US3926775A - Hydrogenation of coal - Google Patents

Hydrogenation of coal Download PDF

Info

Publication number
US3926775A
US3926775A US412026A US41202673A US3926775A US 3926775 A US3926775 A US 3926775A US 412026 A US412026 A US 412026A US 41202673 A US41202673 A US 41202673A US 3926775 A US3926775 A US 3926775A
Authority
US
United States
Prior art keywords
coal
hydrogenation
steam
zone
stream
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
US412026A
Other languages
English (en)
Inventor
Wilburn C Schroeder
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.)
Individual
Original Assignee
Individual
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 Individual filed Critical Individual
Priority to US412026A priority Critical patent/US3926775A/en
Priority to CA210,971A priority patent/CA1030470A/en
Priority to DE19742449531 priority patent/DE2449531A1/de
Priority to JP49126499A priority patent/JPS5743117B2/ja
Application granted granted Critical
Publication of US3926775A publication Critical patent/US3926775A/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
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • 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
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes

Definitions

  • ABSTRACT heats the coal to hydrogenation temperature and the coal is hydrogenated by hydrogen which to a large extent is produced in situ in contact with the coal through steam-carbon monoxide and steam-carbon reactions.
  • the coal is effectively and economically hydrogenated to produce liquid hydrocarbon products and gases for recycling.
  • Tars recovered from the product stream may be hydrogenated in like manner at system pressure with the products of tar hydrogenation being combined with the main product steam.
  • This invention comprises a simplified coal hydrogenation process which substantially reduces capital and operating costs for the commercial production of oil, oil products, and gas from coal.
  • This invention broadly comprises establishing a closed high pressure cyclic system through which a stream of hydrogen containing gases is continuously circulated, such system including a hydrogenation zone, a product separation zone, a gas-purification zone and a reforming and heating zone, adding steam, oxygen and coal (if necessary) at system pressure to the circulating gases in the reforming zone, adding coal at system pressure to the hydrogenation zone, withdraw ing liquid hydrocarbon products from the circulating gases in the product separation zone and removing H 8 and CO from the circulating gases in the gas purification zone.
  • the process of the invention comprises circulating hydrogen-containing gases continuously through a closed cyclic system which is maintained at hydrogenation pressure above about 1000 psi and which includes a reforming zone and a hydrogenation zone; introducing steam, oxygen and, if necessary, coal or other carbonaceous material, into the circulating hydro gen-containing gases in the reforming zone to cause reaction between part of the steam and the oxygen with hydrocarbons present in the circulating gases and with any added carbonaceous material, to form hydrogen and carbon monoxide, and to raise the temperature of the gaseous stream to that sufficient to provide heat necessary in the hydrogenation zone, introducing the hot gaseous steam from the reforming zone and coal into the hydrogenation zone, heating the coal to hydrogenation temperature (at least 750F) in the hydrogenation zone by contact with said hot gaseous stream and hydrogenating the coal in said zone, preferably in the presence of a hydrogenation catalyst, by hydrogen produced in situ in contact with the coal by the reaction of steam with CO and carbon as well as with that present in the hot gases, to produce liquid and gas
  • Coals ranging from bituminous through sub-bituminous to lignite are the preferred carbonaceous materials for use in the present invention. These coals normally contain 4 to 6 percent hydrogen. Other materials present in addition to ash and carbon are oxygen, sulfur, and nitrogen. Petroleum products on the other hand contain from about 10 to percent hydrogen with the remainder being essentially carbon. To convert coal to a liquid hydrocarbon it must react with hydrogen to raise the hydrogen content to the range from 10 to 15 percent and at the same time oxygen, sulfur and nitrogen must be reduced or eliminated.
  • the hydrogen does this by the formation of H 0, H 5 and NH Coal for the hydrogenation process is usually washed to reduce the ash as much as possible and dried to 3 or 4 percent moisture although a greater amount of moisture can be left in the coal where it is desired for producing additional steam for the hydrogenation reaction. It is then crushed or pulverized, often to about 60 or 70 percent through 200 mesh which is about normal pulverizing for large size utility boilers. Pulverizing is not always a requirement for some coals have been found to disintegrate on introduction into the hot hydrogenation zone.
  • Past commercial practice for getting the coal into the high pressure hydrogenation zone was to mix it with about an equal amount of heavy oil and use slurry pumps to force it into the reaction zone.
  • the operating pressure for the coal hydrogenation process of this invention is between about 1000 and 10,000 psi, but with hydrogenation catalysts now commercially available pressures between about 1000 and 5000 psi are usually satisfactory.
  • the temperatures required for hydrogenation of coal to oil and gas cover a range from approximately 750 to l500F, depending on pressure, time, catalyst, type of coal, and products desired. The effect of various factors has been described in my aforementioned U.S. Pat. Nos. 3,030,297 and 3,152,063. At temperatures from about 750 to about l050F the products are largely liquid with relatively small amounts of gas. From l0O0F to 1300F gas production increases and liquid decreases. The liquid that is produced at this temperature range is aromatic in nature. Above 1300F the hydrocarbon products are largely gas and any liquids are essentially completely aromatic. The preferred temperature for producing liquid products for refining into gasoline and light oil fractions is in the range of about 800 to 1000F.
  • a hydrogenation catalyst be present.
  • These are usually compounds of heavy metals in the form of oxides or sulfides.
  • These catalysts are well known to those skilled in the art and need no detailed description herein. They may, for example, comprise compounds of cobalt, molybdenum, iron, tin, nickel other The and mixtures thereof.
  • the catalysts may be sprayed on the coal in a water soluble solution, or be present in the form of a fixed or fluidized bed. Where the catalyst is directly sprayed on the "coal it may be applied in an amount of about 0.1 to 'l% by weight of metal based on the weight of the coal.
  • FIG. 1 is part of a flow diagram of an improved coal liquification process embodying the principles of the invention.
  • FIG. 2 is the remainder of the flow diagram showing, in particular, the means for providing the hot gaseous stream for contacting the coal.
  • a preferred type of feeder is one which feeds pulverized coal at the full pressure of the system without loss of pressurized gas and without recovery steps that involve mechanically compressing dirty gas that may contain coal particles.
  • Such a feeder is disclosed in my aforementioned U.S. Pat. No. 3,762,773.
  • opening valve 4 which allows gas to flow through line 5 to equalize the pressure between the feeder and the hydrogenation system.
  • Feeders 2 and 3 may be used alternately by proper manipulation of the valves and controls.
  • Coal for the hydrogenation process flows, for example, from feeder 2 through line 6, valve 7 and line 8 into line 9 at the bottom of reactor 10.
  • the rate of flow is controlled by a screw or vibratory feeder 11, or other suitable means.
  • a portion of the H for hydrogenation is generated and coal is converted to hydrocarbon liquids and gases in reactor 10.
  • This is a steel vessel capable of operating at the desired pressures and temperatures e.g., at a selected set of pressure and temperature conditions between about 1000 to 10,000 psi and about 750F to 1500F.
  • Gas at high temperature containing hydrogen, carbon monoxide and steam enters the reactor through the line 9 at the bottom of the reactor.
  • the method for producing the hydrogen entering through line 9 will be described hereafter.
  • the coalstructure disintegrates and the hydrogen present and produced in situ reacts with the resulting fragments to produce smaller molecules which are hydrocarbon liquids and gases.
  • the oxygen in the coal reacts with C or hydrogen to produce CO or H O, the sulfur and nitrogen react with hydrogen to form H 5 and NH respectively.
  • These compounds (CO H 0, H 5 and NH are all gaseous materials under the conditions in the reactor.
  • a substantial amount of CO is formed in the reaction zone in reactor 10, which reduces the partial pressure of hydrogen.
  • Lime (CaO) or other suitable solid alkaline material can be used to react with the CO as follows: Ca0 CO CaCO This will remove the CO, from the gas phase and increase the hydrogen partial pressure. Removal of the CO also promotes the formation of additional H from C0, as follows: C0 H O CD H As the CO is removed from the gas the reaction moves to the right.
  • Pulverized lime may be fed with the coal into the pressurized coal feeders 2 and 3 by means not shown.
  • a catalyst is desired to promote the reaction between hydrogen and coal in vessel 10 at the lower temperatures.
  • the catalyst e.g., molybdenum
  • the catalyst may be applied by converting it to a water soluble compound such as ammonium molybdate, and spraying this solution on the coal in suitable known concentrations by well-known means not shown in the flow diagram.
  • the catalyst may also be used in the form of pellets of such size that they form a fluidized or ebullating bed in reactor 10. In this case the pellets should be large enough so that they are not carried out of reactor 10 by the rising gas stream. Alternatively, a fixed bed of catalyst materialmay be placed in reactor 10.
  • gas coming through line 9 may enter the reactor 10 at the bottom as shown, or it may enter at the top (not shown). Coal may be put in at the top, or it may enter at the bottom with the gas stream as shown. The coal may be entrained in the stream strem or it may be present as a fluidized bed in the reaction zone.
  • the outlet line 12 leaving reactor 10 will be at the opposite end of the reactor from the point of gas entry.
  • the gas must enter at the bottom. Coal may enter at the top or with the gas stream at the bottom. Outlet 12 leaving reactor 10 will then be near the top as shown.
  • the gas and/or the coal may enter at the top or bottom of the reactor with the exit gases, liquids and solids leaving from the opposite end of the reactor.
  • Gases, oil, and solids leave reactor 10 through line 12 and enter heat exchanger 14, where the temperature is reduced to about 400F by indirect heat exchange with water and solids and some heavy tars separate out.
  • This material is discharged through line 15 and is pumped by means of pump 16 into tar reactor 17 where it is hydrogenated by contact with hot steam and hydrogen containing gases entering through line 18.
  • Alternate methods of separating and hydrogenatin g the tar Within the closed cyclic system can be used.
  • the temperature of the steam and hydrogen containing gases in lines 9 and 18 may be, for example about 1300F. This is usually sufficient to maintain a hydro genation temperature of about 875F in reactors 10 and 17.
  • the effluent from the tar reactor 17 leaves the reactor through line 19 and enters cyclone separator 20 where solids are separated from the oils and gases. The solids are removed through pressure reduction device 21 and line 22.
  • Gases and oils leave cyclone separator 20 through line 23 and join the product in stream 24 from heat exchanger 14.
  • the combined streams in line 25 enter heat exchanger 26 where further cooling by indirect heat ex change with water reduces the temperature to about F.
  • the oils are taken from this heat exchanger through line 27.and pressure reduction device 28 and enter oil-gas separator 29. Oils go to refining through line 30. Recovered gases, which were dissolved in the oil, are recycled to the hydrogenation system through line 31 and compressor 32. These gases are primarily hydrogen and methane.
  • the water is in direct contact with the gases in tower 34.
  • the water will remove H 8 from the gas to below 0.1 volume percent and will remove most of the C0
  • the gas leaving through line 35 is primarily H with small amounts of CH, and CO.
  • the hydrogen concentration will be above about 70% and the methane concentration will be from about 5 to 15%.
  • the gases in line 35 may be partially vented through line 35a to other uses as desired. This will prevent build-upp of inert gases in the recycle stream and serve to control the volume of recycle gas.
  • Wash water leaving through line 36 goes through pressure reducer 37 and line 38 to gas stripper 39.
  • the gases leaving the stripper through line 40 are H 8 and CO These are treated in a Claus plant 41 to convert the H 8 to solid or liquid sulfur.
  • the CO is vented.
  • the degassed water leaves stripper 39 through line 42 and may be recycled, after cooling and filtering, to the wash tower 34.
  • Gas from line 35 is returned to the system through recycle compressor 43 where the initial operating pressure is restored. Relatively little energy is required for this operation.
  • the remainder of the recycle gas from line 44 may be passed through line 45 and valve 46 to join the recycle gases from compressor 32.
  • the combined recycle gases are passed through line 47 into heat exchanger 48 where they are heated to a temperature of from about 800 900F.
  • the hot recycle gases then pass through line 49 into reformer 50.
  • This is a refractory lined, water jacketed vessel operating at a temperature above about 1800F, and preferably near 2600F, in which the gas is reacted with oxygen coming through line 51 and superheated steam (at a maximum temperature of about 1200F) coming through line 52. It is important that the amount of steam in the reformer 50 be in excess of that required to produce CO and H from all the carbon or hydrocarbon materials in the gasification zone. At least twice the stoichiometric amount of steam required for hydrogen make-up in the closed cyclic system is introduced at this point. Coal for supplying heat and make-up hydrogen may be introduced into the reformer 50 through line 53 from a pressurized feeder such as those shown at 2 and 3.
  • the gases at this point may have a temperature of about 2200F.
  • the temperature of the gases is reduced to that which is just sufficient to maintain the necessary hydrogenation temperature in reactor 10.
  • the steam and hydrogen containing gases in line 55 which supplies lines 9 and 18, respectively may be about 1300F.
  • a portion of the recycle gases from line 44 may be introduced into the gases in line 54 through line 56 and valve 57, provided the amount of methane in the gases to be introduced into the reactor is below about 10%. This is a further means for control of temperature and gaseous components in the stream to the reactor 10.
  • Superheated steam necessary for the system is supplied by steam boiler 58 which may burn coal as shown.
  • This steam may readily be produced at pressures above 1000 psi and at a maximum temperature of about 1200F as known in the art. Desirably it is supplied to the system at a temperature above 800F.
  • Part of the steam is supplied to line 52 and is further heated and partially reacted in reformer 50.
  • Another part of the steam may be supplied through line 59 to supply power for oxygen plant 60.
  • the oxygen is also delivered at system pressure.
  • the coal gasifier is virtually eliminated by the generation of most of the hydrogen from very high temperature steam and recycle gases in the hydrogenation reactor and reformer.
  • This reaction is favored at temperatures between 800- 1 F.
  • Hydrogen compression required about 77 percent of the total power used in the former commercial processes. Since hydrogen compression is eliminated in the present process, the power plant is reduced to about l/S of its former size.
  • the process will require pressurized coal feeders and oxygen must be delivered to the process at high pressure. Oxygen compression may be carried out while the oxygen is in the form of a liquid and the equipment will be comparatively small.
  • the pressurized coal feeders are estimated to add 3 or 4 percent to the capital costs and oxygen compression about 1 percent. The net capital savings are estimated to amount to at least 65-75 percent.
  • EXAMPLE As an example of one application of this invention, 120 tons of bituminous coal (moisture and ash free) per hour is converted to hydrocarbon products at 4000 psi and 850F. An additional 30 tons of coal per hour is required to generate electric power and raise steam.
  • the ultimate analysis of the coal is 5.3% H, 80.6% C, 2.0% N, 10.0% 0, and 2.1% S.
  • the coal contains 8% moisture and 6.2% ash.
  • the heating value on a moisture and ash free basis (MAF) is 29 million Btu per ton.
  • the coal is first washed and separated into a high and low ash fraction.
  • the high ash fraction is used in the electric power plant and 'for steam raising, while the low ash fraction goes to the hydrogenation process.
  • the coal for hydrogenation is dried to about 3 to 4% moisture and pulverized to about 70% through 200 mesh.
  • High pressure coal feeders supply coal continuously to the coal hydrogenation reactor.
  • the hydrogen content of the coal in the reactor increases from 5.3% to 13 or 14%, which gives a product yield of about 528 barrels per hour of middle and light oils.
  • Coal for hydrogenation is contacted by the hot gas stream from the gas reformer which contains hydrogen, carbon monoxide and steam in some excess of that required for production of the necessary hydrogen for the coal hydrogenation reaction.
  • Total steam requirements are about 170 tons per hour.
  • the temperature of the combined gas and steam flow from the reformer is adjusted to about 1300F. These gases heat the coal and furnish heat to produce hydrogen from the carbon monoxide, carbon and steam. This lowers the gas and steam temperature and raises the coal temperature to about 850F. If necessary, the temperature of the incoming gas stream may be increased or decreased to maintain this temperature in the reactor. The result of the reactions in the hydrogenator provide the hydrocarbon liquid product.
  • Oil produced is approximately 3.5 barrels per ton of coal. Thermal efficiency of the process, is above 65 percent based on heat in the products divided by the heating value of the total MAF coal fed. (120 30 tons).
  • a process for hydrogenating coal comprising: continuously circulating a stream of hydrogen-containing gases including CO and steam at coal hydrogenation pressure between about 1000 to 5000 psi through a 10 closed cyclic system including a hydrogenation zone and an oxygen-steam reforming zone, adding coal in the substantial absence of a pasting medium under system pressure to the hydrogenation zone and hydrogenating the coal in said zone at a temperature in the range of about 750F to l250F by contact with said gases to produce liquid and gaseous hydrocarbons in the circulating stream, removing liquid hydrocarbons from the circulating stream without substantially reducing the pressure of such stream, introducing the resulting gaseous stream containing gaseous hydrocarhens and hydrogen into the reforming zone, introducing oxygen and steam at system pressure into said reforming zone for reaction with the gaseous hydrocarbon components of the gaseous stream to produce carbon monoxide and hydrogen and to raise the temperature of the gaseous stream sufficently to bring the coal to coal hydrogenation temperature in said range, the amount of steam introduced into the reforming zone being in excess

Landscapes

  • 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)
US412026A 1973-11-01 1973-11-01 Hydrogenation of coal Expired - Lifetime US3926775A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US412026A US3926775A (en) 1973-11-01 1973-11-01 Hydrogenation of coal
CA210,971A CA1030470A (en) 1973-11-01 1974-10-08 Hydrogenation of coal
DE19742449531 DE2449531A1 (de) 1973-11-01 1974-10-17 Verfahren zum hydrieren von kohle
JP49126499A JPS5743117B2 (https=) 1973-11-01 1974-11-01

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US412026A US3926775A (en) 1973-11-01 1973-11-01 Hydrogenation of coal

Publications (1)

Publication Number Publication Date
US3926775A true US3926775A (en) 1975-12-16

Family

ID=23631268

Family Applications (1)

Application Number Title Priority Date Filing Date
US412026A Expired - Lifetime US3926775A (en) 1973-11-01 1973-11-01 Hydrogenation of coal

Country Status (4)

Country Link
US (1) US3926775A (https=)
JP (1) JPS5743117B2 (https=)
CA (1) CA1030470A (https=)
DE (1) DE2449531A1 (https=)

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4007108A (en) * 1975-06-02 1977-02-08 Arnold Marcel Leas Converting solid fuels to gaseous and liquid fuels
US4011153A (en) * 1975-04-01 1977-03-08 The United States Of America As Represented By The United States Energy Research And Development Administration Liquefaction and desulfurization of coal using synthesis gas
US4038172A (en) * 1974-10-16 1977-07-26 Agency Of Industrial Science & Technology Method for removal of oxygen from oxygen-containing compounds
US4144033A (en) * 1976-09-20 1979-03-13 Kobe Steel, Ltd. Process for manufacturing metallurgical cabonaceous materials from coals
US4206033A (en) * 1978-08-14 1980-06-03 Exxon Research & Engineering Co. CO2 Pretreatment prevents calcium carbonate formation
US4226698A (en) * 1978-08-04 1980-10-07 Schroeder Wilburn C Ash removal and synthesis gas generation from heavy oils produced by coal hydrogenation
US4266083A (en) * 1979-06-08 1981-05-05 The Rust Engineering Company Biomass liquefaction process
US4331530A (en) * 1978-02-27 1982-05-25 Occidental Research Corporation Process for the conversion of coal
DE3114766A1 (de) * 1980-04-15 1982-06-16 Rollan Dr. 89316 Eureka Nev. Swanson Verfahren zum umwandeln von kohle oder torf in gasfoermige kohlenwasserstoffe oder fluechtige destillate oder gemische hiervon
US4366045A (en) * 1980-01-22 1982-12-28 Rollan Swanson Process for conversion of coal to gaseous hydrocarbons
US4468316A (en) * 1983-03-03 1984-08-28 Chemroll Enterprises, Inc. Hydrogenation of asphaltenes and the like
US4578175A (en) * 1984-04-02 1986-03-25 Conoco Inc. Combined process for coal pyrolysis and char gasification
US4597851A (en) * 1983-06-24 1986-07-01 Ruhrkohle Aktiengesellschaft Process for the utilization of waste waters in the hydrogenation of coal
US4636300A (en) * 1984-09-13 1987-01-13 Ruhrkohle Aktiengesellschaft Integrated gas-phase hydrogenation process using heat recovered from sump-phase hydrogenation for temperature regulation
US4661237A (en) * 1982-03-29 1987-04-28 Asahi Kasei Kogyo Kabushiki Kaisha Process for thermal cracking of carbonaceous substances which increases gasoline fraction and light oil conversions
US4696735A (en) * 1984-10-20 1987-09-29 Ruhrkohle Aktiengesellschaft Method and apparatus for multiphase coal hydrogenation reactors with exothermal heat of reaction having gas cooling in sump-phase reactors
US6558441B1 (en) 1999-08-19 2003-05-06 Agency Of Industrial Science And Technology Process of upgrading low rank coal
US20070227069A1 (en) * 2002-02-05 2007-10-04 The Regents Of The University Of California Production of synthetic transportation fuels from carbonaceous materials using self-sustained hydro-gasification
US20080021122A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification
US20080021121A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US20090221721A1 (en) * 2002-02-05 2009-09-03 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US8349288B2 (en) 2006-12-06 2013-01-08 The Regents Of The University Of California Process for enhancing the operability of hot gas cleanup for the production of synthesis gas from steam-hydrogasification producer gas

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5936191A (ja) * 1982-08-24 1984-02-28 Asahi Chem Ind Co Ltd 炭素質物質の処理方法
JPS59124990A (ja) * 1983-01-04 1984-07-19 Asahi Chem Ind Co Ltd 石炭の水添熱分解法
JP2009035946A (ja) * 2007-08-02 2009-02-19 Taisei Corp 柱状構造物の動揺防止構造、柱状構造物の設置システム及び柱状構造物の設置方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2840462A (en) * 1955-05-12 1958-06-24 Consolidation Coal Co Production of high btu-content gas from carbonaceous solid fuels
US3194644A (en) * 1965-07-13 Production of pipeline gas from
US3527691A (en) * 1968-12-31 1970-09-08 Shell Oil Co Process for conversion of coal
US3556749A (en) * 1968-07-05 1971-01-19 Gen Electric Apparatus and method for the hydrogenation of coal
US3708269A (en) * 1970-11-12 1973-01-02 Inst Gas Technology Fossil fuel hydrogasification process for production of synthetic pipeline gas
US3755137A (en) * 1971-03-24 1973-08-28 Hydrocarbon Research Inc Multi-stage ebullated bed coal-oil hydrogenation and hydrocracking process
US3823084A (en) * 1972-06-30 1974-07-09 W Schroeder Hydrogenation of coal

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3194644A (en) * 1965-07-13 Production of pipeline gas from
US2840462A (en) * 1955-05-12 1958-06-24 Consolidation Coal Co Production of high btu-content gas from carbonaceous solid fuels
US3556749A (en) * 1968-07-05 1971-01-19 Gen Electric Apparatus and method for the hydrogenation of coal
US3527691A (en) * 1968-12-31 1970-09-08 Shell Oil Co Process for conversion of coal
US3708269A (en) * 1970-11-12 1973-01-02 Inst Gas Technology Fossil fuel hydrogasification process for production of synthetic pipeline gas
US3755137A (en) * 1971-03-24 1973-08-28 Hydrocarbon Research Inc Multi-stage ebullated bed coal-oil hydrogenation and hydrocracking process
US3823084A (en) * 1972-06-30 1974-07-09 W Schroeder Hydrogenation of coal

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4038172A (en) * 1974-10-16 1977-07-26 Agency Of Industrial Science & Technology Method for removal of oxygen from oxygen-containing compounds
US4011153A (en) * 1975-04-01 1977-03-08 The United States Of America As Represented By The United States Energy Research And Development Administration Liquefaction and desulfurization of coal using synthesis gas
US4007108A (en) * 1975-06-02 1977-02-08 Arnold Marcel Leas Converting solid fuels to gaseous and liquid fuels
US4144033A (en) * 1976-09-20 1979-03-13 Kobe Steel, Ltd. Process for manufacturing metallurgical cabonaceous materials from coals
US4331530A (en) * 1978-02-27 1982-05-25 Occidental Research Corporation Process for the conversion of coal
US4226698A (en) * 1978-08-04 1980-10-07 Schroeder Wilburn C Ash removal and synthesis gas generation from heavy oils produced by coal hydrogenation
US4206033A (en) * 1978-08-14 1980-06-03 Exxon Research & Engineering Co. CO2 Pretreatment prevents calcium carbonate formation
US4266083A (en) * 1979-06-08 1981-05-05 The Rust Engineering Company Biomass liquefaction process
US4366045A (en) * 1980-01-22 1982-12-28 Rollan Swanson Process for conversion of coal to gaseous hydrocarbons
DE3114766A1 (de) * 1980-04-15 1982-06-16 Rollan Dr. 89316 Eureka Nev. Swanson Verfahren zum umwandeln von kohle oder torf in gasfoermige kohlenwasserstoffe oder fluechtige destillate oder gemische hiervon
US4661237A (en) * 1982-03-29 1987-04-28 Asahi Kasei Kogyo Kabushiki Kaisha Process for thermal cracking of carbonaceous substances which increases gasoline fraction and light oil conversions
US4468316A (en) * 1983-03-03 1984-08-28 Chemroll Enterprises, Inc. Hydrogenation of asphaltenes and the like
US4597851A (en) * 1983-06-24 1986-07-01 Ruhrkohle Aktiengesellschaft Process for the utilization of waste waters in the hydrogenation of coal
US4578175A (en) * 1984-04-02 1986-03-25 Conoco Inc. Combined process for coal pyrolysis and char gasification
US4636300A (en) * 1984-09-13 1987-01-13 Ruhrkohle Aktiengesellschaft Integrated gas-phase hydrogenation process using heat recovered from sump-phase hydrogenation for temperature regulation
US4696735A (en) * 1984-10-20 1987-09-29 Ruhrkohle Aktiengesellschaft Method and apparatus for multiphase coal hydrogenation reactors with exothermal heat of reaction having gas cooling in sump-phase reactors
US6558441B1 (en) 1999-08-19 2003-05-06 Agency Of Industrial Science And Technology Process of upgrading low rank coal
US20070227069A1 (en) * 2002-02-05 2007-10-04 The Regents Of The University Of California Production of synthetic transportation fuels from carbonaceous materials using self-sustained hydro-gasification
US20090221721A1 (en) * 2002-02-05 2009-09-03 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US8603430B2 (en) 2002-02-05 2013-12-10 The Regents Of The University Of California Controlling the synthesis gas composition of a steam methane reformer
US20080021122A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification
US20080021121A1 (en) * 2006-07-18 2008-01-24 Norbeck Joseph M Controlling the synthesis gas composition of a steam methane reformer
US7897649B2 (en) 2006-07-18 2011-03-01 The Regents Of The University Of California Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification
US8268026B2 (en) 2006-07-18 2012-09-18 The Regents Of The University Of California Controlling the synthesis gas composition of a steam methane reformer
US8349288B2 (en) 2006-12-06 2013-01-08 The Regents Of The University Of California Process for enhancing the operability of hot gas cleanup for the production of synthesis gas from steam-hydrogasification producer gas

Also Published As

Publication number Publication date
CA1030470A (en) 1978-05-02
JPS5075202A (https=) 1975-06-20
DE2449531A1 (de) 1975-05-07
JPS5743117B2 (https=) 1982-09-13

Similar Documents

Publication Publication Date Title
US3926775A (en) Hydrogenation of coal
JP7813790B2 (ja) 金属鉱石のバイオ還元、水素生成、及び／又は活性炭生成と統合されたバイオマス熱分解
US4211538A (en) Process for the production of an intermediate Btu gas
US4597776A (en) Hydropyrolysis process
US4118204A (en) Process for the production of an intermediate Btu gas
CA2827916C (en) Hydromethanation of a carbonaceous feedstock with nickel recovery
CA2624626C (en) Catalytic steam gasification of petroleum coke to methane
KR101440710B1 (ko) 바나듐 회수를 동반한 탄소질 공급원료의 히드로메탄화
US5021148A (en) Method of refining coal by short residence time partial liquefaction to produce petroleum substitutes and chemical feedstocks
US3944480A (en) Production of oil and high Btu gas from coal
US10106753B1 (en) Coal gasification process with conversion of CO2 to oxygen gasifier feed producing carbon by-product
WO1980001283A1 (en) Integrated coal liquefaction-gasification process
US4842615A (en) Utilization of low rank and waste coals in transportable fluidic fuel systems
US3960701A (en) Hydrogenation of coal to produce coke, pitch and electrode carbon
US5110452A (en) Method of refining coal by catalyzed short residence time hydrodisproportionation to form a novel coal-derived fuel system
US4526903A (en) Process for the production of synthesis gas from coal
US4560547A (en) Production of hydrogen from oil shale
CA1199039A (en) Hydropyrolysis process
US3954596A (en) Production of low sulfur heavy oil from coal
EP0020663A4 (en) COAL LIQUIDATION PROCESS WITH IMPROVED SLUDGE RETURN SYSTEM.
US4971683A (en) Method of refining coal by short residence time hydrodisproportionation to co-produce coal-based petroleum substitutes and methanol
US4007108A (en) Converting solid fuels to gaseous and liquid fuels
CA1124666A (en) Coal liquefaction process
Schlinger Coal gasification development and commercialization of the texaco coal gasification process
Van Heek General aspects and engineering principles for technical application of coal gasification