US3642607A - Coal dissolution process - Google Patents

Coal dissolution process Download PDF

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US3642607A
US3642607A US63334A US3642607DA US3642607A US 3642607 A US3642607 A US 3642607A US 63334 A US63334 A US 63334A US 3642607D A US3642607D A US 3642607DA US 3642607 A US3642607 A US 3642607A
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coal
oil
alkali metal
promoter
pressure
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Walter H Seitzer
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Sunoco Inc
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Sun Oil Co
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    • 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
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent

Definitions

  • ABSTRACT Process for dissolving bituminous coal by heating a mixture of said coal, a hydrogen donor oil, carbon monoxide, water, and an alkali metal hydroxide or its preoursor at a temperature of about 400-450 C. and under a total pressure of at least about 4,000 p.s.i.g.
  • bituminous coal may readily be essentially completely solubilized by an economical highly efficient process. This is accomplished by subjecting a mixture of powdered coal, a donor solvent oil, carbon monoxide, water, and an alkali metal hydroxide (or an alkali metal hydroxide precursor) to an elevated temperature of about 400-450 C. at a pressure of at least about 4,000 p.s.i.g. In this way the coal is essentially completely solubilized and the liquid which is obtained is readily handled and subjected to normal refinery operations to provide useful liquid fuels.
  • Coal useful in the process will be a bituminous coal and Illinois bituminous coal is particularly useful. However, other bituminous coals are also useful such as Rock Springs Wyoming coal, Utah coal, Western Pennsylvania coal, and the like.
  • the oil used in the process of the invention is a hydrogen donor solvent.
  • These donor solvent materials are well known and comprise aromatic hydrocarbons which are partially hydrogenated, generally having one or more of the nuclei at least partially saturated.
  • Several examples of such materials are tetralin. dihydronaphthalene, dihydroalkylnaphthalenes, dihydrophenanthrene, dihydroanthracene, dihydrochrysenes, tetrahydrochrysenes, tetrahydropyrenes, tetrahydrofluoranthenes and the like.
  • hydrogen donor solvents are the hydrophenanthrenes and hydroanthracenes such as dihydroanthracene. It will be understood that these materials may be'obtained from any source, but are readily available from coal processing systems as anthracene oil, and the like. Of particular value are recycle oils from the coal dissolving process of the invention.
  • the alkali hydroxides which appear to promote solution of the coal will preferably be an alkali metal hydroxide, ammonium hydroxide, or any precursor of these materials.
  • precursor is meant a material which under conditions of the process will be converted to an alkali and thereby serve to function in the manner of an alkali metal or ammonium hydroxide.
  • examples of such materials are alkali metal and ammonium salts of carbonates, acetates, nitrates, oxalates, halides (e.g., chlorides, bromides, and iodides) and the like, which under the reaction conditions are hydrolyzed to alkali metal or ammonium hydroxides. It is surprising that hydroxides such as magnesium, calcium and the like are not operable.
  • coal is powdered and mixed with the donor solvent, which is preferably anthracene oil, recycle oil, or its equivalent.
  • the donor solvent which is preferably anthracene oil, recycle oil, or its equivalent.
  • the ratio of coal to oil will be from about 1:4 to about 1:1 on a weight basis with a 1 to 1 ratio being preferred.
  • Water and the base are then added to the mixture and preferably this is added in the form of a solution of the base or precursor in water.
  • the amount of water present should be sufficient to generate a water vapor pressure in the system of at least about one-fifth of the total pressure.
  • the amount of carbon monoxide will be sufficient to generate at least one-fifth of the total pressure. It will be understood that the water pressure and carbon monoxide pressure account primarily for the total pressure in the system.
  • the mixture of coal, oil, water and base is then placed in a pressure vessel and pressured with carbon monoxide to the desired pressure and the contents of the pressure vessel heated to a temperature of about 400450 C.
  • Total pressure generated will be between about 4,000 and about 6,000 p.s.i.g. Dissolution of the coal occurs in a relative- 1y short time, being on the order of about 0.5 to about 3 hours, and solution is essentially complete with very little if any insoluble material being present.
  • Liquefied coal produced by the method of the invention is then subjected to normal cracking and hydrocracking reactions to obtain a liquid fuel such as gasoline, fuel oil, kerosene and the like.
  • EXAMPLE 1 A 1 liter rocking autoclave was charged with 75 g. of powdered bituminous coal (Illinois No. 6) and 75 g. of anthracene oil and then 75 g. of water containing 2.5 g. of NH OH. This represents 3.2 percent of NI-I OH based on the coal charged.
  • the reactor was sealed, pressure tested, and then pressured with carbon monoxide to 1,200 p.s.i.g.
  • the reactor was heated to 415 C. for one hour, allowed to cool, and the product then filtered to remove the solids which were washed with a toluene acetone mixture, dried, and weighed. The percent of organic solids undissolved was 14 percent whereas 33 percent was undissolved when the run was repeated without the ammonium hydroxide.
  • Example 1 When the process of Example 1 is repeated with 3 percent magnesium acetate and 7 percent calcium acetate, the maximum pressure being 4,800 p.s.i.g., the amount of undissolved organic solids is 30 percent and 20 percent respectively, thus showing the high specificity of the process for alkali metal hydroxides.
  • a process for dissolving bituminous coal which comprises heating at about 400 C. to about 450 C. under a total pressure of at least about 4,000 p.s.i.g., a mixture of said finely di- 5.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Liquid Carbonaceous Fuels (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

Process for dissolving bituminous coal by heating a mixture of said coal, a hydrogen donor oil, carbon monoxide, water, and an alkali metal hydroxide or its precursor at a temperature of about 400*-450* C. and under a total pressure of at least about 4,000 p.s.i.g.

Description

United States Patent Seitzer 154] COAL DISSOLUTION PROCESS [21] Appl. No.: 63,334
52 US. Cl ..208/8, 208/10 51 1111.01 ..Cl0g 1/00 [58] Field of Search ..208/10, 8
[56] References Cited UNITED STATES PATENTS 1,445,423 2/1923 Ulke ..208/8 1,838,548 12/1931 Haslam et al... ...208/8 2,034,818 3/1936 Loughrey .208/8 3,341,447 9/1967 Bull 61 al..... ...208/8 3,477,941 11/1969 Nelson ..208/8 1451 Feb. 15, 1972 Primary Examiner-De1bert E. Gantz Assistant ExaminerVeronica OKeefe Attorney-George L. Church, Donald R. Johnson, Wilmer E. McCorquodale, Jr. and Paul Lipsitz [57] ABSTRACT Process for dissolving bituminous coal by heating a mixture of said coal, a hydrogen donor oil, carbon monoxide, water, and an alkali metal hydroxide or its preoursor at a temperature of about 400-450 C. and under a total pressure of at least about 4,000 p.s.i.g.
8 Claims, No Drawings COAL DISSOLUTION PROCESS Much effort has been expended in attempting to convert coal into useful liquid fuels. A desirable approach is to liquefy the coal and subject it to the usual cracking and hydrocracking operations to provide fuel oils, gasoline, and the like. Much difficulty has been encountered, however, in the step of bringing the solid coal into liquid form so that it can be readily subjected to refinery operations and this has been particularly true with bituminous coals. Heretofore, available processes have yielded only limited solubility of bituminous coals and significant amounts of insolubles had to be removed by one means or another, all of which were expensive and decreased the efficiency of the overall process.
It has now been found that bituminous coal may readily be essentially completely solubilized by an economical highly efficient process. This is accomplished by subjecting a mixture of powdered coal, a donor solvent oil, carbon monoxide, water, and an alkali metal hydroxide (or an alkali metal hydroxide precursor) to an elevated temperature of about 400-450 C. at a pressure of at least about 4,000 p.s.i.g. In this way the coal is essentially completely solubilized and the liquid which is obtained is readily handled and subjected to normal refinery operations to provide useful liquid fuels. Coal useful in the process will be a bituminous coal and Illinois bituminous coal is particularly useful. However, other bituminous coals are also useful such as Rock Springs Wyoming coal, Utah coal, Western Pennsylvania coal, and the like.
As indicated the oil used in the process of the invention is a hydrogen donor solvent. These donor solvent materials are well known and comprise aromatic hydrocarbons which are partially hydrogenated, generally having one or more of the nuclei at least partially saturated. Several examples of such materials are tetralin. dihydronaphthalene, dihydroalkylnaphthalenes, dihydrophenanthrene, dihydroanthracene, dihydrochrysenes, tetrahydrochrysenes, tetrahydropyrenes, tetrahydrofluoranthenes and the like. Of particular value in the process of this invention as hydrogen donor solvents are the hydrophenanthrenes and hydroanthracenes such as dihydroanthracene. It will be understood that these materials may be'obtained from any source, but are readily available from coal processing systems as anthracene oil, and the like. Of particular value are recycle oils from the coal dissolving process of the invention.
The alkali hydroxides which appear to promote solution of the coal will preferably be an alkali metal hydroxide, ammonium hydroxide, or any precursor of these materials. By precursor is meant a material which under conditions of the process will be converted to an alkali and thereby serve to function in the manner of an alkali metal or ammonium hydroxide. Examples of such materials are alkali metal and ammonium salts of carbonates, acetates, nitrates, oxalates, halides (e.g., chlorides, bromides, and iodides) and the like, which under the reaction conditions are hydrolyzed to alkali metal or ammonium hydroxides. It is surprising that hydroxides such as magnesium, calcium and the like are not operable.
In carrying out the process of the invention coal is powdered and mixed with the donor solvent, which is preferably anthracene oil, recycle oil, or its equivalent. Generally the ratio of coal to oil will be from about 1:4 to about 1:1 on a weight basis with a 1 to 1 ratio being preferred. Water and the base are then added to the mixture and preferably this is added in the form of a solution of the base or precursor in water. The amount of water present should be sufficient to generate a water vapor pressure in the system of at least about one-fifth of the total pressure. Similarly, the amount of carbon monoxide will be sufficient to generate at least one-fifth of the total pressure. It will be understood that the water pressure and carbon monoxide pressure account primarily for the total pressure in the system. The mixture of coal, oil, water and base is then placed in a pressure vessel and pressured with carbon monoxide to the desired pressure and the contents of the pressure vessel heated to a temperature of about 400450 C. Total pressure generated will be between about 4,000 and about 6,000 p.s.i.g. Dissolution of the coal occurs in a relative- 1y short time, being on the order of about 0.5 to about 3 hours, and solution is essentially complete with very little if any insoluble material being present. Liquefied coal produced by the method of the invention is then subjected to normal cracking and hydrocracking reactions to obtain a liquid fuel such as gasoline, fuel oil, kerosene and the like.
The following examples will serve to further illustrate the invention:
EXAMPLE 1 A 1 liter rocking autoclave was charged with 75 g. of powdered bituminous coal (Illinois No. 6) and 75 g. of anthracene oil and then 75 g. of water containing 2.5 g. of NH OH. This represents 3.2 percent of NI-I OH based on the coal charged. The reactor was sealed, pressure tested, and then pressured with carbon monoxide to 1,200 p.s.i.g. The reactor was heated to 415 C. for one hour, allowed to cool, and the product then filtered to remove the solids which were washed with a toluene acetone mixture, dried, and weighed. The percent of organic solids undissolved was 14 percent whereas 33 percent was undissolved when the run was repeated without the ammonium hydroxide.
EXAMPLE 2 Following the details and procedure of Example 1, runs were made with various alkali metal hydroxides. The following Table I indicates the results obtained:
TABLE I Percent Alkali Hydroxide Max. Ci Undissulvcd (Based On Coal Charged) Pressure Organic Solids None 5,800 33 2% NaOH 5,800 10 3% NaOH 5,l00 5 2% KOH 4,800 0 2% LiOH 4,700 It) EXAMPLE 3 The process of Example 1 was repeated with various precursors of alkali metal hydroxides with the results shown in Table II.
When the process of Example 1 is repeated with 3 percent magnesium acetate and 7 percent calcium acetate, the maximum pressure being 4,800 p.s.i.g., the amount of undissolved organic solids is 30 percent and 20 percent respectively, thus showing the high specificity of the process for alkali metal hydroxides.
The invention claimed is:
1. A process for dissolving bituminous coal which comprises heating at about 400 C. to about 450 C. under a total pressure of at least about 4,000 p.s.i.g., a mixture of said finely di- 5. The process of claim 4 where the promoter is potassium oxalate.
6. The process of claim 1 where the promoter is an alkali metal acetate.
7. The process of claim 1 where the oil is recycle oil and the promoter is sodium acetate.
8. The process of claim 1 where the oil is recycle oil and the promoter is an alkali metal nitrate.

Claims (7)

  1. 2. The process of claim 1 where the coal is an Illinois No. 6 coal, the oil is anthracene oil and the promoter is an alkali metal carbonate.
  2. 3. The process of claim 1 where the oil is a recycle oil and the promoter is sodium carbonate.
  3. 4. The process of claim 1 where the oil is a recycle oil and the promoter is an alkali metal oxalate.
  4. 5. The process of claim 4 where the promoter is potassium oxalate.
  5. 6. The process of claim 1 where the promoter is an alkali metal acetate.
  6. 7. The process of claim 1 where the oil is recycle oil and the promoter is sodium acetate.
  7. 8. The process of claim 1 where the oil is recycle oil and the promoter is an alkali metal nitrate.
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Cited By (44)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3819506A (en) * 1971-09-16 1974-06-25 Sun Research Development Coal dissolving process
DE2452663A1 (en) * 1973-11-08 1975-05-22 Coal Industry Patents Ltd PROCESS FOR CARBON HYDROGENATION
US3909390A (en) * 1972-09-15 1975-09-30 Universal Oil Prod Co Coal liquefaction process
US3930984A (en) * 1970-10-01 1976-01-06 Phillips Petroleum Company Coal-anthracene oil slurry liquefied with carbon monoxide and barium-promoted catalysts
US3983028A (en) * 1974-07-01 1976-09-28 Standard Oil Company (Indiana) Process for recovering upgraded products from coal
US3988238A (en) * 1974-07-01 1976-10-26 Standard Oil Company (Indiana) Process for recovering upgraded products from coal
US4021329A (en) * 1976-01-15 1977-05-03 Suntech, Inc. Process for dissolving sub-bituminous coal
US4028220A (en) * 1974-11-19 1977-06-07 Coal Industry (Patents) Limited Gas extraction of coal
US4036731A (en) * 1974-12-19 1977-07-19 Coal Industry (Patents) Limited Hydrogenation of coal
US4038172A (en) * 1974-10-16 1977-07-26 Agency Of Industrial Science & Technology Method for removal of oxygen from oxygen-containing compounds
US4057484A (en) * 1975-12-15 1977-11-08 John Michael Malek Process for hydroliquefying coal or like carbonaceous solid materials
US4089773A (en) * 1976-12-01 1978-05-16 Mobil Oil Corporation Liquefaction of solid carbonaceous materials
US4128471A (en) * 1976-11-30 1978-12-05 Gulf Research & Development Company Coal liquefaction process employing carbon monoxide
US4222849A (en) * 1979-07-05 1980-09-16 Kunitoshi Shimizu Process of liquefaction of coal
US4247384A (en) * 1979-03-15 1981-01-27 Mobil Oil Corporation Liquefaction of carbonaceous materials
US4263123A (en) * 1978-05-01 1981-04-21 Exxon Research & Engineering Co. Anionic grafts of monomers onto coal substrates
US4266083A (en) * 1979-06-08 1981-05-05 The Rust Engineering Company Biomass liquefaction process
US4345989A (en) * 1980-08-27 1982-08-24 Exxon Research & Engineering Co. Catalytic hydrogen-donor liquefaction process
WO1982004060A1 (en) * 1981-05-13 1982-11-25 Zandona Oliver J Progressive flow cracking of coal/oil mixtures with high metals content catalyst
US4437980A (en) 1982-07-30 1984-03-20 Rockwell International Corporation Molten salt hydrotreatment process
US4451351A (en) * 1980-11-17 1984-05-29 Pentanyl Technologies, Inc. Method of liquefaction of carbonaceous materials
US4455215A (en) * 1982-04-29 1984-06-19 Jarrott David M Process for the geoconversion of coal into oil
US4539094A (en) * 1984-04-19 1985-09-03 Air Products And Chemicals, Inc. Extraction of depolymerized carbonaceous material using supercritical ammonia
US4539095A (en) * 1984-04-19 1985-09-03 Air Products And Chemicals, Inc. Aqueous alkali depolymerization of coal with a quinone
WO1987006254A1 (en) * 1986-04-18 1987-10-22 Carbon Resources, Inc. Integrated ionic liquefaction process
US4968414A (en) * 1987-10-02 1990-11-06 Eniricerche S.P.A. Process for single-step coal liquefaction
US5017282A (en) * 1987-10-02 1991-05-21 Eniricerche, S.P.A. Single-step coal liquefaction process
US5026475A (en) * 1989-12-21 1991-06-25 Exxon Research & Engineering Company Coal hydroconversion process comprising solvent extraction (OP-3472)
US5110450A (en) * 1989-12-21 1992-05-05 Exxon Research And Engineering Company Coal extract hydroconversion process comprising solvent enhanced carbon monoxide pretreatment
US5120430A (en) * 1989-09-28 1992-06-09 National Energy Council Coal solubilization
US5128017A (en) * 1987-10-02 1992-07-07 Eniricerche, S.P.A. Single-step coal liquefaction process
US5151173A (en) * 1989-12-21 1992-09-29 Exxon Research And Engineering Company Conversion of coal with promoted carbon monoxide pretreatment
US5336395A (en) * 1989-12-21 1994-08-09 Exxon Research And Engineering Company Liquefaction of coal with aqueous carbon monoxide pretreatment
US20050271579A1 (en) * 2004-06-03 2005-12-08 Rogers Charles J Low temperature methods for hydrogen production
US20080256852A1 (en) * 2007-04-20 2008-10-23 Schobert Harold H Integrated process and apparatus for producing coal-based jet fuel, diesel fuel, and distillate fuels
US20090236263A1 (en) * 2008-03-24 2009-09-24 Baker Hughes Incorporated Method for Reducing Acids in Crude or Refined Hydrocarbons
WO2009085700A3 (en) * 2007-12-20 2009-12-10 Chevron U.S.A. Inc. Integrated process for in-field upgrading of hydrocarbons
WO2012167792A3 (en) * 2011-06-10 2013-04-11 Steeper Energy Aps Process and apparatus for producing liquid hydrocarbon
WO2012167794A3 (en) * 2011-06-10 2013-04-25 Steeper Energy Aps Process for producing liquid hydrocarbon
US9061953B2 (en) 2013-11-19 2015-06-23 Uop Llc Process for converting polycyclic aromatic compounds to monocyclic aromatic compounds
US9982199B2 (en) 2012-08-30 2018-05-29 Steeper Energy Aps Method for preparing start up of process and equipment for producing liquid hydrocarbons
US10005962B2 (en) 2012-08-30 2018-06-26 Steeper Energy Aps Method for preparing shut down of process and equipment for producing liquid hydrocarbons
US10087373B2 (en) 2012-08-30 2018-10-02 Steeper Energy Aps Method for controlling cleaning of an apparatus for producing liquid hydrocarbons
EP2661477B1 (en) 2011-01-05 2019-06-26 Licella Pty Limited Processing of organic matter

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US1711499A (en) * 1925-12-02 1929-05-07 Hofsass Max Method of hydrogenating and treating carbonaceous materials
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Cited By (62)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3930984A (en) * 1970-10-01 1976-01-06 Phillips Petroleum Company Coal-anthracene oil slurry liquefied with carbon monoxide and barium-promoted catalysts
US3819506A (en) * 1971-09-16 1974-06-25 Sun Research Development Coal dissolving process
US3909390A (en) * 1972-09-15 1975-09-30 Universal Oil Prod Co Coal liquefaction process
DE2452663A1 (en) * 1973-11-08 1975-05-22 Coal Industry Patents Ltd PROCESS FOR CARBON HYDROGENATION
US4019975A (en) * 1973-11-08 1977-04-26 Coal Industry (Patents) Limited Hydrogenation of coal
US3983028A (en) * 1974-07-01 1976-09-28 Standard Oil Company (Indiana) Process for recovering upgraded products from coal
US3988238A (en) * 1974-07-01 1976-10-26 Standard Oil Company (Indiana) Process for recovering upgraded products from coal
US4038172A (en) * 1974-10-16 1977-07-26 Agency Of Industrial Science & Technology Method for removal of oxygen from oxygen-containing compounds
US4028220A (en) * 1974-11-19 1977-06-07 Coal Industry (Patents) Limited Gas extraction of coal
US4036731A (en) * 1974-12-19 1977-07-19 Coal Industry (Patents) Limited Hydrogenation of coal
US4057484A (en) * 1975-12-15 1977-11-08 John Michael Malek Process for hydroliquefying coal or like carbonaceous solid materials
US4021329A (en) * 1976-01-15 1977-05-03 Suntech, Inc. Process for dissolving sub-bituminous coal
US4128471A (en) * 1976-11-30 1978-12-05 Gulf Research & Development Company Coal liquefaction process employing carbon monoxide
US4089773A (en) * 1976-12-01 1978-05-16 Mobil Oil Corporation Liquefaction of solid carbonaceous materials
US4263123A (en) * 1978-05-01 1981-04-21 Exxon Research & Engineering Co. Anionic grafts of monomers onto coal substrates
US4247384A (en) * 1979-03-15 1981-01-27 Mobil Oil Corporation Liquefaction of carbonaceous materials
US4266083A (en) * 1979-06-08 1981-05-05 The Rust Engineering Company Biomass liquefaction process
US4222849A (en) * 1979-07-05 1980-09-16 Kunitoshi Shimizu Process of liquefaction of coal
US4345989A (en) * 1980-08-27 1982-08-24 Exxon Research & Engineering Co. Catalytic hydrogen-donor liquefaction process
US4451351A (en) * 1980-11-17 1984-05-29 Pentanyl Technologies, Inc. Method of liquefaction of carbonaceous materials
WO1982004060A1 (en) * 1981-05-13 1982-11-25 Zandona Oliver J Progressive flow cracking of coal/oil mixtures with high metals content catalyst
US4455215A (en) * 1982-04-29 1984-06-19 Jarrott David M Process for the geoconversion of coal into oil
US4437980A (en) 1982-07-30 1984-03-20 Rockwell International Corporation Molten salt hydrotreatment process
US4539095A (en) * 1984-04-19 1985-09-03 Air Products And Chemicals, Inc. Aqueous alkali depolymerization of coal with a quinone
US4539094A (en) * 1984-04-19 1985-09-03 Air Products And Chemicals, Inc. Extraction of depolymerized carbonaceous material using supercritical ammonia
WO1987006254A1 (en) * 1986-04-18 1987-10-22 Carbon Resources, Inc. Integrated ionic liquefaction process
US4846963A (en) * 1986-04-18 1989-07-11 Knudson Curtis L Ionic liquefaction process
US4968414A (en) * 1987-10-02 1990-11-06 Eniricerche S.P.A. Process for single-step coal liquefaction
US5017282A (en) * 1987-10-02 1991-05-21 Eniricerche, S.P.A. Single-step coal liquefaction process
US5128017A (en) * 1987-10-02 1992-07-07 Eniricerche, S.P.A. Single-step coal liquefaction process
US5120430A (en) * 1989-09-28 1992-06-09 National Energy Council Coal solubilization
US5026475A (en) * 1989-12-21 1991-06-25 Exxon Research & Engineering Company Coal hydroconversion process comprising solvent extraction (OP-3472)
US5151173A (en) * 1989-12-21 1992-09-29 Exxon Research And Engineering Company Conversion of coal with promoted carbon monoxide pretreatment
US5336395A (en) * 1989-12-21 1994-08-09 Exxon Research And Engineering Company Liquefaction of coal with aqueous carbon monoxide pretreatment
US5110450A (en) * 1989-12-21 1992-05-05 Exxon Research And Engineering Company Coal extract hydroconversion process comprising solvent enhanced carbon monoxide pretreatment
US20050271579A1 (en) * 2004-06-03 2005-12-08 Rogers Charles J Low temperature methods for hydrogen production
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