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US3929193A - Recovery of organic matter from organic mineral-containing deposits - Google Patents

Recovery of organic matter from organic mineral-containing deposits Download PDF

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US3929193A
US3929193A US508585A US50858574A US3929193A US 3929193 A US3929193 A US 3929193A US 508585 A US508585 A US 508585A US 50858574 A US50858574 A US 50858574A US 3929193 A US3929193 A US 3929193A
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organic
extraction fluid
process according
sulfur
extraction
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Roy B Duke
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Marathon Oil Co
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    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
    • C09K8/58—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
    • C09K8/58—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids
    • C09K8/592—Compositions used in combination with generated heat, e.g. by steam injection
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
    • E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection

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  • ABSTRACT Organic matter, including valuable hydrocarbons, are recovered from organic mineral-containing deposits such as oil shale, tar sands, etc., by treating them with molecular sulfur and an extraction fluid, e.g., benzene, at temperatures ranging from about 200 to about 1000F.
  • the present invention relates to the general area of recovery of the organic matter from organic mineralcontaining deposits found in subterranean formations.
  • organic matter is recovered from organic mineral-containing deposits, e.g., oil shale, by contacting oil shale with elemental sulfur, [S and an extraction fluid at temperatures in the range of from about 200 to about 1,000F.
  • the extraction fluids should not react substantially with the elemental sulfur.
  • the invention may be practiced above ground after first mining the organic mineral-containing matter from a subterranean deposit, or more preferably, in situ by injecting the extraction fluid and elemental sulfur into the organic mineral-containing deposit.
  • the injection of elemental sulfur along with the extraction fluid results in increased extraction rates of the organic matter as compared to the corresponding extraction rate with the same extraction fluid in the absence of sulfur.
  • the present invention is useful for the recovery of organic matter, including valuable hydrocarbons, from naturally occurring organic mineral-containing deposits.
  • FIGS. 1 and 2 each graphically depict the extraction of shale oil with benzene and sulfur according to the present invention.
  • FIG. 3 shows the use of a single well recovery system for the in-sity extraction of the shale oil.
  • FIG. 4 schematically shows the in-situ extraction of shale oil from a formation using a two well system.
  • FIG. 5 schematically shows the in-situ extraction of shale oil from a cavity created in an oil shale formation.
  • Extraction Fluids useful in the present invention are organic or inorganic compounds or mixtures thereof which will dissolve substantial amounts of extracted shale oil without entering into substantial reaction with either the elemental sulfur or the hydrogen sulfide produced in the reaction.
  • a partial list of the type of compounds useful as extraction fluids in the present invention is as follows:
  • Aliphatic hydrocarbons e.g., methane, hexane
  • Aromatic hydrocarbons e.g., benzene, naphthalene, tert-butylbenzene, etc.
  • Halogenated organic compounds e.g., chlorobenzene, dichlorobenzene, bromonaphthalene, dodecylchloride, etc.
  • I-Ieterocyclic compounds e.g., pyridine, quinoline,
  • Ethers e.g., diphenyl ether, anisole, polyethylene oxide, etc.
  • Amines e.g. triethylamine, triphenylamine, aniline, etc.
  • Nitrated organic compounds e.g., nitrobenzene.
  • Inorganic compounds e.g., water (steam).
  • Sulfur-containing compounds e.g., dimethylsulfoxide, diphenyl sulfone, diibutylsulfide, etc.
  • Sulfur Sulfur employed with the present invention will preferably be of common commercial purity or may be as mined since impurities will not normally be of serious consequence and can readily be separated by conventional processing of the recovered shale oil.
  • the sulfur will preferably be comminuted to promote dissolving.
  • the temperature of the extraction fluid when it contacts the oil shale or other organic mineral-containing deposit should be in the general range of from I50F to about l,000F, more preferably from 200F to about 900F, and most preferably from 300F to about 800F.
  • the pressure employed in the present extraction process ranges from atmospheric pressure to 20,000 psig.
  • the pressures on the extraction fluid are preferably sufficient to maintain it in a liquid phase in the reactor or subterranean formation; however, the ideal temperature ranges necessary to maintain high extraction rates are often above the critical temperature of the extraction fluid. As a result, no amount of pressure would produce a liquid phase.
  • pressure is controlled to change the density of the critical fluid which :in turn governs the heat capacity and extractive properties of the extraction fluid.
  • the contact time between the extraction fluid and the organic mineral containing deposit is not narrowly critical but will generally be in the range of from about 3 0.01 to about 1,000, more preferably from 0.1 to about 500, and most preferably from 1 to about 250 hours.
  • the present invention can be employed in continuous or batch operations. Furthermore, in continuous operation, the same well can serve as both the injection well and withdrawal well so that the quantity of extraction fluid-elemental sulfur mixture is first injected then allowed to contact the organic mineral-containing deposit for a sufficient time and the recovered organic matter then withdrawn through the same well.
  • Extraction Apparatus The experimental extractions are carried out in a high-pressure autoclave into which the extraction fluid is pumped upflow through a bed of oil shale. Pressure on the system is maintained by a backpressure relief valve. The shale oil extract is collected in high-pressure cylinders which can be isolated from the extraction system, depressurized, and the shale oil-extraction fluid mixture collected.
  • the reactor is filled with a known amount of preassayed oil shale in either lump or core form. Under the desired operating pressure, 300 ml of extraction fluid is charged to liquid fill the reactor. The flow rate through the reactor is then adjusted and the reactor heated rapidly to the desired extraction temperature. When sulfur is used, it is dissolved in the extraction fluid-and pumped along with the latter to the reactor.
  • the product reservoir is drained.
  • the oil recovered during warmup is not used in the subsequent yield calculations.
  • the initial time of the reaction i.e., zero time, is taken the moment the extraction unit reaches the desired temperature. Subsequent time measurements are also taken from this reference point. Samples are then taken periodically and the oil yield determined.
  • the shale oil yields are determined by first filtering or centrifuging the shale oil-extraction fluid mixture to remove the small amount of insoluble matter carried along in the extractate. The extract is then distilled to separate the extraction fluid from the shale oil. The shale oil is subsequently vacuum dried to a constant weight to. ascertain the yield. When sulfur is used to promote the extraction, some unreacted molecular sulfur is carried over into the product. To compensate for this, each shale oil sample is analyzed for sulfur. The shale oil yields are then reported on a sulfur-free basis;
  • EXAMPLE n EXAMPLE III
  • the extraction apparatus was filled with the same oil shale described in Example I and extracted with benzene at 608F. The results are shown in FIG. 2.
  • an extraction fluid containing sulfur is injected through inner well pipe 41 at a temperature of about 600F to the bottom of the well where a packer 42 causes it to exit through a perforation 43 into an oil shale formation 40 which has previously been fractured by conventional techniques, e.g., explosive fracturing, leaching of sodium-containing minerals, mining, mining and explosive rubblizing, etc., in order to render theformation permeable to the flow of fluids.
  • the hot extraction fluid, together with extracted shale oil removed from the formation enter the anular well pipe 44 through a second, higher, perforation 45.
  • the mixture flows upward to the surface and into pipe 15, and then into settling tank 17 to remove the inorganic residue.
  • Centrifuges or filters may be used in the place of or in addition to the settling tank. From the settling tank the extractate is transferred to the fractionator 18 from which a bottoms fraction 25 of shale oil is withdrawn for refinery processing. An overhead of H 8 30 is withdrawn from the top of the fractionating tower l8, oxidized to $0 in burner 31 to which air is fed, and then fed together with another portion of H 5 to reactor 32 in which the H 8 and S0 react to form elemental sulfur for recycle through line 33. Fractionation tower 18 also separates the extraction fluid used in the process and recycles it to line 33 through line 19 where it is recombined with sulfur in tank 20. Pump 21 then injects this benzene-sulfur mixture after heating, back into inner pipe 41, repeating the process.
  • FIG. 4 shows, schematically, an injection well 51 penetrating a permeable formation 52 which is also penetrated by a production well 53.
  • an extraction fluidsulfur mixture is injected into well 51, moves into a permeable zone, established by fracturing, leaching of a soluble sodium-containing salt, or other methods through perforation 55, and subsequently enters production well 53 through suitable perforations.
  • the output from production well 53 is then treated according to the techniques described in Example V1 and the recovered extraction fluid and sulfur are' recycled.
  • a cavity 10 has been created by a nuclear blast, conventional explosive, a combination of both mining and a conventional explosive, or by fracturing.
  • a drift or adit may be mined into the face of a cliff to establish the cavity and communication established between the adit and thee surface of the cliff where the extraction fluid processing equipment is located.
  • Still another way of establishing the permeability is to simply connect two adits by a horizontal drift.
  • the cavity may or may not be filled with rubble, 11.
  • a hot extraction fluid containing elemental sulfur is pumped downward through injection pipe 12 forming a layer 13 on top of the fine silt-like material 14 at the bottom of the cavity.
  • An extraction fluid-oil shale mixture is withdrawn through induction tube 15 located on the other side of the cavity from injection tube 12. Both tubes have means for gradually raising the level at which they communicate with the cavity in order to maintain their communication above the level of silt in the cavity. AS the extraction proceeds, the oil shale decomposes largely to silt and fllls the cavity. Pump 16 located downhole removes the solvent-hydrocarbon mixture. The withdrawn liquids are processes as described in Example VI.
  • the extraction fluid is selected from the group consisting of aliphatic hydrocarbons, aromatic compounds, halogenated organic compounds, heterocyclic organic compounds, organic ether compounds, organic nitrogencontaining compounds, petroleum refinery products, and organic sulfur-containing compounds and mixtures thereof.

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Abstract

Organic matter, including valuable hydrocarbons, are recovered from organic mineral-containing deposits such as oil shale, tar sands, etc., by treating them with molecular sulfur and an extraction fluid, e.g., benzene, at temperatures ranging from about 200* to about 1000*F.

Description

llnited States Patent 1 Duke [ Dec. 30, 1975 1 RECOVERY OF ORGANIC MATTER FROM ORGANIC MINERAL-CONTAINING DEPOSITS Related U.S. Aliplication Data [63] Continuation-impart of Ser. No. 380,783, Aug. 9,
[52] U.S. Cl. 166/303; 208/11 [51] Int. Cl. E21B 43/24 [58] Field of Search 299/4, 5, 3; 166/272, 302, 166/303, 311, 312; 208/11 3,070,162 12/1962 Barnard, Jr. 166/312 X 3,415,573 12/1968 Fraser i 299/5 X 3,488,092 1/1970 Dean et a1. 299/5 3,498,887 3/1970 McClintock et al.. 299/5 X 3,531,160 9/1970 Fisher 299/5 3,645,551 2/1972 Thompson 299/5 Primary EXaminer Stephen J. Novosad Attorney, Agent, or Firm-Joseph C. Herring; Jack L. Hummel; Richard C. Willson, Jr.
[ 57] ABSTRACT Organic matter, including valuable hydrocarbons, are recovered from organic mineral-containing deposits such as oil shale, tar sands, etc., by treating them with molecular sulfur and an extraction fluid, e.g., benzene, at temperatures ranging from about 200 to about 1000F.
[56] References Cited 9 ClalmS, 5 Drawlng Flgures 2,172,683 9/1939 Reed 1. 299/4 BENZENE PLUS 0.11% SULFUR\ BENZENE TEMPERATURE, 625F PRESSURE, 1500 F516 FLOW RATE, 5o ML/HIR l 1 l I l TIME, HOURS Figure l. Extraction of oil shale with benzene and sulfur.
U.S. Patent Dec.30, 1975 Sheetf4 3,929,193
1.20 I I I I I I I I I I I I I g BENZENE PLUS a 0.11% SULFUR\ LLI I U 0.80 2
z Q n- U 040- E a TEMPERATURE, 625F E PRESSURE, 1500 PSIG I FLOW RATE, ML/HR 0.00 l l l I I T l l l TIME, HOURS Figure l. Extraction of oil shale with benzene and sulfur.
US. Patent Dec.30, 1975 Sheet2of4 3,929,193
BENZENE PLUS 0.084% SULFUR\ 0.8 BENZENE PLUS 0.82% SULFUR TEMPERATURE, 608F PRESSURE, I500 PSIG FLOW RATE, 50 ML/HR I I l I l 4O TIME, HOURS YIELD FRACTION OF FISCHER ASSAY Figure 2. Extraction of oil shale with benzene and sulfur.
AIR-P 2O Figure 4. In situ extraction of shale oil.
US. Patent Dec. 30, 1975 Sheet4 of4 3,929,193
Figure 5. In situ extraction of shale oil.
RECOVERY OF ORGANIC MATTER FROM ORGANIC MINERAL-CONTAINING DEPOSITS This application is a continuation-impart of our copending US. Pat. application Ser. No. 380,783, filed Aug. 9, I973.
BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to the general area of recovery of the organic matter from organic mineralcontaining deposits found in subterranean formations.
2. Description of the Prior Art US. Pat. Nos. 3,527,692 and 3,474,863 have taught the recovery of hydrocarbons from oil shale by treatment with a sulfur-containing compound, i.e., hydrogen sulfide, in the presence of an extraction fluid. The sulfur employed in these inventions is in the -2 oxidation state [8]. The present invention employes sulfur in the zero oxidation state [8]. The latter is capable of undergoing redox reactions with the organic and inorganic matter in the organic mineral-containing-deposit, e. g., oil shale, thereby accelerating the rate of oil recovery.
SUMMARY OF THE INVENTION General Statement of the Invention According to the present invention, organic matter is recovered from organic mineral-containing deposits, e.g., oil shale, by contacting oil shale with elemental sulfur, [S and an extraction fluid at temperatures in the range of from about 200 to about 1,000F. Ideally, the extraction fluids should not react substantially with the elemental sulfur.
The invention may be practiced above ground after first mining the organic mineral-containing matter from a subterranean deposit, or more preferably, in situ by injecting the extraction fluid and elemental sulfur into the organic mineral-containing deposit. The injection of elemental sulfur along with the extraction fluid results in increased extraction rates of the organic matter as compared to the corresponding extraction rate with the same extraction fluid in the absence of sulfur.
Utility of the Invention The present invention is useful for the recovery of organic matter, including valuable hydrocarbons, from naturally occurring organic mineral-containing deposits.
BRIEF DESCRIPTION OF THE DRAWINGS FIGS. 1 and 2 each graphically depict the extraction of shale oil with benzene and sulfur according to the present invention.
FIG. 3 shows the use of a single well recovery system for the in-sity extraction of the shale oil.
FIG. 4 schematically shows the in-situ extraction of shale oil from a formation using a two well system.
FIG. 5 schematically shows the in-situ extraction of shale oil from a cavity created in an oil shale formation.
DESCRIPTION OF THE PREFERRED EMBODIMENTS Organic and Mineral-Containing Natural Deposit The present invention is useful for the recovery of hydrocarbons from naturally occurring organic mineral-containing deposits, including tar sands, oil shale, lignite, torbanite, coorongite, kukersite, etc. Extraction Fluids Extraction fluids useful in the present invention are organic or inorganic compounds or mixtures thereof which will dissolve substantial amounts of extracted shale oil without entering into substantial reaction with either the elemental sulfur or the hydrogen sulfide produced in the reaction. A partial list of the type of compounds useful as extraction fluids in the present invention is as follows:
1. Aliphatic hydrocarbons, e.g., methane, hexane,
dodecane, isooctane, etc. 2. Aromatic hydrocarbons, e.g., benzene, naphthalene, tert-butylbenzene, etc.
3. Halogenated organic compounds, e.g., chlorobenzene, dichlorobenzene, bromonaphthalene, dodecylchloride, etc.
4. I-Ieterocyclic compounds, e.g., pyridine, quinoline,
thiophene, benzothiophene, etc.
5. Ethers, e.g., diphenyl ether, anisole, polyethylene oxide, etc.
6. Amines, e.g. triethylamine, triphenylamine, aniline, etc.
7. Nitrated organic compounds, e.g., nitrobenzene.
8. Inorganic compounds, e.g., water (steam).
9. Various petroleum products, e.g., kerosine, fuel oil, gas oil, whole crude oil, etc.
10. Various cuts from the fractional distillations of shale oil or whole shale oil.
11. Sulfur-containing compounds, e.g., dimethylsulfoxide, diphenyl sulfone, diibutylsulfide, etc.
12. Combinations of the above-mentioned compounds.
Sulfur Sulfur employed with the present invention will preferably be of common commercial purity or may be as mined since impurities will not normally be of serious consequence and can readily be separated by conventional processing of the recovered shale oil. For best results, the sulfur will preferably be comminuted to promote dissolving.
Temperature Though not narrowly critical, the temperature of the extraction fluid when it contacts the oil shale or other organic mineral-containing deposit should be in the general range of from I50F to about l,000F, more preferably from 200F to about 900F, and most preferably from 300F to about 800F.
Pressure The pressure employed in the present extraction process ranges from atmospheric pressure to 20,000 psig. In an in situ extraction, the pressures on the extraction fluid are preferably sufficient to maintain it in a liquid phase in the reactor or subterranean formation; however, the ideal temperature ranges necessary to maintain high extraction rates are often above the critical temperature of the extraction fluid. As a result, no amount of pressure would produce a liquid phase. In cases where the extraction fluid is above its critical temperature, pressure is controlled to change the density of the critical fluid which :in turn governs the heat capacity and extractive properties of the extraction fluid.
Extraction Time The contact time between the extraction fluid and the organic mineral containing deposit is not narrowly critical but will generally be in the range of from about 3 0.01 to about 1,000, more preferably from 0.1 to about 500, and most preferably from 1 to about 250 hours.
The present invention can be employed in continuous or batch operations. Furthermore, in continuous operation, the same well can serve as both the injection well and withdrawal well so that the quantity of extraction fluid-elemental sulfur mixture is first injected then allowed to contact the organic mineral-containing deposit for a sufficient time and the recovered organic matter then withdrawn through the same well. Extraction Apparatus The experimental extractions are carried out in a high-pressure autoclave into which the extraction fluid is pumped upflow through a bed of oil shale. Pressure on the system is maintained by a backpressure relief valve. The shale oil extract is collected in high-pressure cylinders which can be isolated from the extraction system, depressurized, and the shale oil-extraction fluid mixture collected.
Procedure The reactor is filled with a known amount of preassayed oil shale in either lump or core form. Under the desired operating pressure, 300 ml of extraction fluid is charged to liquid fill the reactor. The flow rate through the reactor is then adjusted and the reactor heated rapidly to the desired extraction temperature. When sulfur is used, it is dissolved in the extraction fluid-and pumped along with the latter to the reactor.
When the reactor reaches the desired temperature, the product reservoir is drained. The oil recovered during warmup is not used in the subsequent yield calculations. The initial time of the reaction, i.e., zero time, is taken the moment the extraction unit reaches the desired temperature. Subsequent time measurements are also taken from this reference point. Samples are then taken periodically and the oil yield determined.
The shale oil yields are determined by first filtering or centrifuging the shale oil-extraction fluid mixture to remove the small amount of insoluble matter carried along in the extractate. The extract is then distilled to separate the extraction fluid from the shale oil. The shale oil is subsequently vacuum dried to a constant weight to. ascertain the yield. When sulfur is used to promote the extraction, some unreacted molecular sulfur is carried over into the product. To compensate for this, each shale oil sample is analyzed for sulfur. The shale oil yields are then reported on a sulfur-free basis;
' 4 EXAMPLE I The extraction apparatus is filled with lump-size oil shale to mesh) and extracted with benzene at 625F and 1,500 psig. The oil shale had a Fischer assay of-33p4 gal/ton (12.45 weight percent oil). The results are shown in FIG. 1.
EXAMPLE n EXAMPLE III The extraction apparatus was filled with the same oil shale described in Example I and extracted with benzene at 608F. The results are shown in FIG. 2.
EXAMPLE IV The extraction apparatus was filled with the same oil shale described in Example I and extracted with benzene containing 0.084 percent sulfur at 608F.
EXAMPLE V The extraction apparatus was filled with the same oil shale described in Example I and extracted with benzene containing 0.82 percent sulfur at 608F.
EXAMPLE VI Referring to FIG. 3, an extraction fluid containing sulfur is injected through inner well pipe 41 at a temperature of about 600F to the bottom of the well where a packer 42 causes it to exit through a perforation 43 into an oil shale formation 40 which has previously been fractured by conventional techniques, e.g., explosive fracturing, leaching of sodium-containing minerals, mining, mining and explosive rubblizing, etc., in order to render theformation permeable to the flow of fluids. The hot extraction fluid, together with extracted shale oil removed from the formation enter the anular well pipe 44 through a second, higher, perforation 45. The mixture flows upward to the surface and into pipe 15, and then into settling tank 17 to remove the inorganic residue. Centrifuges or filters may be used in the place of or in addition to the settling tank. From the settling tank the extractate is transferred to the fractionator 18 from which a bottoms fraction 25 of shale oil is withdrawn for refinery processing. An overhead of H 8 30 is withdrawn from the top of the fractionating tower l8, oxidized to $0 in burner 31 to which air is fed, and then fed together with another portion of H 5 to reactor 32 in which the H 8 and S0 react to form elemental sulfur for recycle through line 33. Fractionation tower 18 also separates the extraction fluid used in the process and recycles it to line 33 through line 19 where it is recombined with sulfur in tank 20. Pump 21 then injects this benzene-sulfur mixture after heating, back into inner pipe 41, repeating the process.
EXAMPLE VII FIG. 4 shows, schematically, an injection well 51 penetrating a permeable formation 52 which is also penetrated by a production well 53. In a process analogous to that described in Example I, an extraction fluidsulfur mixture is injected into well 51, moves into a permeable zone, established by fracturing, leaching of a soluble sodium-containing salt, or other methods through perforation 55, and subsequently enters production well 53 through suitable perforations. The output from production well 53 is then treated according to the techniques described in Example V1 and the recovered extraction fluid and sulfur are' recycled.
EXAMPLE VIIl Referring to FIG. 5, a cavity 10 has been created by a nuclear blast, conventional explosive, a combination of both mining and a conventional explosive, or by fracturing. Alternatively, a drift or adit may be mined into the face of a cliff to establish the cavity and communication established between the adit and thee surface of the cliff where the extraction fluid processing equipment is located. Still another way of establishing the permeability is to simply connect two adits by a horizontal drift. The cavity may or may not be filled with rubble, 11. A hot extraction fluid containing elemental sulfur is pumped downward through injection pipe 12 forming a layer 13 on top of the fine silt-like material 14 at the bottom of the cavity. An extraction fluid-oil shale mixture is withdrawn through induction tube 15 located on the other side of the cavity from injection tube 12. Both tubes have means for gradually raising the level at which they communicate with the cavity in order to maintain their communication above the level of silt in the cavity. AS the extraction proceeds, the oil shale decomposes largely to silt and fllls the cavity. Pump 16 located downhole removes the solvent-hydrocarbon mixture. The withdrawn liquids are processes as described in Example VI.
Modifications of the Invention Variations on the invention, obvious to those skilled in the art, are to be included within the scope of the invention as claimed.
What is claimed is:
l. A process for the recovery of organic matter from organic mineral-containing deposits selected from the groups consisting of tar sands, oil shale, lignite, torbanite, coorongite and kukersite, by contacting the organic mineral-containing deposits at a temperature of from about 200 to about l00OF with an extraction fluid and elemental sulfur, said elemental sulfur being present in the range of from about 0.001 to about 0.5
parts by weight of sulfur per part by weight of extraction fluid.
2. The process according to claim 1 wherein the contact time between said organic mineral containing deposit and said extraction fluid and elemental sulfur is in the range of from about 0.01 to about 2000 hours.
3. The process according to claim 1 wherein the pressure is maintained in the range of zero to 5000 psig.
4. The process according to claim 1 wherein the extraction fluid is contacted with the organic mineralcontaining deposit at temperatures above its critical temperature.
5. The process according to claim 1 wherein the extraction fluid is selected from the group consisting of aliphatic hydrocarbons, aromatic compounds, halogenated organic compounds, heterocyclic organic compounds, organic ether compounds, organic nitrogencontaining compounds, petroleum refinery products, and organic sulfur-containing compounds and mixtures thereof.
6. The process according to claim 1 wherein the extraction fluid comprises at least one cut from the fractional distillation of shale oil.
7. The process according to claim 1 wherein the extraction fluid is water.
8. A process according to claim 1 wherein the organic matter comprises hydrocarbons.
9. A process according to claim 8 wherein the organic mineral-containing deposits comprise oil shale.

Claims (9)

1. A PROCESS FOR THE RECOVERY OF ORGANIC MATTER FROM ORGANIC MINERAL-CONTAINING DEPOSITS SELECTED FROM THE GROUPS CONSISTING OF TAR SANDS, OIL SHALE, LIGNITE, TORBANITE, COORONGITE AND KUKERSITE, BY CONTACTING THE ORGANIC MINERALERAL-CONTAINING DEPOSITS AT A TEMPERATURE OF FROM ABOUT 200 TO ABOUT 1000*F WITH AN EXTRACTION FLUID AND ELEMENTAL SULFUR, SAID ELEMENTAL SULFUR BEING PRESENT IN THE RANGE OF FROM ABOUT 0.001 TO ABOUT 0.5 PARTS BY WEIGHT OF SULFUR PER PART BY WEIGHT OF EXTRACTION FLUID.
2. The process according to claim 1 wherein the contact time between said organic mineral containing deposit and said extraction fluid and elemental sulfur is in the range of from about 0.01 to about 2000 hours.
3. The process according to claim 1 wherein the pressure is maintained in the range of zero to 5000 psig.
4. The process according to claim 1 wherein the extraction fluid is contacted with the organic mineral-containing deposit at temperatures above its critical temperature.
5. The process according to claim 1 wherein the extraction fluid is selected from the group consisting of aliphatic hydrocarbons, aromatic compounds, halogenated organic compounds, heterocyclic organic compounds, organic ether compounds, organic nitrogen-containing compounds, petroleum refinery products, and organic sulfur-containing compounds and mixtureS thereof.
6. The process according to claim 1 wherein the extraction fluid comprises at least one cut from the fractional distillation of shale oil.
7. The process according to claim 1 wherein the extraction fluid is water.
8. A process according to claim 1 wherein the organic matter comprises hydrocarbons.
9. A process according to claim 8 wherein the organic mineral-containing deposits comprise oil shale.
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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4005005A (en) * 1974-05-31 1977-01-25 Standard Oil Company (Indiana) Process for recovering and upgrading hydrocarbons from tar sands
US4029568A (en) * 1974-02-04 1977-06-14 Minerals Research Corporation Method of recovery of oil and bitumen from oil-sands and oil shale
US4094768A (en) * 1977-01-04 1978-06-13 Exxon Research & Engineering Co. Separation of bitumen from tar sands using sulfur and water
DE2702789A1 (en) * 1977-01-24 1978-07-27 Coal Industry Patents Ltd Oil shale or tar sand extraction - using extractant, e.g. benzene, at above critical temp.
US4108760A (en) * 1974-07-25 1978-08-22 Coal Industry (Patents) Limited Extraction of oil shales and tar sands
US4139450A (en) * 1977-10-12 1979-02-13 Phillips Petroleum Company Solvent extraction of tar sand
US4306960A (en) * 1980-03-28 1981-12-22 Energy Modification Inc. Coal liquefaction and oil upgrading process to obtain maximum yield of distillate
US4381035A (en) * 1980-02-25 1983-04-26 Hradel Joseph R Simultaneous recovery of thermal values and organic materials from solid carbonaceous fuels and waste disposal process
US4387016A (en) * 1980-11-10 1983-06-07 Gagon Hugh W Method for extraction of bituminous material
US4388171A (en) * 1981-10-30 1983-06-14 Beggs James M Administrator Of Supercritical multicomponent solvent coal extraction
US4397736A (en) * 1981-04-01 1983-08-09 Phillips Petroleum Company Hydrotreating supercritical solvent extracts in the presence of alkane extractants
US4443321A (en) * 1981-11-17 1984-04-17 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Supercritical solvent coal extraction
USRE32120E (en) * 1981-04-01 1986-04-22 Phillips Petroleum Company Hydrotreating supercritical solvent extracts in the presence of alkane extractants
US4610776A (en) * 1984-06-29 1986-09-09 Uop Inc. Coal liquefaction process
US5047143A (en) * 1987-05-08 1991-09-10 Chevron Research Company Method for converting lower grade uintaite to higher grade materials
WO2011116148A2 (en) * 2010-03-16 2011-09-22 Dana Todd C Systems, apparatus and methods for extraction of hydrocarbons from organic materials
US9321967B2 (en) 2009-08-17 2016-04-26 Brack Capital Energy Technologies Limited Oil sands extraction

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Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4029568A (en) * 1974-02-04 1977-06-14 Minerals Research Corporation Method of recovery of oil and bitumen from oil-sands and oil shale
US4005005A (en) * 1974-05-31 1977-01-25 Standard Oil Company (Indiana) Process for recovering and upgrading hydrocarbons from tar sands
US4108760A (en) * 1974-07-25 1978-08-22 Coal Industry (Patents) Limited Extraction of oil shales and tar sands
US4094768A (en) * 1977-01-04 1978-06-13 Exxon Research & Engineering Co. Separation of bitumen from tar sands using sulfur and water
DE2702789A1 (en) * 1977-01-24 1978-07-27 Coal Industry Patents Ltd Oil shale or tar sand extraction - using extractant, e.g. benzene, at above critical temp.
US4139450A (en) * 1977-10-12 1979-02-13 Phillips Petroleum Company Solvent extraction of tar sand
US4381035A (en) * 1980-02-25 1983-04-26 Hradel Joseph R Simultaneous recovery of thermal values and organic materials from solid carbonaceous fuels and waste disposal process
US4306960A (en) * 1980-03-28 1981-12-22 Energy Modification Inc. Coal liquefaction and oil upgrading process to obtain maximum yield of distillate
US4387016A (en) * 1980-11-10 1983-06-07 Gagon Hugh W Method for extraction of bituminous material
US4397736A (en) * 1981-04-01 1983-08-09 Phillips Petroleum Company Hydrotreating supercritical solvent extracts in the presence of alkane extractants
USRE32120E (en) * 1981-04-01 1986-04-22 Phillips Petroleum Company Hydrotreating supercritical solvent extracts in the presence of alkane extractants
US4388171A (en) * 1981-10-30 1983-06-14 Beggs James M Administrator Of Supercritical multicomponent solvent coal extraction
US4443321A (en) * 1981-11-17 1984-04-17 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Supercritical solvent coal extraction
US4610776A (en) * 1984-06-29 1986-09-09 Uop Inc. Coal liquefaction process
US5047143A (en) * 1987-05-08 1991-09-10 Chevron Research Company Method for converting lower grade uintaite to higher grade materials
US9321967B2 (en) 2009-08-17 2016-04-26 Brack Capital Energy Technologies Limited Oil sands extraction
WO2011116148A2 (en) * 2010-03-16 2011-09-22 Dana Todd C Systems, apparatus and methods for extraction of hydrocarbons from organic materials
WO2011116148A3 (en) * 2010-03-16 2011-11-24 Dana Todd C Systems, apparatus and methods for extraction of hydrocarbons from organic materials

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