GB2086389A - Installation for producing methanol - Google Patents
Installation for producing methanol Download PDFInfo
- Publication number
- GB2086389A GB2086389A GB8132172A GB8132172A GB2086389A GB 2086389 A GB2086389 A GB 2086389A GB 8132172 A GB8132172 A GB 8132172A GB 8132172 A GB8132172 A GB 8132172A GB 2086389 A GB2086389 A GB 2086389A
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- GB
- United Kingdom
- Prior art keywords
- methane
- methanol
- installation
- gas
- produced
- 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.)
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1512—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by reaction conditions
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0966—Hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1665—Conversion of synthesis gas to chemicals to alcohols, e.g. methanol or ethanol
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The installation has both a hydrogenating coal-gasifier (1) and a methane-decomposition furnace (6), the latter preferably being heated by a high temperature nuclear reactor (25). The two gas mixtures obtained from the gasifier (1) and the furnace (6) are freed of carbon dioxide, and, when mixed, are supplied to a methanol- synthesis reactor (11). The methanol produced is separated in a separator (13) from the gas, and the latter is separated in a low temperature separation process (14) into its components. The hydrogen flows back to the gasifier (1) and the methane to the furnace (6), whilst the nitrogen is removed and the carbon monoxide is conveyed back to the reactor (11). By integration, the amount of hydrogen conveyed in the installation is greatly reduced, which leads to savings in piping, pumps, etc. The heating fluid emerging from the furnace (6) can be used to heat a steam producer (19) in the lower temperature range, with which vapour a turbo-generator (20, 21) is driven. Leakage steam is supplied to the furnace (6) from the turbine (20).
Description
SPECIFICATION
Installation for producing methanol
The present invention relates to an installation for the production of methanol from gasified coal, in particular using nuclear energy.
Methanol will in the future be of greater importance both directly as a motor fuel and also as an
intermediate product for the production of petroleum from coal. For the production of methanol from
coal there are used coal gasification processes which produce so-called synthesis gas. Such a synthesis
gas consists for the major part of hydrogen and carbon monoxide, and also contains small amounts of
carbon dioxide. Synthesis gas can be produced by reaction of methane, produced in a hydrogenating
coal-gasification process, with water vapour in a heated methane-decomposition furnace at very high
temperatures.
In German Offenlegungschrift No. 2,837,988 there is described an installation for the production
of synthesis gas from coal, in particular by using nuclear energy.
In the German magazine "Kerntechnik", (1975), No.4, pages 181-187, a coal-gasification
process using heat from high temperature nuclear reactors is described. In the book "Chemierohstoffe
aus Kohle", Jurgen Falbe, 1 977, Georg-Thieme-Verlag, Stuttgart, pages 300-322, information is given
on the latest state of methanol production from synthesis gas. From Figure 1 57 on page 306, it can be seen that a large part of the hydrogen used must be conveyed practically in a circuit from the methanol separator to a methanol-synthesis reactor via a gas circuit and a compressor. In the above-described hydrogenating coal-gasification process also, an excess amount of hydrogen is necessary so that a large
amount of hydrogen flow is conveyed practically in the circuit.These hydrogen circuits involve
considerable expenditure on piping and compressors.
According to the present invention there is provided an installation for producing methanol,
comprising a hydrogenating coal-gasifier for producing a methane-containing gas; a methanedecomposition furnace for producing a synthesis gas; a methanol-synthesis reactor for producing a methanol-containing gas from said methane-containing gas and said synthesis gas; means for feeding said methane-containing gas and said synthesis gas to said methanol-synthesis reactor; means for removing methanol'from said methanol-containing gas; means for subjecting said methanol-containing gas, after said removal of methanol therefrom, to ä low temperature gas separation process to produce methane, hydrogen and carbon monoxide; means for passing said methane to said methanedecomposition furnace; means for passing said hydrogen to said hydrogenating coal-gasifier; and means for passing said carbon monoxide to said methanol-synthesis reactor
The installation may include means for cooling the methane-containing gas produced in the coalgasifier, and/or means for removing carbon dioxide and hydrogen sulphide from the methane-containing gas produced in the coal-gasifier, and/or means for removing dust and water from the methanecontaining gas produced in the coal-gasifier. Preferably, the means for cooling the methane-containing gas is a heat exchanger in which in use the methane-containing gas undergoes heat exchange with the hydrogen produced by the low temperature gas separation process and passed to the coal-gasifier.
The installation may include means for cooling the synthesis gas produced in the methanedecomposition furnace, and/or means for removing carbon dioxide from the synthesis gas produced in the methane-decomposition furnace, and/or means for compressing the synthesis gas produced in the methane-decomposition furnace. In this case, the installation may include means for compressing at least part of the carbon dioxide removed from the synthesis gas and for returning it to the methanedecomposition furnace.
The installation may include means for cooling the methanol-containing gas produced in the
methanol-synthesis reactor.
The installation may include means for compressing the methane produced by the low temperature gas separation process, and/or means for compressing the hydrogen produced by the low temperature gas separation process, and/or means for compressing the carbon monoxide produced by the low temperature gas separation process.
The installation is preferably in association with a nuclear reactor having a coolant circuit which is adapted to heat the methane-decomposition furnace.
The installation according to the invention is one in which a methanol-synthesis installation is integrated with a coal-gasification installation, whereby the amount of hydrogen conveyed in the installation as a whole is altogether considerably smaller, so that the corresponding pipelines and compressors can be produced with considerably less expense. The coal used is gasified in a
hydrogenating manner by means of hydrogen, and the crude gas produced, preferably after cooling and separation of carbon dioxide and hydrogen sulphide, is mixed with the synthesis gas produced in a
methane-decomposition furnace. This mixture is supplied to a methanol-synthesis reactor and
preferably over 90% thereof is converted to methanol in a single throughflow.The gas mixture obtained
upon condensation and separation of methanol, which mixture contains a high amount of hydrogen, an amount of methane and a small amount of unreacted carbon monoxide, is separated into these three
components by a low temperature gas separation process. The methane is passed, with water vapour, to the methane-decomposition furnace, the hydrogen is passed to the coal-gasifier and the carbon monoxide is passed to the methanol-synthesis reactor. The heat necessary for the decomposition of the methane is preferably obtained from a nuclear reactor or from the coke produced in the coal-gasifier. In use of the installation, there is obtained upon effecting methanol synthesis, a very high proportion of hydrogen to carbon monoxide, so that in a single throughflow a very large amount of methanol is produced.Whilst on page 305 of the above-mentioned book by Falbe, reference is made to a H2:CO ratio of the synthesis gas of 3.5 : 1 the present installation can be operated with a ratio or 5 1 or more.
The extent of low temperature gas separation necessary in a hydrogenating coal-gasification installation is substantially reduced in accordance with the invention in view of the fact that the coal-gasification installation is integrated with a methanol-synthesis installation. In conventional processes for methanol synthesis, no low temperature gas separation is carried out, so that the nitrogen in the installation after separation of the methanol, must be removed. This results inevitably in a loss of hydrogen and carbon monoxide, which, because of the amount of nitrogen, can no longer be used in the installation but only burned off.
The single Figure of the drawing schematically shown, by way of example, an installation of the invention. The individual parts of the installation are, as usual, designated with numerals whilst the letters in the Figure relate to Table 1 below, in which the gas compositions and conditions at the respective locations are given. Table 2 below gives the composition of the coal used and of the coke that results therefrom. Table 3 below contains data relevant to the installation.
In a hydrogenating coal-gasifier 1, coal is gasified (see Table 2) and the residual coke is drawn off.
The outgoing gas from the gasifier 1 heats the incoming gas in a heat exchanger 2. In a heat exchanger 3, the outgoing gas is cooled, in a device 4 it is freed of dust and water, and in a device 5 it is freed of carbon dioxide and hydrogen sulphide. In a methane-decomposition furnace 6, a mixture of methane, water vapour and carbon dioxide is decomposed to form a synthesis gas. In heat exchangers 7 and 8 the synthesis gas is cooled, in device 9 it is freed of carbon dioxide, and in a compressor 10 it is compressed. The gases from the device 5 and the compressor 10 are mixed and supplied to a methanol-synthesis reactor 11.The methanol-gas mixture obtained in the reactor 11 is cooled in a heat exchanger 12, and methanol is separated in a device 1 3. The gas mixture substantially freed of methanol is separated into carbon monoxide, hydrogen, methane and nitrogen by a low temperature gas separation process in a device 14. The carbon monoxide obtained is compressed in a compressor 1 5 and is returned to the methanol-synthesis reactor 11. The hydrogen obtained is compressed in a compressor 1 6 and is supplied via the heat exchanger 2 to the hydrogenating coal-gasifier 1 , whilst the methane obtained is compressed in a compressor 1 7 and is supplied to the methane-decomposition furnace 6. The nitrogen obtained is not further used in the installation. The carbon dioxide obtained from device 9 can be at least partially compressed in a compressor 1 8 and supplied to the methanedecomposition furnace 6. The methane-decomposition furnace 6 can be heated by the helium cooling circuit of a high temperature nuclear reactor 25. -In this case the helium from the methane decomposition furnace 6 is used for producing steam in a heat exchanger 19, and the steam is expanded in a turbine 20 driving a generator 21 and is used for the production of electricity. The steam is then partially expanded again in the same turbine and supplied in part to the methane-decomposition furnace 6. The steam circuit also includes a condenser 22 and a feed pump 23, whilst the helium circuit includes a compressor 24.
TABLE 1
Gas composition in mN/s Pressure Temp.
Location H2 CO CO2 CH4 C2H5 H2S N2 H2O Total bar C A 173.3 8.2 0.7 75.7 2.3 0.8 1.1 10.2 272.2 80 900 B 173.3 8.2 - 75.7 2.3 - 1.1 0.9 261.5 77 65 C 261.5 67.8 96.9 58.1 - - - 371.8 856.0 39 363 D 261.5 67.8 - 58.1 - - - 1.3 388.6 77 151 E - 5.7 - - - - - - 5.7 1.5 20 F 278.3 - - - - - - - 278.3 73.5 20 G - - - 133.8 2.3 - - - 136.1 1.7 20 H 173.3 13.9 - 75.7 2.3 - 1.1 0.9 267.2 77 69 J 434.7 81.7 - 133.8 2.3 - 1.1 2.1 655.8 77 117 K 278.3 5.7 - 133.8 2.3 - 1.1 0.1 421.3 78 5 L - - - - - - 1.1 - 1.1 1.5 20 M - - 96.9 - - - - 3.3 100.2 1.7 35 N - - 82.2 - - - - 2.8 85.0 45 250 O - - 14.6 - - - - 0.5 15.1 1.7 35 P - - 0.7 - - 0.8 - 0.1 1.5 1.7 35 Q - - 82.2 133.8 2.3 - - 468.0 686.3 45 281 TABLE 2
Composition (%) C H O N S H2O ash German gas flame coal 75.3 4.6 6.5 1.5 1.1 6.7 4.3 Residual coke 86.39 0.97 0.51 0.76 0.41 - 10.96 TABLE 3
Nuclear reactor Thermal efficiency 3000 MW Helium discharge temperature (core) 900C Helium discharge temperature (furnace 6) 700 C Helium entry temperature (core) 250'C Overall flow production 602.8 MW Flow requirement for entire installation 530.8 MW Flow yield to outside 72 MW Coal gasification Coal consumption (Ho = 29977 KJ/Kg) 415.7 t/h Residual coke production (Ho = 26052 KJ/Kg) 163.1 t/h Synthesis gas (H2:CO= 2.06: 1) (converted in methanol synethesis) 837 x 1o3mn3t/h Methanol production 1 391.0 t/h
Claims (9)
1. An installation for producing methanol, comprising a hydrogenating coal-gasifier for producing a methane-containing gas; a methane-decomposition furnace for producing a synthesis gas; a methanol-synthesis reactor for producing a methanol-containing gas from said methane-containing gas and said synthesis gas; means for feeding said methane-containing gas and said synthesis gas to said methanol-synthesis reactor; means for removing methanol from said methanol-containing gas; means for subjecting said methanol-containing gas, after said removal of methanol therefrom, to a low temperature gas separation process to produce methane, hydrogen and carbon monoxide; means for passing said methane to said methane-decomposition furnace; means for passing said hydrogen to said hydrogenating coal-gasifier; and means for passing said carbon monoxide to said methanol-synthesis reactor.
2. An installation-as claimed in claim 1, including means for cooling the methane-containing gas produced in the coal-gasifier, and/or means for removing carbon dioxide and hydrogen sulphide from the methane-containing gas produced in the coal-gasifier, and/or means for removing dust and water from the methane-containing gas produced in the coal-gasifier.
3. An installation as claimed in claim 2, wherein the means for cooling the methane-containing gas is a heat exchanger in which in use the methane-containing gas undergoes heat exchange with the hydrogen produced by the low temperature gas separation process and passed to the coal-gasifier.
4. An installation as claimed in claim 1,2 or 3, including means for cooling the synthesis gas produced in the methane-decomposition furnace, and/or means for removing carbon dioxide from the synthesis gas produced in the methane-decomposition furnace, and/or means for compressing the synthesis gas produced in the methane-decomposition furnace.
5. An installation as claimed in claim 4, inculding means for compressing at least part of the carbon dioxide removed from the synthesis gas and for returning it to the methane-decomposition furnace.
6. An installation as claimed in any of claims 1 to 5, including means for cooling the methanolcontaining gas produced in the methanol-synthesis reactor.
7. An installation as claimed in any of claims 1 to 6, including means for compressing the methane produced by the low temperature gas separation process, and/or means for compressing the hydrogen produced by the low temperature gas separation process, and/or means for compressing the carbon monoxide produced by the low temperature gas separation process.
8. An installation as claimed in any of claims 1 to 7, in association with a nuclear reactor having a coolant circuit which is adapted to heat the methane-decomposition furnace.
9. An installation as claimed in claim 8, substantially as herinbefore described with reference to, and as shown in, the accompanying drawing.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3041054A DE3041054C2 (en) | 1980-10-31 | 1980-10-31 | Process for producing methanol from gasified coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2086389A true GB2086389A (en) | 1982-05-12 |
| GB2086389B GB2086389B (en) | 1984-06-13 |
Family
ID=6115650
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8132172A Expired GB2086389B (en) | 1980-10-31 | 1981-10-26 | Installation for producing methanol |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JPS57106629A (en) |
| AU (1) | AU541196B2 (en) |
| DE (1) | DE3041054C2 (en) |
| FR (1) | FR2493308A1 (en) |
| GB (1) | GB2086389B (en) |
| ZA (1) | ZA817535B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0159610A1 (en) * | 1984-04-21 | 1985-10-30 | Siemens Aktiengesellschaft | Gas turbines and steam power plant with integrated coal gasification |
| WO1991005734A1 (en) * | 1989-10-20 | 1991-05-02 | Grohse Edward W | Process for the conversion of carbonaceous feedstocks to particulate carbon and methanol |
| EP0497226A2 (en) * | 1991-01-29 | 1992-08-05 | Mitsubishi Jukogyo Kabushiki Kaisha | Method for producing methanol by use of nuclear heat and power generating plant |
| US5427762A (en) * | 1987-05-27 | 1995-06-27 | Hydrocarb Corporation | Process for the conversion of carbonaceous feedstocks to particulate carbon and methanol |
| CN101191084B (en) * | 2007-11-16 | 2010-12-08 | 清华大学 | Multi-coproduction energy method and system by using coal gasification heat with methane reforming manner |
| CN103524299A (en) * | 2012-07-06 | 2014-01-22 | 杭州林达化工技术工程有限公司 | Synthesized methanol and synthesized methane co-production method and equipment |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4618732A (en) * | 1985-05-20 | 1986-10-21 | Gesser Hyman D | Direct conversion of natural gas to methanol by controlled oxidation |
| JP2007254306A (en) * | 2006-03-20 | 2007-10-04 | Mitsubishi Heavy Ind Ltd | Methanol synthesis installation and method |
| US20130237618A1 (en) * | 2010-11-19 | 2013-09-12 | Mitsui Chemicals, Inc. | Process for producing methanol |
| JP2012201610A (en) * | 2011-03-24 | 2012-10-22 | Hiroshima Univ | Method for producing alcohol and apparatus therefor |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE964234C (en) * | 1951-10-12 | 1957-05-23 | Metallgesellschaft Ag | Process for increasing the yield of hydrocarbons or oxygen-containing hydrocarbons in carbohydrate hydrogenation |
| FR1203696A (en) * | 1957-03-27 | 1960-01-20 | Ici Ltd | Improvements in the manufacture of unsaturated hydrocarbons and methanol |
| CH566677A5 (en) * | 1972-11-17 | 1975-09-15 | Blaupunkt Werke Gmbh | |
| DE2603204C2 (en) * | 1976-01-29 | 1982-12-02 | Metallgesellschaft Ag, 6000 Frankfurt | Process for the production of methanol |
| DE2837988A1 (en) * | 1978-08-31 | 1980-03-13 | Ght Hochtemperaturreak Tech | COAL GASIFICATION |
-
1980
- 1980-10-31 DE DE3041054A patent/DE3041054C2/en not_active Expired
-
1981
- 1981-10-26 GB GB8132172A patent/GB2086389B/en not_active Expired
- 1981-10-28 FR FR8120265A patent/FR2493308A1/en active Granted
- 1981-10-30 JP JP56174392A patent/JPS57106629A/en active Granted
- 1981-10-30 ZA ZA817535A patent/ZA817535B/en unknown
- 1981-10-30 AU AU77000/81A patent/AU541196B2/en not_active Ceased
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0159610A1 (en) * | 1984-04-21 | 1985-10-30 | Siemens Aktiengesellschaft | Gas turbines and steam power plant with integrated coal gasification |
| US5427762A (en) * | 1987-05-27 | 1995-06-27 | Hydrocarb Corporation | Process for the conversion of carbonaceous feedstocks to particulate carbon and methanol |
| WO1991005734A1 (en) * | 1989-10-20 | 1991-05-02 | Grohse Edward W | Process for the conversion of carbonaceous feedstocks to particulate carbon and methanol |
| EP0497226A2 (en) * | 1991-01-29 | 1992-08-05 | Mitsubishi Jukogyo Kabushiki Kaisha | Method for producing methanol by use of nuclear heat and power generating plant |
| EP0497226A3 (en) * | 1991-01-29 | 1994-12-28 | Mitsubishi Heavy Ind Ltd | |
| US5479462A (en) * | 1991-01-29 | 1995-12-26 | Mitsubishi Jukogyo Kabushiki Kaisha | Method for producing methanol by use of nuclear heat and power generating plant |
| CN101191084B (en) * | 2007-11-16 | 2010-12-08 | 清华大学 | Multi-coproduction energy method and system by using coal gasification heat with methane reforming manner |
| CN103524299A (en) * | 2012-07-06 | 2014-01-22 | 杭州林达化工技术工程有限公司 | Synthesized methanol and synthesized methane co-production method and equipment |
| CN103524299B (en) * | 2012-07-06 | 2017-08-25 | 杭州林达化工技术工程有限公司 | A kind of synthesizing methanol and synthesizing methane cogeneration facility |
Also Published As
| Publication number | Publication date |
|---|---|
| ZA817535B (en) | 1982-10-27 |
| FR2493308B1 (en) | 1985-01-11 |
| DE3041054C2 (en) | 1987-04-02 |
| JPH0250888B2 (en) | 1990-11-05 |
| AU7700081A (en) | 1982-05-06 |
| JPS57106629A (en) | 1982-07-02 |
| AU541196B2 (en) | 1984-12-20 |
| GB2086389B (en) | 1984-06-13 |
| FR2493308A1 (en) | 1982-05-07 |
| DE3041054A1 (en) | 1982-06-09 |
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Effective date: 19941026 |