CA1309589C - Method of producing a clean gas containing carbon monoxide and hydrogen - Google Patents
Method of producing a clean gas containing carbon monoxide and hydrogenInfo
- Publication number
- CA1309589C CA1309589C CA000518961A CA518961A CA1309589C CA 1309589 C CA1309589 C CA 1309589C CA 000518961 A CA000518961 A CA 000518961A CA 518961 A CA518961 A CA 518961A CA 1309589 C CA1309589 C CA 1309589C
- Authority
- CA
- Canada
- Prior art keywords
- gas
- hydrocarbon
- containing carbon
- reaction chamber
- hydrogen
- 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 - Fee Related
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Carbon And Carbon Compounds (AREA)
- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
The present invention relates to a method of producing a gas containing carbon monoxide and hydrogen, permitting the use of commercially known technology and utilizing any form of starting material containing carbon and/or hydrocarbon, according to which the gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas. The gas produced from material con-taining carbon and/or hydrocarbon and oxidant is supplied to a reaction chamber simultaneously with a gas heated by plasma generator , in order to crack the hydrocarbon in the gas.
The present invention relates to a method of producing a gas containing carbon monoxide and hydrogen, permitting the use of commercially known technology and utilizing any form of starting material containing carbon and/or hydrocarbon, according to which the gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas. The gas produced from material con-taining carbon and/or hydrocarbon and oxidant is supplied to a reaction chamber simultaneously with a gas heated by plasma generator , in order to crack the hydrocarbon in the gas.
Description
The present invention relates to a method of producing a gas containing carbon monoxide and hydrogen, permitting the use of commercially known technology and utilizing any form of starting material containing carbon and/or hydrocarbon, according to which the gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas.
In processes utilizing combustion to supply energyl and in processes utilizing starting materials other than dried coke, such as bituminous coal, peat and the like, a gas is obtained which contains H2O and hydrocarbon as well as CO + H2.
Normally a maximum CO2 + H2O content of about 10~ in the gas is aimed at, while at the same time the content of heavy hydrocarbons should be as close to 0~ as possible.
In traditional gasification processes using oxygen gas (air) and steam, where gas and carbonaceous material move in counter-flow, it is possible to make extremely good use of the heat but, due to the low reaction temperature, this gas will contain large amounts of tar. Furthermore, a residual product is obtained in the form of ash, which is difficult to dispose of in a manner not detrimental to the environment. Considerable advantages can be gained by increasing the reaction temperature in the combustion stage so that the ash melts, and by increasing the pro-cess pressure. The solidified slag drawn off is extremely resistant to leaching and the production per unit volume of the reactor is increased. Furthermore, the excess oxy-gen can be kept at a reasonable level for reduction pro-cesses, i.e. less of the carbon monoxide formed need becombusted to CO2 to cover thermal losses, for instance.
However, the problem of tar still remains, and the gas 1309~89 therefore cannot be used directly as reduction gas, for instance.
The present method permits the use of any form of starting material containing carbon and/or hydrocarbon for the gas generation, while also utilizing commercially known technology, in which the gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas.
The method according to the present invention is substantially characterised in that the gas produced from material containing carbon and/or hydrocarbon and oxidant is supplied to a supplementary reaction chamber simultaneously with a gas heated by plasma generator, in order to crack the hydrocarbon in the gas.
It has been found that by supplying a hot gas, heated by plasma generator and thus having extremely high energy density, a thermal disintegration of the hydrocarbon in the gas from the gasifier is obtained, as well as the reaction with H20, 2 and/or C02 in the gas to form H2 and C0. Due to the high energy density in the gas supplied, a comparatively small volume of gas is re~uired, which thus makes the process possible.
The gas can be produced by means of pyrolysis or partial combustion of material containing carbon and/or hydrocarbon, such as peat, pit coal, anthracite, or forest waste. If coke-oven gas derived from pyrolysis of pit coal is to be used there will be other contaminants as well as hydrocarbons. A great advantage with the invention is that these will also be cracked in the supplementary reaction chamber.
1 3 0 9 ~ 8 9 According to one embodiment of the invention, after passing the supplementary reaction chamber, the gas is conducted through a limestone or dolomite filling to remove sulphur.
The limestone or dolomite used for said sulphur purifica-tion will also act as catalyst in cracking hydrocarbon andin the reaction with oxidant. This enables the electrical energy consumption to be correspondingly lowered in the supplementary reaction chamber.
According to another embodiment of the invention the content of CO2 + H2O in the gas from the supplementary reaction cham-ber is controlled to below 5%.
Additional advantages and features of the invention will be revealed in the following detailed description with refe-rence to the accompanying drawing showing schematically the flowchart for a gas-producing process according to the pre-sent invention connected to a subsequent reduction process.
A crude gas is produced in a gasifier or coke oven desig-nated 1. The crude gas generated is supplied to a supple-mentary reaction chamber 2. At least one plasma generator 3 is arranged in conjunction with the supplementary reac-tion chamber, for the supply of a hot gas having high ener-gy density. The hydrocarbon in the crude gas is cracked in the supplementary reaction chamber and reacts to form CO + H2. Finely divided coke or H2O may be introduced through lances 4 in the supplementary reaction chamber, to adjust the hydrogen/carbon ratio.
After this the gas is subjected to sulphur purification in the shaft 5 which contains a filling 6 of limestone or do-lomite supplied through a gastight sluice arrangement 7 and consumed filling is withdrawn at the bottom of the shaft through a gastight sluice arrangement 8. Any hydrocarbons remaining in the gas are also catalytically cracked in 130~8q the limestone or dolomite filling. This can be utilized to reduce the electric energy consumed in the plasma generator 3 used for thermal disintegration of the hydrocarbon con-tent.
The gas purified in this way and containing substantially only H2 + CO and a small quantity of H2O + CO2, can then be transported to a chamber 9 to be controlled with respect to temperature and composition before entering a shaft furnace 10 for reduction of oxidic material.
The gas produced is supplied through an inlet 12 at the bottom of the shaft furnace 10 and is caused to flow in counter-flow with the material containing metal oxide. The partially consumed gas containing impurities and dust is withdrawn through an outlet 13 and cleaned in a scrubber 14.
The cleaned, partially consumed gas can then be used for other purposes, as indicated by the filter 15. If neces-sary, some of the gas can be recirculated in the process via pipes 16, 16a, 16b and may be used, for instance, in the mixing chamber 9 to control the temperature and compo-sition of the gas to be introduced into the shaft. Part ofthe recirculated gas may also be used in the plasma genera-tor in conjunction with the supplementary reaction chamber.
The invention is further illustrated by the following example.
Example 10 ton forest waste containing 30% water and the following composition C H O N S Ash 51 6,2 42 0,2 0,5 0,5 %
1303~89 is introduced at the top of a counter-flow gasifier per hour while an oxidant is introduced at the bottom of the gasifier in the form of air heated to 1000C. The air added is 3700 Nm . The composition of the top gas will be 25,8 9,8 41,1 4,8 15,8 2,9 %
At the same time a tar sample is withdrawn which indicates that the gas contains 3,2 gram tar/Nm3.
The temperature of the gas leaving is 550C and its volume is approximately 17200 Nm . The gas is now supplied to a supplementary reaction chamber and heated using air heated in plasma generators. The quantity of air required is only about 2100 Nm3. With the aid of the plasma generator the temperature of the gas entering is increased to 1250C, with a consumption of approximately 8,7 MWh electric ener-gy.
The methane and tar contents are thus removed from the heated pyrolysis gas and the gas leaving the chamber will have the following composition CO CO2 H2 H2o 2 28,6 4,8 29,6 13,6 23,4 The quantity of gas leaving will be approximately 19900 Nm .
In processes utilizing combustion to supply energyl and in processes utilizing starting materials other than dried coke, such as bituminous coal, peat and the like, a gas is obtained which contains H2O and hydrocarbon as well as CO + H2.
Normally a maximum CO2 + H2O content of about 10~ in the gas is aimed at, while at the same time the content of heavy hydrocarbons should be as close to 0~ as possible.
In traditional gasification processes using oxygen gas (air) and steam, where gas and carbonaceous material move in counter-flow, it is possible to make extremely good use of the heat but, due to the low reaction temperature, this gas will contain large amounts of tar. Furthermore, a residual product is obtained in the form of ash, which is difficult to dispose of in a manner not detrimental to the environment. Considerable advantages can be gained by increasing the reaction temperature in the combustion stage so that the ash melts, and by increasing the pro-cess pressure. The solidified slag drawn off is extremely resistant to leaching and the production per unit volume of the reactor is increased. Furthermore, the excess oxy-gen can be kept at a reasonable level for reduction pro-cesses, i.e. less of the carbon monoxide formed need becombusted to CO2 to cover thermal losses, for instance.
However, the problem of tar still remains, and the gas 1309~89 therefore cannot be used directly as reduction gas, for instance.
The present method permits the use of any form of starting material containing carbon and/or hydrocarbon for the gas generation, while also utilizing commercially known technology, in which the gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas.
The method according to the present invention is substantially characterised in that the gas produced from material containing carbon and/or hydrocarbon and oxidant is supplied to a supplementary reaction chamber simultaneously with a gas heated by plasma generator, in order to crack the hydrocarbon in the gas.
It has been found that by supplying a hot gas, heated by plasma generator and thus having extremely high energy density, a thermal disintegration of the hydrocarbon in the gas from the gasifier is obtained, as well as the reaction with H20, 2 and/or C02 in the gas to form H2 and C0. Due to the high energy density in the gas supplied, a comparatively small volume of gas is re~uired, which thus makes the process possible.
The gas can be produced by means of pyrolysis or partial combustion of material containing carbon and/or hydrocarbon, such as peat, pit coal, anthracite, or forest waste. If coke-oven gas derived from pyrolysis of pit coal is to be used there will be other contaminants as well as hydrocarbons. A great advantage with the invention is that these will also be cracked in the supplementary reaction chamber.
1 3 0 9 ~ 8 9 According to one embodiment of the invention, after passing the supplementary reaction chamber, the gas is conducted through a limestone or dolomite filling to remove sulphur.
The limestone or dolomite used for said sulphur purifica-tion will also act as catalyst in cracking hydrocarbon andin the reaction with oxidant. This enables the electrical energy consumption to be correspondingly lowered in the supplementary reaction chamber.
According to another embodiment of the invention the content of CO2 + H2O in the gas from the supplementary reaction cham-ber is controlled to below 5%.
Additional advantages and features of the invention will be revealed in the following detailed description with refe-rence to the accompanying drawing showing schematically the flowchart for a gas-producing process according to the pre-sent invention connected to a subsequent reduction process.
A crude gas is produced in a gasifier or coke oven desig-nated 1. The crude gas generated is supplied to a supple-mentary reaction chamber 2. At least one plasma generator 3 is arranged in conjunction with the supplementary reac-tion chamber, for the supply of a hot gas having high ener-gy density. The hydrocarbon in the crude gas is cracked in the supplementary reaction chamber and reacts to form CO + H2. Finely divided coke or H2O may be introduced through lances 4 in the supplementary reaction chamber, to adjust the hydrogen/carbon ratio.
After this the gas is subjected to sulphur purification in the shaft 5 which contains a filling 6 of limestone or do-lomite supplied through a gastight sluice arrangement 7 and consumed filling is withdrawn at the bottom of the shaft through a gastight sluice arrangement 8. Any hydrocarbons remaining in the gas are also catalytically cracked in 130~8q the limestone or dolomite filling. This can be utilized to reduce the electric energy consumed in the plasma generator 3 used for thermal disintegration of the hydrocarbon con-tent.
The gas purified in this way and containing substantially only H2 + CO and a small quantity of H2O + CO2, can then be transported to a chamber 9 to be controlled with respect to temperature and composition before entering a shaft furnace 10 for reduction of oxidic material.
The gas produced is supplied through an inlet 12 at the bottom of the shaft furnace 10 and is caused to flow in counter-flow with the material containing metal oxide. The partially consumed gas containing impurities and dust is withdrawn through an outlet 13 and cleaned in a scrubber 14.
The cleaned, partially consumed gas can then be used for other purposes, as indicated by the filter 15. If neces-sary, some of the gas can be recirculated in the process via pipes 16, 16a, 16b and may be used, for instance, in the mixing chamber 9 to control the temperature and compo-sition of the gas to be introduced into the shaft. Part ofthe recirculated gas may also be used in the plasma genera-tor in conjunction with the supplementary reaction chamber.
The invention is further illustrated by the following example.
Example 10 ton forest waste containing 30% water and the following composition C H O N S Ash 51 6,2 42 0,2 0,5 0,5 %
1303~89 is introduced at the top of a counter-flow gasifier per hour while an oxidant is introduced at the bottom of the gasifier in the form of air heated to 1000C. The air added is 3700 Nm . The composition of the top gas will be 25,8 9,8 41,1 4,8 15,8 2,9 %
At the same time a tar sample is withdrawn which indicates that the gas contains 3,2 gram tar/Nm3.
The temperature of the gas leaving is 550C and its volume is approximately 17200 Nm . The gas is now supplied to a supplementary reaction chamber and heated using air heated in plasma generators. The quantity of air required is only about 2100 Nm3. With the aid of the plasma generator the temperature of the gas entering is increased to 1250C, with a consumption of approximately 8,7 MWh electric ener-gy.
The methane and tar contents are thus removed from the heated pyrolysis gas and the gas leaving the chamber will have the following composition CO CO2 H2 H2o 2 28,6 4,8 29,6 13,6 23,4 The quantity of gas leaving will be approximately 19900 Nm .
Claims (4)
1. A method of producing a gas containing carbon monoxide and hydrogen, using conventional means and utilizing any form of starting material containing carbon, hydrocarbon or both, which gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas, wherein the gas produced from the material containing carbon or hydrocarbon and an oxidant are supplied to a supplementary reaction chamber simultaneously with a gas heated by a plasma generator, in order to crack the hydrocarbon in the gas.
2. A method according to claim 1, wherein after passing the supplementary reaction chamber, the gas is conducted through a limestone or dolomite filling to remove sulphur, to crack any remaining hydrocarbon, and to achieve reaction with the oxidant.
3. A method according to claim 1 or 2, wherein finely divided coke, H2O or both is injected into the supplementary reaction chamber.
4. A method according to claim 1 or 2, wherein the content of CO2 + H2O in the gas from the supplementary reaction chamber is controlled to below 5%.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE8504439-4 | 1985-09-25 | ||
| SE8504439A SE457355B (en) | 1985-09-25 | 1985-09-25 | MAKE SURE TO PREPARE A CLEAN, CARBON OXIDE AND GAS GAS INCLUDING GAS |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1309589C true CA1309589C (en) | 1992-11-03 |
Family
ID=20361519
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000518961A Expired - Fee Related CA1309589C (en) | 1985-09-25 | 1986-09-24 | Method of producing a clean gas containing carbon monoxide and hydrogen |
Country Status (13)
| Country | Link |
|---|---|
| JP (1) | JP2509192B2 (en) |
| AT (1) | AT396366B (en) |
| AU (1) | AU589997B2 (en) |
| BE (1) | BE905480A (en) |
| BR (1) | BR8701328A (en) |
| CA (1) | CA1309589C (en) |
| DE (1) | DE3631015A1 (en) |
| FI (1) | FI863726A (en) |
| FR (1) | FR2587717B1 (en) |
| GB (1) | GB2180849B (en) |
| IL (1) | IL80027A0 (en) |
| IT (1) | IT1213497B (en) |
| SE (1) | SE457355B (en) |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE8605211L (en) * | 1986-12-04 | 1988-06-05 | Skf Steel Eng Ab | SET TO MAKE A GAS EMERGENCY FOR ENERGY PRODUCTION |
| US5213587A (en) * | 1987-10-02 | 1993-05-25 | Studsvik Ab | Refining of raw gas |
| SE459584B (en) * | 1987-10-02 | 1989-07-17 | Studsvik Ab | PROCEDURES FOR PROCESSING OF RAAGAS MANUFACTURED FROM COAL CONTENTS |
| US4880439A (en) * | 1988-05-05 | 1989-11-14 | Texaco Inc. | High temperature desulfurization of synthesis gas |
| NO174471C (en) * | 1991-12-12 | 1994-05-11 | Kvaerner Eng | Method of preventing and removing fouling by pyrolytic cleavage of hydrocarbons |
| FI96321C (en) * | 1993-06-11 | 1996-06-10 | Enviropower Oy | Method and reactor for treating process gas |
| NL1001555C2 (en) * | 1995-10-27 | 1997-05-02 | Biomass Technology Group B V | Catalytically producing combustible gases, e.g., for generating energy |
| DE69613811D1 (en) * | 1996-04-09 | 2001-08-16 | Ansaldo Ricerche S R L | Method and system for the production and use of fuel gases, in particular gases made from biomass and waste |
| CN101233215B (en) * | 2005-06-03 | 2013-05-15 | 普拉斯科能源Ip控股公司毕尔巴鄂-沙夫豪森分公司 | A system for the conversion of carbonaceous feedstocks to a gas of a specified composition |
| DE102008049579A1 (en) * | 2008-09-30 | 2010-04-01 | Uhde Gmbh | Hot gas cleaning |
| KR101570882B1 (en) * | 2009-08-04 | 2015-11-23 | 에스케이이노베이션 주식회사 | Method for gasification of carbon containing material comprising methane decomposition and conversion of carbon dioxide |
| US9611437B2 (en) * | 2010-01-12 | 2017-04-04 | Lummus Technology Inc. | Producing low methane syngas from a two-stage gasifier |
| RO126941B1 (en) * | 2011-05-03 | 2013-12-30 | Costin-Marian Frâncu | Process and installation for thermally plasma treating a gaseous mixture |
| CA2966243A1 (en) | 2014-10-31 | 2016-05-06 | Deutsche Lufthansa Ag | Method and plant for the production of synthesis gas |
| CN104629779A (en) * | 2014-12-12 | 2015-05-20 | 中山大学 | Process for producing synthetic gas from urban garbage by virtue of combination of pyrolysis and plasma |
| WO2023155975A1 (en) | 2022-02-15 | 2023-08-24 | Universität Stuttgart | Process and device for obtaining carbon monoxide from atmospheric carbon dioxide, using a solid-plasma reactor |
| WO2023155974A1 (en) | 2022-02-15 | 2023-08-24 | Universität Stuttgart | Solid plasma reactor and method of operating a fixed bed reactor |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR948266A (en) * | 1946-06-24 | 1949-07-27 | Nat Smelting Co Ltd | Process for removing sulfur compounds from gases |
| US2701757A (en) * | 1946-12-17 | 1955-02-08 | Texaco Development Corp | Process of making synthesis gas |
| SE371453C (en) * | 1973-03-26 | 1978-01-23 | Skf Ind Trading & Dev | KIT FOR PRODUCTION OF REDUCTION GAS |
| GB1475731A (en) * | 1973-03-26 | 1977-06-01 | Skf Ind Trading & Dev | Method of producing reduction gas |
| BE814899A (en) * | 1974-05-10 | 1974-11-12 | PROCESS FOR MANUFACTURING HOT REDUCING GAS. | |
| BE815963A (en) * | 1974-06-05 | 1974-09-30 | HOT REDUCING GAS MANUFACTURING PROCESS. | |
| US4123502A (en) * | 1975-02-06 | 1978-10-31 | Heinz Holter | Process for the purification of gas generated in the pressure gasification of coal |
| DE2532197C3 (en) * | 1975-07-18 | 1980-05-22 | Metallgesellschaft Ag, 6000 Frankfurt | Process for the production of synthesis gases |
| DE2638348A1 (en) * | 1976-08-26 | 1978-07-13 | Didier Eng | PROCESS FOR PROCESSING COOKING GAS |
| IT1101408B (en) * | 1977-11-15 | 1985-09-28 | Babcock Krauss Maffei Ind | PROCEDURE FOR THE WASTE PYROLYSIS |
| NL8302281A (en) * | 1983-06-28 | 1985-01-16 | Shell Int Research | PROCESS FOR PREPARING A CARBON MONOXIDE AND HYDROGEN-CONTAINING GAS. |
| CA1228482A (en) * | 1983-11-29 | 1987-10-27 | Jan C. De Waal | Reduction of metal compounds |
| FR2559776B1 (en) * | 1984-02-16 | 1987-07-17 | Creusot Loire | SYNTHESIS GAS PRODUCTION PROCESS |
| SE453920B (en) * | 1985-03-01 | 1988-03-14 | Skf Steel Eng Ab | SET AND DEVICE FOR GASING OF FOSSIL FUEL AND REFORM OF GAS FUEL |
-
1985
- 1985-09-25 SE SE8504439A patent/SE457355B/en not_active IP Right Cessation
-
1986
- 1986-09-11 AU AU62582/86A patent/AU589997B2/en not_active Ceased
- 1986-09-12 DE DE19863631015 patent/DE3631015A1/en active Granted
- 1986-09-15 FI FI863726A patent/FI863726A/en not_active Application Discontinuation
- 1986-09-15 IL IL80027A patent/IL80027A0/en unknown
- 1986-09-23 IT IT8621793A patent/IT1213497B/en active
- 1986-09-23 GB GB8622866A patent/GB2180849B/en not_active Expired
- 1986-09-24 AT AT0256086A patent/AT396366B/en not_active IP Right Cessation
- 1986-09-24 CA CA000518961A patent/CA1309589C/en not_active Expired - Fee Related
- 1986-09-24 JP JP61223929A patent/JP2509192B2/en not_active Expired - Lifetime
- 1986-09-24 BE BE0/217201A patent/BE905480A/en not_active IP Right Cessation
- 1986-09-24 FR FR868613342A patent/FR2587717B1/en not_active Expired - Fee Related
-
1987
- 1987-03-24 BR BR8701328A patent/BR8701328A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| SE457355B (en) | 1988-12-19 |
| AU589997B2 (en) | 1989-10-26 |
| FR2587717B1 (en) | 1990-03-02 |
| GB2180849A (en) | 1987-04-08 |
| GB8622866D0 (en) | 1986-10-29 |
| AT396366B (en) | 1993-08-25 |
| FR2587717A1 (en) | 1987-03-27 |
| ATA256086A (en) | 1992-12-15 |
| DE3631015C2 (en) | 1988-10-06 |
| IT1213497B (en) | 1989-12-20 |
| JPS6274993A (en) | 1987-04-06 |
| JP2509192B2 (en) | 1996-06-19 |
| FI863726A0 (en) | 1986-09-15 |
| SE8504439L (en) | 1987-03-26 |
| SE8504439D0 (en) | 1985-09-25 |
| AU6258286A (en) | 1987-03-26 |
| IT8621793A0 (en) | 1986-09-23 |
| IL80027A0 (en) | 1986-12-31 |
| GB2180849B (en) | 1989-12-28 |
| FI863726A (en) | 1987-03-26 |
| DE3631015A1 (en) | 1987-04-16 |
| BR8701328A (en) | 1988-09-27 |
| BE905480A (en) | 1987-01-16 |
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