US20080016768A1 - Chemically-modified mixed fuels, methods of production and used thereof - Google Patents

Chemically-modified mixed fuels, methods of production and used thereof Download PDF

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Publication number
US20080016768A1
US20080016768A1 US11/489,143 US48914306A US2008016768A1 US 20080016768 A1 US20080016768 A1 US 20080016768A1 US 48914306 A US48914306 A US 48914306A US 2008016768 A1 US2008016768 A1 US 2008016768A1
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methane
gas
fuel
chemically
source
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US11/489,143
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Keith A. Togna
Craig T. Euen
Steven W. Weeks
Mohammed I. Loya
Matthew C. Warren
Richard H. Kendrick
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Honeywell International Inc
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Honeywell International Inc
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Priority to US11/489,143 priority Critical patent/US20080016768A1/en
Assigned to HONEYWELL INTERNATIONAL INC. reassignment HONEYWELL INTERNATIONAL INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WEEKS, STEVEN W., EUEN, CRAIG T., KENDRICK, RICHARD H., LOYA, MOHAMMED I., TONGA, KEITH A., WARREN, MATTHEW C.
Publication of US20080016768A1 publication Critical patent/US20080016768A1/en
Priority to US13/412,094 priority patent/US8545580B2/en
Priority to US13/971,999 priority patent/US8980802B2/en
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the field of the subject matter disclosed herein is chemically-modified mixed fuels comprising at least one natural gas source. Methods of production of these fuels and appropriate uses are also disclosed.
  • New and modified fuels are being investigated for both their abilities to efficiently and effectively provide energy, while at the same time lowering the cost of acquiring and utilizing the fuel.
  • fuel that is provided from renewable or consistent resources will be the most cost efficient option in the long-term, but the fuel should be accessible and relatively easy to use from the standpoint that it is clean fuel which is provided in its usable form.
  • a Kellogg Reforming System or Kellogg Primary Reformer can be utilized in the formation of ammonia.
  • the Kellogg Reformer ( 100 ) uses natural gas as a fuel source for the process and a combination of natural gas and steam as reactants during the process. While natural gas is a cleaner burning fuel that other fuel sources, it can be expensive to acquire and utilize on a regular basis.
  • fuel ( 110 ) and a combination of natural gas and steam ( 120 ) is introduced into the primary reformer ( 130 ), which contains a plurality of catalyst tubes ( 140 ).
  • natural gas primarily comes from the breakdown of fossils in the earth's crust, which is obviously neither a renewable or consistent resource.
  • Other sources of natural gas are so-called “unconventional” resources, which includes “deep natural gas”, “tight natural gas”, “Devonian shale gas”, “coalbed methane”, “geopressurized zones” and “methane hydrates”. All of these sources are considered “unconventional”, because they are either difficult to reach or extract or not certain to produce large quantities of natural gas.
  • ideal fuels and fuel sources should be a) renewable and/or a consistent resource (e.g. biogenic fuels), b) easy to use, c) easy to transport and d) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form.
  • a consistent resource e.g. biogenic fuels
  • a chemically-modified mixed fuel has been produced, wherein at least part of the fuel is a) cost-efficient, b) renewable and/or a consistent resource (e.g. biogenic fuels), c) easy to use, d) easy to transport and e) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form.
  • a consistent resource e.g. biogenic fuels
  • a chemically-modified mixed fuel that comprises methane gas from at least two methane-production sources.
  • this chemically-modified mixed fuel can be utilized in any process that incorporates a Kellogg Primary Reformer.
  • a method for producing the chemically-modified mixed fuel described herein comprises a) providing a first methane-containing gas from a first methane-production source, b) providing a second methane-containing gas from a second methane-production source, c) blending the first methane-containing gas with the second methane-containing gas at a suitable pressure to form a chemically-modified mixed fuel.
  • at least one additional methane-containing gas can be provided from at least one additional methane-production source and blended with the chemically-modified fuel.
  • FIG. 1 shows a contemplated Kellogg Reforming Exchanger System
  • FIG. 2 shows a contemplated Kellogg System.
  • FIG. 3 shows a contemplated Kellogg System wherein landfill gas is introduced to form a chemically-modified mixed fuel.
  • a chemically-modified mixed fuel has been produced, wherein at least part of the fuel is a) cost-efficient, b) renewable and/or a consistent resource (e.g. biogenic fuels), c) easy to use, d) easy to transport and e) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form.
  • a consistent resource e.g. biogenic fuels
  • a chemically-modified fuel that comprises methane gas from at least two methane-production sources.
  • this chemically-modified fuel can be utilized in any process that incorporates a Kellogg Primary Reformer.
  • a “methane-production source”, as it sounds, is used herein to describe a source of methane gas and/or methane gas production.
  • Contemplated “methane-production sources” may comprise a general natural gas source, a fossil fuel source, a biogenic fuel source, such as a landfill, an abiogenic source, an “unconventional” source, such as those described herein previously or a combination thereof.
  • a first methane-production source comprises a fossil fuel source and a second methane-production source comprises a landfill.
  • First and second gas streams that comprise methane come from the first methane-production source and second methane-production source respectively.
  • the at least one methane-production source produces gas and/or gas streams that comprise natural gas, Area-6 gas, landfill gas or a combination thereof.
  • gas streams that come from each of the methane-production sources are contemplated to comprise various components, in addition to methane. It should be understood, however, that methane is a significant component of each gas stream.
  • typical natural gas from a fossil fuel source comprises 70-90% of methane, 0-20% of propane, 0-8% of carbon dioxide, 0-0.2% of oxygen, 0-5% of nitrogen, 0-5% of hydrogen sulphide and trace amounts of rare gases, such as argon, helium, neon or xenon.
  • Landfill gas from a biogenic fuel source generally comprises about 45-50% of methane, about 35% of carbon dioxide about 12% of nitrogen, about 1-4% of oxygen, and trace amounts of ethane, propane, isobutane, n-butane, isopentane and other organics.
  • the heat value of landfill gas is approximately 500 BTU's/scf (standard cubic foot), which is about half the heat value of natural gas. In fuel applications, approximately one scf of landfill gas will displace 1 ⁇ 2 scf of natural gas.
  • landfill gas As a viable fuel alternative. There are about 120 landfill gas projects in the United States wherein landfill gas is being utilized as an alternative fuel source. As solid waste decomposes in the landfill, methane and carbon dioxide gases are produced. Some landfills, such as the Waverly landfill, increase the decomposition rate in the landfill by reclaiming the landfill's leachate and applying it on the landfill's contents. As the gas is generated, large underground pockets are formed, which eventually will percolate to the surface and discharge to the environment. To prevent this environmental problem, landfills have historically captured the gas before it reaches the surface and burned it in a flare.
  • a method for producing the chemically-modified mixed fuel described herein comprises a) providing a first methane-containing gas from a first methane-production source, b) providing a second methane-containing gas from a second methane-production source, c) blending the first methane-containing gas with the second methane-containing gas at a suitable pressure to form a chemically-modified mixed fuel.
  • at least one additional methane-containing gas can be provided from at least one additional methane-production source and blended with the chemically-modified fuel. Therefore, in the chemically-modified fuels produced herein, there will be at least two methane-containing gas streams that are combined to form the fuel.
  • a chemically-modified fuel is produced specifically for use in a Kellogg Primary Reformer.
  • natural gas is burned in three places within the Kellogg facility—the primary reformer arch burners, the primary reformer tunnel burners and the auxiliary boiler.
  • the auxiliary boiler provides supplemental high-pressure steam that is used as a process reactant and to provide mechanical work in various turbine-driven machines locally.
  • the tunnel burners provide supplemental heat to the primary reformer furnace, and the arch burners are the main source of heat for the reaction of methane and water occurring in the primary reformer.
  • the auxiliary boiler burns approximately 3000 scfm (standard cubic feet per minute) of 100% natural gas.
  • the firing of this boiler is tightly controlled to maintain a consistent total steam rate and pressure.
  • the tunnel burners consume approximately 800 scfm of 100% natural gas.
  • the firing of the tunnel burners is controlled automatically based on the desired temperature within the convection section of the furnace.
  • the arch burners consume a blend of approximately 2000 scfm of “Area-6 recycle gas”, which comprises 43% hydrogen, 40% nitrogen and 17% methane and about 8000 scfm of natural gas.
  • the firing of the arch burners is controlled automatically to maintain the desired temperature in the radiant section of the furnace.
  • Combustion air is provided to the three burner applications via a single forced draft (FD) fan and duct system.
  • the combustion flue gases from the three burner applications combine in a common duct system where process heaters and a combustion air pre-heater recover heat from the flue gas stream, as it is pulled from the furnace via a single induced draft (ID) fan and exits through a single stack.
  • FIG. 2 shows the fuel/flue gas system described herein.
  • combustion air ( 210 ) is provided into the system ( 200 ) by a forced draft fan and duct arrangement ( 220 ), as previously described. This air ( 210 ) travels to the auxiliary boiler ( 230 ) and the primary reformer ( 240 ).
  • Natural gas ( 250 ) is introduced to the system ( 200 ) as the fuel source, with “Area-6 gas” ( 255 ) also introduced in the natural gas stream ( 250 ) for the primary reformer ( 240 ).
  • the flue gas stream ( 260 ) is pulled from the furnace via a single induced draft fan ( 270 ) and exits through a stack ( 280 ).
  • Tables 1 and 2 are directly related to the process shown in FIG. 2 , in that the numbers 1-15 shown in FIG. 2 are shown also in Tables 1 and 2. The data measured at those locations are also presented in Tables 1 and 2.
  • Contemplated chemically-modified fuel produced for use in this Kellogg Primary Reformer comprises methane-containing gas from a natural gas source and methane-containing gas from a biogenic gas source.
  • the biogenic gas source in this example is a landfill. Only the fuel portion of the natural gas is displaced with landfill gas in this case. The use of landfill gas to displace a portion of the natural gas will significantly reduce the Kellogg Primary Reformer's fuel costs, not to mention the fact that landfill gas can be considered a “renewable resource”.
  • a detailed example showing this particular embodiment is shown in the Examples Section as Example 1. Practical considerations and typical equipment arrangements are also disclosed in the Examples section.
  • FIG. 3 shows an updated arrangement of FIG. 2 , including a landfill gas stream.
  • combustion air ( 310 ) is provided into the system ( 300 ) by a forced draft fan and duct arrangement ( 320 ), as previously described. This air ( 310 ) travels to the auxiliary boiler ( 330 ) and the primary reformer ( 340 ).
  • Natural gas ( 350 ) is introduced to the system ( 300 ) as the fuel source, with “Area-6 gas” ( 355 ) and Land Fill Gas ( 357 ) also introduced in the natural gas stream ( 350 ) for the primary reformer ( 340 ).
  • the flue gas stream ( 360 ) is pulled from the furnace via a single induced draft fan ( 370 ) and exits through a stack ( 380 ).
  • Tables 3 and 4 are directly related to the process shown in FIG. 3 , in that the numbers 1-16 shown in FIG. 3 are shown also in Tables 3 and 4. The data measured at those locations are also presented in Tables 3 and 4.
  • a chemically-modified mixed fuel can be produced that combines three or more methane-containing gas streams from at least two different sources. It should also be understood that other gas streams—such as recycle gas, inert gases, non-methane-based hydrocarbon gases, etc can be added to the chemically-modified mixed fuel, as long as there is at least a first methane-containing gas and a second methane-containing gas that are mixed to form the chemically-modified mixed fuel.
  • synthetic gases including those that may contain significant amounts of methane, may be utilized alone or in combination with natural, non-synthetic gases. These synthetic gases would need to be able to replace some of the natural gases currently being used in the target process without leading to expensive apparatus modifications or expensive starting materials.
  • the methane-containing gases utilized in the production of the chemically-modified mixed fuels, along with any other additional gases, should be blended at a suitable pressure in order to address concerns with respect to flow rate and also to address additional pressure considerations needed later in the particular process.
  • the first methane-containing gas may be held at a lower pressure initially in order to affect blending with the second methane-containing gas.
  • the chemically-modified mixed gas may then be transported under increasing pressure until reaching the optimum pressure for the particular process—such as the Kellogg process described herein.
  • the suitable pressure does not necessarily refer to the pressure needed for the process that is utilizing the fuel, but instead refers to the pressure needed to optimally blend the gas streams to form the mixed gas fuel.
  • Enerdyne Power Systems, Inc. in conjunction with Waverly Gas Producers, LLC has proposed to supply landfill gas to the Honeywell Hopewell Plant (Kellogg site).
  • the source of the landfill gas is the landfill located in Waverly, Va.
  • landfill gas Approximately 3000 scfm of landfill gas is currently available to displace approximately 1500 scfm of natural gas in the Kellogg plant.
  • the available landfill gas is used to displace the natural gas being burned in the arch burners of the primary reformer.
  • the arch burners are the best option for the chemically-modified fuels because they already burn a blended fuel stream containing inerts (the A-6 recycle gas described herein).
  • the displaced natural gas volume in this Example is relatively small compared to the total fuel volume and there is minimal risk to process reliability.
  • the price of landfill gas is fixed for the first 18 months at $3.20/DKT, and thereafter, the price of landfill gas will be based on the price of natural gas at that time.
  • the landfill gas price is determined by averaging the current delivered cost of natural gas and the delivered floor price of landfill gas.
  • the total savings expected over the 15-year life of the project for this Example is projected to be $15-30 million.
  • the gas is then transferred via an 18′′ pipeline from the landfill site to the Kellogg site.
  • the landfill gas reaches the Kellogg site, its pressure is approximately 40 psig (pounds per square inch gauge).
  • the flow rate of the landfill gas is metered for billing purposes.
  • the landfill gas can be sampled and analyzed at this point to review and ensure gas quality and requirements.
  • An on-site compression station is utilized at this point to increase the pressure of the gas from about 40 psig to a minimum of 75 psig that is required for use in the Kellogg Primary Reformer arch burners.
  • a typical compressor used for this purpose is installed in a modular fashion, with the initial, single compressor powered by one 300 HP, 3600 RPM motor and is designed to handle 4000 scfm of landfill gas. Single compressors can be added over time as the volume of landfill gas is increased.
  • the landfill gas After compression, the landfill gas passes through a coalescing filter to assure the dryness of the gas before being routed to the Primary Reformer. The landfill gas is then blended with the Reformer's arch burner fuel stream. Table 5 shows the existing and modified fuel flow rates at the initial flow rate of the landfill gas (3000 scfm).
  • the combustion air requirement is expected to be similar to existing conditions. Specifically, the calculated combustion air requirement for landfill gas is 0.40% less than existing conditions.
  • the total volume of flue gas will not significantly change with landfill gas. Specifically, the total volume of flue gas will increase by only about 0.61%.
  • GC-21 On-Site Landfill Gas Compressor Vilter Model VSSG-1501 oil flooded screw compressor, 4000 scfm capacity, 30 psig suction, 75 psig discharge.
  • the compressor is capable of a continuous 100 psig discharge.
  • the compressor has a 300 HP, 3600 RPM, 4160 VAC, 3 phase capacity.
  • a Modicon PLC control panel is included.
  • the overall goal is to burn all of the landfill gas that is available all of the time.
  • the capacity of the landfill gas compressor will be controlled from the skid-mounted Modicon PLC controller utilizing the slide valve (essentially an internal recycle valve) on the compressor and an external recycle valve.
  • a split pressure control system will be used. If the discharge pressure reaches 85 psig, the compressor will go to recycle control and will hold a fixed discharge pressure at approximately 85 psig. When the discharge pressure falls below 85 psig, the compressor will switch over to suction pressure control and will then control to a suction pressure set point (preliminarily set for 20 psig). This control will all be done by the PLC-based control system supplied with the compressor.
  • the process effluent temperature from the primary reformer will continue to be controlled by TIC-117 cascading to HFC-2700 (BTU controller), cascading to FIC-778 (natural gas fuel to the primary reformer).
  • BTU controller cascading to HFC-2700
  • FIC-778 natural gas fuel to the primary reformer
  • the BTU calculation is modified to include the energy input from the landfill gas in the calculation (it currently includes the Area-6 return gas and the natural gas to the primary reformer). This control scheme will allow for constant BTU supply to the reformer with any (or no) landfill gas flow.
  • a double block and bleed system is installed in the landfill gas line similar to that which is installed into the Area-6 return gas line. This system will activate via a single solenoid valve to positively block off the landfill gas flow to the fuel system. The double block and bleeds will trip and will close HV-721A and HV-721B and open HV-721C on the following conditions:
  • Restriction orifice is 4′′, 300# flanges, 0.723′′ orifice (designed to pass 2000 scfm maximum at a 250 psig inlet pressure).
  • This relief valve will protect the landfill gas suction piping from natural gas overpressurization when purging back to the landfill.
  • This valve should be a 2J3 for natural gas service.
  • Set pressure is 60 psig.
  • the compressor has a suction scrubber that discharges moisture to drain. Little to no moisture is expected to be present.
  • the loss of landfill gas pressure is seen because of on-site compression failure. On-site compression failure could cause low gas pressure at the burners resulting in a plant trip.
  • the natural gas control valve which is upstream of the blending point, is designed to control the desired pressure at the burners. In the event of loss of on-site landfill gas compression, the natural gas control valve will open to provide the additional fuel required for maintaining adequate pressure.
  • the loss of landfill pressure could also occur because of off-site compression failure at the landfill site, for example. This risk can be minimized by providing adequate notification and adjustment points along the pipeline at designated points.
  • the existing natural gas control valve system is designed to compensate for the loss of landfill gas flow.
  • Supply piping corrosion may also occur as a function of moisture content in the landfill gas and its dew point. This concern can be addressed by the use of HDPE piping underground and installation of the coalescing filter to remove traces of moisture in the gas. Also, exiting the on-site compressor, the temperature of the landfill gas will be approximately 160° F.—well above its dew point.
  • Landfill gas comprises 1-4% oxygen. Since Area-6 return gas or Kellogg purge gas (when Cryo is down) contain hydrogen, there is a concern regarding the hydrogen explosion limits of the blended fuel stream.
  • Computer modeling was utilized to determine the potential for explosion under a worst case scenario: 4% oxygen in landfill gas and Kellogg burning 6000 scfm purge gas with 70% hydrogen. The results of the computer modeling indicate that the addition of air (additional oxygen) is required to combust the blend of gases, and therefore, the stream is not explosive. In order to address this concern, redundant oxygen analyzers have been installed to monitor the oxygen content of the landfill gas.
  • Interlocks have been set up to trip the double block and bleed system that will stop the flow of landfill gas if an oxygen content of 4% or greater is detected on either analyzer.
  • Thermocouples have also been installed in multiple locations that will also trip the landfill gas should a high temperature be reached—which indicates combustion within the pipe. If high oxygen is detected, it will be necessary to purge the piping of the gas prior to reintroduction into the fuel gas system. This reintroduction can be accomplished by using natural gas to push the landfill gas backward through the pipeline into the landfill.
  • a restriction orifice has been sized to allow a maximum of 2000 scfm of natural gas for this purpose. Since the natural gas is at a normal supply pressure of 250 psig, a relief valve will be set for 60 psig and can pass in excess of 2400 scfm.
  • Siloxane is a compound contained in many consumer products, and therefore, it can be found in landfills.
  • the siloxane contaminates the landfill gas, and when combusted, forms a fine, white dust on furnace surfaces. If the furnace surface temperature exceeds 1900° F., the white siloxane dust transforms into an adherent glassy compound. This deposition will severely foul the process heat transfer coils within the convection section and force a Kellogg shutdown. The coils may also have to be replaced, as a result of the deposition, which would lead to a prolonged shutdown.

Abstract

A chemically-modified mixed fuel has been produced, wherein at least part of the fuel is a) cost-efficient, b) renewable and/or a consistent resource (e.g. biogenic fuels), c) easy to use, d) easy to transport and e) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form. Specifically, a chemically-modified mixed fuel has been developed that comprises methane gas from at least two methane-production sources. In addition, this chemically-modified mixed fuel can be utilized in any process that incorporates a Kellogg Primary Reformer. A method for producing the chemically-modified mixed fuel described herein comprises a) providing a first methane-containing gas from a first methane-production source, b) providing a second methane-containing gas from a second methane-production source, c) blending the first methane-containing gas with the second methane-containing gas at a suitable pressure to form a chemically-modified mixed fuel. In additional embodiments, at least one additional methane-containing gas can be provided from at least one additional methane-production source and blended with the chemically-modified fuel.

Description

    FIELD OF THE SUBJECT MATTER
  • The field of the subject matter disclosed herein is chemically-modified mixed fuels comprising at least one natural gas source. Methods of production of these fuels and appropriate uses are also disclosed.
    • BACKGROUND
  • New and modified fuels are being investigated for both their abilities to efficiently and effectively provide energy, while at the same time lowering the cost of acquiring and utilizing the fuel. Obviously, fuel that is provided from renewable or consistent resources will be the most cost efficient option in the long-term, but the fuel should be accessible and relatively easy to use from the standpoint that it is clean fuel which is provided in its usable form.
  • One process that uses fuel is the synthesis of ammonia. A Kellogg Reforming System or Kellogg Primary Reformer, as shown in Prior Art FIG. 1, can be utilized in the formation of ammonia. The Kellogg Reformer (100) uses natural gas as a fuel source for the process and a combination of natural gas and steam as reactants during the process. While natural gas is a cleaner burning fuel that other fuel sources, it can be expensive to acquire and utilize on a regular basis. As shown in Prior Art FIG. 1, fuel (110) and a combination of natural gas and steam (120) is introduced into the primary reformer (130), which contains a plurality of catalyst tubes (140). Flue gas (150) exits from the primary reformer (130), while at the same time, fuel (160) for the secondary reformer (170) travels from the primary reformer (130) into the secondary reformer (170) and is mixed with air (180). Reformed gas (190) then exits the secondary reformer (170).
  • In addition, natural gas primarily comes from the breakdown of fossils in the earth's crust, which is obviously neither a renewable or consistent resource. Other sources of natural gas are so-called “unconventional” resources, which includes “deep natural gas”, “tight natural gas”, “Devonian shale gas”, “coalbed methane”, “geopressurized zones” and “methane hydrates”. All of these sources are considered “unconventional”, because they are either difficult to reach or extract or not certain to produce large quantities of natural gas.
  • Therefore, it would be ideal to find a more cost-efficient fuel source which can displace at least part of the natural gas required for the process to run. In addition to being cost-efficient, ideal fuels and fuel sources should be a) renewable and/or a consistent resource (e.g. biogenic fuels), b) easy to use, c) easy to transport and d) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form.
    • SUMMARY OF THE SUBJECT MATTER
  • A chemically-modified mixed fuel has been produced, wherein at least part of the fuel is a) cost-efficient, b) renewable and/or a consistent resource (e.g. biogenic fuels), c) easy to use, d) easy to transport and e) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form.
  • Specifically, a chemically-modified mixed fuel has been developed that comprises methane gas from at least two methane-production sources. In addition, this chemically-modified mixed fuel can be utilized in any process that incorporates a Kellogg Primary Reformer.
  • A method for producing the chemically-modified mixed fuel described herein comprises a) providing a first methane-containing gas from a first methane-production source, b) providing a second methane-containing gas from a second methane-production source, c) blending the first methane-containing gas with the second methane-containing gas at a suitable pressure to form a chemically-modified mixed fuel. In additional embodiments, at least one additional methane-containing gas can be provided from at least one additional methane-production source and blended with the chemically-modified fuel.
    • BRIEF DESCRIPTION OF THE FIGURES
  • Prior Art FIG. 1 shows a contemplated Kellogg Reforming Exchanger System
  • FIG. 2 shows a contemplated Kellogg System.
  • FIG. 3 shows a contemplated Kellogg System wherein landfill gas is introduced to form a chemically-modified mixed fuel.
    •  DETAILED DESCRIPTION
  • A chemically-modified mixed fuel has been produced, wherein at least part of the fuel is a) cost-efficient, b) renewable and/or a consistent resource (e.g. biogenic fuels), c) easy to use, d) easy to transport and e) relatively “clean” with respect to the amount of time/resources it requires to convert the fuel to a “useable” form.
  • Specifically, a chemically-modified fuel has been developed that comprises methane gas from at least two methane-production sources. In addition, this chemically-modified fuel can be utilized in any process that incorporates a Kellogg Primary Reformer.
  • A “methane-production source”, as it sounds, is used herein to describe a source of methane gas and/or methane gas production. Contemplated “methane-production sources” may comprise a general natural gas source, a fossil fuel source, a biogenic fuel source, such as a landfill, an abiogenic source, an “unconventional” source, such as those described herein previously or a combination thereof. In some embodiments, a first methane-production source comprises a fossil fuel source and a second methane-production source comprises a landfill. First and second gas streams that comprise methane come from the first methane-production source and second methane-production source respectively. The at least one methane-production source produces gas and/or gas streams that comprise natural gas, Area-6 gas, landfill gas or a combination thereof.
  • The gas streams that come from each of the methane-production sources are contemplated to comprise various components, in addition to methane. It should be understood, however, that methane is a significant component of each gas stream. For example, typical natural gas from a fossil fuel source comprises 70-90% of methane, 0-20% of propane, 0-8% of carbon dioxide, 0-0.2% of oxygen, 0-5% of nitrogen, 0-5% of hydrogen sulphide and trace amounts of rare gases, such as argon, helium, neon or xenon. Landfill gas from a biogenic fuel source generally comprises about 45-50% of methane, about 35% of carbon dioxide about 12% of nitrogen, about 1-4% of oxygen, and trace amounts of ethane, propane, isobutane, n-butane, isopentane and other organics. The heat value of landfill gas is approximately 500 BTU's/scf (standard cubic foot), which is about half the heat value of natural gas. In fuel applications, approximately one scf of landfill gas will displace ½ scf of natural gas.
  • The fuel industry has recognized landfill gas as a viable fuel alternative. There are about 120 landfill gas projects in the United States wherein landfill gas is being utilized as an alternative fuel source. As solid waste decomposes in the landfill, methane and carbon dioxide gases are produced. Some landfills, such as the Waverly landfill, increase the decomposition rate in the landfill by reclaiming the landfill's leachate and applying it on the landfill's contents. As the gas is generated, large underground pockets are formed, which eventually will percolate to the surface and discharge to the environment. To prevent this environmental problem, landfills have historically captured the gas before it reaches the surface and burned it in a flare.
  • A method for producing the chemically-modified mixed fuel described herein comprises a) providing a first methane-containing gas from a first methane-production source, b) providing a second methane-containing gas from a second methane-production source, c) blending the first methane-containing gas with the second methane-containing gas at a suitable pressure to form a chemically-modified mixed fuel. In additional embodiments, at least one additional methane-containing gas can be provided from at least one additional methane-production source and blended with the chemically-modified fuel. Therefore, in the chemically-modified fuels produced herein, there will be at least two methane-containing gas streams that are combined to form the fuel.
  • In one contemplated embodiment, a chemically-modified fuel is produced specifically for use in a Kellogg Primary Reformer. As a fuel, natural gas is burned in three places within the Kellogg facility—the primary reformer arch burners, the primary reformer tunnel burners and the auxiliary boiler. The auxiliary boiler provides supplemental high-pressure steam that is used as a process reactant and to provide mechanical work in various turbine-driven machines locally. The tunnel burners provide supplemental heat to the primary reformer furnace, and the arch burners are the main source of heat for the reaction of methane and water occurring in the primary reformer.
  • The auxiliary boiler burns approximately 3000 scfm (standard cubic feet per minute) of 100% natural gas. The firing of this boiler is tightly controlled to maintain a consistent total steam rate and pressure. The tunnel burners consume approximately 800 scfm of 100% natural gas. The firing of the tunnel burners is controlled automatically based on the desired temperature within the convection section of the furnace. The arch burners consume a blend of approximately 2000 scfm of “Area-6 recycle gas”, which comprises 43% hydrogen, 40% nitrogen and 17% methane and about 8000 scfm of natural gas. The firing of the arch burners is controlled automatically to maintain the desired temperature in the radiant section of the furnace.
  • Combustion air is provided to the three burner applications via a single forced draft (FD) fan and duct system. The combustion flue gases from the three burner applications combine in a common duct system where process heaters and a combustion air pre-heater recover heat from the flue gas stream, as it is pulled from the furnace via a single induced draft (ID) fan and exits through a single stack. FIG. 2 shows the fuel/flue gas system described herein. In this Figure, combustion air (210) is provided into the system (200) by a forced draft fan and duct arrangement (220), as previously described. This air (210) travels to the auxiliary boiler (230) and the primary reformer (240). Natural gas (250) is introduced to the system (200) as the fuel source, with “Area-6 gas” (255) also introduced in the natural gas stream (250) for the primary reformer (240). The flue gas stream (260) is pulled from the furnace via a single induced draft fan (270) and exits through a stack (280). Tables 1 and 2 are directly related to the process shown in FIG. 2, in that the numbers 1-15 shown in FIG. 2 are shown also in Tables 1 and 2. The data measured at those locations are also presented in Tables 1 and 2.
  • TABLES 1 and 2
    Combustion Air and Flue Gas System
    Stream Number
    0 1 2 3 4 5 6 7 8 9
    Compo- MW
    nent
    Nitro- 28.0 77.50% 77.50% 77.50% 77.50% 77.50%
    gen
    Carbon 44.0 0.10% 0.10% 0.10% 0.10% 0.10%
    Dioxide
    Carbon 28.0 0.00% 0.00% 0.00% 0.00% 0.00%
    Mon-
    oxide
    Oxygen 32.0 20.80% 20.80% 20.80% 20.80% 20.80%
    Argon 40.0 0.90% 0.90% 0.90% 0.90% 0.90%
    Water 18.0 0.70% 0.70% 0.70% 0.70% 0.70%
    Total 100.00% 100.00% 100.00% 100.00% 100.00%
    Mol 28.886 28.886 28.886 28.886 28.886 27.71 27.82 27.74 27.74 27.74
    Weight
    Total MPH 19420 19420 14100 5320 1391 17150 5822 22972 22972 22972
    Mole
    Total lb/hr 560963 560963 407287 153677 40194 475305 161978 637283 637283 637283
    Wgt
    Std SCFM 122669 122669 89064 33605 8790 108330 36775 145105 145105 145105
    Volume
    Actual ACFM 127387 257429 187812 70865 9132 502685 140509 332676 212204 202309
    Volume
    Excess % 10% 10% 10%
    Air
    Excess % 2.1% 2.1% 2.1%
    O2
    Pressure “H2O 0.0 7.0 5.0 5.0 −0.2 −0.5 −5.5 −11.0 −19.0 0.0
    Temp- Deg F. 80 650 650 650 80 1950 1500 700 265 265
    erature
    Total Primary Reformer Heat 513.0 MBTU/Hr
    Input:
    Total Auxilliary Boiler Heat Input 175.0 MBTU/Hr
    BTU/Burner 3.03 MBTU/Hr
    Fuel Gas System
    Stream Number
    10 11 12 13 14 15 Pri Tot
    Component MW LHV HHV
    Nitrogen 28.0 0.0 0.0 1.00% 1.00% 1.00% 1.00% 9.98% 32.00% 9.31%
    Oxygen 32.0 0.0 0.0 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00%
    Carbon Dioxide 44.0 0.0 0.0 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00%
    Carbon 28.0 321.0 321.0 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00%
    Monoxide
    Methane CH4 16.0 911.0 1012.0 94.30 94.30% 94.30% 94.30% 74.23% 25.00% 75.72%
    Ethane C2H6 30.0 1622.0 1773.0 2.50 2.50% 2.50% 2.50% 1.78% 0.00% 1.83%
    Propane C3H8 44.1 2322.0 2524.0 1.00% 1.00% 1.00% 1.00% 0.71% 0.00% 0.73%
    Butane C4H10 58.1 3018.0 3271.0 1.00% 1.00% 1.00% 1.00% 0.71% 0.00% 0.73%
    Hydrogen  2.0 275.0 325.0 0.20% 0.20% 0.20% 0.20% 12.59% 43.00% 11.68%
    Water 18.0 0.0 0.0 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00%
    Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%
    MW 17.14 17.14 17.14 17.14 16.18 13.82 16.25
    Net LHV BTU/SCF 954 954 954 954 778 346 791
    Net HHV BTU/SCF 1057 1057 1057 1057 865 393 879
    Total Mole MPH 1737 484 1126 127 1585 459 1712
    Total Wgt lb/hr 29781 8302 19308 2171 25653 6345 27824
    Std Volume SCFM 10973 3059 7114 800 10014 2900 10814
    Heat Input KBTU/Min 10463 2917 6784 763 7787 1003 8550
    Pressure PSIG 135 10 135 10 75 75 75
    Temperature Deg F. 60 60 360 360 279 80 100
    A/F Ratio 10.99 10.99 8.89 9.05
  • Contemplated chemically-modified fuel produced for use in this Kellogg Primary Reformer comprises methane-containing gas from a natural gas source and methane-containing gas from a biogenic gas source. The biogenic gas source in this example is a landfill. Only the fuel portion of the natural gas is displaced with landfill gas in this case. The use of landfill gas to displace a portion of the natural gas will significantly reduce the Kellogg Primary Reformer's fuel costs, not to mention the fact that landfill gas can be considered a “renewable resource”. A detailed example showing this particular embodiment is shown in the Examples Section as Example 1. Practical considerations and typical equipment arrangements are also disclosed in the Examples section. FIG. 3 shows an updated arrangement of FIG. 2, including a landfill gas stream. In this Figure, combustion air (310) is provided into the system (300) by a forced draft fan and duct arrangement (320), as previously described. This air (310) travels to the auxiliary boiler (330) and the primary reformer (340). Natural gas (350) is introduced to the system (300) as the fuel source, with “Area-6 gas” (355) and Land Fill Gas (357) also introduced in the natural gas stream (350) for the primary reformer (340). The flue gas stream (360) is pulled from the furnace via a single induced draft fan (370) and exits through a stack (380). Tables 3 and 4 are directly related to the process shown in FIG. 3, in that the numbers 1-16 shown in FIG. 3 are shown also in Tables 3 and 4. The data measured at those locations are also presented in Tables 3 and 4.
  • TABLES 3 and 4
    Combustion Air and Flue Gas System
    Stream Number
    0 1 2 3 4 5 6 7 8 9
    Component MW
    Nitrogen 28.0 77.50% 77.50% 77.50% 77.50% 77.50%
    Carbon 44.0 0.10% 0.10% 0.10% 0.10% 0.10%
    Dioxide
    Carbon 28.0 0.00% 0.00% 0.00% 0.00% 0.00%
    Monoxide
    Oxygen 32.0 20.80% 20.80% 20.80% 20.80% 20.80%
    Argon 40.0 0.90% 0.90% 0.90% 0.90% 0.90%
    Water 18.0 0.70% 0.70% 0.70% 0.70% 0.70%
    Total 100.00% 100.00% 100.00% 100.00% 100.00%
    Mol Weight 28.886 28.886 28.886 28.886 28.886 25.59 27.82 26.15 26.15 26.15
    Total Mole MPH 19420 19420 14099 5320 1391 17372 5822 23194 23194 23194
    Total Wgt lb/hr 560954 560954 407277 153677 40194 444616 161978 606594 606594 606594
    Std Volume SCFM 122667 122667 89062 33605 8790 109734 36775 146508 146508 146508
    Actual ACFM 127385 257425 187808 70865 9132 509198 140509 335894 214257 204266
    Volume
    Excess Air % 10% 10% 10%
    Excess O2 % 2.1% 2.1% 2.1%
    Pressure “H2O 0.0 7.0 5.0 5.0 −0.2 −0.5 −5.5 −11.0 −19.0 0.0
    Temperature Deg F. 80 650 650 650 80 1950 1500 700 265 265
    Total Primary Reformer Heat Input: 513.0 MBTU/Hr
    Total Auxilliary Boiler Heat Input 175.0 MBTU/Hr
    % Change in FD Fan Suction 0.00% Decrease in Flow as Compared to As
    Flow Is Case
    % Change in ID Fan Suction 0.97% Increase in Flow as Compared to As Is
    Flow Case
    CO2 Available in Land Fill 113.3 TPD
    Gas:
    Fuel Gas System
    Stream Number
    10 11 12 13 14 15 16 Pri Tot
    Component MW LHV HHV
    Nitrogen 28.0 0.0 0.0 1.00% 1.00% 1.00% 1.00% 8.84% 32.00% 1.00% 8.33%
    Oxygen 32.0 0.0 0.0 0.00% 0.00% 0.00% 0.00% 0.05% 0.00% 0.20% 0.05%
    Carbon 44.0 0.0 0.0 0.00% 0.00% 0.00% 0.00% 11.82% 0.00% 45.20% 11.05%
    Dioxide
    Carbon 28.0 321.0 321.0 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00%
    Monoxide
    Methane 16.0 911.0 1012.0 94.30% 94.30% 94.30% 94.30% 66.10% 25.00% 53.45% 67.94%
    CH4
    Ethane 30.0 1622.0 1773.0 2.50% 2.50% 2.50% 2.50% 1.23% 0.00% 0.05% 1.31%
    C2H6
    Propane 44.1 2322.0 2524.0 1.00% 1.00% 1.00% 1.00% 0.50% 0.00% 0.04% 0.53%
    C3H8
    Butane 58.1 3018.0 3217.0 1.00% 1.00% 1.00% 1.00% 0.50% 0.00% 0.06% 0.53%
    C4H10
    Hydrogen  2.0 275.0 325.0 0.20% 0.20% 0.20% 0.20% 10.97% 43.00% 0.00% 10.27%
    Water 18.0 0.0 0.0 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00% 0.00%
    Total 100.00% 100.00% 100.00% 100.00% 100.00% 100.00% 100.00% 100.00%
    MW 17.14 17.14 17.14 17.14 19.37 13.82 28.85 19.22
    Net LHV BTU/SCF 954 954 954 954 679 346 490 697
    Net HHV BTU/SCF 1057 1057 1057 1057 755 393 545 775
    Total Mole MPH 1493 484 882 127 1816 459 475 1943
    Total Wgt lb/hr 25593 8302 15120 2171 35167 6345 13703 37339
    Std Volume SCFM 9430 3059 5571 800 11471 2900 3000 12271
    Heat Input KBTU/ 8992 2917 5312 763 7787 1003 1471 8550
    Min
    Pressure PSIG 135 10 135 25 75 75 75 0
    Temperature Deg F. 60 60 360 360 236 80 157 0
    Gas Density lb/ft♯ ♭3 0.4607 0.0760 0.2921 0.0775 0.2329 0.2143 0.3915
    Line ID Inches 6.065 6.065 7.981 3.068 7.981 6.065 12.390
    Line FPS 76.9 151.2 41.4 151.6 120.7 41.0 11.6
    Velocity
    Line FPM 4615 9073 2483 9099 7244 2460 697
    Velocity
    A/F Ratio 10.99 10.99 7.76 7.97
  • In another embodiment, a chemically-modified mixed fuel can be produced that combines three or more methane-containing gas streams from at least two different sources. It should also be understood that other gas streams—such as recycle gas, inert gases, non-methane-based hydrocarbon gases, etc can be added to the chemically-modified mixed fuel, as long as there is at least a first methane-containing gas and a second methane-containing gas that are mixed to form the chemically-modified mixed fuel.
  • In some embodiments, synthetic gases including those that may contain significant amounts of methane, may be utilized alone or in combination with natural, non-synthetic gases. These synthetic gases would need to be able to replace some of the natural gases currently being used in the target process without leading to expensive apparatus modifications or expensive starting materials.
  • The methane-containing gases utilized in the production of the chemically-modified mixed fuels, along with any other additional gases, should be blended at a suitable pressure in order to address concerns with respect to flow rate and also to address additional pressure considerations needed later in the particular process. For example, the first methane-containing gas may be held at a lower pressure initially in order to affect blending with the second methane-containing gas. Once blended, the chemically-modified mixed gas may then be transported under increasing pressure until reaching the optimum pressure for the particular process—such as the Kellogg process described herein. The suitable pressure does not necessarily refer to the pressure needed for the process that is utilizing the fuel, but instead refers to the pressure needed to optimally blend the gas streams to form the mixed gas fuel.
    • EXAMPLES Example 1 The Waverly, Va. Site
  • Enerdyne Power Systems, Inc. in conjunction with Waverly Gas Producers, LLC has proposed to supply landfill gas to the Honeywell Hopewell Plant (Kellogg site). The source of the landfill gas is the landfill located in Waverly, Va.
  • Approximately 3000 scfm of landfill gas is currently available to displace approximately 1500 scfm of natural gas in the Kellogg plant. The available landfill gas is used to displace the natural gas being burned in the arch burners of the primary reformer. The arch burners are the best option for the chemically-modified fuels because they already burn a blended fuel stream containing inerts (the A-6 recycle gas described herein). The displaced natural gas volume in this Example is relatively small compared to the total fuel volume and there is minimal risk to process reliability.
  • In this Example, the price of landfill gas is fixed for the first 18 months at $3.20/DKT, and thereafter, the price of landfill gas will be based on the price of natural gas at that time. The landfill gas price is determined by averaging the current delivered cost of natural gas and the delivered floor price of landfill gas. The total savings expected over the 15-year life of the project for this Example is projected to be $15-30 million.
  • At the landfill site, multiple vertical wells are utilized under vacuum to extract the gas from the landfill. At the landfill site, the extracted gas will be processed in the following manner:
  • Filtration to remove particulate matter
  • Carbon filtration to remove siloxane and organics
  • Refrigeration to remove water moisture and dry the gas
  • Compression for transferring gas through the supply pipeline
  • The gas is then transferred via an 18″ pipeline from the landfill site to the Kellogg site. When the landfill gas reaches the Kellogg site, its pressure is approximately 40 psig (pounds per square inch gauge). At this point, the flow rate of the landfill gas is metered for billing purposes. Also, the landfill gas can be sampled and analyzed at this point to review and ensure gas quality and requirements.
  • An on-site compression station is utilized at this point to increase the pressure of the gas from about 40 psig to a minimum of 75 psig that is required for use in the Kellogg Primary Reformer arch burners. A typical compressor used for this purpose is installed in a modular fashion, with the initial, single compressor powered by one 300 HP, 3600 RPM motor and is designed to handle 4000 scfm of landfill gas. Single compressors can be added over time as the volume of landfill gas is increased.
  • After compression, the landfill gas passes through a coalescing filter to assure the dryness of the gas before being routed to the Primary Reformer. The landfill gas is then blended with the Reformer's arch burner fuel stream. Table 5 shows the existing and modified fuel flow rates at the initial flow rate of the landfill gas (3000 scfm).
  • TABLE 5
    Operating Parameter Initial Scenario Modified Scenario
    Total Fuel Flow 10000 scfm  11500 scfm 
    Natural Gas Flow 8000 scfm 6500 scfm
    Area-6 Recycle Gas Flow 2000 scfm 2000 scfm
    Landfill Gas Flow   0 scfm 3000 scfm
    % Natural Gas 80%  57%
    % Area-6 Recycle Gas Flow 20%  17%
    % Landfill Gas 0% 26%
    Inerts Flow  800 scfm 1500 scfm
    % Inerts
    8% 20%
    % Increase in Total Flow 0% 15%
    Natural Gas Displaced   0 scfm 1500 scfm
    % Natural Gas Displaced 0% 19%
  • At 3000 scfm of landfill gas, the combustion air requirement is expected to be similar to existing conditions. Specifically, the calculated combustion air requirement for landfill gas is 0.40% less than existing conditions. The total volume of flue gas will not significantly change with landfill gas. Specifically, the total volume of flue gas will increase by only about 0.61%.
  • At the initial volume of landfill gas (3000 scfm), the following updates will be to be made to a conventional system:
  • Replacement of burner tips
  • Installation of tie-in for landfill gas
  • Installation of electronic over-speed trip capability on the ID and FD fans
  • Installation of various instrumentation and controls
  • As the volume of landfill gas increases, the following updates should be considered:
  • Piping size increase from blend point to burners
  • ID fan capacity increase
  • Installation of balancing ball valves for splitting flow in each of the arch burners
  • Installation of an additional fuel header and control valves on the Reformer
  • Installation of future blend point for tunnel burners
  • Ties into additional fuel gas systems
    • Primary Equipment List/Specifications
  • This list of equipment and specifications is for illustrative purposes and should provide enough information to one of ordinary skill in the art to practice the subject matter disclosed herein. GC-21 On-Site Landfill Gas Compressor: Vilter Model VSSG-1501 oil flooded screw compressor, 4000 scfm capacity, 30 psig suction, 75 psig discharge. The compressor is capable of a continuous 100 psig discharge. In addition, the compressor has a 300 HP, 3600 RPM, 4160 VAC, 3 phase capacity. A Modicon PLC control panel is included.
  • John Zinc Arch Burner Assemblies: Model FFC-PC-10; quantity 154.
  • Fuel Tie-ins and Isolation Valves
    • Instrumentation, Control Logic and Piping
  • The overall goal is to burn all of the landfill gas that is available all of the time. The capacity of the landfill gas compressor will be controlled from the skid-mounted Modicon PLC controller utilizing the slide valve (essentially an internal recycle valve) on the compressor and an external recycle valve.
  • To allow the new compressor to maximize the landfill gas being used, a split pressure control system will be used. If the discharge pressure reaches 85 psig, the compressor will go to recycle control and will hold a fixed discharge pressure at approximately 85 psig. When the discharge pressure falls below 85 psig, the compressor will switch over to suction pressure control and will then control to a suction pressure set point (preliminarily set for 20 psig). This control will all be done by the PLC-based control system supplied with the compressor.
  • The process effluent temperature from the primary reformer will continue to be controlled by TIC-117 cascading to HFC-2700 (BTU controller), cascading to FIC-778 (natural gas fuel to the primary reformer). The BTU calculation is modified to include the energy input from the landfill gas in the calculation (it currently includes the Area-6 return gas and the natural gas to the primary reformer). This control scheme will allow for constant BTU supply to the reformer with any (or no) landfill gas flow.
  • A double block and bleed system is installed in the landfill gas line similar to that which is installed into the Area-6 return gas line. This system will activate via a single solenoid valve to positively block off the landfill gas flow to the fuel system. The double block and bleeds will trip and will close HV-721A and HV-721B and open HV-721C on the following conditions:
  • High oxygen content (>4.0% on AI-720A or AI-720B)
  • High Temperature (>350° F. on TI-721)
  • GC-21 Status=Down/Trip
  • Reformer Trip (DCS or Hardware—Anytime V-101A/C are tripped or FCV-778 is closed)
    • Piping and Instrumentation Process Conditions: Fluid (Gas): Landfill Gas Composition (Mole %): Methane (53.45%) Carbon Dioxide (45.20%) Nitrogen (1.00%) Oxygen (0.20%) Ethane (0.05%) Propane (0.04%) Isobutane (0.03%)
  • n-Butane (0.02%)
    • Isopentane (0.01%) 100% Total Average Molecular Weight: 28.879 Mixture Cp/Cv Ratio: 1.212 Process Conditions—Compressor Suction: Pressure: 30 psig normal (design pressure 60 psig) Temperature: 70° F. Process Conditions—Compressor Discharge: Pressure: 75 psig normal (design pressure 280 psig) Temperature: 157° F. Line Size: 12″ SCH 10S 304 LSS, HP Spec. 5210 Natural Gas Piping for Purging Purposes:
  • 2″ 5210 to just upstream of restriction orifice. Increase to 4″ 5210 at restriction orifice inlet. Restriction orifice is 4″, 300# flanges, 0.723″ orifice (designed to pass 2000 scfm maximum at a 250 psig inlet pressure).
    • Natural Gas Relief Valve on Purge Supply:
  • This relief valve will protect the landfill gas suction piping from natural gas overpressurization when purging back to the landfill. This valve should be a 2J3 for natural gas service. Set pressure is 60 psig.
    • Energy and Utility Requirements Electrical Supply: 1 300-HP motor; 3 phase, 4160 VAC, 60 Hz 1 10-HP motor for oil pump; 3 phase, 480 VAC, 60 Hz 1 7.5-HP motor for oil cooler and recycle cooler fan; 3 phase, 460 VAC, 60 Hz 1 2-HP motor for oil system charge pump; 3 phase, 460 VAC, 60 Hz Instrument Air:
  • Less than 10 scfm required
    • Process Sewer:
  • The compressor has a suction scrubber that discharges moisture to drain. Little to no moisture is expected to be present.
    • Practical Considerations:
  • The loss of landfill gas pressure is seen because of on-site compression failure. On-site compression failure could cause low gas pressure at the burners resulting in a plant trip. The natural gas control valve, which is upstream of the blending point, is designed to control the desired pressure at the burners. In the event of loss of on-site landfill gas compression, the natural gas control valve will open to provide the additional fuel required for maintaining adequate pressure.
  • The loss of landfill pressure could also occur because of off-site compression failure at the landfill site, for example. This risk can be minimized by providing adequate notification and adjustment points along the pipeline at designated points. In addition, the existing natural gas control valve system is designed to compensate for the loss of landfill gas flow.
  • Supply piping corrosion may also occur as a function of moisture content in the landfill gas and its dew point. This concern can be addressed by the use of HDPE piping underground and installation of the coalescing filter to remove traces of moisture in the gas. Also, exiting the on-site compressor, the temperature of the landfill gas will be approximately 160° F.—well above its dew point.
  • Landfill gas comprises 1-4% oxygen. Since Area-6 return gas or Kellogg purge gas (when Cryo is down) contain hydrogen, there is a concern regarding the hydrogen explosion limits of the blended fuel stream. Computer modeling was utilized to determine the potential for explosion under a worst case scenario: 4% oxygen in landfill gas and Kellogg burning 6000 scfm purge gas with 70% hydrogen. The results of the computer modeling indicate that the addition of air (additional oxygen) is required to combust the blend of gases, and therefore, the stream is not explosive. In order to address this concern, redundant oxygen analyzers have been installed to monitor the oxygen content of the landfill gas. Interlocks have been set up to trip the double block and bleed system that will stop the flow of landfill gas if an oxygen content of 4% or greater is detected on either analyzer. Thermocouples have also been installed in multiple locations that will also trip the landfill gas should a high temperature be reached—which indicates combustion within the pipe. If high oxygen is detected, it will be necessary to purge the piping of the gas prior to reintroduction into the fuel gas system. This reintroduction can be accomplished by using natural gas to push the landfill gas backward through the pipeline into the landfill. A restriction orifice has been sized to allow a maximum of 2000 scfm of natural gas for this purpose. Since the natural gas is at a normal supply pressure of 250 psig, a relief valve will be set for 60 psig and can pass in excess of 2400 scfm.
  • Deposition in the radiant and convection sections of the Primary Reformer furnace is addressed by the removal of siloxane from the landfill gas. Siloxane is a compound contained in many consumer products, and therefore, it can be found in landfills. The siloxane contaminates the landfill gas, and when combusted, forms a fine, white dust on furnace surfaces. If the furnace surface temperature exceeds 1900° F., the white siloxane dust transforms into an adherent glassy compound. This deposition will severely foul the process heat transfer coils within the convection section and force a Kellogg shutdown. The coils may also have to be replaced, as a result of the deposition, which would lead to a prolonged shutdown.
  • Thus, specific embodiments and applications of chemically-modified fuels, their uses and their methods of production have been disclosed. It should be apparent, however, to those skilled in the art that many more modifications besides those already described are possible without departing from the inventive concepts herein. The inventive subject matter, therefore, is not to be restricted except in the spirit of the disclosure. Moreover, in interpreting the disclosure, all terms should be interpreted in the broadest possible manner consistent with the context. In particular, the terms “comprises” and “comprising” should be interpreted as referring to elements, components, or steps in a non-exclusive manner, indicating that the referenced elements, components, or steps may be present, or utilized, or combined with other elements, components, or steps that are not expressly referenced.

Claims (20)

1. A chemically-modified mixed fuel, wherein the fuel comprises methane gas from at least two methane-production sources.
2. The chemically-modified fuel of claim 1, wherein the at least two sources comprises at least one fossil source, at least one biogenic source, at least one abiogenic source or a combination thereof.
3. The chemically-modified fuel of claim 2, wherein the at least two sources comprises at least one fossil source and at least one biogenic source.
4. The chemically-modified fuel of claim 3, wherein the at least two sources consists of at least one fossil source and at least one biogenic source.
5. The chemically-modified fuel of claim 2, wherein the at least one biogenic source comprises landfill gas.
6. The chemically-modified fuel of claim 1, wherein at least one of the methane-production sources comprises natural gas, Area-6 gas, landfill gas or a combination thereof.
7. The chemically-modified fuel of claim 1, wherein the percentage of methane in each of the at least two methane-production sources is greater than about 40%.
8. The chemically-modified fuel of claim 1, wherein the percentage of methane in each of the at least two methane-production sources is greater than about 50%.
9. The chemically-modified fuel of claim 1, wherein the percentage of methane in at least one of the at least two methane-production sources is greater than about 70%.
10. A fuel-burning process, comprising:
a Kellogg Primary Reformer System, and
a chemically-modified mixed fuel, wherein the fuel comprises methane gas from at least two methane-production sources.
11. The chemically-modified fuel of claim 10, wherein at least one of the methane-production sources comprises natural gas, Area-6 gas, landfill gas or a combination thereof.
12. A method for producing the chemically-modified mixed fuel, comprising:
providing a first methane-containing gas from a first methane-production source,
providing a second methane-containing gas from a second methane-production source, and
blending the first methane-containing gas with the second methane-containing gas at a suitable pressure to form a chemically-modified mixed fuel.
13. The method of claim 12, further comprising at least one additional methane-containing gas which is provided from at least one additional methane-production source and blended with the chemically-modified fuel.
14. The method of claim 12, wherein the first methane-production source and the second methane-production source comprise at least one fossil source, at least one biogenic source, at least one abiogenic source or a combination thereof.
15. The method of claim 14, wherein the first methane-production source and the second methane-production source comprise at least one fossil source and at least one biogenic source.
16. The method of claim 15, wherein the first methane-production source and the second methane-production source comprise consists of at least one fossil source and at least one biogenic source.
17. The method of claim 14, wherein the at least one biogenic source comprises landfill gas.
18. The method of claim 13, wherein the percentage of methane in each of the at least two methane-production sources is greater than about 40%.
19. The method of claim 13, wherein the percentage of methane in each of the at least two methane-production sources is greater than about 50%.
20. The method of claim 13, wherein the percentage of methane in at least one of the at least two methane-production sources is greater than about 70%.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2726406A1 (en) * 2011-06-30 2014-05-07 Fluor Technologies Corporation Stand-alone flue gas recirculation fan

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10183267B2 (en) 2014-10-23 2019-01-22 Ashley Day Gas-to-liquids conversion process using electron beam irradiation

Citations (95)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4568530A (en) * 1984-10-16 1986-02-04 The M. W. Kellogg Company Ammonia synthesis
US4571384A (en) * 1982-10-18 1986-02-18 State Of Oregon Acting By And Through The State Board Of Higher Education On Behalf Of Oregon State University Methane production
US4576005A (en) * 1985-01-07 1986-03-18 Force Louis W Wellhead gas treatment and co-generation method and system
US4582475A (en) * 1980-06-27 1986-04-15 Eaton Corporation Method and apparatus for igniting combustible mixtures
US4583994A (en) * 1980-06-12 1986-04-22 Union Carbide Corporation Cyclic process for producing methane in a tubular reactor with effective heat removal
US4642125A (en) * 1981-03-27 1987-02-10 Trw Inc. Carbonaceous material and methods for making hydrogen and light hydrocarbons from such materials
US4727207A (en) * 1986-07-02 1988-02-23 Standard Oil Company Process for converting methane and/or natural gas to more readily transportable materials
US4727205A (en) * 1986-08-28 1988-02-23 The Standard Oil Company Process for converting methane and/or natural gas to more readily transportable materials
US4728506A (en) * 1986-05-16 1988-03-01 Catalyst Services, Inc. Start-up method for ammonia plants
US4738699A (en) * 1982-03-10 1988-04-19 Flexivol, Inc. Process for recovering ethane, propane and heavier hydrocarbons from a natural gas stream
US4795842A (en) * 1987-08-04 1989-01-03 Atlantic Richfield Company Methane conversion process
US4795849A (en) * 1987-08-04 1989-01-03 Atlantic Richfield Company Methane conversion process
US4801762A (en) * 1987-02-13 1989-01-31 Atlantic Richfield Company Methane conversion process
US4805881A (en) * 1987-05-28 1989-02-21 Gas Research Institute Internal gas generator for heat treating furnace
US4814534A (en) * 1985-10-31 1989-03-21 Chevron Research Company Addition of hydrogen and C2 to C4 hydrocarbons to the feed gas in the catalytic conversion of methane to higher molecular weight hydrocarbons
US4906447A (en) * 1988-02-12 1990-03-06 Schwarzenbek Eugene F Synthetic ammonia process
US4915619A (en) * 1988-05-05 1990-04-10 The Babcock & Wilcox Company Burner for coal, oil or gas firing
US4999030A (en) * 1987-03-06 1991-03-12 Foster Wheeler Usa Corporation Process for producing a methane-containing fuel gas
US5011625A (en) * 1989-12-11 1991-04-30 The M. W. Kellogg Company Autothermal steam reforming process
US5176887A (en) * 1991-10-07 1993-01-05 Ford Motor Company Treating emissions from engines fueled by compressed natural gas
US5180570A (en) * 1992-01-23 1993-01-19 Lee Jing M Integrated process for making methanol and ammonia
US5180703A (en) * 1991-04-24 1993-01-19 W. R. Grace & Co.-Conn. Sox/nox sorbent and process of use
US5385646A (en) * 1993-09-03 1995-01-31 Farmland Industries, Inc. Method of treating chemical process effluent
US5385176A (en) * 1993-07-19 1995-01-31 Price Compressor Company, Inc. Natural gas dispensing
US5386699A (en) * 1993-05-12 1995-02-07 American Gas & Technology, Inc. Method and apparatus for liquifying natural gas for fuel for vehicles and fuel tank for use therewith
US5387322A (en) * 1993-05-14 1995-02-07 The M. W. Kellogg Company Fusel oil stripping
US5388456A (en) * 1990-07-05 1995-02-14 Kettel; Dirk Procedure in order to detect the gas potential in sedimentary basins and the oil potential obtained from this
US5390499A (en) * 1993-10-27 1995-02-21 Liquid Carbonic Corporation Process to increase natural gas methane content
US5490377A (en) * 1993-10-19 1996-02-13 California Energy Commission Performance enhanced gas turbine powerplants
US5501722A (en) * 1992-11-04 1996-03-26 Membrane Technology And Research, Inc. Natural gas treatment process using PTMSP membrane
US5709733A (en) * 1995-05-29 1998-01-20 Nitto Denko Corporation Gas separation method
US5711770A (en) * 1996-01-04 1998-01-27 Malina; Mylan Energy conversion system
US5719097A (en) * 1993-07-22 1998-02-17 Chang; Clarence D. Catalyst comprising a modified solid oxide
US5727903A (en) * 1996-03-28 1998-03-17 Genesis Energy Systems, Inc. Process and apparatus for purification and compression of raw landfill gas for vehicle fuel
US5733454A (en) * 1996-04-26 1998-03-31 Ehh Holding Co., Inc. Process and apparatus for the treatment of flowable waste
US5855631A (en) * 1994-12-02 1999-01-05 Leas; Arnold M. Catalytic gasification process and system
US5869013A (en) * 1993-11-04 1999-02-09 Osaka Gas Company Limited Process and catalyst for reducing Nox in exhaust combustion gases
US5883138A (en) * 1997-04-25 1999-03-16 Exxon Research And Engineering Company Rapid injection catalytic partial oxidation process and apparatus for producing synthesis gas (law 562)
US5886056A (en) * 1997-04-25 1999-03-23 Exxon Research And Engineering Company Rapid injection process and apparatus for producing synthesis gas (law 560)
US6011073A (en) * 1997-10-10 2000-01-04 Syntroleum Corporation System and method for converting light hydrocarbons to heavier hydrocarbons with separation of water into oxygen and hydrogen
US6011192A (en) * 1998-05-22 2000-01-04 Membrane Technology And Research, Inc. Membrane-based conditioning for adsorption system feed gases
US6013158A (en) * 1994-02-02 2000-01-11 Wootten; William A. Apparatus for converting coal to hydrocarbons
US6015450A (en) * 1998-08-13 2000-01-18 The M. W. Kellogg Company Reducing methanol emissions from a syngas unit
US6021647A (en) * 1998-05-22 2000-02-08 Greg E. Ameringer Ethylene processing using components of natural gas processing
US6034031A (en) * 1995-09-18 2000-03-07 Nec Corporation Catalyst material for use in producing substitute natural gas and method for producing substitute natural gas
US6035550A (en) * 1997-04-28 2000-03-14 Tokyo Gas Co., Ltd. Method and apparatus for treating bog in a low temperature liquid storage tank
US6168768B1 (en) * 1998-01-23 2001-01-02 Exxon Research And Engineering Company Production of low sulfer syngas from natural gas with C4+/C5+ hydrocarbon recovery
US6176224B1 (en) * 1998-03-30 2001-01-23 Caterpillar Inc. Method of operating an internal combustion engine which uses a low energy gaseous fuel
US6187226B1 (en) * 1995-03-14 2001-02-13 Bechtel Bwxt Idaho, Llc Thermal device and method for production of carbon monoxide and hydrogen by thermal dissociation of hydrocarbon gases
US6205793B1 (en) * 1999-07-06 2001-03-27 Christopher E. Schimp Method and apparatus for recovering and transporting methane mine gas
US6340437B1 (en) * 1997-04-11 2002-01-22 Chiyoda Corporation Process for preparing synthesis gas by autothermal reforming
US6350394B1 (en) * 1996-12-23 2002-02-26 Egt Developments, Llc Method and apparatus for total energy fuel conversion systems
US6353133B1 (en) * 1999-11-01 2002-03-05 Acetex (Cyprus) Limited Methanol plant retrofit
US6355456B1 (en) * 2000-01-19 2002-03-12 Dakota Ag Energy, Inc. Process of using wet grain residue from ethanol production to feed livestock for methane production
US20020029770A1 (en) * 2000-08-11 2002-03-14 The Regents Of The University Of California Apparatus and method for operating internal combustion engines from variable mixtures of gaseous fuels
US20020029513A1 (en) * 2000-07-31 2002-03-14 William Shaw Ground organic fuel
US6503295B1 (en) * 2000-09-20 2003-01-07 Chevron U.S.A. Inc. Gas separations using mixed matrix membranes
US20030006129A1 (en) * 2001-06-28 2003-01-09 Kazuo Imasaki Methane/methanol producing system
US20030008381A1 (en) * 2001-05-03 2003-01-09 Augenstein Don C. Landfill biofiltration system and methods for removal of gas-phase pollutants and contaminants
US6509566B1 (en) * 2000-06-22 2003-01-21 Ophir Corporation Oil and gas exploration system and method for detecting trace amounts of hydrocarbon gases in the atmosphere
US6508209B1 (en) * 2000-04-03 2003-01-21 R. Kirk Collier, Jr. Reformed natural gas for powering an internal combustion engine
US20030027096A1 (en) * 2001-07-18 2003-02-06 Daniel Barnett Steam-methane reformer furnace with convection-heated pre-reformer
US6523351B2 (en) * 1999-12-13 2003-02-25 Exxonmobil Chemical Patents Inc. Method for utilizing gas reserves with low methane concentrations and high inert gas concentration for fueling gas turbines
US6531630B2 (en) * 2000-12-29 2003-03-11 Kenneth Ebenes Vidalin Bimodal acetic acid manufacture
US6685754B2 (en) * 2001-03-06 2004-02-03 Alchemix Corporation Method for the production of hydrogen-containing gaseous mixtures
US6691531B1 (en) * 2002-10-07 2004-02-17 Conocophillips Company Driver and compressor system for natural gas liquefaction
US6692544B1 (en) * 2000-04-12 2004-02-17 Ecosystems Projects, Llc Municipal waste briquetting system and method of filling land
US6692554B1 (en) * 2002-12-10 2004-02-17 Visteon Global Technologies, Inc. Methane storage device
US6698237B2 (en) * 2001-12-11 2004-03-02 Advanced Extraction Technologies, Inc. Use of stripping gas in flash regeneration solvent absorption systems
US20040057898A1 (en) * 2002-09-23 2004-03-25 Kellogg Brown & Root, Inc. Hydrogen enrichment scheme for autothermal reforming
US6844292B1 (en) * 2000-04-19 2005-01-18 Osaka Gas Co., Ltd. Method for preparing catalyst for reforming methanol
US20050013768A1 (en) * 2003-07-17 2005-01-20 Kellogg Brown And Root, Inc. Low-delta p purifier for nitrogen, methane, and argon removal from syngas
US20050016725A1 (en) * 2003-07-22 2005-01-27 Pfefferle William C. Method for natural gas production
US6855852B1 (en) * 1999-06-24 2005-02-15 Metasource Pty Ltd Natural gas hydrate and method for producing same
US6855272B2 (en) * 2001-07-18 2005-02-15 Kellogg Brown & Root, Inc. Low pressure drop reforming exchanger
US6858049B2 (en) * 1999-12-13 2005-02-22 Exxonmobil Chemical Patents Inc. Method for utilizing gas reserves with low methane concentrations for fueling gas turbines
US6860257B2 (en) * 2003-01-03 2005-03-01 James L. Wood Processing apparatus and method
US6866779B1 (en) * 2002-07-22 2005-03-15 Western Environmental Engineering Company Nitrogen recovery system and method
US20050061029A1 (en) * 2003-09-22 2005-03-24 Narinsky George B. Process and apparatus for LNG enriching in methane
US20050061001A1 (en) * 2003-01-29 2005-03-24 Maston Valerie A. Streamlined methane gas generation system
US20050066815A1 (en) * 2003-09-26 2005-03-31 Consortium Services Management Group, Inc. CO2 separator method and apparatus
US20060002840A1 (en) * 2004-07-02 2006-01-05 Kellogg Brown & Root, Inc. Pseudoisothermal ammonia process
US6986388B2 (en) * 2001-01-30 2006-01-17 Cdx Gas, Llc Method and system for accessing a subterranean zone from a limited surface area
US6988492B2 (en) * 2003-06-12 2006-01-24 Michael Shetley Hydrogen and liquid fuel injection system
US6991048B2 (en) * 2002-07-12 2006-01-31 Cdx Gas, Llc Wellbore plug system and method
US6991047B2 (en) * 2002-07-12 2006-01-31 Cdx Gas, Llc Wellbore sealing system and method
US6995846B2 (en) * 2003-12-19 2006-02-07 Itt Manufacturing Enterprises, Inc. System and method for remote quantitative detection of fluid leaks from a natural gas or oil pipeline
US6998098B2 (en) * 2002-11-11 2006-02-14 Conocophillips Company Removal of gases from a feed
US6997055B2 (en) * 2004-05-26 2006-02-14 Baker Hughes Incorporated System and method for determining formation fluid parameters using refractive index
US6997703B2 (en) * 2003-07-15 2006-02-14 Ngk Insulators, Ltd. Firing furnace and firing method
US20060036123A1 (en) * 2004-08-13 2006-02-16 Hughes W J Underground treatment of biowaste
US7005405B2 (en) * 2001-09-21 2006-02-28 Kabushiki Kaisha Toshiba Metal oxide sintered structure and production method therefor
US7014822B1 (en) * 1998-12-15 2006-03-21 Osaka Gas Co., Ltd Fluid treating device
US20060060525A1 (en) * 2001-02-20 2006-03-23 Hoffland Robert O Method and apparatus for treating animal waste and wastewater
US20070066495A1 (en) * 2005-09-21 2007-03-22 Ian Macpherson Lubricant compositions including gas to liquid base oils

Family Cites Families (277)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4289625A (en) 1980-01-18 1981-09-15 Institute Of Gas Technology Hybrid bio-thermal gasification
US4833171A (en) 1981-01-27 1989-05-23 Sweeney Maxwell P Synthesis gas system
US4842615A (en) 1981-03-24 1989-06-27 Carbon Fuels Corporation Utilization of low rank and waste coals in transportable fluidic fuel systems
US4592762A (en) 1981-10-22 1986-06-03 Institute Of Gas Technology Process for gasification of cellulosic biomass
US4597788A (en) 1982-03-10 1986-07-01 Flexivol, Inc. Process for recovering ethane, propane and heavier hydrocarbons from a natural gas stream
US4773255A (en) 1983-03-02 1988-09-27 Columbia Gas System Service Corporation Apparatus for injecting gas into a pipeline
US4699632A (en) 1983-08-02 1987-10-13 Institute Of Gas Technology Process for gasification of cellulosic materials
US4592903A (en) 1983-11-10 1986-06-03 Exxon Research & Engineering Co. Low severity hydrocarbon steam reforming process
DE3445995A1 (en) 1984-12-17 1986-06-19 Linde Ag METHOD FOR OBTAINING C (DOWN ARROW) 2 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) - OR FROM C (DOWN ARROW) 3 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) CARBON
US4588427A (en) 1985-03-13 1986-05-13 Dm International Inc. Method and apparatus for purification of high N2 content gas
US4690743A (en) 1985-05-02 1987-09-01 Al-Chem Fuels, Inc. Method for gas synthesis
EP0226487B1 (en) 1985-11-08 1990-01-10 Institut Français du Pétrole Process for the thermal conversion of methane into hydrocarbons with a higher molecular weight
US4869819A (en) 1986-05-16 1989-09-26 Michigan Biotechnology Institute Apparatus for biomethanation
US4781836A (en) 1986-05-16 1988-11-01 Michigan Biotechnology Institute Method for biomethanation
US4710212A (en) 1986-09-24 1987-12-01 Union Carbide Corporation Process to produce high pressure methane gas
US4788372A (en) 1987-02-13 1988-11-29 Atlantic Richfield Company Methane conversion process
US4831206A (en) 1987-03-05 1989-05-16 Uop Chemical processing with an operational step sensitive to a feedstream component
US4831207A (en) 1987-03-05 1989-05-16 Uop Chemical processing with an operational step sensitive to a feedstream component
US4831208A (en) 1987-03-05 1989-05-16 Uop Chemical processing with an operational step sensitive to a feedstream component
US4857081A (en) 1987-10-15 1989-08-15 Separation Dynamics, Inc. Separation of water from hydrocarbons and halogenated hydrocarbons
US4973786A (en) 1987-10-19 1990-11-27 Karra Sankaram B Process for the pyrolytic oxidation of methane to higher molecular weight hydrocarbons and synthesis gas
JPH01194927A (en) 1988-01-27 1989-08-04 Japan Gore Tex Inc Steam permselective membrane
US4960801A (en) 1988-08-29 1990-10-02 Exxon Research And Engineering Company Synthesis gas to heavy hydrocarbons on SiO2 promoted CO/TiO2
US4961758A (en) 1988-11-15 1990-10-09 Texaco Inc. Liquid membrane process for separating gases
US4851020A (en) 1988-11-21 1989-07-25 Mcdermott International, Inc. Ethane recovery system
US4921685A (en) 1988-12-12 1990-05-01 Massachusetts Institute Of Technology Method for methane conversion
US5246550A (en) 1988-12-12 1993-09-21 Massachusetts Institute Of Technology Method for methane conversion
US5232679A (en) 1989-05-22 1993-08-03 Jha Mahesh C Process for production of value-added coproducts from coal and other carbonaceous materials
US5107906A (en) 1989-10-02 1992-04-28 Swenson Paul F System for fast-filling compressed natural gas powered vehicles
US5409046A (en) 1989-10-02 1995-04-25 Swenson; Paul F. System for fast-filling compressed natural gas powered vehicles
FR2655038B1 (en) 1989-11-28 1993-05-14 Inst Francais Du Petrole PROCESS FOR PRODUCING ALKYLAROMATIC HYDROCARBONS FROM NATURAL GAS. INVENTION OF MM. BERNARD JUGUIN, JEAN-CLAUDE COLLIN, JOSEPH LARUE AND CHRISTIAN BUSSON.
US5122299A (en) 1989-12-11 1992-06-16 The M. W. Kellogg Company Autothermal steam reforming process
US5013334A (en) 1990-01-09 1991-05-07 Uop Methane purification by pressure swing adsorption
US5171333A (en) 1990-01-09 1992-12-15 Uop Methane purification by pressure swing adsorption
US5229017A (en) 1990-03-01 1993-07-20 Dowell Schlumberger Incorporated Method of enhancing methane production from coal seams by dewatering
JPH0639403B2 (en) 1990-03-31 1994-05-25 工業技術院長 Hydrocarbon production method
US5026947A (en) 1990-04-09 1991-06-25 Atlantic Richfield Company Methane conversion process
US5033550A (en) 1990-04-16 1991-07-23 Otis Engineering Corporation Well production method
US5560819A (en) 1990-04-19 1996-10-01 Mori-Gumi Co., Ltd. Treating system for organic wastes and waste water
US5069775A (en) 1990-05-07 1991-12-03 Atlantic Richfield Company Heavy crude upgrading using remote natural gas
US5426550A (en) 1990-06-08 1995-06-20 Matsushita Electric Industrial Co., Ltd. Multitrack magnetic head assembly for scanning a magnetic tape with a plurality of magnetic head tips
US5424195A (en) 1990-06-20 1995-06-13 Secretary Of The Interior Method for in situ biological conversion of coal to methane
US5131224A (en) 1990-07-23 1992-07-21 General Motors Corporation Method for reducing methane exhaust emissions from natural gas fueled engines
US5139365A (en) 1990-09-04 1992-08-18 Warren Chesner Process for waste injection into landfills for waste management, landfill reclamation, enhanced biodegradation and enhanced methane gas generation and recovery
US5139543A (en) 1991-02-22 1992-08-18 Sowinski Richard F Method for filtering benz-a-anthracene from a gas stream
US5141533A (en) 1991-02-22 1992-08-25 Sowinski Richard F Method for filtering benzene from a gas stream
US5139542A (en) 1991-02-22 1992-08-18 Sowinski Richard F Method for filtering benzo-a-pyrene from a gas stream
US5134944A (en) 1991-02-28 1992-08-04 Keller Leonard J Processes and means for waste resources utilization
US5527464A (en) 1991-06-24 1996-06-18 Bartha; Istvan Method and system for the treatment and utilization of waste products
US5256277A (en) 1991-07-24 1993-10-26 Mobil Oil Corporation Paraffin isomerization process utilizing a catalyst comprising a mesoporous crystalline material
US5245110A (en) 1991-09-19 1993-09-14 Starchem, Inc. Process for producing and utilizing an oxygen enriched gas
US5616163A (en) 1991-09-20 1997-04-01 Halfter; Georg Method for processing animal excrement and liquid manure
US5208204A (en) 1991-10-07 1993-05-04 Ford Motor Company Three-way catalyst for treating emissions from compressed natural gas fueled engines
US5174796A (en) 1991-10-09 1992-12-29 Uop Process for the purification of natural gas
US5201581A (en) 1991-11-18 1993-04-13 Badger Meter, Inc. Method and apparatus for measuring mass flow and energy content using a linear flow meter
US5223238A (en) 1992-01-16 1993-06-29 The M. W. Kellogg Company Method for treating ammonia and urea condensates
US5254934A (en) 1992-01-28 1993-10-19 The United States Of America As Represented By The United States Department Of Energy Method of and system for producing electrical power
US5260640A (en) 1992-01-28 1993-11-09 The United States Of America As Represented By The United States Department Of Energy Method of and system for producing electrical power
US5214226A (en) 1992-03-13 1993-05-25 Cornell Research Foundation, Inc. Method and apparatus for the homogeneous conversion of methane
US5228995A (en) 1992-04-23 1993-07-20 Stover Enos L Biochemically enhanced hybrid anaerobic reactor
US5461023A (en) 1992-07-01 1995-10-24 Alliedsignal Inc. Storage of natural gas
US5336825A (en) 1992-07-10 1994-08-09 Council Of Scientific & Industrial Research Integrated two step process for conversion of methane to liquid hydrocarbons of gasoline range
US5269634A (en) 1992-08-31 1993-12-14 University Of Florida Apparatus and method for sequential batch anaerobic composting of high-solids organic feedstocks
FR2696109B1 (en) 1992-09-28 1994-11-04 Inst Francais Du Petrole Oxidation catalyst and partial methane oxidation process.
US5821111A (en) 1994-03-31 1998-10-13 Bioengineering Resources, Inc. Bioconversion of waste biomass to useful products
DE4237620A1 (en) 1992-11-06 1994-05-11 Linde Ag Process for the production of high-purity liquid methane
US5366945A (en) 1992-12-22 1994-11-22 Mobil Oil Corp. Supported heteropoly acid catalysts
US5315831A (en) 1993-01-22 1994-05-31 Hydra-Rig, Incorporated Liquid natural gas and compressed natural gas total fueling system
US5360139A (en) 1993-01-22 1994-11-01 Hydra Rig, Inc. Liquified natural gas fueling facility
US5364606A (en) 1993-03-01 1994-11-15 General Electric Company NOx reduction through the use of methane
US5450205A (en) 1993-05-28 1995-09-12 Massachusetts Institute Of Technology Apparatus and method for real-time measurement of thin film layer thickness and changes thereof
US5434330A (en) 1993-06-23 1995-07-18 Hnatow; Miguel A. Process and apparatus for separation of constituents of gases using gas hydrates
US5362454A (en) 1993-06-28 1994-11-08 The M. W. Kellogg Company High temperature heat exchanger
US6080904A (en) 1993-07-22 2000-06-27 Mobil Oil Corporation Isomerization process
AU688351B2 (en) 1993-07-22 1998-03-12 Mobil Oil Corporation Modified solid oxide catalyst and process for producing same
US5854170A (en) 1993-07-22 1998-12-29 Mobil Oil Corporation Method for preparing a modified solid oxide
US5365902A (en) 1993-09-10 1994-11-22 General Electric Company Method and apparatus for introducing fuel into a duel fuel system using the H-combustion process
US5413699A (en) 1993-10-14 1995-05-09 Mobil Oil Corporation FCC process with fines tolerant SCR reactor
US5535584A (en) 1993-10-19 1996-07-16 California Energy Commission Performance enhanced gas turbine powerplants
WO1995011376A1 (en) 1993-10-19 1995-04-27 State Of California Energy Resources Conservation And Development Commission Performance enhanced gas turbine powerplants
ATE191363T1 (en) 1993-11-04 2000-04-15 Enitecnologie Spa METHOD AND CATALYST FOR REDUCING NOX IN COMBUSTION EXHAUSTS
US5453210A (en) 1994-01-24 1995-09-26 The Lubrizol Corporation Method of treating the products of combustion of landfill gas
US5447850A (en) 1994-01-31 1995-09-05 Mccann; James L. Method of producing methane from organic waste
US5457625A (en) 1994-04-13 1995-10-10 The M. W. Kellogg Company Maximizing process production rates using permanent constraints
US5573737A (en) 1994-09-27 1996-11-12 The United States Of America As Represented By The United States Department Of Energy Functionally gradient material for membrane reactors to convert methane gas into value-added products
US5507146A (en) 1994-10-12 1996-04-16 Consolidated Natural Gas Service Company, Inc. Method and apparatus for condensing fugitive methane vapors
US5462116A (en) 1994-10-26 1995-10-31 Carroll; Walter D. Method of producing methane gas from a coal seam
US5615561A (en) 1994-11-08 1997-04-01 Williams Field Services Company LNG production in cryogenic natural gas processing plants
US5641327A (en) 1994-12-02 1997-06-24 Leas; Arnold M. Catalytic gasification process and system for producing medium grade BTU gas
JP2925963B2 (en) 1994-12-05 1999-07-28 石油公団 Method and apparatus for oxidative coupling of methane
US5676070A (en) 1994-12-27 1997-10-14 Maganas; Thomas C. Apparatus and methods for catalytic, low temperature degradation of medical waste and other organic materials
US5681360A (en) 1995-01-11 1997-10-28 Acrion Technologies, Inc. Landfill gas recovery
US5767388A (en) 1995-04-26 1998-06-16 Siemens Aktiengesellschaft Methane sensor and method for operating a sensor
DE69621996T2 (en) 1995-04-27 2003-06-18 Nippon Oxygen Co Ltd CARBON-BASED ADSORBES, METHOD FOR THE PRODUCTION THEREOF AND METHOD AND DEVICE FOR GAS SEPARATION
US5537827A (en) 1995-06-07 1996-07-23 Low; William R. Method for liquefaction of natural gas
US5523483A (en) 1995-06-16 1996-06-04 The M. W. Kellogg Company Integrated urea/ammonia process
US5653282A (en) 1995-07-19 1997-08-05 The M. W. Kellogg Company Shell and tube heat exchanger with impingement distributor
US6137017A (en) 1995-09-25 2000-10-24 Stauffer; John E. Methanol process for natural gas conversion
DE69626665T2 (en) 1995-10-05 2004-02-05 Bhp Petroleum Pty. Ltd. LIQUEFACTION PROCESS
US6956371B2 (en) 1995-10-12 2005-10-18 Halliburton Energy Services, Inc. Method and apparatus for detecting diffusion sensitive phases with estimation of residual error in NMR logs
JP3486022B2 (en) 1995-10-16 2004-01-13 ジャパン・エア・ガシズ株式会社 Exhaust gas treatment equipment
US5736116A (en) 1995-10-25 1998-04-07 The M. W. Kellogg Company Ammonia production with enriched air reforming and nitrogen injection into the synthesis loop
US5902927A (en) 1995-12-01 1999-05-11 Perception Incorporated Fluid metering apparatus and method
ES2182921T3 (en) 1995-12-08 2003-03-16 Megtec Systems Ab A METHOD AND A DEVICE FOR ENERGY RECOVERY OF MEDIA CONTAINING COMBUSTIBLE SUBSTANCES, INCLUDING LOW CONCENTRATIONS.
US5964908A (en) 1996-01-04 1999-10-12 Malina; Mylan Closed loop energy conversion process
US5642630A (en) 1996-01-16 1997-07-01 Abdelmalek; Fawzy T. Process for solids waste landfill gas treatment and separation of methane and carbon dioxide
US5964923A (en) 1996-02-29 1999-10-12 Membrane Technology And Research, Inc. Natural gas treatment train
US5669958A (en) 1996-02-29 1997-09-23 Membrane Technology And Research, Inc. Methane/nitrogen separation process
ATE196511T1 (en) 1996-03-20 2000-10-15 Sol Spa METHOD AND DEVICE FOR THE HEAT TREATMENT OF METAL WORKPIECES UNDER SHELTERING GAS
US5700311A (en) 1996-04-30 1997-12-23 Spencer; Dwain F. Methods of selectively separating CO2 from a multicomponent gaseous stream
US6800665B1 (en) 1996-05-13 2004-10-05 Jfe Holdings, Inc. Method for producing dimethyl ether
US6797325B2 (en) 1996-05-31 2004-09-28 The Regents Of The University Of California Permeable polyaniline articles for gas separation
DE69703840T3 (en) 1996-06-10 2010-08-26 Hitachi, Ltd. Exhaust gas purification device for an internal combustion engine and catalyst for purifying the exhaust gas of the internal combustion engine
CA2259267A1 (en) 1996-06-28 1998-01-15 Stewart E. Erickson Pipeline utilization enhancement including carbon dioxide gas transmission, distribution, and delivery technique
US5900515A (en) 1996-08-20 1999-05-04 The Board Of Regents Of The University Of Oklahoma High energy density storage of methane in light hydrocarbon solutions
NO964298L (en) 1996-10-10 1998-04-14 Solco Offshore Services As Method of supplying combustion air to a combustion chamber, apparatus at said combustion chamber, and using oxygen-containing exhaust gas from a gas turbine
JPH1135950A (en) 1996-12-26 1999-02-09 Mitsubishi Heavy Ind Ltd Process for generation of electric power and power generation apparatus
US6159432A (en) 1997-01-23 2000-12-12 The Board Of Regents Of The University Of Oklahoma Conversion method for gas streams containing hydrocarbons
US6446014B1 (en) 1997-02-25 2002-09-03 Cham Ocondi Method and apparatus for measuring and controlling the flow of fluids from coal seam gas wells
US5950732A (en) 1997-04-02 1999-09-14 Syntroleum Corporation System and method for hydrate recovery
US5970726A (en) 1997-04-08 1999-10-26 Heatcraft Inc. Defrost control for space cooling system
MY128194A (en) 1997-04-11 2007-01-31 Chiyoda Corp Process for the production of synthesis gas
ATE273238T1 (en) 1997-04-11 2004-08-15 Chiyoda Chem Eng Construct Co CATALYST FOR PRODUCING SYNTHESIS GAS AND METHOD FOR PRODUCING CARBON MONOXIDE
US5915365A (en) 1997-04-11 1999-06-29 Engine World, Inc. Combined system using a vaporous fuel mixture energy source and an internal combustion engine and method therefor
US5935489A (en) 1997-04-25 1999-08-10 Exxon Research And Engineering Co. Distributed injection process and apparatus for producing synthesis gas
US5980596A (en) 1997-04-25 1999-11-09 Exxon Research And Engineering Co. Multi-injector autothermal reforming process and apparatus for producing synthesis gas (law 565).
US5980782A (en) 1997-04-25 1999-11-09 Exxon Research And Engineering Co. Face-mixing fluid bed process and apparatus for producing synthesis gas
US6267912B1 (en) 1997-04-25 2001-07-31 Exxon Research And Engineering Co. Distributed injection catalytic partial oxidation process and apparatus for producing synthesis gas
EP0979134A1 (en) 1997-04-28 2000-02-16 British Nuclear Fuels PLC Improvements in and relating to gas generators
US5852061A (en) 1997-05-06 1998-12-22 Exxon Research And Engineering Company Hydrocarbon synthesis with cryogenic nitrogen removal upstream of the syngas generation
US6077323A (en) 1997-06-06 2000-06-20 Air Products And Chemicals, Inc. Synthesis gas production by ion transport membranes
US5922974A (en) 1997-07-03 1999-07-13 Davison; J. Lynne Geochemical soil sampling for oil and gas exploration
DE19735153C2 (en) 1997-08-13 2003-10-16 Linde Kca Dresden Gmbh Process and device for gasifying waste materials
US5976721A (en) 1997-09-15 1999-11-02 Limaye; Santosh Y. Chemical cogeneration process
US6200541B1 (en) 1997-10-28 2001-03-13 Bp Amoco Corporation Composite materials for membrane reactors
DK128697A (en) 1997-11-12 1999-05-13 Niels J Bjerrum Catalysis Process
US5928618A (en) 1997-12-04 1999-07-27 Thomas C. Maganas Methods for low temperature degradation of diesel exhaust and other organic matter
JP2002508498A (en) 1997-12-16 2002-03-19 ロッキード・マーティン・アイダホ・テクノロジーズ・カンパニー Apparatus and method for cooling, liquefying and separating gases of different purity
US6494191B2 (en) 1997-12-16 2002-12-17 Bechtel Bwxt Idaho, Llc Systems and method for delivering liquified gas to an engine
US5816792A (en) 1997-12-22 1998-10-06 Roberts-Gordon, Inc. Alternate gas fuel burning system
US6048472A (en) 1997-12-23 2000-04-11 Air Products And Chemicals, Inc. Production of synthesis gas by mixed conducting membranes
NO315194B1 (en) 1998-01-30 2003-07-28 Navion As Process and system for export of LNG and condensate from a floating production, storage and unloading vessel
US6254775B1 (en) 1998-03-09 2001-07-03 Mcelvaney James D. Anaerobic digester system and method
US6602481B1 (en) 1998-03-09 2003-08-05 Osaka Gas Company Limited Catalyst for removing hydrocarbons from exhaust gas and method for clarification of exhaust gas
US5980857A (en) 1998-03-18 1999-11-09 The Boc Group, Inc. Production of carbon monoxide from syngas
AUPP274998A0 (en) 1998-04-03 1998-04-30 Isentropic Systems Ltd Improvements in the generation of electricity and the treatment and disposal of sewage
US6328854B1 (en) 1998-04-10 2001-12-11 Grt, Inc. Method of and apparatus for manufacturing methanol
US6129818A (en) 1998-04-10 2000-10-10 Grt, Inc. Method of and apparatus for manufacturing methanol
US6375691B1 (en) 1998-04-30 2002-04-23 Pirelli Ambiente S.P.A. Fuel composition which combusts instantaneously, method and plant therefor
US6244338B1 (en) 1998-06-23 2001-06-12 The University Of Wyoming Research Corp., System for improving coalbed gas production
US6481217B1 (en) 1998-07-03 2002-11-19 Toyota Jidosha Kabushiki Kaisha Gas storage method and system, and gas occluding material
US6214258B1 (en) 1998-08-13 2001-04-10 Air Products And Chemicals, Inc. Feed gas pretreatment in synthesis gas production
US6393821B1 (en) 1998-08-21 2002-05-28 Edan Prabhu Method for collection and use of low-level methane emissions
EP0985635B1 (en) 1998-09-09 2005-04-13 Matsushita Electric Industrial Co., Ltd. Hydrogen generating apparatus
US6531704B2 (en) 1998-09-14 2003-03-11 Nanoproducts Corporation Nanotechnology for engineering the performance of substances
US6921597B2 (en) 1998-09-14 2005-07-26 Questair Technologies Inc. Electrical current generation system
US6114400A (en) 1998-09-21 2000-09-05 Air Products And Chemicals, Inc. Synthesis gas production by mixed conducting membranes with integrated conversion into liquid products
US6613126B2 (en) 1998-09-30 2003-09-02 Toyota Jidosha Kabushiki Kaisha Method for storing natural gas by adsorption and adsorbing agent for use therein
US6753353B2 (en) 1998-11-13 2004-06-22 Powerenercat, Inc. Method for production of mixed alcohols from synthesis gas
US6248796B1 (en) 1999-11-13 2001-06-19 Powerenercat. Inc. Method for production of mixed alcohols from synthesis gas
US6309612B1 (en) 1998-11-18 2001-10-30 The United States Of America As Represented By The United States Department Of Energy Ceramic membrane reactor with two reactant gases at different pressures
US6280000B1 (en) 1998-11-20 2001-08-28 Joseph A. Zupanick Method for production of gas from a coal seam using intersecting well bores
US6679322B1 (en) 1998-11-20 2004-01-20 Cdx Gas, Llc Method and system for accessing subterranean deposits from the surface
US7025154B2 (en) 1998-11-20 2006-04-11 Cdx Gas, Llc Method and system for circulating fluid in a well system
US7048049B2 (en) 2001-10-30 2006-05-23 Cdx Gas, Llc Slant entry well system and method
US7073595B2 (en) 2002-09-12 2006-07-11 Cdx Gas, Llc Method and system for controlling pressure in a dual well system
US6116050A (en) 1998-12-04 2000-09-12 Ipsi Llc Propane recovery methods
DE69905543T3 (en) 1998-12-07 2006-10-19 Mitsubishi Heavy Industries, Ltd. Process for the production of methanol
WO2000036335A1 (en) 1998-12-15 2000-06-22 Toyota Jidosha Kabushiki Kaisha System for storing dissolved methane-base gas
US6106594A (en) 1999-01-22 2000-08-22 Mobil Oil Corporation Method for separating methane from natural gas using bisglycoluril derivatives
US6223519B1 (en) 1999-02-11 2001-05-01 Bp Amoco Corporation Method of generating power using an advanced thermal recuperation cycle
EP1036757B1 (en) 1999-03-15 2004-05-12 Matsushita Electric Industrial Co., Ltd. Hydrogen generating apparatus
CA2300521C (en) 1999-03-15 2004-11-30 Takahiro Kimura Production method for hydrate and device for proceeding the same
JP2000274311A (en) 1999-03-19 2000-10-03 Honda Motor Co Ltd Gas fuel feeding system for vehicle
JP2000282956A (en) 1999-03-29 2000-10-10 Honda Motor Co Ltd Gas fuel supply system for vehicle
US6070429A (en) 1999-03-30 2000-06-06 Phillips Petroleum Company Nitrogen rejection system for liquified natural gas
JP3625770B2 (en) 1999-04-20 2005-03-02 東京瓦斯株式会社 Single tube cylindrical reformer and its operating method
US6125653A (en) 1999-04-26 2000-10-03 Texaco Inc. LNG with ethane enrichment and reinjection gas as refrigerant
PL203744B1 (en) 1999-04-28 2009-11-30 Commonwealth Scientific And Industrial Research Organisation A thermodynamic apparatus
US6291232B1 (en) 1999-05-12 2001-09-18 Miller, Iii Herman P. Anaerobic digestion system and process
US6308553B1 (en) 1999-06-04 2001-10-30 Honeywell International Inc Self-normalizing flow sensor and method for the same
US6220052B1 (en) 1999-08-17 2001-04-24 Liberty Fuels, Inc. Apparatus and method for liquefying natural gas for vehicular use
US6380126B1 (en) 1999-08-20 2002-04-30 Medis El Ltd Class of electrocatalysts and a gas diffusion electrode based thereon for fuel cells
US6451589B1 (en) 1999-10-25 2002-09-17 Ghd, Inc. Method and apparatus for solids processing
US6232352B1 (en) 1999-11-01 2001-05-15 Acetex Limited Methanol plant retrofit for acetic acid manufacture
US6781014B1 (en) 1999-11-01 2004-08-24 Acetex (Cyprus) Limited Methanol plant retrofit for manufacture of acetic acid
US6296766B1 (en) 1999-11-12 2001-10-02 Leon Breckenridge Anaerobic digester system
WO2001046067A1 (en) 1999-12-21 2001-06-28 Bechtel Bwxt Idaho, Llc Hydrogen and elemental carbon production from natural gas and other hydrocarbons
CN1280933C (en) 1999-12-28 2006-10-18 松下电器产业株式会社 Power generation device and operation method therefor
US6972119B2 (en) 1999-12-28 2005-12-06 Matsushita Electric Industrial Co., Ltd. Apparatus for forming hydrogen
US6489787B1 (en) 2000-01-11 2002-12-03 Bacharach, Inc. Gas detection circuit
FR2804042B1 (en) 2000-01-25 2002-07-12 Air Liquide PROCESS FOR THE PURIFICATION OF A GAS BY ADSORPTION OF IMPURITIES ON SEVERAL ACTIVE COAL
CA2340822C (en) 2000-03-17 2010-08-03 Snamprogetti S.P.A. Process for the production of hydrogen
EP1136444B1 (en) 2000-03-22 2012-05-09 Ammonia Casale S.A. Process for hydrocarbon reforming
US6387281B2 (en) 2000-03-25 2002-05-14 R3 Management Limited Processes and apparatus for treating sewage or like sludge
US6397790B1 (en) 2000-04-03 2002-06-04 R. Kirk Collier, Jr. Octane enhanced natural gas for internal combustion engine
US6670058B2 (en) 2000-04-05 2003-12-30 University Of Central Florida Thermocatalytic process for CO2-free production of hydrogen and carbon from hydrocarbons
US6604051B1 (en) 2000-04-17 2003-08-05 Southwest Research Institute System and method to determine thermophysical properties of a multi-component gas
US6755965B2 (en) 2000-05-08 2004-06-29 Inelectra S.A. Ethane extraction process for a hydrocarbon gas stream
IL153677A0 (en) 2000-07-18 2003-07-06 Suellen A Vanooteghem A process for generating hydrogen
US20030154651A1 (en) 2000-07-31 2003-08-21 William Shaw Ground organic fuel
AU2001286433A1 (en) 2000-08-11 2002-02-25 Nisource Energy Technologies Energy management system and methods for the optimization of distributed generation
US6492290B1 (en) 2000-08-22 2002-12-10 Air Products And Chemicals, Inc. Mixed conducting membranes for syngas production
US6578559B2 (en) 2000-08-31 2003-06-17 Hadoga Industries, Inc. Methane gas control system
JP4830197B2 (en) 2000-09-13 2011-12-07 トヨタ自動車株式会社 Fuel reformer
US6444012B1 (en) 2000-10-30 2002-09-03 Engelhard Corporation Selective removal of nitrogen from natural gas by pressure swing adsorption
US6367286B1 (en) 2000-11-01 2002-04-09 Black & Veatch Pritchard, Inc. System and process for liquefying high pressure natural gas
US6454944B1 (en) 2000-11-08 2002-09-24 Larry J. Raven Process and apparatus for conversion of biodegradable organic materials into product gas
AUPR216700A0 (en) 2000-12-19 2001-01-25 Woodside Energy Limited Method for separation of non-hydrocarbon gases from hydrocarbon gases
US7095012B2 (en) 2000-12-19 2006-08-22 Schlumberger Technology Corporation Methods and apparatus for determining chemical composition of reservoir fluids
US6544439B1 (en) 2000-12-22 2003-04-08 Uop Llc Low coke formation catalysts and process for reforming and synthesis gas production
CN100506349C (en) 2000-12-25 2009-07-01 住友精化株式会社 Method for separating hydrogen gas
GB0031710D0 (en) 2000-12-27 2001-02-07 Dyno Oil Field Chemicals Process for the reduction or elimination of hydrogen sulphide
US6878664B1 (en) 2001-01-16 2005-04-12 Medis El Ltd. Class of electrocatalysts and a gas diffusion electrode based thereon for fuel cells
US6632362B2 (en) 2001-01-19 2003-10-14 Miller, Iii Herman P. Vacuum retort anaerobic digestion (VRAD) system and process
US6942798B2 (en) 2001-01-19 2005-09-13 Miller, Iii Herman P. Vacuum retort anaerobic digestion system and process
US6599491B2 (en) 2001-01-22 2003-07-29 Kenneth Ebenes Vidalin Bimodal hydrogen manufacture
JP4393002B2 (en) 2001-02-01 2010-01-06 ヤンマー株式会社 Gas engine
US6663681B2 (en) 2001-03-06 2003-12-16 Alchemix Corporation Method for the production of hydrogen and applications thereof
US20020139049A1 (en) 2001-03-06 2002-10-03 Kindig J. Kelly Method for the production of a methane-containing gas
US6500313B2 (en) 2001-03-12 2002-12-31 Steven P. Sherwood Method for production of hydrocarbons
US7118606B2 (en) 2001-03-21 2006-10-10 Ut-Battelle, Llc Fossil fuel combined cycle power system
US6497457B1 (en) 2001-05-31 2002-12-24 Larry G. Stolarczyk Drilling, image, and coal-bed methane production ahead of mining
US6892815B2 (en) 2001-03-28 2005-05-17 Larry G. Stolarczyk Coal bed methane borehole pipe liner perforation system
US6653517B2 (en) 2001-04-03 2003-11-25 Billy P Bullock Hydrocarbon conversion apparatus and method
US6808693B2 (en) 2001-06-12 2004-10-26 Hydrotreat, Inc. Methods and apparatus for increasing and extending oil production from underground formations nearly depleted of natural gas drive
US6790359B2 (en) 2001-08-21 2004-09-14 Miller, Iii Herman P. Vertical phase separation in anaerobic digestion
US6751958B1 (en) 2001-09-06 2004-06-22 Honeywell International Inc. Physical chemistry compression
US6667347B2 (en) 2001-09-14 2003-12-23 Chevron U.S.A. Inc. Scrubbing CO2 from methane-containing gases using an aqueous stream
US6638416B2 (en) 2001-09-24 2003-10-28 Delphi Technologies, Inc. Hydrogen sensing process
US7100994B2 (en) 2001-10-24 2006-09-05 Shell Oil Company Producing hydrocarbons and non-hydrocarbon containing materials when treating a hydrocarbon containing formation
AU2002342107A1 (en) 2001-10-26 2003-05-12 Electro-Petroleum, Inc. Electrochemical process for effecting redox-enhanced oil recovery
WO2003043939A2 (en) 2001-11-16 2003-05-30 Ch2M Hill, Inc. Method and apparatus for the treatment of particulate biodegradable organic waste
US6832485B2 (en) 2001-11-26 2004-12-21 Ormat Industries Ltd. Method of and apparatus for producing power using a reformer and gas turbine unit
EP1461278A4 (en) 2001-12-04 2005-06-22 Ecotechnology Ltd Flow development chamber
JP3479699B2 (en) 2002-01-18 2003-12-15 飛島建設株式会社 Gas hydrate mining method and equipment
US6758060B2 (en) 2002-02-15 2004-07-06 Chart Inc. Separating nitrogen from methane in the production of LNG
US6716269B1 (en) 2002-03-05 2004-04-06 Energent Corporation Centrifuge and cascade for the separation of gases
US6610124B1 (en) 2002-03-12 2003-08-26 Engelhard Corporation Heavy hydrocarbon recovery from pressure swing adsorption unit tail gas
US7060233B1 (en) 2002-03-25 2006-06-13 Tda Research, Inc. Process for the simultaneous removal of sulfur and mercury
US6878362B2 (en) 2002-04-05 2005-04-12 General Electric Company Fuel processor apparatus and method based on autothermal cyclic reforming
US7507690B2 (en) 2002-04-30 2009-03-24 Uchicago Argonne, Llc. Autothermal reforming catalyst having perovskite structure
US7045231B2 (en) 2002-05-22 2006-05-16 Protonetics International, Inc. Direct hydrocarbon reforming in protonic ceramic fuel cells by electrolyte steam permeation
US6750453B1 (en) 2002-05-25 2004-06-15 Ophir Corporation Methods of and apparatus for detecting low concentrations of target gases in the free atmosphere
US6824224B1 (en) 2002-06-19 2004-11-30 Cimarron Technology, Ltd. Coalbed methane extraction process
US6911161B2 (en) 2002-07-02 2005-06-28 Conocophillips Company Stabilized nickel-containing catalysts and process for production of syngas
US6896717B2 (en) 2002-07-05 2005-05-24 Membrane Technology And Research, Inc. Gas separation using coated membranes
US6820689B2 (en) 2002-07-18 2004-11-23 Production Resources, Inc. Method and apparatus for generating pollution free electrical energy from hydrocarbons
AU2003260210A1 (en) 2002-08-21 2004-03-11 Presssol Ltd. Reverse circulation directional and horizontal drilling using concentric coil tubing
US7025137B2 (en) 2002-09-12 2006-04-11 Cdx Gas, Llc Three-dimensional well system for accessing subterranean zones
US6733573B2 (en) 2002-09-27 2004-05-11 General Electric Company Catalyst allowing conversion of natural gas hydrate and liquid CO2 to CO2 hydrate and natural gas
US6640586B1 (en) 2002-11-01 2003-11-04 Conocophillips Company Motor driven compressor system for natural gas liquefaction
US6962056B2 (en) 2002-11-13 2005-11-08 Carrier Corporation Combined rankine and vapor compression cycles
US6892522B2 (en) 2002-11-13 2005-05-17 Carrier Corporation Combined rankine and vapor compression cycles
US7080686B2 (en) 2002-11-13 2006-07-25 David Beckhardt Devices and methods for extraction, transportation and/or release of material
US6880344B2 (en) 2002-11-13 2005-04-19 Utc Power, Llc Combined rankine and vapor compression cycles
US7025803B2 (en) 2002-12-02 2006-04-11 L'Air Liquide Societe Anonyme A Directoire et Counsel de Surveillance Pour L'Etude et L'Exploration des Procedes Georges Claude Methane recovery process
US7033822B2 (en) 2003-01-29 2006-04-25 New Energy Solutions, Inc. Self-contained and streamlined methane and/or high purity hydrogen generation system
US20060120953A1 (en) 2003-03-06 2006-06-08 Keiichi Okuyama Method for preparing synthesis gas, method for preparing dimethyl ether using synthesis gas, and furnace for preparing synthesis gas
US7138001B2 (en) 2003-03-16 2006-11-21 Kellogg Brown & Root Llc Partial oxidation reformer-reforming exchanger arrangement for hydrogen production
RU2343109C2 (en) 2003-03-18 2009-01-10 КЕЛЛОГГ БРАУН ЭНД РУТ ЭлЭлСи Method for producing hydrogen-rich flow, method for electric current generation, method of hydrofining, device for hydrogen-rich flow creation
US7074033B2 (en) 2003-03-22 2006-07-11 David Lloyd Neary Partially-open fired heater cycle providing high thermal efficiencies and ultra-low emissions
US20040244279A1 (en) 2003-03-27 2004-12-09 Briscoe Michael D. Fuel compositions comprising natural gas and dimethyl ether and methods for preparation of the same
US6796369B1 (en) 2003-04-04 2004-09-28 Air Products And Chemicals, Inc. Method and apparatus to prevent metal dusting
US6959764B2 (en) 2003-06-05 2005-11-01 Yale Matthew Preston Baffle system for two-phase annular flow
US6942719B2 (en) 2003-06-30 2005-09-13 The Boeing Company Methods and systems for pressure swing regeneration for hydrogen generation
US7073597B2 (en) 2003-09-10 2006-07-11 Williams Danny T Downhole draw down pump and method
US6929753B1 (en) 2003-09-22 2005-08-16 Aqua-Envirotech Mfg., Inc. Coal bed methane wastewater treatment system
US20050082058A1 (en) 2003-09-23 2005-04-21 Bustin Robert M. Method for enhancing methane production from coal seams
CR7129A (en) 2003-10-29 2003-11-17 Carlos Eduardo Rold N Villalobos METHOD AND APPARATUS FOR STORAGE GASES AT LOW TEMPERATURE USING A REFRIGERATION RECOVERY SYSTEM
US6978837B2 (en) 2003-11-13 2005-12-27 Yemington Charles R Production of natural gas from hydrates
US6946017B2 (en) 2003-12-04 2005-09-20 Gas Technology Institute Process for separating carbon dioxide and methane
US20050189211A1 (en) 2004-02-26 2005-09-01 Morton Glenn R. Process and apparatus for the conversion of methane gas to higher hydrocarbons
US20050204625A1 (en) 2004-03-22 2005-09-22 Briscoe Michael D Fuel compositions comprising natural gas and synthetic hydrocarbons and methods for preparation of same
US7594356B2 (en) 2004-06-14 2009-09-29 Freund Matthew R Agricultural products developed from manure
JP4477432B2 (en) 2004-06-29 2010-06-09 東洋エンジニアリング株式会社 Reformer
US7137945B2 (en) 2004-08-13 2006-11-21 Sunstone Corporation Underground treatment of biowaste

Patent Citations (99)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4583994A (en) * 1980-06-12 1986-04-22 Union Carbide Corporation Cyclic process for producing methane in a tubular reactor with effective heat removal
US4582475A (en) * 1980-06-27 1986-04-15 Eaton Corporation Method and apparatus for igniting combustible mixtures
US4642125A (en) * 1981-03-27 1987-02-10 Trw Inc. Carbonaceous material and methods for making hydrogen and light hydrocarbons from such materials
US4738699A (en) * 1982-03-10 1988-04-19 Flexivol, Inc. Process for recovering ethane, propane and heavier hydrocarbons from a natural gas stream
US4571384A (en) * 1982-10-18 1986-02-18 State Of Oregon Acting By And Through The State Board Of Higher Education On Behalf Of Oregon State University Methane production
US4568530A (en) * 1984-10-16 1986-02-04 The M. W. Kellogg Company Ammonia synthesis
US4576005A (en) * 1985-01-07 1986-03-18 Force Louis W Wellhead gas treatment and co-generation method and system
US4814534A (en) * 1985-10-31 1989-03-21 Chevron Research Company Addition of hydrogen and C2 to C4 hydrocarbons to the feed gas in the catalytic conversion of methane to higher molecular weight hydrocarbons
US4728506A (en) * 1986-05-16 1988-03-01 Catalyst Services, Inc. Start-up method for ammonia plants
US4727207A (en) * 1986-07-02 1988-02-23 Standard Oil Company Process for converting methane and/or natural gas to more readily transportable materials
US4727205A (en) * 1986-08-28 1988-02-23 The Standard Oil Company Process for converting methane and/or natural gas to more readily transportable materials
US4801762A (en) * 1987-02-13 1989-01-31 Atlantic Richfield Company Methane conversion process
US4999030A (en) * 1987-03-06 1991-03-12 Foster Wheeler Usa Corporation Process for producing a methane-containing fuel gas
US4805881A (en) * 1987-05-28 1989-02-21 Gas Research Institute Internal gas generator for heat treating furnace
US4795849A (en) * 1987-08-04 1989-01-03 Atlantic Richfield Company Methane conversion process
US4795842A (en) * 1987-08-04 1989-01-03 Atlantic Richfield Company Methane conversion process
US4906447A (en) * 1988-02-12 1990-03-06 Schwarzenbek Eugene F Synthetic ammonia process
US4915619A (en) * 1988-05-05 1990-04-10 The Babcock & Wilcox Company Burner for coal, oil or gas firing
US5011625A (en) * 1989-12-11 1991-04-30 The M. W. Kellogg Company Autothermal steam reforming process
US5388456A (en) * 1990-07-05 1995-02-14 Kettel; Dirk Procedure in order to detect the gas potential in sedimentary basins and the oil potential obtained from this
US5180703A (en) * 1991-04-24 1993-01-19 W. R. Grace & Co.-Conn. Sox/nox sorbent and process of use
US5176887A (en) * 1991-10-07 1993-01-05 Ford Motor Company Treating emissions from engines fueled by compressed natural gas
US5180570A (en) * 1992-01-23 1993-01-19 Lee Jing M Integrated process for making methanol and ammonia
US5501722A (en) * 1992-11-04 1996-03-26 Membrane Technology And Research, Inc. Natural gas treatment process using PTMSP membrane
US5386699A (en) * 1993-05-12 1995-02-07 American Gas & Technology, Inc. Method and apparatus for liquifying natural gas for fuel for vehicles and fuel tank for use therewith
US5387322A (en) * 1993-05-14 1995-02-07 The M. W. Kellogg Company Fusel oil stripping
US5385176A (en) * 1993-07-19 1995-01-31 Price Compressor Company, Inc. Natural gas dispensing
US5719097A (en) * 1993-07-22 1998-02-17 Chang; Clarence D. Catalyst comprising a modified solid oxide
US5385646A (en) * 1993-09-03 1995-01-31 Farmland Industries, Inc. Method of treating chemical process effluent
US5490377A (en) * 1993-10-19 1996-02-13 California Energy Commission Performance enhanced gas turbine powerplants
US5390499A (en) * 1993-10-27 1995-02-21 Liquid Carbonic Corporation Process to increase natural gas methane content
US5869013A (en) * 1993-11-04 1999-02-09 Osaka Gas Company Limited Process and catalyst for reducing Nox in exhaust combustion gases
US6013158A (en) * 1994-02-02 2000-01-11 Wootten; William A. Apparatus for converting coal to hydrocarbons
US5855631A (en) * 1994-12-02 1999-01-05 Leas; Arnold M. Catalytic gasification process and system
US6187226B1 (en) * 1995-03-14 2001-02-13 Bechtel Bwxt Idaho, Llc Thermal device and method for production of carbon monoxide and hydrogen by thermal dissociation of hydrocarbon gases
US5709733A (en) * 1995-05-29 1998-01-20 Nitto Denko Corporation Gas separation method
US6034031A (en) * 1995-09-18 2000-03-07 Nec Corporation Catalyst material for use in producing substitute natural gas and method for producing substitute natural gas
US5711770A (en) * 1996-01-04 1998-01-27 Malina; Mylan Energy conversion system
US5727903A (en) * 1996-03-28 1998-03-17 Genesis Energy Systems, Inc. Process and apparatus for purification and compression of raw landfill gas for vehicle fuel
US5733454A (en) * 1996-04-26 1998-03-31 Ehh Holding Co., Inc. Process and apparatus for the treatment of flowable waste
US6350394B1 (en) * 1996-12-23 2002-02-26 Egt Developments, Llc Method and apparatus for total energy fuel conversion systems
US6340437B1 (en) * 1997-04-11 2002-01-22 Chiyoda Corporation Process for preparing synthesis gas by autothermal reforming
US5883138A (en) * 1997-04-25 1999-03-16 Exxon Research And Engineering Company Rapid injection catalytic partial oxidation process and apparatus for producing synthesis gas (law 562)
US5886056A (en) * 1997-04-25 1999-03-23 Exxon Research And Engineering Company Rapid injection process and apparatus for producing synthesis gas (law 560)
US6035550A (en) * 1997-04-28 2000-03-14 Tokyo Gas Co., Ltd. Method and apparatus for treating bog in a low temperature liquid storage tank
US6011073A (en) * 1997-10-10 2000-01-04 Syntroleum Corporation System and method for converting light hydrocarbons to heavier hydrocarbons with separation of water into oxygen and hydrogen
US6692711B1 (en) * 1998-01-23 2004-02-17 Exxonmobil Research And Engineering Company Production of low sulfur syngas from natural gas with C4+/C5+ hydrocarbon recovery
US6168768B1 (en) * 1998-01-23 2001-01-02 Exxon Research And Engineering Company Production of low sulfer syngas from natural gas with C4+/C5+ hydrocarbon recovery
US6176224B1 (en) * 1998-03-30 2001-01-23 Caterpillar Inc. Method of operating an internal combustion engine which uses a low energy gaseous fuel
US6011192A (en) * 1998-05-22 2000-01-04 Membrane Technology And Research, Inc. Membrane-based conditioning for adsorption system feed gases
US6021647A (en) * 1998-05-22 2000-02-08 Greg E. Ameringer Ethylene processing using components of natural gas processing
US6015450A (en) * 1998-08-13 2000-01-18 The M. W. Kellogg Company Reducing methanol emissions from a syngas unit
US7014822B1 (en) * 1998-12-15 2006-03-21 Osaka Gas Co., Ltd Fluid treating device
US6855852B1 (en) * 1999-06-24 2005-02-15 Metasource Pty Ltd Natural gas hydrate and method for producing same
US6205793B1 (en) * 1999-07-06 2001-03-27 Christopher E. Schimp Method and apparatus for recovering and transporting methane mine gas
US6353133B1 (en) * 1999-11-01 2002-03-05 Acetex (Cyprus) Limited Methanol plant retrofit
US6858049B2 (en) * 1999-12-13 2005-02-22 Exxonmobil Chemical Patents Inc. Method for utilizing gas reserves with low methane concentrations for fueling gas turbines
US6684644B2 (en) * 1999-12-13 2004-02-03 Exxonmobil Chemical Patents Inc. Method for utilizing gas reserves with low methane concentrations and high inert gas concentrations for fueling gas turbines
US6523351B2 (en) * 1999-12-13 2003-02-25 Exxonmobil Chemical Patents Inc. Method for utilizing gas reserves with low methane concentrations and high inert gas concentration for fueling gas turbines
US6355456B1 (en) * 2000-01-19 2002-03-12 Dakota Ag Energy, Inc. Process of using wet grain residue from ethanol production to feed livestock for methane production
US6508209B1 (en) * 2000-04-03 2003-01-21 R. Kirk Collier, Jr. Reformed natural gas for powering an internal combustion engine
US6692544B1 (en) * 2000-04-12 2004-02-17 Ecosystems Projects, Llc Municipal waste briquetting system and method of filling land
US6844292B1 (en) * 2000-04-19 2005-01-18 Osaka Gas Co., Ltd. Method for preparing catalyst for reforming methanol
US6509566B1 (en) * 2000-06-22 2003-01-21 Ophir Corporation Oil and gas exploration system and method for detecting trace amounts of hydrocarbon gases in the atmosphere
US20020029513A1 (en) * 2000-07-31 2002-03-14 William Shaw Ground organic fuel
US20020029770A1 (en) * 2000-08-11 2002-03-14 The Regents Of The University Of California Apparatus and method for operating internal combustion engines from variable mixtures of gaseous fuels
US6503295B1 (en) * 2000-09-20 2003-01-07 Chevron U.S.A. Inc. Gas separations using mixed matrix membranes
US6531630B2 (en) * 2000-12-29 2003-03-11 Kenneth Ebenes Vidalin Bimodal acetic acid manufacture
US6986388B2 (en) * 2001-01-30 2006-01-17 Cdx Gas, Llc Method and system for accessing a subterranean zone from a limited surface area
US20060060525A1 (en) * 2001-02-20 2006-03-23 Hoffland Robert O Method and apparatus for treating animal waste and wastewater
US6685754B2 (en) * 2001-03-06 2004-02-03 Alchemix Corporation Method for the production of hydrogen-containing gaseous mixtures
US20050042166A1 (en) * 2001-03-06 2005-02-24 Kindig James Kelly Method for the production of hydrogen-containing gaseous mixtures
US20030008381A1 (en) * 2001-05-03 2003-01-09 Augenstein Don C. Landfill biofiltration system and methods for removal of gas-phase pollutants and contaminants
US20030006129A1 (en) * 2001-06-28 2003-01-09 Kazuo Imasaki Methane/methanol producing system
US20030027096A1 (en) * 2001-07-18 2003-02-06 Daniel Barnett Steam-methane reformer furnace with convection-heated pre-reformer
US6855272B2 (en) * 2001-07-18 2005-02-15 Kellogg Brown & Root, Inc. Low pressure drop reforming exchanger
US7005405B2 (en) * 2001-09-21 2006-02-28 Kabushiki Kaisha Toshiba Metal oxide sintered structure and production method therefor
US6698237B2 (en) * 2001-12-11 2004-03-02 Advanced Extraction Technologies, Inc. Use of stripping gas in flash regeneration solvent absorption systems
US6991047B2 (en) * 2002-07-12 2006-01-31 Cdx Gas, Llc Wellbore sealing system and method
US6991048B2 (en) * 2002-07-12 2006-01-31 Cdx Gas, Llc Wellbore plug system and method
US6866779B1 (en) * 2002-07-22 2005-03-15 Western Environmental Engineering Company Nitrogen recovery system and method
US20040057898A1 (en) * 2002-09-23 2004-03-25 Kellogg Brown & Root, Inc. Hydrogen enrichment scheme for autothermal reforming
US6691531B1 (en) * 2002-10-07 2004-02-17 Conocophillips Company Driver and compressor system for natural gas liquefaction
US6998098B2 (en) * 2002-11-11 2006-02-14 Conocophillips Company Removal of gases from a feed
US6692554B1 (en) * 2002-12-10 2004-02-17 Visteon Global Technologies, Inc. Methane storage device
US6860257B2 (en) * 2003-01-03 2005-03-01 James L. Wood Processing apparatus and method
US20050061001A1 (en) * 2003-01-29 2005-03-24 Maston Valerie A. Streamlined methane gas generation system
US6988492B2 (en) * 2003-06-12 2006-01-24 Michael Shetley Hydrogen and liquid fuel injection system
US6997703B2 (en) * 2003-07-15 2006-02-14 Ngk Insulators, Ltd. Firing furnace and firing method
US20050013768A1 (en) * 2003-07-17 2005-01-20 Kellogg Brown And Root, Inc. Low-delta p purifier for nitrogen, methane, and argon removal from syngas
US20050016725A1 (en) * 2003-07-22 2005-01-27 Pfefferle William C. Method for natural gas production
US6986266B2 (en) * 2003-09-22 2006-01-17 Cryogenic Group, Inc. Process and apparatus for LNG enriching in methane
US20050061029A1 (en) * 2003-09-22 2005-03-24 Narinsky George B. Process and apparatus for LNG enriching in methane
US20050066815A1 (en) * 2003-09-26 2005-03-31 Consortium Services Management Group, Inc. CO2 separator method and apparatus
US6995846B2 (en) * 2003-12-19 2006-02-07 Itt Manufacturing Enterprises, Inc. System and method for remote quantitative detection of fluid leaks from a natural gas or oil pipeline
US6997055B2 (en) * 2004-05-26 2006-02-14 Baker Hughes Incorporated System and method for determining formation fluid parameters using refractive index
US20060002840A1 (en) * 2004-07-02 2006-01-05 Kellogg Brown & Root, Inc. Pseudoisothermal ammonia process
US20060036123A1 (en) * 2004-08-13 2006-02-16 Hughes W J Underground treatment of biowaste
US20070066495A1 (en) * 2005-09-21 2007-03-22 Ian Macpherson Lubricant compositions including gas to liquid base oils

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2726406A1 (en) * 2011-06-30 2014-05-07 Fluor Technologies Corporation Stand-alone flue gas recirculation fan
EP2726406A4 (en) * 2011-06-30 2014-12-10 Fluor Tech Corp Stand-alone flue gas recirculation fan

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