fluids, and separating at least a portion ofthe pyridines from the naphtha fraction.

6050. The method ofclaim 6041, wherein separathig at least some pyridines from the produced fluids further comprises removing an pyridines fraction from the produced fluids, and separating at least a portion ofthe pyridines from the pyridines fraction.

6051. The method ofclaim 6041, wherein separating the pyridines from the produced fluids further comprises removing pyridines using distillation.

6052. The method of claim 6041 , wherein separating the pyridines from the produced fluids further comprises removing pyridines using crystallization.

6053. The method ofclaim 6041, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

6054. The method ofclaim 6041, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6055. The method of claim 6041 , wherein at least one heat source comprises a heater.

6056. A method of enhancing pynoles production from a relatively low permeability formation containing heavy hydrocarbons, comprising: confrolling at least one condition within at least a portion ofthe formation to enhance production of pynoles in formation fluid, wherein the formation fluid is obtained by: providing heat from one or more heat sources to at least a portion ofthe fonnation; allowing the heat to transfer from at least one or more heat sources to a selected section ofthe foπnation; and producing foπnation fluids from the foπnation.

6057. The method ofclaim 6056, further comprising separating at least a portion ofthe py oles from the produced fluids.

6058. The method of clahn 6056 wherein controlling at least one condition in the formation comprises controlling a fluid pressure within at least a portion of the foimation.

6059. The method of claim 6056 wherein confrolling at least one condition in the formation comprises controlling a temperature gradient within at least a portion ofthe foimation.

6060. The method of claim 6056 wherein controlling at least one condition in the fonnation comprises controlling a temperature withhi at least a portion ofthe formation.

6061. The method of claim 6056 wherein controlling at least one condition in the formation comprises confroUhig a heating rate within at least a portion ofthe foimation.

6062. The method of claim 6056, further comprising separating the produced fluids into one or more fractions using distillation.

6063. The method ofclaim 6056, further comprising separating the produced fluids into one or more fractions using condensation.

6064. The method of clahn 6056, further comprismg separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and further comprising providing the heart cut to an extraction unit, and separating at least some pynoles from the heart cut.

6065. The method ofclaim 6056, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a pynoles fraction, and further comprising providing the pynoles fraction to an exfraction unit, and separating at least some pynoles from the pynoles fraction.

6066. The method of claim 6056, wherein the heat provided from at least one heat source is transfened to the formation substantially by conduction.

6067. The method of claim 6056, wherein the formation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the foimation is at least about 0.5 bars absolute.

6068. The method ofclaim 6056, wherein at least one heat source comprises a heater.

6069. A method of separating pynoles from fluids produced from a relatively low permeability foπnation containing heavy hydrocarbons, comprising: separating pynoles from the produced fluids, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe foπnation; allowing the heat to transfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the foπnation wherein the produced fluids comprise pynoles.

6070. The method ofclaim 6069, further comprising confrolling a fluid pressure within at least a portion ofthe formation.

6071. The method of claim 6069, further comprismg controlling a temperature gradient within at least a portion ofthe formation.

6072. The method ofclaim 6069, further comprising confrolling a temperature within at least a portion ofthe formation.

6073. The method of claim 6069, further comprising controlling a heating rate within at least a portion ofthe formation

6074. The method ofclaim 6069, wherein separating at least some pynoles from the produced fluids further comprises separating the produced fluids into one or more fractions using distillation.

6075. The method of claim 6069, wherein separating at least some pynoles from the produced fluids further comprises separating the produced fluids into one or more fractions using condensation.

6076. The method of clahn 6069, wherehi separating at least some pynoles from the produced fluids further comprises separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and extracting at least a portion ofthe pynoles from the heart cut.

6077. The method ofclaim 6069, wherein separating at least some pynoles from the produced fluids ftirther comprises removing a naphtha fraction from the produced fluids, and separating at least a portion ofthe pynoles from the naphtha fraction.

6078. The method ofclaim 6069, wherein separating at least some pynoles from the produced fluids further comprises removing an pynoles fraction from the produced fluids, and separating at least a portion ofthe pynoles from the pynoles fraction.

6079. The method of claim 6069, wherein separating the pynoles from the produced fluids further comprises removing pynoles using distillation.

6080. The method of claim 6069, wherein separating the pynoles from the produced fluids further comprises removing pynoles using crystallization.

6081. The method of claim 6069, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

6082. The method of claim 6069, wherein the fluids are produced from the foimation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6083. The method of claim 6069, wherein at least one heat source comprises a heater.

6084. A method of enhancing thiophenes production from a relatively low permeability formation containing heavy hydrocarbons, comprising: confrolling at least one condition within at least a portion ofthe foπnation to enhance production of thiophenes in formation fluid, wherein the formation fluid is obtained by: providing heat from one or more heat sources to at least a portion ofthe fonnation; allowing the heat to fransfer from at least one or more heat sources to a selected section ofthe formation; and producing formation fluids from the fonnation.

6085. The method ofclaim 6084, further comprising separating at least a portion ofthe thiophenes from the produced fluids.

6086. The method of claim 6084, wherein controlling at least one condition in the foπnation comprises controlling a fluid pressure within at least a portion ofthe formation.

6087. The method ofclaim 6084, wherein confrolling at least one condition in the formation comprises confrolling a temperature gradient within at least a portion ofthe formation.

6088. The method ofclaim 6084, wherein controlling at least one condition in the formation comprises confrolling a temperature withhi at least a portion ofthe formation.

6089. The method ofclaim 6084, wherein controlling at least one condition in the formation comprises confrolling a heating rate within at least a portion ofthe foimation.

6090. The method ofclaim 6084, further comprising separating the produced fluids into one or more fractions using distillation.

6091. The method of claim 6084, further comprising separating the produced fluids into one or more fractions using condensation.

6092. The method ofclaim 6084, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and further comprising providing the heart cut to an exfraction unit, and separating at least some thiophenes from the heart cut.

6093. The method of claim 6084, further comprising separating the produced fluids into one or more fractions wherein the one or more fractions comprise a thiophenes fraction, and further comprising providing the thiophenes fraction to an extraction unit, and separating at least some thiophenes from the thiophenes fraction.

6094. The method ofclaim 6084, wherehi the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

6095. The method of claim 6084, wherein the formation fluids are produced from the formation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6096. The method of claim 6084, wherein at least one heat source comprises a heater.

6097. A method of separating thiophenes from fluids produced from a relatively low peπneability formation containing heavy hydrocarbons, comprising: separating thiophenes from the produced fluids, wherein the produced fluids are obtained by: providing heat from one or more heat sources to at least a portion ofthe foimation; allowing the heat to transfer from at least one or more heat sources to a selected section ofthe formation; and producing fluids from the formation wherein the produced fluids comprise thiophenes.

6098. The method ofclaim 6097, further comprising confrolling a fluid pressure within at least a portion ofthe formation.

6099. The method of claim 6097, further comprising controlling a temperature gradient within at least a portion ofthe formation.

6100. The method ofclaim 6097, further comprising conttoUing a temperature within at least a portion ofthe foπnation.

6101. The method ofclaim 6097, further comprising controlling a heating rate within at least a portion ofthe fonnation

6102. The method of claim 6097, wherein separating at least some thiophenes from the produced fluids further comprises separating the produced fluids into one or more fractions using distillation.

6103. The method ofclaim 6097, wherein separating at least some thiophenes from the produced fluids further comprises separating the produced fluids into one or more fractions using condensation.

6104. The method of claim 6097, wherein separating at least some thiophenes from the produced fluids further comprises separating the produced fluids into one or more fractions wherein the one or more fractions comprise a heart cut, and extracting at least a portion ofthe thiophenes from the heart cut.

6105. The method of claim 6097, wherein separating at least some thiophenes from the produced fluids further comprises removing a naphtha fraction from the produced fluids, and separating at least a portion ofthe thiophenes from the naphtha fraction.

6106. The method ofclaim 6097, wherein separating at least some thiophenes from the produced fluids further comprises removing an thiophenes fraction from the produced fluids, and separating at least a portion ofthe thiophenes from the thiophenes fraction.

6107. The method of claim 6097, wherein separating the thiophenes from the produced fluids further comprises removing thiophenes using distillation.

6108. The method of claim 6097, wherein separating the thiophenes from the produced fluids further comprises removing thiophenes using crystallization.

6109. The method ofclaim 6084, wherein the heat provided from at least one heat source is fransfened to the formation substantially by conduction.

6110. The method of claim 6084, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the foimation is at least about 0.5 bars absolute.

6111. The method of clahn 6084, wherein at least one heat source comprises a heater.

6112. A method of treating a relatively low permeability formation containing heavy hydrocarbons comprising: providing a barrier to at least a portion ofthe formation to inhibit migration of fluids into or out of a freatment area ofthe foimation; providing heat from one or more heat sources to the freatment area; allowing the heat to transfer from the treatment area to a selected section ofthe formation; and producing fluids from the formation.

6113. The method of claim 6112, wherein the heat provided from at least one of the one or more heat sources is fransfened to at least a portion ofthe foimation substantially by conduction.

6114. The method of claim 6112, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the fonnation is at least about 0.5 bars absolute.

6115. The method of claim 6112, wherein at least one of the one or more of the heat sources comprises a heater.

6116. The method of claim 6112, further comprising hydraulically isolating the treatment area from a sunounding portion of the formation.

6117. The method ofclaim 6112, further comprising pyrolyzing at least a portion of hydrocarbon containing material within the treatment area.

6118. The method of claim 6112, further comprising generating synthesis gas in at least a portion of the treatment area.

6119. The method ofclaim 6112, further comprising controlling a pressure within the freatment area.

6120. The method ofclaim 6112, further comprising controlling a temperature within the freatment area.

6121. The method of claim 6112, further comprising confrolling a heating rate within the freatment area.

6122. The method ofclaim 6112, further comprising controlling an amount of fluid removed from the freatment area.

6123. The method of claim 6112, wherein at least section of the banier comprises one or more sulfur wells.

6124. The method ofclaim 6112, wherein at least section ofthe banier comprises one or more dewatering wells.

6125. The method ofclaim 6112, wherein at least section ofthe banier comprises one or more injection wells and one or more dewatering wells.

6126. The method ofclaim 6112, wherein providing a banier comprises: providing a circulating fluid to the a portion ofthe formation sunounding the treatment area; and removing the circulating fluid proximate the freatment area.

6127. The method ofclaim 6112, wherein at least section ofthe banier comprises a ground cover on a surface of the earth.

6128. The method ofclaim 6127, wherein at least section ofthe ground cover is sealed to a surface ofthe earth.

6129. The method ofclaim 6112, further comprising inhibiting a release of formation fluid to the earth's atmosphere with a ground cover; and freezing at least a portion ofthe ground cover to a surface ofthe earth.

6130. The method of claim 6112, further comprising inhibiting a release of formation fluid to the earth's atmosphere.

6131. The method ofclaim 6112, further comprising inhibiting fluid seepage from a surface ofthe earth into the freatment area.

6132. The method ofclaim 6112, wherein at least a section ofthe banier is naturally occuning.

6133. The method ofclaim 6112, wherein at least a section ofthe banier comprises a low temperature zone.

6134. The method ofclaim 6112, wherein at least a section ofthe banier comprises a frozen zone.

6135. The method of claim 6112, wherein the banier comprises an installed portion and a naturally occuning portion.

6136. The method of claim 6112, further comprising: hydraulically isolating the treatment area from a sunounding portion ofthe formation; and maintaining a fluid pressure within the freatment area at a pressure greater than about a fluid pressure within the sunounding portion ofthe foπnation.

6137. The method of claim 6112, wherein at least a section of the banier comprises an impermeable section of the formation.

6138. The method of claim 6112, wherein the banier comprises a self-sealing portion.

6139. The method of claim 6112, wherein the one or more heat sources are positioned at a distance greater than about 5 m from the banier.

6140. The method ofclaim 6112, wherein at least one ofthe one or more heat sources is positioned at a distance less than about 1.5 m from the banier.

6141. The method ofclaim 6112, wherein at least a portion ofthe banier comprises a low temperature zone, and further comprising lowering a temperature within the low temperature zone to a temperature less than about a freezing temperature of water.

6142. The method ofclaim 6112, wherein the banier comprises a banier well and further comprising positioning at least a portion ofthe banier well below a water table ofthe foimation.

6143. The method of claim 6112, wherein the freatment area comprises a ffrst freatment area and a second freatment area, and further comprising: freating the first freatment area using a first freatment process; and freating the second treatment area using a second freatment process.

6144. A method of freating a relatively low peπneability foπnation containing heavy hydrocarbons in situ, comprising: providing a refrigerant to a plurality of banier wells placed in a portion ofthe formation; establishing a frozen banier zone to inhibit migration of fluids into or out of a freatment area; providing heat from one or more heat sources to the treatment area; allowing the heat to transfer from the freatment area to a selected section; and producing fluids from the formation.

6145. The method ofclaim 6144, wherein the heat provided from at least one ofthe one or more heat sources is transfened to at least a portion ofthe fomiation substantially by conduction.

6146. The method ofclaim 6144, wherein the fluids are produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6147. The method ofclaim 6144, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6148. The method of claim 6144, further comprising controlling a fluid pressure within the freatment area;

6149. The method ofclaim 6144, wherein the frozen banier zone is proximate the treatment area ofthe formation

6150. The method ofclaim 6144, further comprising hydraulically isolating the treatment area from a sunounding portion ofthe formation.

6151. The method of claim 6144, further comprising thermally isolating the treatment area from a sunounding portion ofthe formation

6152. The method of claim 6144, further comprising maintaining the fluid pressure above a hydrostatic pressure ofthe foimation

6153. The method ofclaim 6144, further comprising removing liquid water from at least a portion ofthe freatment area.

6154. The method ofclaim 6144, wherein the treatment area is below a water table ofthe formation.

6155. The method ofclaim 6144, wherein at least one banier well ofthe plurality of banier wells comprises a conosion inhibitor.

6156. The method of claim 6144, wherein heating is initiated after foimation ofthe frozen banier zone.

6157. The method ofclaim 6144, wherein the refrigerant comprises one or more hydrocarbons.

6158. The method of claim 6144, wherein the refrigerant comprises propane. ^'

6159. The method ofclaim 6144, wherein the refrigerant comprises isobutane.

6160. The method of claim 6144, wherein the refrigerant comprises cyclopentane.

6161. The method of claim 6144, wherein the refrigerant comprises ammonia.

6162. The method ofclaim 6144, wherehi the refrigerant comprises an aqueous salt mixture.

6163. The method of claim 6144, wherein the refrigerant comprises an organic acid salt.

6164. The method of claim 6144, wherein the refrigerant comprises a salt of an organic acid.

6165. The method of claim 6144, wherein the refrigerant comprises an organic acid.

6166. The method ofclaim 6144, wherein the refrigerant has a freezing point of less than about minus 60 degrees Celsius.

6167. The method ofclaim 6144, wherein the refrigerant comprises calcium chloride.

6168. The method ofclaim 6144, wherein the refrigerant comprises lithium chloride.

6169. The method ofclaim 6144, wherein the refrigerant comprises liquid nifrogen.

6170. The method of claim 6144, wherein the refrigerant is provided at a temperature of less than about minus 50 degrees Celsius.

6171. The method of claim 6144, wherein the refrigerant comprises carbon dioxide.

6172. The method of claim 6144, wherein at least one ofthe plurality of banier wells is located along sfrike of a hydrocarbon containing portion ofthe foimation.

6173. The method of claim 6144, wherein at least one of the plurality of banier wells is located along dip of a hydrocarbon containing portion ofthe formation.

6174. The method ofclaim 6144, wherein the one or more heat sources are placed greater than about 5 m from a frozen banier zone.

6175. The method ofclaim 6144, wherein at least one ofthe one or more heat sources is positioned less than about 1.5 m from a frozen banier zone.

6176. The method ofclaim 6144, wherein a distance between a center of at least one banier well and a center of at least one adjacent banier well is greater than about 2 m.

6177. The method of claim 6144, further comprising desorbing methane from the formation.

6178. The method ofclaim 6144, further comprising pyrolyzing at least some hydrocarbon containing material within the freatment area.

6179. The method ofclaim 6144, further comprising producing synthesis gas from at least a portion ofthe formation.

6180. The method ofclaim 6144, further comprising: providing a solvent to the treatment area such that the solvent dissolves a component in the treatment area; and removing the solvent from the treatment area, wherehi the removed solvent comprises the component.

6181. The method of claim 6144, further comprising sequestering a compound in at least a portion of the freatment area.

6182. The method of clahn 6144, further comprising thawing at least a portion ofthe frozen banier zone; and wherein material in a thawed banier zone area is substantially unaltered by the application of heat.

6183. The method of claim 6144, wherein a location ofthe frozen banier zone has been selected using a flow rate of groundwater and wherein the selected groundwater flow rate is less than about 50 m/day.

6184. The method of claim 6144, further comprising providing water to the frozen banier zone.

6185. The method ofclaim 6144, further comprising positioning one or more monitoring wells outside the frozen banier zone, and then providing a tracer to the freatment area, and then monitoring for movement ofthe tracer at the monitoring wells.

6186. The method of claim 6144, further comprising: positioning one or more monitoring wells outside the frozen banier zone; then providing an acoustic pulse to the treatment area; and then monitoring for the acoustic pulse at the monitoring wells.

6187. The method ofclaim 6144, wherein a fluid pressure within the treatment area can be controlled at fluid pressures different from a fluid pressure that exists in a sunounding portion ofthe formation.

6188. The method ofclaim 6144, wherein fluid pressure within an area at least partially bounded by the frozen banier zone can be confrolled higher than, or lower than, hydrostatic pressures that exist in a sunounding portion of the formation.

6189. The method ofclaim 6144, further comprising controlling compositions of fluids produced from the formation by confrolling the fluid pressure within an area at least partially bounded by the frozen banier zone.

6190. The method of claim 6144, wherein a portion of at least one ofthe plurality of banier wells is positioned below a water table ofthe foimation.

6191. A method of treating a relatively low permeability formation containing heavy hydrocarbons comprising: providing a refrigerant to one or more banier wells placed in a portion ofthe formation; establishing a low temperature zone proxhnate a treatment area ofthe foimation; providing heat from one or more heat sources to a freatment area ofthe formation; allowing the heat to fransfer from the treatment area to a selected section ofthe formation; and producing fluids from the formation.

6192. The method of claim 6191, further comprising forming a frozen banier zone within the low temperature zone, wherein the frozen barrier zone hydraulically isolates the freatment area from a sunounding portion ofthe foimation.

6193. The method of claim 6191, further comprising forming a frozen banier zone within the low temperature zone, and wherein fluid pressure within an area at least partially bounded by the frozen banier zone can be confrolled at different fluid pressures from the fluid pressures that exist outside ofthe frozen banier zone.

6194. The method of claim 6191, further comprising fonning a frozen banier zone within the low temperature zone, and wherein fluid pressure within an area at least partially bounded by the frozen banier zone can be controlled higher than, or lower than, hydrostatic pressures that exist outside ofthe frozen banier zone.

6195. The method of claim 6191, further comprising forming a frozen banier zone within the low temperature zone, and wherein fluid pressure within an area at least partially bounded by the frozen banier zone can be confrolled higher than, or lower than, hydrostatic pressures that exist outside ofthe frozen banier zone, and further comprising controlling compositions of fluids produced from the formation by controlling the fluid pressure within the area at least partially bounded by the frozen banier zone.

6196. The method of claim 6191, further comprising thawing at least a portion of the low temperature zone, wherein material within the thawed portion is substantially unaltered by the application of heat such that the structural integrity ofthe relatively low permeability formation containing heavy hydrocarbons is substantially maintained.

6197. The method of claim 6191, wherein an inner boundary ofthe low temperature zone is determined by monitoring a pressure wave using one or more piezometers.

6198. The method ofclaim 6191, further comprising confrolling a fluid pressure within the treatment area at a pressure less than about a foimation fracture pressure.

6199. The method of claim 6191, further comprising positioning one or more monitoring wells outside the frozen banier zone, and then providing an acoustic pulse to the treatment area, and then monitoring for the acoustic pulse at the monitoring wells.

6200. The method ofclaim 6191, further comprising positioning a segment of at least one ofthe one or more banier wells below a water table ofthe formation.

6201. The method of claim 6191, further comprising positioning the one or more banier wells to establish a continuous low temperature zone.

6202. The method ofclaim 6191, wherein the refrigerant comprises one or more hydrocarbons.

6203. The method ofclaim 6191, wherein the refrigerant comprises propane.

6204. The method ofclaim 6191, wherein the refrigerant comprises isobutane.

6205. The method of claim 6191, wherein the refrigerant comprises cyclopentane.

6206. The method of claim 6191, wherein the refrigerant comprises ammonia.

6207. The method of claim 6191, wherein the refrigerant comprises an aqueous salt mixture.

6208. The method ofclaim 6191, wherein the refrigerant comprises an organic acid salt.

6209. The method of claim 6191, wherein the refrigerant comprises a salt of an organic acid.

6210. The method ofclaim 6191, wherein the refrigerant comprises an organic acid.

6211. The method ofclaim 6191, wherein the refrigerant has a freezing point of less than about minus 60 degrees Celsius.

6212. The method of claim 6191, wherein the refrigerant is provided at a temperature of less than about minus 50 degrees Celsius.

6213. The method of claim 6191, wherein the refrigerant is provided at a temperature of less than about minus 25 degrees Celsius.

6214. The method ofclaim 6191, wherein the refrigerant comprises carbon dioxide.

6215. The method of claim 6191, further comprising: cooling at least a portion ofthe refrigerant in an absoφtion refrigeration unit; and providing a thermal energy source to the absoφtion refrigeration unit.

6216. The method ofclaim 6191, wherein the thermal energy source comprises water.

6217. The method of claim 6191, wherein the theπnal energy source comprises steam.

6218. The method of claim 6191, wherein the thermal energy source comprises at least a portion of the produced fluids.

6219. The method ofclaim 6191, wherein the thermal energy source comprises exhaust gas.

6220. A method of treating a relatively low permeability foπnation containing heavy hydrocarbons, comprising: inhibiting migration of fluids into or out of a treatment area ofthe formation from a sunounding portion of the foπnation; providing heat from one or more heat sources to at least a portion ofthe freatment area; allowing the heat to transfer from at least the portion to a selected section ofthe formation; and producing fluids from the foπnation.

6221. The method of claim 6220, wherein the heat provided from at least one ofthe one or more heat sources is fransfened to at least a portion ofthe formation substantially by conduction.

6222. The method of claim 6220, wherein the fluids are produced from the foimation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6223. The method of claim 6220, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6224. The method of claim 6220, further comprising providing a banier to at least a portion ofthe formation.

6225. The method ofclaim 6224, wherein at least section ofthe banier comprises one or more sulfur wells.

6226. The method of claim 6224, wherein at least section ofthe banier comprises one or more pumping wells.

6227. The method ofclaim 6224, wherein at least section ofthe banier comprises one or more injection wells and one or more pumping wells.

6228. The method of claim 6224, wherein at least a section ofthe banier is naturally occuning.

6229. The method of claim 6220, further comprises establishing a banier in at least a portion ofthe foπnation, and wherein heat is provided after at least a portion ofthe banier has been established.

6230. The method ofclaim 6220, further comprising establishing a banier in at least a portion ofthe formation, and wherein heat is provided while at least a portion ofthe banier is being established.

6231. The method of claim 6220, further comprising providing a banier to at least a portion ofthe formation, and wherein heat is provided before the banier is established.

6232. The method ofclaim 6220, further comprising controlling an amount of fluid removed from the freatment area.

6233. The method ofclaim 6220, wherein isolating a freattnent area from a sunounding portion ofthe formation comprises providing a low temperature zone to at least a portion ofthe foimation.

6234. The method ofclaim 6220, wherein isolating a treatment area from a sunounding portion ofthe formation comprises providing a frozen banier zone to at least a portion ofthe formation.

6235. The method ofclaim 6220, wherein isolating a treatment area from a sunounding portion ofthe formation comprises providing a grout wall.

6236. The method of clahn 6220, further comprising inhibiting flow of water into or out of at least a portion of a treatment area.

6237. The method of claim 6220, further comprising: providing a material to the treatment area; and storing at least some ofthe material within the freatment area.

6238. A method of treating a relatively low peπneability fonnation containing heavy hydrocarbons, comprising: providing a barrier to a portion ofthe foπnation, wherein the portion has previously undergone an in situ conversion process; and inhibiting migration of fluids into and out ofthe converted portion to a sunounding portion ofthe formation.

6239. The method of claim 6238, wherein the banier comprises a frozen banier zone.

6240. The method ofclaim 6238, wherein the banier comprises a low temperature zone.

6241. The method ofclaim 6238, wherein the banier comprises a sealing mineral phase.

6242. The method of claim 6238, wherein the banier comprises a sulfur banier.

6243. The method of claim 6238, wherein the contaminant comprises a metal.

6244. The method ofclaim 6238, wherein the contaminant comprises organic residue.

6245. A method of freating a relatively low penneability foimation containing heavy hydrocarbons, comprising: infroducing a first fluid into at least a portion ofthe formation, wherein the portion has previously undergone an in situ conversion process; producing a mixture ofthe ffrst fluid and a second fluid from the formation; and providing at least a portion ofthe mixture to an energy producing unit.

6246. The method of claim 6245, wherein the ffrst fluid is selected to recover heat from the foπnation.

6247. The method of claim 6245, wherein the first fluid is selected to recover heavy compounds from the formation.

6248. The method ofclaim 6245, wherein the first fluid is selected to recover hydrocarbons from the fonnation.

6249. The method of clahn 6245, wherein the mixture comprises an oxidizable heat recovery fluid.

6250. The method of claim 6245, wherein producing the mixture remediates the portion ofthe foimation by removing contaminants from the formation in the mixture.

6251. The method of clahn 6245, wherein the first fluid comprises a hydrocarbon fluid.

6252. The method of claim 6245, wherein the first fluid comprises methane.

6253. The method of claim 6245, wherein the first fluid comprises ethane.

6254. The method of claim 6245, wherein the first fluid comprises molecular hydrogen.

6255. The method of claim 6245, wherein the energy producing unit comprises a turbine, and generating electricity by passing mixture through the energy producing unit.

6256. The method of claim 6245, further comprising combusting mixture within the energy producing unit.

6257. The method ofclaim 6245, further comprising inhibiting spread ofthe mixttire from the portion ofthe formation with a banier.

6258. A method of freating a relatively low peπneability formation containing heavy hydrocarbons, comprising: providing a first fluid to at least a portion of a freatment area, wherein the freatment area includes one or more components; producing a fluid from the foimation wherein the produced fluid comprises first fluid and at least some of the one or more components; and wherein the freatment area is obtained by providing heat from heat sources to a portion of a relatively low permeability foπnation containing heavy hydrocarbons to convert a portion of hydrocarbons to desired products and removing a portion ofthe desfred hydrocarbons from the foimation.

6259. The method of claim 6258, wherein the first fluid comprises water.

6260. The method ofclaim 6258, wherein the first fluid comprises carbon dioxide.

6261. The method ofclaim 6258, wherein the first fluid comprises steam.

6262. The method ofclaim 6258, wherein the ffrst fluid comprises afr.

6263. The method ofclaim 6258, wherein the first fluid comprises a combustible gas.

6264. The method of clahn 6258, wherein the first fluid comprises hydrocarbons.

6265. The method of clahn 6258, wherein the first fluid comprises methane.

6266. The method ofclaim 6258, wherein the first fluid comprises ethane.

6267. The method ofclaim 6258, wherein the first fluid comprises molecular hydrogen.

6268. The method ofclaim 6258, wherein the first fluid comprises propane.

6269. The method ofclaim 6258, further comprising reacting a portion ofthe contaminants with the first fluid.

6270. The method of claim 6258, further comprising providing at least a portion ofthe produced fluid to an energy generating unit to generate electticity.

6271. The method ofclaim 6258, further comprising providing at least a portion ofthe produced fluid to a combustor.

6272. The method ofclaim 6258, wherein a frozen banier defines at least a segment of a banier within the formation, allowing a portion ofthe frozen banier to thaw prior to providing the first fluid to the treatment area, and providing at least some ofthe first fluid into the thawed portion ofthe barrier.

6273. The method of claim 6258, wherein a volume of first fluid provided to the freatment area is greater than about one pore volume ofthe treatment area.

6274. The method of claim 6258, further comprising separating contaminants from the first fluid.

6275. A method of recovering thermal energy from a heated relatively low permeability foπnation containing heavy hydrocarbons, comprising: injecting a heat recovery fluid into a heated portion ofthe formation; allowing heat from the portion ofthe foimation to transfer to the heat recovery fluid; and producing fluids from the foimation.

6276. The method of claim 6275, wherein the heat recovery fluid comprises water.

6277. The method of claim 6275, wherein the heat recovery fluid comprises saline water.

6278. The method of claim 6275, wherein the heat recovery fluid comprises non-potable water.

6279. The method ofclaim 6275, wherein the heat recovery fluid comprises alkaline water.

6280. The method of claim 6275, wherein the heat recovery fluid comprises hydrocarbons.

6281. The method of claim 6275, wherein the heat recovery fluid comprises an inert gas.

6282. The method of claim 6275, wherein the heat recovery fluid comprises carbon dioxide.

6283. The method of claim 6275, wherein the heat recovery fluid comprises a product stteam produced by an in situ conversion process.

6284. The method of claim 6275, further comprising vaporizing at least some ofthe heat recovery fluid.

6285. The method ofclaim 6275, wherein an average temperature ofthe portion ofthe post treatment foimation prior to injection of heat recovery fluid is greater than about 300°C.

6286. The method ofclaim 6275, further comprising providing the heat recovery fluid to the formation through a heater well.

6287. The method ofclaim 6275, wherehi fluids are produced from one or more production wells in the foimation.

6288. The method ofclaim 6275, further comprising providing at least some ofthe produced fluids to a treatment process in a section ofthe formation.

6289. The method ofclaim 6275, further comprising recovering at least some ofthe heat from the produced fluids.

6290. The method ofclaim 6275, further comprising providing at least some ofthe produced fluids to a power generating unit.

6291. The method ofclaim 6275, further comprising providing at least some ofthe produced fluids to a heat exchange mechanism.

6292, The method ofclaim 6275, further comprising providing at least some ofthe produced fluids to a steam cracking unit.

6293. The method of clahn 6275, further comprising providing at least some of the produced fluids to a hydrofreating unit.

6294. The method ofclaim 6275, further comprising providing at least some ofthe produced fluids to a distillation column.

6295. The method of claim 6275, wherein the heat recovery fluid comprises carbon dioxide, and wherein at least some ofthe carbon dioxide is adsorbed onto the surface of carbon in the formation.

6296. The method of claim 6275, wherein the heat recovery fluid comprises carbon dioxide, and further comprising: allowing at least some hydrocarbons within the formation to desorb from the formation; and producing at least some ofthe desorbed hydrocarbons from the formation.

6297. The method of claim 6275, further comprising providing at least some ofthe produced fluids to a freatment process in a section ofthe formation.

6298. The method of claim 6275, wherein the heat recovery fluid is saline water, and further comprising: providing carbon dioxide to the portion ofthe formation; and precipitating carbonate compounds.

6299. The method of claim 6275, further comprismg reducing an average temperature ofthe foimation to a temperature less than about an ambient boiling temperature of water at a post freatment pressure.

630,0. The method of claim 6275, wherein the produced fluids comprise low molecular weight hydrocarbons.

6301. The method of claim 6275, wherein the produced fluids comprise hydrocarbons.

6302. The method of claim 6275, wherein the produced fluids comprise heat recovery fluid.

6303. A method of freating a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to at least a portion ofthe formation; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe formation; controlling at least one condition within the selected section; producing a mixture from the formation; and wherein at least the one condition is controlled such that the mixture comprises a carbon dioxide emission level less than about a selected carbon dioxide emission level.

6304. The method ofclaim 6303, wherein the heat provided from at least one heat source is fransfened to at least a portion ofthe foimation substantially by conduction.

6305. The method ofclaim 6303, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6306. The method ofclaim 6303, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6307. The method ofclaim 6303, wherein the selected carbon dioxide emission level is less than about 5.6 x 10-8 kg C02 produced for every Joule of energy.

6308. The method ofclaim 6303, wherein the selected carbon dioxide emission level is less than about 1.6 x 10-8 kg C02 produced for every Joule of energy.

6309. The method ofclaim 6303, wherein the selected carbon dioxide emission level is less than about 1.6 x 10- 10 kg C02 produced for eveiy Joule of energy.

6310. The method ofclaim 6303, further comprising blending the mixture with a fluid to form a blended product comprising a carbon dioxide emission level less than about the selected baseline carbon dioxide emission level.

6311. The method ofclaim 6303, wherein confrolling conditions within a selected section comprises confrolling a pressure within the selected section.

6312. The method ofclaim 6303, wherein confrolling conditions within a selected section comprises controlling an average temperature within the selected section.

6313. The method of claim 6303, wherein confrolling conditions within a selected section comprises controlling an average heating rate within the selected section.

6314. A method for producing molecular hydrogen from a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to at least one portion ofthe formation such that carbon dioxide production is minimized; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe foimation; producing a mixture comprising molecular hydrogen from the formation; and controlling the heat from the one or more heat sources to enhance production of molecular hydrogen.

6315. The method of claim 6314, wherein the heat provided from at least one heat source is transfened to at least a portion ofthe formation substantially by conduction.

6316. The method ofclaim 6314, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6317. The method of claim 6401 , wherein the mixture is produced from the fonnation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6318. The method ofclaim 6314, wherein confrolling the heat comprises confroUing a temperature proximate the production wellbore at or above a decomposition temperature of methane.

6319. The method ofclaim 6314, wherein heat is generated by oxidizing molecular hydrogen in at least one heat source.

6320. The method of claim 6314, wherein heat is generated by electricity produced from wind power.

6321. The method of claim 6314, wherein heat is generated from elecfrical power.

6322. The method of claim 6314, wherein the heat sources form an anay of heat sources.

6323. The method of claim 6314, further comprising heating at least a portion ofthe selected section ofthe formation to greater than about 600 °C.

6324. The method ofclaim 6314, wherein the produced mixture is produced from a production wellbore, and further comprising controlling the heat from one or more heat sources such that the temperature in the formation proximate the production wellbore is at least about 600 °C.

6325. The method ofclaim 6314, wherein the produced mixture is produced from a production wellbore, and further comprising heating at least a portion ofthe formation with a heater proximate the production wellbore.

6326. The method of claim 6314, further comprishig recycling at least a portion ofthe produced molecular hydrogen into the formation.

6327. The method of claim 6314, wherein the produced mixture comprises methane, and ftirther comprising oxidizing at least a portion ofthe methane to provide heat to the foimation.

6328. The method ofclaim 6314, wherein controlling the heat comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

6329. The method of claim 6314, wherein the one or more heat sources comprise one or more electrical heaters powered by a fuel cell, and wherein at least a portion ofthe molecular hydrogen in the produced mixture is used in the fuel cell.

6330. The method of claim 6314, further comprising confrolling a pressure within at least a majority ofthe selected section ofthe foπnation.

6331. The method ofclaim 6314, further comprising confrolling the heat such that an average heating rate ofthe selected section is less than about 3 °C per day during pyrolysis.

6332. The method ofclaim 6314, wherein allowing the heat to ttansfer from the one or more heat sources to the selected section comprises fransfening heat substantially by conduction.

6333. The method ofclaim 6314, wherein at least 50% by volume ofthe produced mixture comprises molecular hydrogen.

6334. The method ofclaim 6314, wherein less than about 3.3 x 10-8 kg C02 is produced for every Joule of energy in the produced mixture.

6335. The method ofclaim 6314, wherein less than about 1.6 x 10-10 kg C02 is produced for every Joule of energy in the produced mixture.

6336. The method ofclaim 6314, wherein less than about 3.3 x 10-10 kg C02 is produced for every Joule of energy in the produced mixture.

6337. The method ofclaim 6314, wherein the produced mixture is produced from a production wellbore, and further comprising controlling the heat from one or more heat sources such that the temperature in the formation proximate the production wellbore is at least about 500 °C.

6338. The method of claim 6314, wherein the produced mixture comprises methane and molecular hydrogen, and further comprising: separating at least a portion ofthe molecular hydrogen from the produced mixture; and providing at least a portion ofthe separated mixture to at least one ofthe one or more heat sources for use as fuel.

6339. The method ofclaim 6314, wherein the produced mixture comprises methane and molecular hydrogen, and further comprising: separating at least a portion ofthe molecular hydrogen from the produced mixture; and providing at least some ofthe molecular hydrogen to a fuel cell to generate electricity.

6340. A method for producing methane from a relatively low permeability foπnation containing heavy hydrocarbons in situ while minimizing production of C02, comprising: providing heat from one or more heat sources to at least one portion ofthe formation such that C02 production is minimized; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe foπnation; producing a mixture comprising methane from the formation; and confrolling the heat from the one or more heat sources to enhance production of methane.

6341. The method ofclaim 6340, wherein the heat provided from at least one ofthe one or more heat source is transfened to at least a portion ofthe foπnation substantially by conduction.

6342. The method ofclaim 6340, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6343. The method ofclaim 6340, wherein controlling the heat comprises confrolling a temperature proximate the production wellbore at or above a decomposition temperature of ethane.

6344. The method ofclaim 6340, wherein heat is generated by oxidizing methane in at least one heat source.

6345. The method ofclaim 6340, wherein heat is generated by electticity produced from wind power.

6346. The method of claim 6340, wherein heat is generated from electtical power.

6347. The method ofclaim 6340, wherein the heat sources form an anay of heat sources.

6348. The method ofclaim 6340, further comprising heating at least a portion ofthe selected section ofthe formation to greater than about 400 °C.

6349. The method of claim 6340, wherein the produced mixture is produced from a production wellbore, and further comprising confrolling the heat from one or more heat sources such that the temperature in the foimation proximate the production wellbore is at least about 400 °C.

6350. The method ofclaim 6340, wherein the produced mixture is produced from a production wellbore, and further comprising heating at least a portion ofthe formation with a heater proximate the production wellbore.

6351. The method ofclaim 6340, further comprising recycling at least a portion ofthe produced methane into the formation.

6352. The method ofclaim 6340, wherein the produced mixture comprises methane, and further comprising oxidizing at least a portion ofthe methane to provide heat to the formation.

6353. The method ofclaim 6340, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section ofthe formation.

6354. The method of claim 6340, wherein confrolling the heat comprises maintaining a temperature within the selected section within a pyrolysis temperature range.

6355. The method ofclaim 6340, wherein the one or more heat sources comprise one or more electrical heaters powered by a fuel cell, and wherein at least a portion ofthe molecular hydrogen in the produced mixture is used in the fuel cell.

6356. The method ofclaim 6340, further comprismg controlling a pressure within at least a majority ofthe selected section ofthe formation.

6357. The method ofclaim 6340, further comprising controlling the heat such that an average heathig rate ofthe selected section is less than about 3 °C per day during pyrolysis.

6358. The method of clahn 6340, wherein allowing the heat to fransfer from the one or more heat sources to the selected section comprises transferring heat substantially by conduction.

6359. The method ofclaim 6340, wherein less than about 8.4 x 10-8 kg C02 is produced for every Joule of energy in the produced mixture.

6360. The method ofclaim 6340, wherein less than about 7.4 x 10-8 kg C02 is produced for every Joule of energy in the produced mixture.

6361. The method ofclaim 6340, wherein less than about 5.6 x 10-8 kg C02 is produced for every Joule of energy in the produced mixture.

6362. A method for upgrading hydrocarbons in a relatively low permeability formation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to a portion ofthe formation; allowing the heat to ttansfer from the first portion to a selected section ofthe formation; providing hydrocarbons to the selected section; and producing a mixture from the formation, wherein the mixture comprises hydrocarbons that were provided to the selected section and upgraded in the formation.

6363. The method of claim 6362, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the foimation is at least about 0.5 bars absolute.

6364. The method ofclaim 6362, wherehi the heat provided from at least one heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6365. The method ofclaim 6362, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6366. The method ofclaim 6362, wherein the provided hydrocarbons comprise heavy hydrocarbons.

6367. The method ofclaim 6362, wherein the provided hydrocarbons comprise naphtha.

6368. The method ofclaim 6362, wherein the provided hydrocarbons comprise asphaltenes.

6369. The method ofclaim 6362, wherehi the provided hydrocarbons comprise crade oil.

6370. The method ofclaim 6362, wherein the provided hydrocarbons comprise surface mined tar from relatively permeable formations.

6371. The method ofclaim 6362 wherein the provided hydrocarbons comprise an emulsion produced from a relatively permeable formation, and further comprising providing the produced emulsion to the first portion after a temperature in the selected section is greater than about a pyrolysis temperature.

6372. The method of clahn 6362, further comprising providing steam to the selected section.

6373. The method of claim 6362, further comprising: producing foimation fluids from the formation; separating the produced formation fluids into one or more components; and wherein the provided hydrocarbons comprise at least one ofthe one or more components.

6374. The method ofclaim 6362, further comprising: providing steam to the selected section, wherein the provided hydrocarbons are mixed with the steam; and controlling an amount of steam such that a residence time ofthe provided hydrocarbons within the selected section is controlled.

6375. The method ofclaim 6362, wherein the produced mixture comprises upgraded hydrocarbons, and ftirther comprising confrolling a residence time ofthe provided hydrocarbons within the selected section to control a molecular weight disttibution within the upgraded hydrocarbons.

6376. The method ofclaim 6362, wherein the produced mixture comprises upgraded hydrocarbons, and further comprising confrolling a residence time ofthe provided hydrocarbons in the selected section to confrol an API gravity ofthe upgraded hydrocarbons.

6377. The method ofclaim 6362, further comprising steam cracking in at least a portion ofthe selected section.

6378. The method ofclaim 6362, wherein the provided hydrocarbons are produced from a second portion ofthe foimation.

6379. The method of claim 6362, further comprising allowing some ofthe provided hydrocarbons to crack in the foimation to generate upgraded hydrocarbons.

6380. The method of claim 6362, further comprising controlling a temperature ofthe ffrst portion ofthe formation by confrolling a pressure and a temperature within at least a majority ofthe selected section ofthe foimation, wherein the pressure is conttolled as a function of temperature, or the temperature is conttolled as a function of pressure.

6381. The method of claim 6362, further comprising confrolling a pressure within at least a majority ofthe selected section ofthe formation.

6382. The method ofclaim 6362, wherein a temperature in the first portion is greater than about a pyrolysis temperature.

6383. The method of claim 6362, further comprising: confrolling the heat such that a temperature ofthe ffrst portion is greater than about a pyrolysis temperature of hydrocarbons; and producing at least some ofthe provided hydrocarbons from the first portion ofthe formation.

6384. The method of claim 6362, further comprising producing at least some ofthe provided hydrocarbons from a second portion of the formation.

6385. The method of claim 6362, further comprising: confrolling the heat such that a temperature of a second portion is less than about a pyrolysis temperature of hydrocarbons; and producing at least some ofthe provided hydrocarbons from the second portion ofthe formation..

6386. The method of claim 6362, further comprismg producing at least some ofthe provided hydrocarbons from a second portion ofthe foimation and wherein a temperature ofthe second portion is about an ambient temperature ofthe formation.

6387. The method of claim 6362, wherein the upgraded hydrocarbons are produced from a production well and wherehi the heat is confrolled such that the upgraded hydrocarbons can be produced from the formation as a vapor.

6388. A method for producing methane from a relatively low penneability foπnation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least one portion ofthe formation; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe foimation; providing hydrocarbon fluids to at least the selected section ofthe formation; and producing mixture comprising methane from the foimation.

6389. The method ofclaim 6388, wherein the heat provided from at least one heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6390. The method ofclaim 6388, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6391. The method ofclaim 6388, further comprising controlling heat from at least one ofthe heat sources to enhance production of methane from the hydrocarbon fluids.

6392. The method ofclaim 6388, further comprising confrolling a temperature within at least a selected section in a range to from greater than about 400 °C to less than about 600 °C.

6393. The method ofclaim 6388, further comprising cooling the mixture to inhibit further reaction ofthe methane.

6394. The method ofclaim 6388, further comprising controlling at least some condition in the formation to enhance production of methane.

6395. The method of claim 6388, further comprising adding water to the formation.

6396. The method ofclaim 6388, further comprising separating at least a portion ofthe methane from the mixture and recycling at least some ofthe separated mixture to the formation.

6397. The method ofclaim 6388, further comprising cracking the hydrocarbon fluids to form methane.

6398. The method ofclaim 6388, wherein the mixture is produced from the foπnation through a production well, and wherein the heat is conttolled such that the mixture can be produced from the formation as a vapor.

6399. The method ofclaim 6388, wherein the mixture is produced from the formation through a production well, and further comprising heating a wellbore ofthe production well to inhibit condensation ofthe mixture within the wellbore.

6400. The method ofclaim 6388, wherein the mixture is produced from the formation through a production well, wherein a wellbore ofthe production well comprises a heater element configured to heat the formation adjacent to the wellbore, and further comprising heating the formation with the heater element to produce the mixture.

6401. A method for hydrotreating a fluid in a heated formation in situ, comprising: providing heat from one or more heat sources to at least one portion ofthe formation; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe formation; providing a fluid to the selected section; confrolling a H2 partial pressure in the selected section ofthe foimation; hydrotreating at least some ofthe fluid in the selected section; and producing a mixture comprising hydrotteated fluids from the formation.

6402. The method ofclaim 6401, wherein the mixture is produced from the foimation when a partial pressure of hydrogen in the selected section is at least about 0.5 bars absolute.

6403. The method of claim 6401 , wherein the heat provided from at least one of the one or more heat source is transfened to at least a portion ofthe formation substantially by conduction.

6404. The method ofclaim 6401, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6405. The method ofclaim 6401, further comprising providing hydrogen to the selected section ofthe formation.

6406. The method of claim 6401 , further comprising controlling the heat such that a temperature within the selected section is in a range from about 200 °C to about 450 °C.

6407. The method of clahn 6401 , wherein the provided fluid comprises an olefin.

6408. The method of claim 6401 , wherein the provided fluid comprises pitch.

6409. The method ofclaim 6401,wherein the provided fluid comprises oxygenated compounds.

6410. The method ofclaim 6401, wherein the provided fluid comprises sulfur containing compounds.

6411. The method of claim 6401 , wherein the provided fluid comprises nifrogen containing compounds.

6412. The method of claim 6401 , wherein the provided fluid comprises crade oil.

6413. The method of claim 6401 , wherein the provided fluid comprises synthetic crade oil.

6414. The method of claim 6401 , wherein the produced mixture comprises a hydrocarbon mixture.

6415. The method of claim 6401 , wherein the produced mixture comprises less than about 1 % by weight ammonia.

6416. The method ofclaim 6401, wherein the produced mixture comprises less than about 1% by weight hydrogen sulfide.

6417. The method of clahn 6401 , wherein the produced mixture comprises less than about 1 % oxygenated compounds.

6418. The method of claim 6401 , further comprising producing the mixture from the formation through a production well, wherein the heating is controlled such that the mixttire can be produced from the formation as a vapor.

6419. A method for producing hydrocarbons from a heated formation in situ, comprising: providing heat from one or more heat sources to at least one portion ofthe foimation; allowmg the heat to fransfer from the one or more heat sources to a selected section ofthe formation such that at least some ofthe selected section comprises a temperature profile; providing a hydrocarbon mixture to the selected section; separating the hydrocarbon mixture into one or more mixtures of components; and producing the one or more mixtures of components from one or more production wells.

6420. The method ofclaim 6419, wherein the heat provided from at least one ofthe one or more heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6421. The method ofclaim 6419, wherein the one or more ofthe heat sources comprise heaters.

6422. The method ofclaim 6419, wherein at least one ofthe one or more mixtures is produced from the foπnation when a partial pressure ofhydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6423. The method o claim 6419, further comprising controlling a pressure within at least a majority ofthe selected section.

6424. The method ofclaim 6419, wherein the temperature proflle extends horizontally through the formation.

6425. The method ofclaim 6419, wherein the temperature profile extends vertically through the formation.

6426. The method ofclaim 6419, wherein the selected section comprises a spent formation.

6427. The method ofclaim 6419, wherein the production well comprises a plurality of production wells placed at various distances from at least one ofthe one or more heat sources along the temperature gradient zone.

6428. The method ofclaim 6419, wherein the production well comprises a first production well and a second production well, further comprising: positioning the first production well at a first distance from a heat source ofthe one or more heat sources; positioning the second production well at a second distance from the heat source ofthe one or more heat sources; producing a first component ofthe one or more portions from the ffrst production well; and producing a second component of the one or more portions from the second production well.

6429. The method ofclaim 6419, further comprising heating a wellbore ofthe production well to inhibit condensation of at least the one component within the wellbore.

6430. The method of clahn 6419, wherein the one or more components comprise hydrocarbons.

6431. The method ofclaim 6419, wherein separating the one or more components further comprises: producing a low molecular weight component ofthe one or more components from the formation; allowing a high molecular weight component ofthe one or more components to remain within the formation; providing additional heat to the formation; and producing at least some ofthe high molecular weight component.

6432. The method ofclaim 6419, further comprising producing at least the one component from the formation through a production well, wherein the heating is confrolled such that the mixture can be produced from the formation as a vapor.

6433. A method of utilizing heat of a heated formation, comprising: placing a conduit in the formation; allowing heat from the foimation to fransfer to at least a portion ofthe conduit; generating a region of reaction in the conduit; allowing a material to flow through the region of reaction; reacting at least some ofthe material in the region of reaction; and producing a mixture from the conduit.

6434. The method ofclaim 6433, wherein a conduit input is located separately from a conduit output.

6435. The method of claim 6433 , wherein the conduit is configured to inhibit contact between the material and the formation.

6436. The method ofclaim 6433, wherein the conduit comprises a u-shaped conduit, and further comprising placing the u-shaped conduit within a heater well in the heated formation.

6437. The method of claim 6433, wherein the material comprises a first hydrocarbon and wherein the first hydrocarbon reacts to form a second hydrocarbon.

6438. The method ofclaim 6433, wherein the material comprises water.

6439. The method ofclaim 6433, wherein the produced mixture comprises hydrocarbons.

6440. A method for storing fluids within a relatively low peπneability formation containing heavy hydrocarbons, comprising: providing a banier to a portion ofthe foπnation to form an in situ storage area, wherein at least a portion ofthe in situ storage area has previously undergone an in situ conversion process, and wherein migration of fluids into or out ofthe storage area is inhibited; providing a material to the in situ storage area; storing at least some ofthe provided fluids within the in situ storage area; and wherein one or more conditions ofthe in situ storage area inhibits reaction within the material.

6441. The method ofclaim 6440, further comprising producing at least some ofthe stored material from the in situ storage area.

6442. The method ofclaim 6440, further comprising producing at least some ofthe stored material from the in situ storage area as a liquid.

6443. The method of claim 6440, further comprismg producing at least some ofthe stored material from the in situ storage area as a gas.

6444. The method of claim 6440, wherein the stored material is a solid, and further comprising: providing a solvent to the in situ storage area; allowing at least a portion ofthe stored material to dissolve; and producing at least some ofthe dissolved material from the in situ storage area.

6445. The method ofclaim 6440, wherein the material comprises inorganic compounds.

6446. The method ofclaim 6440, wherein the material comprises organic compounds.

6447. The method ofclaim 6440, wherein the material comprises hydrocarbons.

6448. The method of claim 6440, wherein the material comprises formation fluids

6449. The method ofclaim 6440, wherein the material comprises synthesis gas.

6450. The method of claim 6440, wherein the material comprises a solid.

6451. The method ofclaim 6440, wherein the material comprises a liquid.

6452. The method ofclaim 6440, wherein the material comprises a gas.

6453. The method ofclaim 6440, wherein the material comprises natural gas.

6454. The method ofclaim 6440, wherein the material comprises compressed afr.

6455. The method ofclaim 6440, wherein the material comprises compressed afr, and wherein the compressed afr is used as a supplement for elecfrical power generation.

6456. The method ofclaim 6440, further comprising: producing at least some ofthe material from the in situ treatment area through a production well; and heating at least a portion of a wellbore ofthe production well to inhibit condensation ofthe material within the wellbore.

6457. The method ofclaim 6440, wherein the in situ conversion process comprises pyrolysis.

6458. The method ofclaim 6440, wherein the in situ conversion process comprises synthesis gas generation.

6459. The method of claim 6440, wherein the in situ conversion process comprises solution mining.

6460. A method of filtering water within a relatively low permeability foimation containing heavy hydrocarbons comprising: providing water to at least a portion ofthe foimation, wherein the portion has previously undergone an in situ conversion process, and wherein the water comprises one or more components; removing at least one ofthe one or more components from the provided water; and producing at least some ofthe water from the formation.

6461. The method ofclaim 6460, wherein at least one ofthe one or more components comprises a dissolved cation, and further comprising: converting at least some ofthe provided water to steam; allowing at least some ofthe dissolved cation to remain in the portion o the formation; and producing at least a portion ofthe steam from the formation.

6462. The method ofclaim 6460, wherein the portion ofthe formation is above the boiling point temperature of the provided water at a pressure ofthe portion, wherein at least one ofthe one or more components comprises mineral cations, and wherein the provided water is converted to steam such that the mineral cations are deposited within the formation.

6463. The method of claim 6460 further comprising converting at least a portion ofthe provided water into steam and wherein at least one ofthe one or more components is separated from the water as the provided water is converted into steam.

6464. The method ofclaim 6460, wherein a temperature ofthe portion ofthe formation is greater than about 90 °C, and further comprising sterilizing at least some ofthe provided water within the portion ofthe formation.

6465. The method of clahn 6460, wherein a temperature within the portion is less than about a boiling temperature ofthe provided water at a fluid pressure ofthe portion.

6466. The method ofclaim 6460, further comprising remediating at least the one portion ofthe foπnation.

6467. The method ofclaim 6460, wherein the one or more components comprise cations.

6468. The method ofclaim 6460, wherein the one or more components comprise calcium.

6469. The method ofclaim 6460, wherein the one or more components comprise magnesium.

6470. The method of claim 6460, wherein the one or more components comprise a microorganism.

6471. The method ofclaim 6460, wherein the converted portion ofthe formation further comprises a pore size such that at least one ofthe one or more components is removed from the provided water.

6472. The method of claim 6460, wherein the converted portion ofthe formation adsorbs at least one ofthe one or more components in the provided water.

6473. The method of claim 6460, wherein the provided water comprises formation water.

6474. The method of claim 6460, wherein the in situ conversion process comprises pyrolysis.

6475. The method ofclaim 6460, wherein the in situ conversion process comprises synthesis gas generation.

6476. The method of claim 6460, wherein the in situ conversion process comprises solution mining.

6477. A method for sequestering carbon dioxide in a relatively low permeability foimation containing heavy hydrocarbons, comprising: providing carbon dioxide to a portion ofthe formation, wherein the portion has previously undergone an in situ conversion process; providing a fluid to the portion; allowing at least some ofthe provided carbon dioxide to contact the fluid in the portion; and precipitating carbonate compounds.

6478. The method of claim 6477, wherein providing a solution to the portion comprises allowing groundwater to flow into the portion.

6479. The method ofclaim 6477, wherein the solution comprises one or more dissolved ions.

6480. The method of claim 6477, wherein the solution comprises a solution obtained from a formation aquifer.

6481. The method of claim 6477, wherein the solution comprises a man-made indusfrial solution.

6482. The method of claim 6477, wherein the solution comprises agricultural run-off.

6483. The method of claim 6477, wherein the solution comprises seawater.

6484. The method ofclaim 6477, wherein the solution comprises a brine solution.

6485. The method ofclaim 6477, further comprising controlling a temperature within the portion.

6486. The method of claim 6477, further comprising confrolling a pressure within the portion.

6487. The method of claim 6477, further comprising removing at least some ofthe solution from the foimation.

6488. The method ofclaim 6477, further comprising removing at least some ofthe solution from the foπnation and recycling at least some ofthe removed solution into the formation.

6489. The method of claim 6477, further comprising providing a buffering compound to the solution.

6490. The method ofclaim 6477, further comprising: providing the solution to the formation; and allowing at least some ofthe solution to migrate through the formation to increase a contact time between the solution and the provided carbon dioxide.

6491. The method of claim 6477, wherein the solution is provided to the formation after carbon dioxide has been provided to the formation.

6492. The method of claim 6477, further comprising providing heat to the portion.

6493. The method of claim 6477, wherein providing carbon dioxide to a portion ofthe formation comprises providing carbon dioxide to a first location, wherein providing a solution to the portion comprises providing the solution to a second location, and wherein the ffrst location is downdip ofthe second location.

6494. The method ofclaim 6477, wherein allowing at least some ofthe provided carbon dioxide to contact the solution in the portion comprises allowing at least some ofthe carbon dioxide and at least some ofthe solution to migrate past each other.

6495. The method of claim 6477, wherein the solution is provided to the formation prior to providing the carbon dioxide, and further comprising providing at least some ofthe carbon dioxide to a location positioned proxhnate a lower surface ofthe portion such that some ofthe carbon dioxide may migrate up through the portion.

6496. The method of claim 6477, wherein the solution is provided to the formation prior to providing the carbon dioxide, and further comprising allowing at least some carbon dioxide to migrate through the portion.

6497. The method of claim 6477, further comprising: providing heat to the portion, wherein the portion comprises a temperature greater than about a boiling point ofthe solution; vaporizing at least some ofthe solution; producing a fluid from the formation.

6498. The method ofclaim 6477, further comprising decreasing leaching of metals from the formation into groundwater.

6499. A method of freathig a relatively low permeability formation containing heavy hydrocarbons, comprising: injecting a recovery fluid into a portion ofthe formation; allowing heat within the recovery fluid, and heat from one or more heat sources, to transfer to a selected section ofthe formation, wherein the selected section comprises hydrocarbons; mobilizing at least some ofthe hydrocarbons within the selected section; and producing a mixture from the formation.

6500. The method ofclaim 6499, wherein the portion has been previously produced.

6501. The method ofclaim 6499, wherein the portion has previously undergone an in situ conversion process.

6502. The method of claim 6499, further comprising upgrading at least some hydrocarbons within the selected section to decrease a viscosity o the hydrocarbons.

6503. The method of claim 6499, wherein the produced mixture comprises hydrocarbons having an average API gravity greater than about 25°.

6504. The method of claim 6499, further comprising vaporizing at least some ofthe hydrocarbons within the selected section.

6505. The method ofclaim 6499, wherein the recovery fluid comprises water.

6506. The method ofclaim 6499, wherein the recovery fluid comprises hydrocarbons.

6507. The method ofclaim 6499, wherein the mixture comprises pyrolyzation fluids.

6508. The method of claim 6499, wherein the mixture comprises hydrocarbons.

6509. The method ofclaim 6499, wherein the mixture is produced from a production well and further comprising confrollmg a pressure such that a fluid pressure proximate to the production well is less than about a fluid pressure proximate to a location where the fluid is injected.

6510. The method of claim 6499, further comprising: monitoring a composition ofthe produced mixture; and controlling a fluid pressure in at least a portion ofthe foimation to confrol the composition ofthe produced mixture.

6511. The method of claim 6499, further comprising pyrolyzing at least some ofthe hydrocarbons within the selected section ofthe foπnation. 6512.

6513. The method of claim 6499, wherein the average temperature ofthe selected section is between about 275 °C to about 375 °C, and wherehi a fluid pressure ofthe recovery fluid is between about 60 bars to about 220 bars, and wherein the recovery fluid comprises steam.

6514. The method of claim 6499, further comprising controlling pressure within the selected section such that a fluid pressure within the selected section is at least about a hydrostatic pressure of a sunounding portion ofthe formation.

6515. The method of claim 6499, further comprising controlling pressure within the selected section such that a fluid pressure within the selected section is greater than about a hydrostatic pressure of a sunounding portion ofthe formation.

6516. The method ofclaim 6499, wherein a depth ofthe selected section is between about 300 m to about 400 m.

6517. The method ofclaim 6499, wherein the mixture comprises pyrolysis products.

6518. The method ofclaim 6499, further comprising vaporizing at least some ofthe hydrocarbons within the selected section and wherein the vaporized hydrocarbons comprise hydrocarbons having a carbon number greater than about 1 and a carbon number less than about 4.

6519. The method of claim 6499, further comprising allowing the injected recovery fluid to contact a substantial portion of a volume ofthe selected section.

6520. The method of claim 6499, wherein the recovery fluid comprises steam, and wherein the pressure ofthe injected steam is at least about 90 bars, and wherein the temperature ofthe injected steam is at least about 300 °C.

6521. The method of clahn 6499, further comprising upgrading at least a portion of the hydrocarbons within the selected section ofthe formation such that a viscosity ofthe portion ofthe hydrocarbons is decreased.

6522. The method of claim 6499, further comprising separating the recovery fluid from pyrolyzation fluid and distilled hydrocarbons in the foπnation, and further comprising producing the pyrolyzation fluid and distilled hydrocarbons.

6523. The method of claim 6499, wherein the ttansfer fluid and vaporized hydrocarbons are separated with membranes.

6524. The method of claim 6499, wherein the selected section comprises a ffrst selected section and a second selected section and further comprising: mobilizing at least some ofthe hydrocarbons within the selected first section ofthe formation; allowing at least some ofthe mobilized hydrocarbons to flow from the selected ffrst section ofthe foπnation to a selected second section ofthe foπnation, and wherein the selected second section comprises hydrocarbons; and heating at least a portion ofthe foπnation using one ore more heat sources; pyrolyzing at least some ofthe hydrocarbons within the selected second section ofthe formation; and producing a mixttire from the foπnation.

6525. The method ofclaim 6499, wherein a residence thne ofthe recovery fluid in the formation is greater than about one month and less than about six months.

6526. The method of claim 6499, further comprising: allowing the recovery fluid to soak in the selected section ofthe foπnation for a selected time period; and producing at least a portion ofthe recovery fluid from the formation.

6527. A method of freating relatively low peπneability formation containing heavy hydrocarbons in situ, comprising: injecting a recovery fluid into the formation; providing heat from one or more heat sources to the formation; allowing the heat to fransfer from one or more ofthe heat sources to a selected section ofthe formation, wherein the selected section comprises hydrocarbons; mobilizing at least some ofthe hydrocarbons; and producing a mixture from the foimation, wherein the produced mixture comprises hydrocarbons having an average API gravity greater than about 25°.

6528. The method ofclaim 6527, wherein the heat provided from at least one ofthe one or more heat sources is fransfened to at least a portion ofthe foπnation substantially by conduction.

6529. The method of claim 6527, wherein the mixture is produced from the foimation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6530. The method ofclaim 6527, wherein at least one ofthe one or more ofthe heat sources comprises a heater.

6531. The method ofclaim 6527, further comprising pyrolyzing at least some ofthe hydrocarbons within selected section.

6532. The method ofclaim 6527, further comprising pyrolyzing at least some ofthe mobilized hydrocarbons.

6533. The method of claim 6527, wherein the recovery fluid comprises water.

6534. The method of claim 6527, wherein the recovery fluid comprises hydrocarbons.

6535. The method of claim 6527, wherein the mixture comprises pyrolyzation fluids.

6536. The method o claim 6527, wherein the mixture comprises steam.

6537. The method of clahn 6527, wherein a pressure is controlled such that a fluid pressure proximate to one or more ofthe heat sources is greater than a fluid pressure proximate to a location where the fluid is produced

6538. The method ofclaim 6527, wherein the one or more heat sources comprise at least two heat sources, and wherein supeφosition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section ofthe formation.

6539. The method ofclaim 6527, wherein the heat is provided such that an average temperature in the selected section ranges from approximately about 270 °C to about 375 °C.

6540. The method ofclaim 6527, further comprising: monitoring a composition ofthe produced mixture; and controlling a pressure in at least a portion ofthe foimation to control the composition ofthe produced mixture.

6541. The method of claim 6540, wherein the pressure is controlled by a valve proximate to a location where the mixture is produced.

6542. The method of claim 6540, wherein the pressure is controlled such that pressure proximate to one or more ofthe heat sources is greater than a pressure proxhnate to a location where the mixture is produced.

6543. The method of clahn 6527, wherein a residence time ofthe recovery fluid in the formation is less than about one month to greater than about six months.

6544. The method ofclaim 6527, further comprising: allowing the recovery fluid to soak in the selected section ofthe formation for a selected time period; and producing at least a portion ofthe recovery fluid from the foπnation.

6545. A method of treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: injecting a recovery fluid into a formation; allowing the recovery fluid to migrate through at least a portion ofthe formation, wherein a size of a selected section increases as a recovery fluid front migrates through an untreated portion ofthe formation, and wherein the selected section is a portion ofthe foπnation treated by the recovery fluid; allowing heat from the recovery fluid to fransfer heat to the selected section, wherein the heat from the recovery fluid, and heat from one or more heat sources, pyrolyzes at least some ofthe hydrocarbons within the selected section of the formation; allowing the heat from the recovery fluid or one or more heat sources to mobilize at least some ofthe hydrocarbons at the recovery fluid front; allowing the heat from the recovery fluid, and heat from one or more heat sources, to pyrolyze at least a portion ofthe hydrocarbons in the mobilized fluid; and producing a mixture from the formation.

6546. The method of clahn 6545, wherein the formation comprises a heavy relatively low permeability formation containing heavy hydrocarbons.

6547. The method of claim 6545, wherein one or more heat sources are heaters.

6548. The method of claim 6545, wherein the mixture is produced as a mixture of vapors.

6549. The method ofclaim 6545, wherein an average temperature o the selected section is about 300 °C, and wherehi the recovery fluid pressure is about 90 bars.

6550. The method of clahn 6545, wherein the mobilized hydrocarbons flow substantially parallel to the recovery fluid front.

6551. The method of claim 6545, wherein the mixture is produced from an upper portion ofthe fonnation.

6552. The method ofclaim 6545, wherein a portion ofthe recovery fluid condenses and migrates due to gravity to a lower portion ofthe selected section, and further comprising producing a portion ofthe condensed recovery fluid.

6553. The method of claim 6545, wherein the pyrolyzed fluid migrates to an upper portion ofthe formation.

6554. The method of claim 6545, wherein the mixture comprises pyrolyzation fluids.

6555. The method ofclaim 6545, wherein the mixture comprises recovery fluid.

6556. The method ofclaim 6545, wherein the recovery fluid comprises steam.

6557. The method ofclaim 6545, wherein the recovery fluid is injected through one or more injection wells.

6558. The method of clahn 6557, wherein the one or more injection wells are located substantially horizontally in the fonnation.

6559. The method of clahn 6557, wherehi the one or more injection wells are located substantially vertically in the foπnation.

6560. The method of clahn 6545, wherein the mixture is produced through one or more production wells.

6561. The method of claim 6560, wherein the one or more production wells are located substantially horizontally in the foimation.

6562. The method of claim 6545, wherein the mixture is produced through a heat source wellbore.

6563. The method of claim 6545, wherein the produced mixture comprises hydrocarbons having an average API gravity at least about 25°.

6564. The method of claim 6545, wherein at least about 20% ofthe hydrocarbons in the selected first section and the selected second section are pyrolyzed.

6565. The method ofclaim 6545, further comprising providing heat from one or more heat sources to at least one portion ofthe formation.

6566. The method of claim 6545, wherein the heat from the one or more heat sources vaporizes water injected into the formation.

6567. The method of clahn 6545, wherein the heat from the one or more heat sources heats recovery fluid in the foimation, wherein the recovery fluid comprises steam.

6568. The method ofclaim 6545, wherein the one or more heat sources comprise electrical heaters.

6569. The method ofclaim 6545, wherein the one or more heat sources comprise flame disfributed combustors.

6570. The method ofclaim 6545, wherein the one or more heat sources comprise natural disfributed combustors.

6571. The method of claim 6545, further comprishig separating recovery fluid from pyrolyzation fluids in the fonnation.

6572. The method of claim 6545, further comprising producing liquid hydrocarbons from the formation, and ftirther comprising reinjecting the produced liquid hydrocarbons into the formation.

6573. The method of claim 6545, further comprising producing a liquid mixture from the formation, wherein the produced liquid mixture comprises substantially of condensed recovery fluid.

6574. The method of claim 6545, further comprising separating condensed recovery fluid from liquid hydrocarbons in the formation, and further comprising producing the condensed recovery fluid from the formation.

6575. The method ofclaim 6545, wherein the recovery fluid is injected into regions of relatively high water saturation.

6576. The method ofclaim 6545, wherein injected recovery fluid contacts a substantial portion of a volume of the selected section.

6577. The method of claim 6545, wherein the recovery fluid comprises steam, and wherein the pressure ofthe injected steam is at least about 90 bars, and wherehi the temperature of the injected steam is at least about 300 °C.

6578. The method ofclaim 6545, wherein at least a portion of sulfur is retained in the formation.

6579. The method of claim 6545, wherein the heat from recovery fluid partially upgrades at least a portion ofthe hydrocarbons within the selected section ofthe formation, and wherein the partial upgrading reduces the viscosity ofthe portion ofthe hydrocarbons.

6580. The method ofclaim 6545, further comprising separating the recovery fluid from pyrolyzation fluid and distilled hydrocarbons in the formation, and further comprising producing the pyrolyzation fluid and distilled hydrocarbons.

6581. The method of claim 6545, wherein the recovery fluid and vaporized hydrocarbons are separated with membranes.

6582. The method ofclaim 6545, wherein a residence time ofthe recovery fluid in the formation is less than about one month to greater than about six months.

6583. The method of claim 6545, further comprising: allowing the heat fransfer fluid to soak in the selected section ofthe formation for a selected time period; and producing at least a portion ofthe heat ttansfer fluid from the foπnation.

6584. A method of shutting-in an in situ treatment process in a relatively low permeability foimation containing heavy hydrocarbons, comprising: terminating heating from one or more heat sources providing heat to a portion ofthe formation; monitoring a pressure in at least a portion ofthe formation; conttoUing the pressure in the portion ofthe formation such that the pressure is maintained approxhnately below a fracturing or breakthrough pressure ofthe formation.

6585. The method ofclaim 6584, wherein monitoring the pressure in the formation comprises detecting fractures ^■ with passive acoustic monitoring.

6586. The method ofclaim 6584, wherein confrolling the pressure in the portion ofthe formation comprises: producing hydrocarbon vapor from the formation when the pressure is greater than approximately the fracturing or breakthrough pressure of the formation; and allowing produced hydrocarbon vapor to oxidize at a surface ofthe formation.

6587. The method ofclaim 6584, wherein controlling the pressure in the portion ofthe foπnation comprises: producing hydrocarbon vapor from the formation when the pressure is greater than approximately the fracturing or breakthrough pressure ofthe formation; and storing at least a portion of the produced hydrocarbon vapor.

6588. A method of shutting-in an in situ treatment process in a relatively low permeability foimation containing heavy hydrocarbons, comprising: terminating heating from one or more heat sources providing heat to a portion ofthe formation; producing hydrocarbon vapor from the foimation; and injecting at least a portion ofthe produced hydrocarbon vapor into a portion of a storage formation.

6589. The method ofclaim 6588, wherein the storage formation comprises a spent formation.

6590. The method of claim 6589, wherein an average temperature ofthe portion of the spent formation is less than about 100°C.

6591. The method of claim 6589, wherein a substantial portion of condensable compounds in the injected hydrocarbon vapor condense in the spent formation.

6592. The method of claim 6588, wherein the storage formation comprises a relatively high temperature foimation, and further comprising converting a substantial portion of injected hydrocarbons into coke and molecular hydrogen.

6593. The method ofclaim 6592, wherein the average temperature ofthe portion ofthe relatively high temperature foimation is greater than about 300°C.

6594. The method of claim 6592, further comprising: producing at least a portion ofthe H2 from the relatively high temperature foπnation; and allowing the produced molecular hydrogen to oxidize at a surface ofthe relatively high temperature formation.

6595. The method of claim 6588, wherein the storage formation comprises a depleted foπnation.

6596. The method of claim 6595, wherein the depleted formation comprises an oil field.

6597. The method of claim 6595, wherein the depleted foπnation comprises a gas field.

6598. The method of claim 6595, wherein the depleted foπnation comprises a water zone comprising seal and trap integrity.

6599. A method of producing a soluble compound from a soluble compound containing formation, comprising: providing heat from one or more heat sources to at least a portion of a hydrocarbon containing layer; producing a mixture comprising hydrocarbons from the fonnation; using heat from the formation, heat from the mixture produced from the formation, or a component from the mixture produced from the formation to adjust a quality of a ffrst fluid; providing the first fluid to a soluble compound containing formation; and producing a second fluid comprishig a soluble compound from the soluble compound containing foimation.

6600. The method ofclaim 6599, further comprising pyrolyzing at least some hydrocarbons in the hydrocarbon containing layer.

6601. The method of claim 6599, further comprising dissolving the soluble compound in the soluble compound containing formation.

6602. The method o claim 6599, wherein the soluble compound comprises a phosphate.

6603. The method of claim 6599, wherein the soluble compound comprises alumina.

6604. The method of claim 6599, wherein the soluble compound comprises a metal.

6605. The method of claim 6599, wherein the soluble compound comprises a carbonate.

6606. The method ofclaim 6599, further comprising separating at least a portion ofthe soluble compound from the second fluid.

6607. The method ofclaim 6599, further comprising separating at least a portion ofthe soluble compound from the second fluid, and then recycling a portion ofthe second fluid into the soluble compound containing formation.

6608. The method ofclaim 6599, wherein heat is provided from the heated formation, or from the mixture produced from the formation, in the form of hot water or steam.

6609. The method ofclaim 6599, wherein the quality ofthe first fluid that is adjusted is pH.

6610. The method ofclaim 6599, wherein the quality ofthe first fluid that is adjusted is temperature.

6611. The method of clahn 6599, further comprising adding a dissolving compound to the first fluid that facilitates dissolution ofthe soluble compound in the soluble containing formation.

6612. The method ofclaim 6599, wherein C02 produced from the hydrocarbon containing layer is used to adjust acidity ofthe solution.

6613. The method of claim 6599, wherein the soluble compound containing foimation is at a different depth than the portion of the hydrocarbon containing layer.

6614. The method ofclaim 6599, wherein heat from the portion ofthe hydrocarbon containing layer migrates and heats at least a portion ofthe soluble compound containing formation.

6615. The method of claim 6599, wherein the soluble compound containing formation is at a different location than the portion ofthe hydrocarbon containing layer.

6616. The method ofclaim 6599, further comprising using openings for providing the heat sources, and further comprising using at least a portion of these openings to provide the first fluid to the soluble compound containing formation.

6617. The method of claim 6599, further comprising providing the solution to the soluble compound containing foπnation in one or more openings that were previously used to (a) provide heat to the hydrocarbon containing layer, or (b) produce the mixture from the hydrocarbon containing layer.

6618. The method of claim 6599, further comprising providing heat to the hydrocarbon containing layer, or producing the mixture from the hydrocarbon containing layer, using one or more openings that were previously used to provide a solution to a soluble compound containing formation.

6619. The method ofclaim 6599, further comprising: separating at least a portion ofthe soluble compound from the second fluid; providing heat to at least the portion ofthe soluble compound; and wherein the provided heat is generated in part using one or more products of an in situ conversion process.

6620. The method of claim 6599, further comprising producing the second fluid when a partial pressure of hydrogen in the portion ofthe hydrocarbon containing layer is at least about 0.5 bars absolute.

6621. The method of claim 6599, wherein the heat provided from at least one heat source is fransfened to at least a part ofthe hydrocarbon containing layer substantially by conduction.

6622. The method of claim 6599, wherein one or more ofthe heat sources comprise heaters.

6623. The method of claim 6599, wherein the soluble compound containing fonnation comprises nahcolite.

6624. The method ofclaim 6599, wherein greater than about 10 % by weight ofthe soluble compound , containing formation comprises nahcolite.

6625. The method ofclaim 6599, wherein the soluble compound containing formation comprises dawsonite.

6626. The method of claim 6599, wherein greater than about 2 % by weight ofthe soluble compound containing formation comprises dawsonite.

6627. The method of claim 6599, wherein the first fluid comprises steam.

6628. The method ofclaim 6599, wherein the ffrst fluid comprises steam, and further comprising providing heat to the soluble compound containing formation by injecting the steam into the formation.

6629. The method of claim 6599, wherein the soluble compound containing foπnation is heated and then the first fluid is provided to the formation.

6630. A method of freating a relatively low peπneability formation containing heavy hydrocarbons in situ, comprising: providing heat to at least a portion ofthe formation; allowing the heat to fransfer from at least the portion to a selected section ofthe formation such that dissociation of carbonate minerals is inhibited; injecting a first fluid into the selected section; producing a second fluid from the formation; and conducting an in situ conversion process in the selected section.

6631. The method ofclaim 6630, wherein the mixture is produced from the formation when a partial pressure of hydrogen in at least a portion the fonnation is at least about 0.5 bars absolute.

6632. The method ofclaim 6630, wherein the heat is provided from at least one heat source, and wherein the heat is transfened to at least the portion ofthe foπnation substantially by conduction.

6633. The method of clahn 6630, wherein the in situ conversion process comprises: providing additional heat to a least a portion ofthe formation; pyrolyzing at least some hydrocarbons in the portion; and producing a mixture from the formation.

6634. The method ofclaim 6630, wherein the selected section comprises nahcolite.

6635. The method of claim 6630, wherein the selected section comprises dawsonite.

6636. The method ofclaim 6630, wherein the selected section comprises frona.

6637. The method ofclaim 6630, wherein the selected section comprises gaylussite.

6638. The method ofclaim 6630, wherein the selected section comprises carbonates.

6639. The method of claim 6630, wherein the selected section comprises carbonate phosphates.

6640. The method ofclaim 6630, wherein the selected section comprises carbonate chlorides.

6641 , The method ofclaim 6630, wherein the selected section comprises silicates.

6642. The method ofclaim 6630, wherein the selected section comprises borosilicates.

6643. The method of clahn 6630, wherein the selected section comprises halides.

6644. The method of claim 6630, wherein the first fluid comprises a pH greater than about 7.

6645. The method ofclaim 6630, wherein the first fluid comprises a temperature less than about 110 °C.

6646. The method ofclaim 6630, wherein the portion has previously undergone an in situ conversion process prior to the injection ofthe first fluid.

6647. The method of clahn 6630, wherein the second fluid comprises hydrocarbons.

6648. The method of claim 6630, wherein the second fluid comprises hydrocarbons, and further comprising: fragmenting at least some ofthe portion prior to providing the ffrst fluid; generating hydrocarbons; and providing at least some ofthe second fluid to a surface freatment unit, wherein the second fluid comprises at least some ofthe generated hydrocarbons.

6649. The method ofclaim 6630, further comprising removing mass from the selected section in the second fluid.

6650. The method of claim 6630, further comprising removing mass from the selected section in the second fluid such that a permeability ofthe selected section increases.

6651. The method of claim 6630, further comprising removing mass from the selected section in the second fluid and decreasing a heat fransfer time in the selected section.

6652. The method ofclaim 6630, further comprising controlling the heat such that the selected section has a temperature of above about 120 °C.

6653. The method of clahn 6630, wherein the selected section comprises nahcolite, and further comprising controlling the heat such that the selected section has a temperature less than about a dissociation temperature of nahcolite.

6654. The method of claim 6630, wherein the second fluid comprises soda ash, and further comprising removing at least a portion ofthe soda ash from the second fluid as sodium carbonate.

6655. The method of claim 6630, wherein the in situ conversion process comprises pyrolyzing hydrocarbon containing material in the selected section.

6656. The method of claim 6630, wherein the second fluid comprises nahcolite, and further comprising: separating at least a portion ofthe nahcolite from the second fluid; providing heat to at least some ofthe separated nahcolite to form a sodium carbonate solution; providing at least some ofthe sodium carbonate solution to at least the portion ofthe foimation; and producing a third fluid comprising alumina from the formation.

6657. The method of claim 6630, further comprising providing a banier to at least the portion ofthe formation to inhibit migration of fluids into or out of the portion.

6658. The method of claim 6630, further comprising controlling the heat such that a temperature within the selected section ofthe portion is less than about 100 °C.

6659. The method of claim 6630, further comprising: providing additional heat from the one or more heat sources to at least the portion ofthe formation; allowing the additional heat to transfer from at least the portion to the selected section ofthe fonnation; pyrolyzing at least some hydrocarbons within the selected section ofthe formation; producing a mixture from the formation; reducing a temperature ofthe selected section ofthe formation injecting a thfrd fluid into the selected section; and producing a fourth fluid from the formation.

6660. The method of claim 6659, wherein the thfrd fluid comprises water.

6661. The method of claim 6659, wherein the thfrd fluid comprises steam.

6662. The method of claim 6659, wherein the fourth fluid comprises a metal.

6663. The method of claim 6659, wherein the fourth fluid comprises a mineral.

6664. The method of clahn 6659, wherein the fourth fluid comprises aluminum.

6665. The method of claim 6659, wherein the fourth fluid comprises a metal, and further comprising producing the metal from the second fluid.

6666. The method of claim 6659, further comprising producing a non-hydrocarbon material from the fourth fluid.

6667. The method of claim 6630, wherein the first fluid comprises steam.

6668. The method ofclaim 6630, wherein the second fluid comprises a metal.

6669. The method of claim 6630, wherein the second fluid comprises a mineral.

6670. The method of claim 6630, wherein the second fluid comprises aluminum.

6671. The method ofclaim 6630, wherein the second fluid comprises a metal, and further comprising separating the metal from the second fluid.

6672. The method of claim 6630, further comprising producing a non-hydrocarbon material from the second fluid.

6673. The method ofclaim 6630, wherein greater than about 10 % by weight ofthe selected section comprises nahcolite.

6674. The method of claim 6630, wherein greater than about 2 % by weight ofthe selected section comprises dawsonite.

6675. The method of claim 6630, wherein the provided heat comprises waste heat from another portion ofthe formation.

6676. The method of clahn 6630, wherein the first fluid comprises steam, and further comprising providing heat to the foπnation by injecting the steam into the formation.

6677. The method of claim 6630, further comprising providing heat to the formation by injecting the first fluid into the formation.

6678. The method ofclaim 6630, further comprising providing heat to the formation by injecting the ffrst fluid into the formation, wherein the first fluid is at a temperature above about 90° C.

6679. The method of claim 6630, further comprising controlling a temperature ofthe selected section while injecting the first fluid, wherein the temperature is less than about a temperature at which nahcolite will dissociate.

6680. The method of claim 6630, wherein a temperature within the selected section is less than about 90 °C prior to injecting the first fluid to the formation.

6681. The method of claim 6630, further comprising providing a banier substantially sunounding the selected section such that the banier inhibits the flow of water into the foπnation.

6682. A method of freating a relatively low peπneability foπnation containing heavy hydrocarbons in situ, comprising: injecting a first fluid into the selected section; producing a second fluid from the formation; providing heat from one or more heat sources to at least a portion ofthe formation, wherein the heat is provided after production ofthe second fluid has begun; allowing the heat to fransfer from at least a portion ofthe foimation; pyrolyzing at least some hydrocarbons within the selected section; and producing a mixture from the formation.

6683. The method of claim 6682, wherein the selected section comprises nahcolite.

6684. The method ofclaim 6682, wherein the selected section comprises dawsonite.

6685. The method ofclaim 6682, wherein the selected section comprises trona.

6686. The method ofclaim 6682, wherein the selected section comprises gaylussite.

6687. The method ofclaim 6682, wherein the selected section comprises carbonates.

6688. The method ofclaim 6682, wherein the selected section comprises carbonate phosphates.

6689. The method ofclaim 6682, wherein the selected section comprises carbonate chlorides.

6690. The method ofclaim 6682, wherein the selected section comprises silicates.

6691. The method of claim 6682, wherein the selected section comprises borosilicates.

6692. The method ofclaim 6682, wherein the selected section comprises halides.

6693. The method of claim 6682, wherein the first fluid comprises a pH greater than about 7.

6694. The method ofclaim 6682, wherein the first fluid comprises a temperature less than about 110 °C.

6695. The method ofclaim 6682, wherein the second fluid comprises hydrocarbons.

6696. The method ofclaim 6682, wherein the second fluid comprises hydrocarbons, and further comprising: fragmenting at least some ofthe portion prior to providing the first fluid; generating hydrocarbons; and providing at least some ofthe second fluid to a surface freatment unit, wherein the second fluid comprises at least some ofthe generated hydrocarbons.

6697. The method ofclaim 6682, further comprising removing mass from the selected section in the second fluid.

6698. The method ofclaim 6682, further comprising removing mass from the selected section in the second fluid such that a permeability ofthe selected section increases.

6699. The method ofclaim 6682, further comprising removing mass from the selected section in the second fluid and decreasing a heat transfer time in the selected section.

6700. The method ofclaim 6682, ftirther comprising controlling the heat such that the selected section has a temperature of above about 270 °C.

6701. The method ofclaim 6682, wherein the second fluid comprises soda ash, and further comprising removing at least a portion ofthe soda ash from the second fluid as sodium carbonate.

6702. The method ofclaim 6682, wherein the second fluid comprises nahcolite, and further comprishig: separating at least a portion ofthe nahcolite from the second fluid; providing heat to at least some ofthe separated nahcolite to foπn a sodium carbonate solution; providing at least some ofthe sodium carbonate solution to at least the portion ofthe formation; and producing a thfrd fluid comprising alumina from the formation.

6703. The method of claim 6682, further comprising providing a banier to at least the portion ofthe formation to inhibit migration of fluids into or out ofthe portion.

6704. The method ofclaim 6682, wherein the first fluid comprises steam.

6705. The method ofclaim 6682, wherein the second fluid comprises a metal.

6706. The method ofclaim 6682, wherein the second fluid comprises a mineral.

6707. The method of claim 6682, wherein the second fluid comprises aluminum.

6708. The method of claim 6682, wherein the second fluid comprises a metal, and further comprising separating the metal from the second fluid.

6709. The method of claim 6682, further comprising producing a non-hydrocarbon material from the second fluid.

6710. The method ofclaim 6682, wherein greater than about 10 % by weight ofthe selected section comprises nahcolite.

6711. The method ofclaim 6682, wherein greater than about 2 % by weight ofthe selected section comprises dawsonite.

6712. The method ofclaim 6682, wherein at least some ofthe provided heat comprises waste heat from another portion ofthe formation.

6713. The method of claim 6682, wherein the ffrst fluid comprises steam, and further comprising providing heat to the fonnation by injecting the steam into the formation.

6714. The method of claim 6682, further comprising providing heat to the formation by injecting the first fluid into the foπnation.

6715. The method of claim 6682, further comprising providing heat to the formation by injecting the first fluid into the formation, wherein the first fluid is at a temperature above about 90° C.

6716. The method of clahn 6682, further comprising confrolling a temperature ofthe selected section while injecting the first fluid, wherein the temperature is less than about a temperature at which nahcolite will dissociate.

6717. The method ofclaim 6682, fuither comprising providing a banier substantiaUy suirounding the selected section such that the banier inhibits the flow of water into the fonnation.

6718. The method ofclaim 6682, wherein the mixture is produced from the foπnation when a partial pressure of hydrogen in at least a portion the formation is at least about 0.5 bars absolute.

6719. The method of claim 6682, wherehi the heat provided from at least one heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6720. The method of claim 6682, wherein the one or more ofthe heat sources comprise heaters.

6721. A method of solution mining alumina from an in situ relatively low permeability foπnation containing heavy hydrocarbons, comprising: providing heat from one or more heat sources to a least a portion ofthe formation; pyrolyzing at least some hydrocarbons in the portion; and producing a mixture from the formation providing a brine solution to a portion ofthe formation; and producing a mixture comprising alumina from the formation.

6722. The method ofclaim 6721, wherein the selected section comprises dawsonite.

6723. The method of claim 6721 , further comprising: separathig at least a portion ofthe alumina from the mixture; and providing heat to at least the portion ofthe alumina to generate aluminum.

6724. The method of claim 6721 , further comprising: separating at least a portion ofthe alumina from the mixture; providing heat to at least the portion ofthe alumina to generate aluminum; and wherein the provided heat is generated in part using one or more products of an in situ conversion process.

6725. The method of claim 6721 , further comprising producing the mixture when a partial pressure of hydrogen in the formation is at least about 0.5 bars absolute.

6726. The method ofclaim 6721, wherein the heat provided from at least one heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6727. The method ofclaim 6721, wherein one or more ofthe heat sources comprise heaters.

6728. A method of freating a relatively low penneability formation containing heavy hydrocarbons in situ, comprising: allowing a temperature of a portion ofthe formation to decrease, wherein the portion has previously undergone an in situ conversion process; injecting a first fluid into the selected section; and producing a second fluid from the formation.

6729. The method of claim 6728, wherein the in situ conversion process comprises: providing heat to a least a portion ofthe foπnation; pyrolyzing at least some hydrocarbons in the portion; and producing a mixture from the formation.

6730. The method ofclaim 6728, wherein the ffrst fluid comprises water.

6731. The method ofclaim 6728, wherein the second fluid comprises a metal.

6732. The method ofclaim 6728, wherehi the second fluid comprises a mineral.

6733. The method of claim 6728, wherein the second fluid comprises aluminum.

6734. The method of claim 6728, wherein the second fluid comprises a metal, and further comprising producing the metal from the second fluid.

6735. The method ofclaim 6728, further comprising producing a non-hydrocarbon material from the second fluid.

6736. The method ofclaim 6728, wherein the selected section comprises nahcolite.

6737. The method ofclaim 6728, wherein greater than about 10 % by weight ofthe selected section comprises nahcolite.

6738. The method ofclaim 6728, wherein the selected section comprises dawsonite.

6739. The method ofclaim 6728, wherein greater than about 2 % by weight ofthe selected section comprises dawsonite.

6740. The method of claim 6728, wherein the provided heat comprises waste heat from another portion ofthe foπnation.

6741. The method of claim 6728, wherein the first fluid comprises steam.

6742. The method of claim 6728, wherein the first fluid comprises steam, and further comprising providing heat to the formation by injecting the steam into the foπnation.

6743. The method of clahn 6728, further comprising providing heat to the foπnation by injecting the first fluid into the formation.

6744. The method of claim 6728, further comprising providing heat to the formation by injecting the first fluid into the formation, wherein the first fluid is at a temperature above about 90° C.

6745. The method ofclaim 6728, wherein the reduced temperature ofthe selected section is less than about 90 °C.

6746. The method ofclaim 6728, wherein an average richness of at least the portion ofthe selected section is greater than about 0.10 liters per kilogram.

6747. A method for treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to at least a portion of a relatively low permeability formation containing heavy hydrocarbons; allowing heat to fransfer from one or more heat sources to a first selected section of a relatively low permeability formation containing heavy hydrocarbons such that the heat reduces the viscosity of at least some hydrocarbons within the first selected section; producing a first mixture from the first selected section; allowing heat to transfer from one or more heat sources to a second selected section of a relatively low permeability formation containing heavy hydrocarbons such that the heat pyrolyzes at least some hydrocarbons within the second selected section; producing a second mixture from the second selected section; and blending at least a portion ofthe first mixture with at least a portion ofthe second mixture to produce a thfrd mixture comprising a selected property.

6748. The method ofclaim 6747, wherein the selected property ofthe thfrd mixture comprises an API gravity.

6749. The method ofclaim 6747, wherein the selected property ofthe thfrd mixture comprises an API gravity of at least about 10°.

6750. The method of claim 6747, wherein the selected property ofthe thfrd mixture comprises a selected viscosity.

6751. The method of claim 6747, wherein the selected property of the thfrd mixture comprises a viscosity less than about 7500 cs.

6752. The method ofclaim 6747, wherein the selected property ofthe thfrd mixture comprises a density.

6753. The method ofclaim 6747, wherein the selected property ofthe third mixture comprises a density less than about 1 g cm3.

6754. The method of claim 6747, wherein the selected property ofthe thfrd mixture comprises an asphaltene to saturated hydrocarbon ratio of less than about 1.

6755. The method ofclaim 6747, wherein the selected property ofthe thfrd mixture comprises an aromatic hydrocarbon to saturated hydrocarbon ratio of less than about 4.

6756. The method of clahn 6747, wherein asphaltenes are substantially stable in the third mixture at ambient temperature.

6757. The method of claim 6747, wherein the third mixture is transportable.

6758. The method of claim 6747, wherein the thfrd mixture is transportable through a pipeline.

6759. The method ofclaim 6747, wherein the first mixture comprises an API gravity less than about 15°.

6760. The method of clahn 6747, wherein the second mixture comprises an API gravity greater than about 25°.

6761. The method of claim 6747, wherein the second mixture comprises an acid number less than about 1.

6762. The method ofclaim 6747, further comprising selecting a ratio ofthe first mixture to the second mixture such that at least about 50% by weight ofthe initial mass of hydrocarbons in a selected portion ofthe formation is produced.

6763. The method of claim 6747, wherein the third mixture comprises less than about 50 % by weight ofthe second mixture.

6764. The method of claim 6747, wherein the first selected section comprises a depth of at least about 500 m below the surface of a relatively low permeability foπnation containing heavy hydrocarbons.

6765. The method of claim 6747, wherein the second selected section comprises a depth less than about 500 m below the surface of a relatively low permeability formation containing heavy hydrocarbons.

6766. The method ofclaim 6747, wherein the ffrst selected section and the second selected section are located in different relatively low permeability fonnations containing heavy hydrocarbons.

6767. The method ofclaim 6747, wherein the ffrst selected section and the second selected section are located in different relatively low permeability formations containing heavy hydrocarbons, and wherein the different relatively low permeability foπnation containing heavy hydrocarbons are vertically displaced.

6768. The method ofclaim 6747, wherein the ffrst selected section and the second selected section are vertically displaced within a single relatively low permeability foπnation containing heavy hydrocarbons.

6769. The method of claim 6747, wherein the ffrst selected section and the second selected section are substantially adjacent within a single relatively low permeability foπnation containing heavy hydrocarbons.

6770. The method ofclaim 6747, wherein blending comprises injecting at least a portion ofthe second mixture into the first selected section such that the second mixture blends with at least a portion ofthe first mixture to produce the thfrd mixttire in the first selected section.

6771. The method ofclaim 6747, wherein blending comprises injecting at least a portion ofthe second mixture into a production well in the first selected section such that the second mixture blends with at least a portion ofthe first mixture to produce the third mixture in the production well.

6772. The method ofclaim 6747, further comprising producing a mixture when a partial pressure ofhydrogen in the formation is at least about 0.5 bars absolute.

6773. The method ofclaim 6747, wherein the heat provided from at least one heat source is transfened to at least a portion ofthe formation substantially by conduction.

6774. The method ofclaim 6747, wherein one or more ofthe heat sources comprise heaters.

The method ofclaim 6747, wherein a ratio of energy output ofthe ffrst or the second produced mixture to energy input into the formation is at least about 5.

6775. A method for freating a relatively low permeability foπnation containing heavy hydrocarbons in situ to produce a blending agent, comprising: providing heat from one or more heat sources to at least a portion ofthe relatively low permeability formation containing heavy hydrocarbons; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe formation such that the heat pyrolyzes at least some hydrocarbons within the selected section; producing a blending agent from the selected section; and wherein at least a portion ofthe blending agent is adapted to blend with a liquid to produce a mixture with a selected property.

6776. The method of claim 6775, wherein the liquid comprises at least some heavy hydrocarbons.

6777. The method ofclaim 6775, wherein the liquid comprises an API gravity below about 15°.

6778. The method of claim 6775, wherein the liquid is viscous, and wherein a mixture produced by blending at least a portion ofthe blending agent with the liquid is less viscous than the liquid.

6779. The method of claim 6775, wherein the selected property ofthe mixture comprises an API gravity.

6780. The method ofclaim 6775, wherein the selected property ofthe mixture comprises an API gravity of at least about 10°.

6781. The method ofclaim 6775, wherein the selected property ofthe mixture comprises a selected viscosity.

6782. The method ofclaim 6775, wherein the selected property ofthe mixture comprises a viscosity less than about 7500 cs.

6783. The method of claim 6775, wherein the selected property of the mixture comprises a density.

6784. The method of claim 6775, wherein the selected property ofthe mixture comprises a density less than about 1 g/cm3.

6785. The method ofclaim 6775, wherein the selected property ofthe mixture comprises an asphaltene to saturated hydrocarbon ratio of less than about 1.

6786. The method of claim 6775, wherein the selected property ofthe mixture comprises an aromatic hydrocarbon to saturated hydrocarbon ratio of less than about 4. 6787 '. The method ofclaim 6775, wherein asphaltenes are substantiaUy stable in the mixture at ambient temperature.

6788. The method of claim 6775, wherein the mixture is transportable.

6789. The method of claim 6775, wherein the mixture is transportable through a pipeline.

6790. The method of claim 6775, wherein the liquid has a viscosity sufficiently high to inhibit economical transport ofthe liquid over 100 km via a pipeline but the mixture has a reduced viscosity that allows economical fransport of the mixture over 100 km via a pipeline.

6791. The method of claim 6775, further comprising producing the liquid from a second section of a relatively low permeability foimation containing heavy hydrocarbons and blending the liquid with the blending agent to produce the mixture.

6792. The method ofclaim 6775, further comprising producing the liquid from a second section of a relatively low permeability formation containing heavy hydrocarbons and blending the liquid with the blending agent to produce the mixture, wherein the mixture comprises less than about 50 % by weight ofthe blending agent.

6793. The method ofclaim 6775, further comprising injecting the blendhig agent into a second section of a relatively low permeability foimation containing heavy hydrocarbons such that the blending agent blends with the liquid in the second section to produce the mixture.

6794. The method of claim 6775, further comprising injecting the blending agent into a production well in a second section of a relatively low permeability formation containing heavy hydrocarbons such that the blending agent blends with the liquid in the production well to produce the mixture.

6795. The method ofclaim 6775, further comprising producing the blending agent when a partial pressure of hydrogen in the formation is at least about 0.5 bars absolute.

6796. The method of claim 6775, wherein the heat provided from at least one heat source is transfened to at least a portion ofthe foπnation substantially by conduction.

6797. The method ofclaim 6775, wherein one or more ofthe heat sources comprise heaters.

6798. The method of claim 6775, wherein a ratio of energy output ofthe blending agent to energy input into the foπnation is at least about 5.

6799. The method ofclaim 6775, wherein the blending agent comprises an acid number less than about 1.

6800. A blending agent produced by a method, comprising: providing heat from one or more heat sources to at least a portion of a relatively low permeability formation containing heavy hydrocarbons; allowing the heat to fransfer from the one or more heat sources to a selected section ofthe formation such that the heat pyrolyzes at least some hydrocarbons within the selected section; and producing the blending agent from the selected section; wherein at least a portion ofthe blending agent is adapted to blend with a liquid to produce a mixture with a selected property. 6801. The blending agent ofclaim 6800, wherein the blending agent comprises an API gravity of at least about 20°.

6802. The blending agent ofclaim 6800, wherein the blendhig agent comprises an acid number less than about 1.

6803. The blending agent ofclaim 6800, wherein the blending agent comprises an asphaltene weight percentage less than about 0.5 % .

6804. The blending agent ofclaim 6800, wherein the blending agent comprises a combined nifrogen, oxygen, and sulfur weight percentage less than about 5 %.

6805. The blending agent ofclaim 6800, wherein asphaltenes are substantially stable in the mixttire at ambient temperature.

6806. The blending agent ofclaim 6800, wherein the method further comprises producing the blending agent when a partial pressure ofhydrogen in the foimation is at least about 0.5 bars absolute.

6807. The blending agent ofclaim 6800, wherein the method further comprises the heat provided from at least one heat source fransfening to at least a portion ofthe foimation substantially by conduction.

6808. The blending agent ofclaim 6800, wherein the method further comprises one or more ofthe heat sources comprising heaters.

6809. The blending agent ofclaim 6800, wherein the method further comprises a ratio of energy output ofthe blending agent to energy input into the formation being at least about 5.

6810. A method for freating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: producing a first mixture from a first selected section of a relatively low peπneability formation containing heavy hydrocarbons, wherein the first mixture comprises heavy hydrocarbons; providing heat from one or more heat sources to a second selected section ofthe relatively low permeability formation containing heavy hydrocarbons such that the heat pyrolyzes at least some hydrocarbons within the second selected section; produchig a second mixture from the second selected section; and blending at least a portion ofthe first mixture with at least a portion ofthe second mixture to produce a third mixture comprising a selected property.

681 1. The method of claim 6810, further comprising cold producing the first mixture from the first selected section.

6812. The method ofclaim 6810, wherein producing the ffrst mixture from the first selected section comprises producing the first mixture through a production well in or proximate the foimation.

6813. The method of claim 6810, wherein the selected property of the thfrd mixture comprises an API gravity.

6814. The method ofclaim 6810, wherein the selected property ofthe third mixture comprises a selected viscosity.

6815. The method ofclaim 6810, wherein the selected property ofthe third mixture comprises a density.

6816. The method of claim 6810, wherein the selected property of the third mixture comprises an asphaltene to saturated hydrocarbon ratio of less than about 1.

6817. The method ofclaim 6810, wherein the selected property ofthe thfrd mixture comprises an aromatic hydrocarbon to saturated hydrocarbon ratio of less than about 4.

6818. The method ofclaim 6810, wherein asphaltenes are substantially stable in the third mixture at ambient temperature.

6819. The method ofclaim 6810, wherein the thfrd mixture is transportable.

6820. The method ofclaim 6810, wherein the third mixture is transportable through a pipeline.

6821. The method of claim 6810, wherein the liquid has a viscosity sufficiently high to inhibit economical transport ofthe liquid over 100 km via a pipeline but the mixture has a reduced viscosity that allows economical transport ofthe mixture over 100 km via a pipeline.

6822. The method ofclaim 6810, wherein the first mixture comprises an API gravity less than about 15°.

6823. The method ofclaim 6810, wherein the second mixture comprises an API gravity greater than about 25°.

6824. The method ofclaim 6810, wherein the second mixture comprises an acid number less than about 1.

6825. The method ofclaim 6810, wherein the thfrd mixture comprises less than about 50 % by weight ofthe second mixture.

6826. The method ofclaim 6810, wherein the ffrst selected section comprises a depth of at least about 500 m below the surface of a relatively low permeability formation containing heavy hydrocarbons.

6827. The method ofclaim 6810, wherein the second selected section comprises a depth less than about 500 m below the surface of a relatively low permeability formation containing heavy hydrocarbons.

6828. The method ofclaim 6810, further comprising producing a mixture when a partial pressure ofhydrogen in the formation is at least about 0.5 bars absolute.

6829. The method of claim 6810, wherein the heat provided from at least one heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6830. The method ofclaim 6810, wherein one or more ofthe heat sources comprise heaters.

6831. The method ofclaim 6810, wherein a ratio of energy output ofthe second mixture to energy input into the formation is at least about 5.

6832. A method for treating a relatively low permeability formation containing heavy hydrocarbons in situ, comprising: providing heat from one or more heat sources to a selected section of a relatively low permeability formation containing heavy hydrocarbons such that the heat pyrolyzes at least some hydrocarbons within the selected section; producing a blending agent from the selected section; and injecting at least a portion ofthe blending agent into a second section of a relatively low permeability formation containing heavy hydrocarbons to produce a mixture having a selected property, wherein the second section comprises at least some heavy hydrocarbons.

6833. The method of claim 6832, wherein the selected property ofthe mixture comprises an API gravity.

6834. The method ofclaim 6832, wherein the selected property ofthe mixture comprises an API gravity of at least about 10°.

6835. The method ofclaim 6832, wherein the selected property ofthe mixture comprises a selected viscosity.

6836. The method ofclaim 6832, wherein the selected property ofthe mixture comprises a viscosity less than about 7500 cs.

6837. The method ofclaim 6832, wherein the selected property ofthe mixture comprises a density.

6838. The method ofclaim 6832, wherein the selected property ofthe mixture comprises a density less than about 1 g/cm3.

6839. The method ofclaim 6832, wherein the selected property ofthe mixture comprises an asphaltene to saturated hydrocarbon ratio of less than about 1.

6840. The method ofclaim 6832, wherein the selected property ofthe mixture comprises an aromatic hydrocarbon to saturated hydrocarbon ratio of less than about 4.

6841. The method ofclaim 6832, wherein asphaltenes are substantially stable in the mixture at ambient temperature.

6842. The method ofclaim 6832, wherein the mixture is transportable.

6843. The method of claim 6832, wherein the mixture is transportable through a pipeline.

6844. The method ofclaim 6832, wherein second section comprises heavy hydrocarbons having an API gravity less than about 15°.

6845. The method of claim 6832, wherein the blending agent comprises an API gravity greater than about 25°.

6846. The method of claim 6832, wherein the blending agent comprises an acid number less than about 1.

6847. The method of claim 6832, wherein the mixture comprises less than about 50 % by weight ofthe blending agent.

6848. The method ofclaim 6832, wherein the selected section comprises a depth of at least about 500 m below the surface of a relatively low permeability formation containing heavy hydrocarbons.

6849. The method of claim 6832, wherein the second section comprises a depth less than about 500 m below the surface of a relatively low permeability formation containing heavy hydrocarbons.

6850. The method ofclaim 6832, wherein the selected section and the second section are located in different relatively low permeability formations containing heavy hydrocarbons.

6851. The method of claim 6832, wherein the selected section and the second section are located in different relatively low permeability formations containing heavy hydrocarbons, and wherein the different relatively low peπneability formation containing heavy hydrocarbons are vertically displaced.

6852. The method ofclaim 6832, wherein the selected section and the second section are vertically displaced within a single relatively low permeability formation containing heavy hydrocarbons.

6853. The method of clahn 6832, wherein the selected section and the second section are substantially adjacent within a single relatively low permeability formation containing heavy hydrocarbons.

6854. The method of claim 6832, wherein the blending agent is injected into a production well in the second section, and wherein the mixture is produced in the production well.

6855. The method ofclaim 6832, further comprising producing the mixture from the second section.

6856. The method ofclaim 6832, further comprising producing the blending agent when a partial pressure of hydrogen in the formation is at least about 0.5 bars absolute.

6857. The method ofclaim 6832, wherein the heat provided from at least one heat source is fransfened to at least a portion ofthe formation substantially by conduction.

6858. The method ofclaim 6832, wherein one or more ofthe heat sources comprise heaters.

6859. The method of claim 6832, wherein a ratio of energy output ofthe produced mixture to energy input into the foimation is at least about 5.