US3131141A - Non-aqueous process for the recovery of bitumen from tar sands - Google Patents

Non-aqueous process for the recovery of bitumen from tar sands Download PDF

Info

Publication number
US3131141A
US3131141A US136617A US13661761A US3131141A US 3131141 A US3131141 A US 3131141A US 136617 A US136617 A US 136617A US 13661761 A US13661761 A US 13661761A US 3131141 A US3131141 A US 3131141A
Authority
US
United States
Prior art keywords
sand
bitumen
gas oil
phase
tar sands
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US136617A
Inventor
Robert C West
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Jersey Production Research Co
Original Assignee
Jersey Production Research Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Jersey Production Research Co filed Critical Jersey Production Research Co
Priority to US136617A priority Critical patent/US3131141A/en
Application granted granted Critical
Publication of US3131141A publication Critical patent/US3131141A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C3/00—Working-up pitch, asphalt, bitumen
    • C10C3/007—Working-up pitch, asphalt, bitumen winning and separation of asphalt from mixtures with aggregates, fillers and other products, e.g. winning from natural asphalt and regeneration of waste asphalt

Definitions

  • the invention is concerned with an improved technique of efliciently removing hydrocarbons, such as bitumen, tars, and the like, from tar sands containing the same, such as Athabaska tar sands.
  • the invention is particularly concerned with an improved integrated process for the recovery of oil from tar sands utilizing a a process which eliminates the use of water, thereby eliminating the problems of sludge separation, oil-Water emulsions.
  • an integrated operation is utilized employing a hydrocarbon fraction in the gas oil boiling range and a light hydrocarbon such as propane and butane, wherein by a particular technique the bitumen is recovered and the gas oil and light hydrocarbon efiiciently recovered.
  • tar sands exist which contain various types of hydrocarbons as, for example, the heavy deposits of Athabaska tar sands existing in Canada. These sands contain tremendous reserves of hydrocarbon constituents.
  • the oil in the sands may vary from about 5% to 21% by volume, generally in the range of about 12% by volume.
  • the gravity of the oil ranges from about 6 to API, generally about 8 API.
  • These sands may lie from about 200 to 300 feet below an overburden and the beds may range from about 100 to 400 feet thick.
  • a typical oil recovered from the sands has an initial boiling point about 300 F., 1.0% distilled to 430 F., 20.0% distilled to 650 F.
  • Some processes as, for example, direct fluid coking are able to handle these widely difierent compositions and, in accordance with the present process, employing a two-phase operation wherein in an initial phase a substantially richened tar sand is produced and wherein in the second phase the enriched sand is for example handled in a fluid coker, surprisingly effective results are secured.
  • bituminous sands at atmospheric temperatures are introduced into heating zone 1 by means of feed line 2.
  • zone 1 the sands are heated to a temperature preferably in the range from to 140 R, such as about F.
  • countercurrent treating zone 4 comprises a bituminous sand solvent contactor maintained at a pressure suflicient to keep hydrocarbons in the liquid phase.
  • a relatively heavy solvent which comprises a conventional light gas oil is introduced into the lower end of zone 4 by means of line 5. Any suitable contacting or distributing means may be employed in zone 4.
  • the solvent is preferably a gas oil boiling in the range from about 400 to 700 F., preferably in the range from 425 to 600 F.
  • the API gravity is in the range from about 28 to 35, preferably about 32 API, while the Saybolt viscosity at 100 F. is in the range from 60 to 100 seconds, preferably about 80 seconds.
  • a bitumen gas oil solution is removed from the top of zone 4 by means of line 6 and handled as hereinafter described.
  • a sand-gas oil mix falls through a screen or separating element 7 and is withdrawn from the bottom of zone 4 by means of line 8.
  • the crushed sand is moved forward by a rock pump, screw conveyor, or any suitable means.
  • This sand-gas oil mix is introduced into the top area of a second countercurrent treating zone 9 by means of line 8.
  • a light hydrocarbon solvent such as a liquefied normally gaseous hydrocarbon as, for example, liquid propane, butane and the like or a mixture thereof is introduced into the bottom of zone 9 by means of line 10.
  • Zone 9 is maintained at a sufiicient pressure to keep the liquefied normally gaseous hydrocarbons in the liquid phase.
  • the light gas oil and the light hydrocarbon solvent is removed overhead from zone 9 by means of line 11 and introduced into a light hydrocarbon stripping zone 12.
  • the light hydrocarbon as for example propane
  • the light hydrocarbon is removed overhead by means of line 13, passed through condenser 14 and recycled to zone 9 by means of line 10.
  • a portion of the condensate may be introduced into the top of zone 12 by means of line 15.
  • the light gas oil free of propane is removed from the bottom of zone 12 by means of line 16 and recycled to zone 4 by means of line 5 as hereinbefore described.
  • the sand and light hydrocarbon solvent is removed from the bottom of zone 9 by means of line 17 and passed at a reduced pressure into flash drum 18.
  • the light hydrocarbon as for example propane, flashes from the sand and is removed overhead from flash drum 1% by means of line 19.
  • This stream is passed into compression condenser 20 wherein the propane is liquefied and recycled to the system by means of line 21.
  • Clean sand is withdrawn from flash drum 18 by means of line 22 and withdrawn from the system and subsequently handled as desired.
  • bitumen and solvent removed by means of line 6 overhead from initial zone 4 is passed to a water knockout drum 23 wherein connate water separates and is removed from the system by means of line 24.
  • the solvent plus the bitumen is removed from knock-out drum 23 by means of line 25 and passed to a solvent or light gas oil stripper 26.
  • the bitumen is removed as a bottom stream by means of line 27 and further handled as desired, as for example by cracking, coking, and the like.
  • the light gas oil solvent is removed overhead by means of line 28, passed through condensing zone, 29 and recycled to the system by means of line 5 as hereinbefore described. A portion of this stream may be recycled to zone 26 by means of line 30.
  • the present process contacts crushed sand countercurrently in a contacting tower, the crushed sand being moved forward by a rock pump, screw conveyor, etc.
  • the contacting media is a light gas oil.
  • the sand and bitumen plus diluent should be warm, in excess of 100 F.
  • the bitumen-gas oil solution is moved from one end of the tower.
  • the sand-gas oil mix is removed from the other end.
  • the sand-gas oil mix is countercurrently contacted with a light hydrocarbon as propane, butane, and the like. Gas oil plus propane is removed from one end of the tower. Sand with propane is removed from the other end.
  • the pressure in the second tower is such that the light hydrocarbon is a liquid.
  • the sand plus propane is removed into a third tower where the light hydrocarbon is flashed off.
  • the clean dry sand is disposed of by conveyor belt-sand-water slurry, and the like.
  • the gas-oil-propane mix is flashed to remove the propane.
  • the flashed propane from both streams is refined and liquefied for further use.
  • the bitumen-gas oil mix is distilled to separate the two components.
  • An integrated multi-stage process for the removal of bitumen from tar sands which comprises heating the bitumen-containing tar sands to a temperature in the range from about 100 to 140 F., contacting the heated tar sands in an initial solvent contacting stage with a light gas oil under conditions to segregate a bitumen-gas oil phase and a sand-gas oil phase, processing the bitumengas oil phase to separate a phase essentially composed of bitumen, removing said sand-gas oil phase and contacting the same in a secondary solvent contacting stage with a liquefied normally gaseous hydrocarbon under conditions to segregate a sand-liquefied normally gaseous hydrocarbon phase and a gas oil-liquefied normally gaseous hydrocarbon phase, passing said latter phase to a separation zone and segregating the liquefied normally gaseous hydrocarbon from the gas oil, passing the sand liquefied normally gaseous hydrocarbon phase to a separation zone and separating sand from said
  • range of said gas oil is in the range from about 400 to 700 F.
  • bitumengas oil phase removed from said initial solvent contactiug stage is passed to a Water removal zone wherein the connate water is segregated and removed, thereafter passing said connate Water free bitumen-gas oil phase to a distillation zone and removing the gas oil therefrom to secure a phase essentially composed of bitumen.

Description

Aprll 28, 1964 c, WEST 3,131,141
NON-AQUEOUS PROCESS FOR THE RECOVERY OF BITUMEN FROM TAR SANDS Filed Sept. 7, 1961 5 S. g m g 5 V N ,5 g 1 3 o HEddlHiS Q 8 t- Q NOBBVOOHCIAH men 8 '6 man-10s 9 (2 c0 0 [J o o N 9 (2 E 22.5 t a t g 05 z 6 J 4 a: a) g m f- 0: 3 +H 5 5 m O. z a m o 3 2 N 1 0 8 o o x o DJ o 2 O m 4 '3 m 20 Ex 25 a m L 2 E E s f\ r 5 a u D L, t r\. t
WARM
SAND HEATER COLD @BITUMINOUS SAND Robert C. West Inventor Patent Attorney United States Patent 3,131,141 NON-AQUEOUS PROCESS FOR THE RECOVERY 6F BITUMEN FRGM TAR SANDS Robert C. West, Tulsa, 01:12., assignor to Jersey Production Research (Zompany, a corporation of Delaware Filed Sept. 7, 1961, Ser. No. 136,617 6 Claims. (Cl. 208-11) The present invention is broadly concerned with the recovery of hydrocarbons from tar sands. More particularly, the invention is concerned with an improved technique of efliciently removing hydrocarbons, such as bitumen, tars, and the like, from tar sands containing the same, such as Athabaska tar sands. The invention is particularly concerned with an improved integrated process for the recovery of oil from tar sands utilizing a a process which eliminates the use of water, thereby eliminating the problems of sludge separation, oil-Water emulsions. In accordance with the present process, an integrated operation is utilized employing a hydrocarbon fraction in the gas oil boiling range and a light hydrocarbon such as propane and butane, wherein by a particular technique the bitumen is recovered and the gas oil and light hydrocarbon efiiciently recovered.
In various areas of the world, tar sands exist which contain various types of hydrocarbons as, for example, the heavy deposits of Athabaska tar sands existing in Canada. These sands contain tremendous reserves of hydrocarbon constituents. For example, the oil in the sands may vary from about 5% to 21% by volume, generally in the range of about 12% by volume. The gravity of the oil ranges from about 6 to API, generally about 8 API. These sands may lie from about 200 to 300 feet below an overburden and the beds may range from about 100 to 400 feet thick. A typical oil recovered from the sands has an initial boiling point about 300 F., 1.0% distilled to 430 F., 20.0% distilled to 650 F. and 50.0% distilled to 980 F. However, the recovery of hydrocarbons in the past has not been effective to any great extent due to the deficiencies in operating techniques for the recovery of these hydrocarbons. For example, a relative small amount of clay (from about 0% to 30%, usually about 5%) in the sand greatly retards recovery of the oil utilizing conventional water techniques. Apparently the oil and the clay form skins which envelope small pockets of water often containing finely divided sand; then the enveloped pockets are distributed in water, thus forming a type of emulsion.
Numerous attempts have been made in the past to recover bitumen from the Athabaska tar sands in various manners. For example, it has been suggested that a solvent be added in order to reduoe the viscosity of the bitumen, and in conjunction with water, to float the bitumen solvent mixture away from the sand. Although this technique achieves a good separation of clean sand, the addition of water results in problems with the formation of stable emulsions and sludges which have been very difficult to separate. Thus, extensive supplementary processing has been required in order to avoid large oil losses.
It has also been suggested in the past that tar sands as they are mined be handled by a thermal process in order to recover the bitumen therefrom. However, this process has been uneconomical due to the large amount of heat which is lost due to the fact that the heat is imparted to the sand and cannot be effectively and efliciently recovered therefrom. It has been suggested for example that tar sands be handled in a direct fluid coking operation. However, as pointed out, this process is uneconomical for the reasons given above. Also, any process that will effectively handle tar sands must have the ability to han- 3,131,141 Patented Apr. 28, 1964 die a very wide range of tar sands and compositions which occur even in an immediate location. Some processes as, for example, direct fluid coking are able to handle these widely difierent compositions and, in accordance with the present process, employing a two-phase operation wherein in an initial phase a substantially richened tar sand is produced and wherein in the second phase the enriched sand is for example handled in a fluid coker, surprisingly effective results are secured.
The present invention which comprises a non-aqueous operation may be readily understood by reference to the drawing illustrating the integrated operation. Referring specifically to the drawing, bituminous sands at atmospheric temperatures are introduced into heating zone 1 by means of feed line 2. In zone 1 the sands are heated to a temperature preferably in the range from to 140 R, such as about F. These sands are then introduced into the upper area of a first countercurrent treating zone 4 by means of line 3. In essence, countercurrent treating zone 4 comprises a bituminous sand solvent contactor maintained at a pressure suflicient to keep hydrocarbons in the liquid phase. A relatively heavy solvent which comprises a conventional light gas oil is introduced into the lower end of zone 4 by means of line 5. Any suitable contacting or distributing means may be employed in zone 4.
The solvent is preferably a gas oil boiling in the range from about 400 to 700 F., preferably in the range from 425 to 600 F. The API gravity is in the range from about 28 to 35, preferably about 32 API, while the Saybolt viscosity at 100 F. is in the range from 60 to 100 seconds, preferably about 80 seconds.
.A bitumen gas oil solution is removed from the top of zone 4 by means of line 6 and handled as hereinafter described. A sand-gas oil mix falls through a screen or separating element 7 and is withdrawn from the bottom of zone 4 by means of line 8. In the operation, the crushed sand is moved forward by a rock pump, screw conveyor, or any suitable means.
This sand-gas oil mix is introduced into the top area of a second countercurrent treating zone 9 by means of line 8. In this zone, the sand is contacted with a light hydrocarbon solvent so as to produce clean sand. A light hydrocarbon solvent such as a liquefied normally gaseous hydrocarbon as, for example, liquid propane, butane and the like or a mixture thereof is introduced into the bottom of zone 9 by means of line 10. Zone 9 is maintained at a sufiicient pressure to keep the liquefied normally gaseous hydrocarbons in the liquid phase. The light gas oil and the light hydrocarbon solvent is removed overhead from zone 9 by means of line 11 and introduced into a light hydrocarbon stripping zone 12. In this zone, the light hydrocarbon, as for example propane, is removed overhead by means of line 13, passed through condenser 14 and recycled to zone 9 by means of line 10. A portion of the condensate may be introduced into the top of zone 12 by means of line 15. The light gas oil free of propane is removed from the bottom of zone 12 by means of line 16 and recycled to zone 4 by means of line 5 as hereinbefore described.
The sand and light hydrocarbon solvent is removed from the bottom of zone 9 by means of line 17 and passed at a reduced pressure into flash drum 18. Under these conditions, the light hydrocarbon, as for example propane, flashes from the sand and is removed overhead from flash drum 1% by means of line 19. This stream is passed into compression condenser 20 wherein the propane is liquefied and recycled to the system by means of line 21. Clean sand is withdrawn from flash drum 18 by means of line 22 and withdrawn from the system and subsequently handled as desired.
The bitumen and solvent removed by means of line 6 overhead from initial zone 4 is passed to a water knockout drum 23 wherein connate water separates and is removed from the system by means of line 24. The solvent plus the bitumen is removed from knock-out drum 23 by means of line 25 and passed to a solvent or light gas oil stripper 26. In this zone, the bitumen is removed as a bottom stream by means of line 27 and further handled as desired, as for example by cracking, coking, and the like. The light gas oil solvent is removed overhead by means of line 28, passed through condensing zone, 29 and recycled to the system by means of line 5 as hereinbefore described. A portion of this stream may be recycled to zone 26 by means of line 30.
Thus, in essence, the present process contacts crushed sand countercurrently in a contacting tower, the crushed sand being moved forward by a rock pump, screw conveyor, etc. The contacting media is a light gas oil. Preferably, the sand and bitumen plus diluent should be warm, in excess of 100 F. The bitumen-gas oil solution is moved from one end of the tower. The sand-gas oil mix is removed from the other end. The sand-gas oil mix is countercurrently contacted with a light hydrocarbon as propane, butane, and the like. Gas oil plus propane is removed from one end of the tower. Sand with propane is removed from the other end. The pressure in the second tower is such that the light hydrocarbon is a liquid. The sand plus propane is removed into a third tower where the light hydrocarbon is flashed off. The clean dry sand is disposed of by conveyor belt-sand-water slurry, and the like. The gas-oil-propane mix is flashed to remove the propane. The flashed propane from both streams is refined and liquefied for further use. The bitumen-gas oil mix is distilled to separate the two components.
What is claimed is:
1. An integrated multi-stage process for the removal of bitumen from tar sands which comprises heating the bitumen-containing tar sands to a temperature in the range from about 100 to 140 F., contacting the heated tar sands in an initial solvent contacting stage with a light gas oil under conditions to segregate a bitumen-gas oil phase and a sand-gas oil phase, processing the bitumengas oil phase to separate a phase essentially composed of bitumen, removing said sand-gas oil phase and contacting the same in a secondary solvent contacting stage with a liquefied normally gaseous hydrocarbon under conditions to segregate a sand-liquefied normally gaseous hydrocarbon phase and a gas oil-liquefied normally gaseous hydrocarbon phase, passing said latter phase to a separation zone and segregating the liquefied normally gaseous hydrocarbon from the gas oil, passing the sand liquefied normally gaseous hydrocarbon phase to a separation zone and separating sand from said liquefied normally gaseous hydrocarbon.
2. Process as defined by claim 1 wherein said liquefied normally gaseous hydrocarbon is separated from the gas oil in said separation zone by reducing the pressure under conditions to flash the same therefrom.
3. Process as defined by claim 1 wherein said liquefied normally gaseous hydrocarbon is selected from the group consisting of propane and butane.
4. Process as defined by claim 3 wherein the boiling,
range of said gas oil is in the range from about 400 to 700 F.
5. Process as defined by claim 1 wherein the bitumengas oil phase removed from said initial solvent contactiug stage is passed to a Water removal zone wherein the connate water is segregated and removed, thereafter passing said connate Water free bitumen-gas oil phase to a distillation zone and removing the gas oil therefrom to secure a phase essentially composed of bitumen.
6. Process as defined by claim 5 wherein the gas oilli'quefied normally gaseous hydrocarbon phase is passed to a separation zone wherein the hydrocarbon is flashed from the gas oil, thereafter condensed and recycled to said secondary stage.
References Cited in the file of this patent UNITED STATES PATENTS 1,607,977 Armstrong Nov. 23, 1926 2,670,317 Adams Feb. 23, 1954 3,050,289 Gerner Aug. 21, 1962

Claims (1)

1. AN INTEGRATED MULTI-STAGE PROCESS FOR THE REMOVAL OF BITUMEN FROM TAR SANDS WHICH COMPRISES HEATING THE BITUMEN-CONTAINING TAR SANDS TO A TEMPERATURE IN THE RANGE FROM ABOUT 100 TO 140*F., CONTACTING THE HEATED TAR SANDS IN AN INITIAL SOLVENT CONTACTING STAGE WITH A LIGHT GAS OIL UNDER CONDITIONS TO SEGREGATE A BITUMEN-GAS OIL PHASE AND A SAND-GAS OIL PHASE, PROCESSING THE BITUMENGAS OIL PHASE TO SEPARATE A PHASE ESSENTIALLY COMPOSED OF BITUMEN, REMOVING SAID SAND-GAS OIL PHASE AND CONTACTING THE SAME IN A SECONDARY SOLVENT CONTACTING STAGE WITH A LIQUEFIED NORMALLY GASEOUS HYDROCARBON UNDER CONDITIONS TO SEGREGATE A SAND-LIQUEFIED NORMALLY GASEOUS HYDROCARBON PHASE AND A GAS OIL-LIQUEFIED NORMALLY GASEOUS HYDROCARBON PHASE, PASSING SAID LATTER PHASE TO A SEPARATION ZONE AND SEGREGATING THE LIQUEFIED NORMALLY GASEOUS HYDROCARBON FROM THE GAS OIL, PASSING THE SAND LIQUEFIED NORMALLY GASEOUS HYDROCARBON PHASE TO A SEPARATION ZONE AND SEPARATING SAND FROM SAID LIQUEFIED NORMALLY GASEOUS HYDROCARBON.
US136617A 1961-09-07 1961-09-07 Non-aqueous process for the recovery of bitumen from tar sands Expired - Lifetime US3131141A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US136617A US3131141A (en) 1961-09-07 1961-09-07 Non-aqueous process for the recovery of bitumen from tar sands

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US136617A US3131141A (en) 1961-09-07 1961-09-07 Non-aqueous process for the recovery of bitumen from tar sands

Publications (1)

Publication Number Publication Date
US3131141A true US3131141A (en) 1964-04-28

Family

ID=22473609

Family Applications (1)

Application Number Title Priority Date Filing Date
US136617A Expired - Lifetime US3131141A (en) 1961-09-07 1961-09-07 Non-aqueous process for the recovery of bitumen from tar sands

Country Status (1)

Country Link
US (1) US3131141A (en)

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3963599A (en) * 1974-11-11 1976-06-15 Sun Oil Company Of Pennsylvania Recovery of bitumen from aqueous streams via superatmospheric pressure aeration
US4342639A (en) * 1980-07-22 1982-08-03 Gagon Hugh W Process to separate bituminous material from sand (Tar Sands)
US4389300A (en) * 1979-09-26 1983-06-21 Chevron Research Company Solvent extraction method
US4460452A (en) * 1982-07-06 1984-07-17 Atlantic Richfield Company Process for separating crude oil from mixtures comprising finely divided inorganic solids, crude oil, and water
US4481099A (en) * 1979-09-26 1984-11-06 Chevron Research Company Solvent extraction method
US4539093A (en) * 1982-12-16 1985-09-03 Getty Oil Company Extraction process and apparatus for hydrocarbon containing ores
US20060076274A1 (en) * 2004-10-13 2006-04-13 The Technology Store, Inc. Method for obtaining bitumen from tar sands
US20070095076A1 (en) * 2005-11-02 2007-05-03 Jay Duke Apparatus, system, and method for separating minerals from mineral feedstock
US20080210602A1 (en) * 2004-10-13 2008-09-04 Marathon Oil Company System and method of separating bitumen from tar sands
US20090301937A1 (en) * 2004-10-13 2009-12-10 Duyvesteyn Willem P C Dry,stackable tailings and methods for producing the same
US20100032348A1 (en) * 2004-10-13 2010-02-11 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US20100264062A1 (en) * 2009-04-15 2010-10-21 Marathon Oil Canada Corporation Nozzle reactor and method of use
US20110017642A1 (en) * 2009-07-24 2011-01-27 Duyvesteyn Willem P C System and method for converting material comprising bitumen into light hydrocarbon liquid product
US20110062057A1 (en) * 2009-09-16 2011-03-17 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US20110155648A1 (en) * 2009-12-28 2011-06-30 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US20110180459A1 (en) * 2010-01-22 2011-07-28 Marathon Oil Canada Corporation Methods for extracting bitumen from bituminous material
US20110180454A1 (en) * 2010-01-28 2011-07-28 Marathon Oil Canada Corporation Methods for preparing solid hydrocarbons for cracking
US20110180458A1 (en) * 2010-01-22 2011-07-28 Marathon Oil Canada Corporation Methods for extracting bitumen from bituminous material
US20110233114A1 (en) * 2010-03-29 2011-09-29 Marathon Oil Canada Corporation Nozzle reactor and method of use
US8586515B2 (en) 2010-10-25 2013-11-19 Marathon Oil Canada Corporation Method for making biofuels and biolubricants
US8636958B2 (en) 2011-09-07 2014-01-28 Marathon Oil Canada Corporation Nozzle reactor and method of use
US8858786B2 (en) 2010-09-01 2014-10-14 Syncrude Canada Ltd Extraction of oil sand bitumen with two solvents
US8920636B2 (en) 2011-06-28 2014-12-30 Shell Canada Energy and Chervon Canada Limited Methods of transporting various bitumen extraction products and compositions thereof
US8968556B2 (en) 2010-12-09 2015-03-03 Shell Canada Energy Cheveron Canada Limited Process for extracting bitumen and drying the tailings
US9023197B2 (en) 2011-07-26 2015-05-05 Shell Oil Company Methods for obtaining bitumen from bituminous materials
US9683175B2 (en) 2011-06-23 2017-06-20 Exxonmobil Upstream Research Company Systems and methods for separating components of a slurry

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1607977A (en) * 1922-05-15 1926-11-23 Harry H Armstrong Method of recovering hydrocarbon oils from oil sands and the like
US2670317A (en) * 1949-05-27 1954-02-23 Universal Oil Prod Co Extraction of oleaginous materials from solid substances
US3050289A (en) * 1960-06-27 1962-08-21 Phillips Petroleum Co Heavy hydrocarbon recovery from petroliferous deposits by hydraulic washing

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1607977A (en) * 1922-05-15 1926-11-23 Harry H Armstrong Method of recovering hydrocarbon oils from oil sands and the like
US2670317A (en) * 1949-05-27 1954-02-23 Universal Oil Prod Co Extraction of oleaginous materials from solid substances
US3050289A (en) * 1960-06-27 1962-08-21 Phillips Petroleum Co Heavy hydrocarbon recovery from petroliferous deposits by hydraulic washing

Cited By (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3963599A (en) * 1974-11-11 1976-06-15 Sun Oil Company Of Pennsylvania Recovery of bitumen from aqueous streams via superatmospheric pressure aeration
US4389300A (en) * 1979-09-26 1983-06-21 Chevron Research Company Solvent extraction method
US4481099A (en) * 1979-09-26 1984-11-06 Chevron Research Company Solvent extraction method
US4342639A (en) * 1980-07-22 1982-08-03 Gagon Hugh W Process to separate bituminous material from sand (Tar Sands)
US4460452A (en) * 1982-07-06 1984-07-17 Atlantic Richfield Company Process for separating crude oil from mixtures comprising finely divided inorganic solids, crude oil, and water
US4539093A (en) * 1982-12-16 1985-09-03 Getty Oil Company Extraction process and apparatus for hydrocarbon containing ores
US20080210602A1 (en) * 2004-10-13 2008-09-04 Marathon Oil Company System and method of separating bitumen from tar sands
US7985333B2 (en) 2004-10-13 2011-07-26 Marathon Oil Canada Corporation System and method of separating bitumen from tar sands
US8257580B2 (en) 2004-10-13 2012-09-04 Marathon Oil Canada Corporation Dry, stackable tailings and methods for producing the same
US8658029B2 (en) 2004-10-13 2014-02-25 Marathon Oil Canada Corporation Dry, stackable tailings and methods for producing the same
US8101067B2 (en) 2004-10-13 2012-01-24 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US20090301937A1 (en) * 2004-10-13 2009-12-10 Duyvesteyn Willem P C Dry,stackable tailings and methods for producing the same
US20100032348A1 (en) * 2004-10-13 2010-02-11 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US20060076274A1 (en) * 2004-10-13 2006-04-13 The Technology Store, Inc. Method for obtaining bitumen from tar sands
US7909989B2 (en) * 2004-10-13 2011-03-22 Marathon Oil Canada Corporation Method for obtaining bitumen from tar sands
US7722759B2 (en) 2005-11-02 2010-05-25 Pariette Ridge Development Company Llc. Apparatus, system, and method for separating minerals from mineral feedstock
US20070095076A1 (en) * 2005-11-02 2007-05-03 Jay Duke Apparatus, system, and method for separating minerals from mineral feedstock
WO2007056670A3 (en) * 2005-11-02 2007-11-01 Jay Duke Apparatus, system, and method for separating minerals from mineral feedstock
WO2007056670A2 (en) * 2005-11-02 2007-05-18 Jay Duke Apparatus, system, and method for separating minerals from mineral feedstock
US20100264062A1 (en) * 2009-04-15 2010-10-21 Marathon Oil Canada Corporation Nozzle reactor and method of use
US20110017642A1 (en) * 2009-07-24 2011-01-27 Duyvesteyn Willem P C System and method for converting material comprising bitumen into light hydrocarbon liquid product
US20110062057A1 (en) * 2009-09-16 2011-03-17 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US8663462B2 (en) 2009-09-16 2014-03-04 Shell Canada Energy Cheveron Canada Limited Methods for obtaining bitumen from bituminous materials
US20110155648A1 (en) * 2009-12-28 2011-06-30 Marathon Oil Canada Corporation Methods for obtaining bitumen from bituminous materials
US8864982B2 (en) 2009-12-28 2014-10-21 Shell Canada Energy Cheveron Canada Limited Methods for obtaining bitumen from bituminous materials
US8877044B2 (en) 2010-01-22 2014-11-04 Shell Canada Energy Cheveron Canada Limited Methods for extracting bitumen from bituminous material
US20110180459A1 (en) * 2010-01-22 2011-07-28 Marathon Oil Canada Corporation Methods for extracting bitumen from bituminous material
US20110180458A1 (en) * 2010-01-22 2011-07-28 Marathon Oil Canada Corporation Methods for extracting bitumen from bituminous material
US20110180454A1 (en) * 2010-01-28 2011-07-28 Marathon Oil Canada Corporation Methods for preparing solid hydrocarbons for cracking
US8435402B2 (en) 2010-03-29 2013-05-07 Marathon Canadian Oil Sands Holding Limited Nozzle reactor and method of use
US20110233114A1 (en) * 2010-03-29 2011-09-29 Marathon Oil Canada Corporation Nozzle reactor and method of use
US8858786B2 (en) 2010-09-01 2014-10-14 Syncrude Canada Ltd Extraction of oil sand bitumen with two solvents
US8586515B2 (en) 2010-10-25 2013-11-19 Marathon Oil Canada Corporation Method for making biofuels and biolubricants
US8968556B2 (en) 2010-12-09 2015-03-03 Shell Canada Energy Cheveron Canada Limited Process for extracting bitumen and drying the tailings
US9683175B2 (en) 2011-06-23 2017-06-20 Exxonmobil Upstream Research Company Systems and methods for separating components of a slurry
US8920636B2 (en) 2011-06-28 2014-12-30 Shell Canada Energy and Chervon Canada Limited Methods of transporting various bitumen extraction products and compositions thereof
US9023197B2 (en) 2011-07-26 2015-05-05 Shell Oil Company Methods for obtaining bitumen from bituminous materials
US8636958B2 (en) 2011-09-07 2014-01-28 Marathon Oil Canada Corporation Nozzle reactor and method of use

Similar Documents

Publication Publication Date Title
US3131141A (en) Non-aqueous process for the recovery of bitumen from tar sands
US4046668A (en) Double solvent extraction of organic constituents from tar sands
US4347118A (en) Solvent extraction process for tar sands
US4239616A (en) Solvent deasphalting
CA1143686A (en) Solvent extraction method
US3159562A (en) Integrated process for effectively recovering oil from tar sands
CA1253104A (en) Process for recovery for solvent from tar sand bitumen
US4036732A (en) Tar sands extraction process
US4125459A (en) Hydrocarbon solvent treatment of bituminous materials
US3475318A (en) Selective solvent extraction plus filtration of tar sands
US4401551A (en) Solvent extraction method
US3532618A (en) Pour point depressant made by hydrovisbreaking and deasphalting a shale oil
US3296117A (en) Dewatering/upgrading athabaska tar sands froth by a two-step chemical treatment
US4046669A (en) Solvent extraction of oil from tar sands utilizing a trichloroethylene solvent
US3152979A (en) Process for the efficient removal of oil from tar sands
US4279739A (en) Process for separating bituminous materials
US3509037A (en) Tar sand separation process using solvent,hot water and correlated conditions
US3161581A (en) Centrifugal processing of tar sands
US3050289A (en) Heavy hydrocarbon recovery from petroliferous deposits by hydraulic washing
US4481099A (en) Solvent extraction method
US4057485A (en) Solvent extraction of oil from tar sands utilizing a chlorinated ethane solvent
US2324955A (en) Process for removing water from hydrocarbon vapors
US4666562A (en) Solvent recovery from solvent process material mixtures
US3422000A (en) Phosphate additives in a tar sand water separation process
US2431677A (en) Process for the recovery of oil from shales