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CA1050271A - Process for the production of hydrogen and carbon monoxide-containing gas - Google Patents

Process for the production of hydrogen and carbon monoxide-containing gas

Info

Publication number
CA1050271A
CA1050271A CA217,858A CA217858A CA1050271A CA 1050271 A CA1050271 A CA 1050271A CA 217858 A CA217858 A CA 217858A CA 1050271 A CA1050271 A CA 1050271A
Authority
CA
Canada
Prior art keywords
reaction zone
fuel
range
residence time
seconds
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
Application number
CA217,858A
Other languages
French (fr)
Other versions
CA217858S (en
Inventor
Pieter Buiter
Maarten J. Van Der Burgt
Henricus J.A. Van Helden
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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 Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Application granted granted Critical
Publication of CA1050271A publication Critical patent/CA1050271A/en
Expired legal-status Critical Current

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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
    • C01B3/34—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 by reaction of hydrocarbons with gasifying agents
    • C01B3/36—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 by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0969—Carbon dioxide
    • 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
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1253—Heating the gasifier by injecting hot 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
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

A B S T R A C T

A process for the production of a hydrogen and carbon monoxide-containing gas from a carbonaceous fuel which comprises reacting diluted oxygen with the carbon-aceous fuel in a first reaction zone which is kept at a relatively high average temperature and introducing the effluent of the first reaction zone into a second re-action zone, the average temperature of which is sub-stantially lower than that of the first reaction zone.

Description

The invention relates to the production of hydrogen and carbon monoxide-containing gas from carbonaceous fuels.
It has been proposed to produce hydrogen and carbon monoxide-containing gas by causing a finely dispersed carbonaceous fuel to react with oxygen diluted with nitrogen and/or steam in a single stage. The high tem-peratures required for such a process result in a high oxygen consumption which leads to a relatively low yield of C0 and H2.
It has now been found that the yield of C0 and H2 can be in-creased by carrying out the process in two stages.
The invention therefore relates to a process for the production of a hydrogen and carbon monoxide-containing gas from a carbonaceous fuel which comprises reacting diluted oxygen with the carbonaceous fuel in a first -reaction zone which is kept at an average temperature in the range of from 1200 to 1700C and introducing the effluent of the first reaction zone into -a second reaction zone, the average temperature of which is at least 100C
lower than that of the first reaction zone.
As a feedstock for the present process any carbonaceous fuel can be used. In this specification by a carbonaceous fuel is meant any combustible material consisting of a substantial part of carbon. The fuel may contain oxygen, sulphur and/or nitrogen. Such a feedstock includes, e.g., lignite, anthracite, bituminous coal, coke, shale oil,mineral oils or oil fractions, tar sand oil or natural gas. The feedstock, if solid, should be in a powdered form so that it can readily react with oxygen in the first : :~

:

.
.
'
- 2 -..A.., ~ . . .

lOS0271 reaction zone. Preferably, the size of solid carbonaceous fuel has been reduced such that 70% of the fuel has a particle size smaller than 200 mesh.
The oxidant includes air and oxygen diluted with steam, carbon dioxide, nitrogen and/or argon. Advantageously, the oxidant is preheated before it is reacted with the carbonaceous fuel. The preheating of the oxidant is ~uitably carried out indirectly by heat exchange with any heat source, e.g., the hot product gas obtained in the present process. The oxidant is preferably preheated to ~`
a temperature in the range of from 200 to 1300C, depending on the type oxidant. After the preheating the hot oxidant is advantageously mixed with carbonaceous fuel and the oxidant/fuel mixture is introduced, preferably as a jet, into the fir~t reaction zone. In one embodiment of the ~l~ present process the amount of fuel to be introduced in the first reaction stage is preferably 50 to 95% of the . , j.
total amountjof fuel to be gasified and the remainder of ~3~ the fuel is introduced either in the first stage effluent or directly into the second reaction zone.
In another embodiment the total amount of fuel is introduced into the first reaction zone and the residence ; t1me is chosen such that the fuel is only partly converted to the desired product, the conversion to the desired ~25 `product being substantially completed in the second reaction zone.

. ,, . ~
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The first reaction zone preferably consists of a void steel vessel, the inside of which has been lined with refractory material.
The partial combustion in the first reaction zone is carried out at a temperature in the range of from 1200 to 1700C, which temperature ~ -results from the reaction of the carbonaceous fuel with the oxidant.
The pressure maintained in the first reaction zone may vary within wide limits and is advantageously kept in the range of from 1 to 200 kg/cm2 absolute. -In a preferred embodiment the mixture of oxidant and carbo- ~
naceous fuel is introduced into the first reaction zone at a high velocity, ;-~ -- A suitable linear introduction velocity is in the range of from 10 to 200 m/
sec.
In order to convert all the carbonaceous fuel which is intro- f duced int~ the first reaction zone into a product gas the solid particles should remain during a certain residence time therein. It has been found , that the residence time of the reactants is advantageously chosen in the -~ range of from 0.02 to 20 seconds. The residence time is relatively short ~ll (preferably 0.02 - 3 seconds) in case the total fuel to be gasified is in- -troduced into the first reaction zone. The residence time is relatively long (preferably 0.5 - 20 seconds) if only part of the fuel to be gasified is introduced into the first reaction zone.

,~: - ~ .

' 1 :
. , ~ 4 -A''' ... . ~ . . .. ~ ..... ~ ` . ` . . ....... .i . ... . . .
... .... . .. .. .... .... . . .. . . ...... . .. . .
~. ... . .... .. . .. . . ~ .. .

105027~
After at least a substantial part of the carbonaceous material has been converted to gas, the reaction product, mainly consisting of H2, C0, N2, C02 and H20 is withdrawn from the first reaction zone and introduced into the second reaction zone. In case only part of the carbonaceous `
material to be gasified is introduced into the first reaction zone, the remaining part of the carbonaceous material is introduced, preferably to-gether with steam, nitrogen and/or C02, into the effluent of the first reac-tion zone and/or the second reaction zone. The amount of fuel to be intro-tuced into the ~i~st seaction zone effluent is prefe~a~ly S to ~0% of the total amount of fuel to be gasified to hydrogen and carbon monoxide. The amount of steam, nitrogen and/or C02 which is introduced together with the remaining part of the fuel into the first reaction zone effluent is prefer- -ably in the range of from 1/10 to 2 Nm3 per kg fuel. This diluent gas ad-vantageously has a pressure in the range of from 2 to 210 kg/cm absolute and a temperature in the range of from 100 to 700C. The mixture of first reac-tion zone effluent and optionally of the remaining part of the fuel, together ' with steam, C02 and/or N2, is then passed to a second reaction zone where , carbonaceous material is substantially completely converted with the C02 ,l and/or the steam into carbon monoxide and hydrogen. This conversion is car-ried out at-a temperature which is at least 100C lower than that of the f:
first stage and is in the range of from 600 to 1400C. The pressure may be ~ atmospheric f~
f`~
'': ~

f~`:

_ 5 _ ~T
:
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.., . .. . . . . . .

~050271 ` ~ :

or superatmospheric, pressures up to 200 kg/cm2 absolute being suitable.
This second reaction zone preferably consists of a void steel vessel, the inner walls of which are lined with refractory material. The capacity of the second re-action zone should be great enough to provide a residence time for the reactants which is sufficiently long to convert the remaining part of the fuel substantially completely into gaseous components. This residence time is preferably ~;
in the range of from 0.5 to 40 seconds.
After the conversion has been terminated, the ultimate gaseous reaction product is withdrawn from the second re- --action zone. This reaction product has a temperature in the range of from 600 to 1400C. The dry gaseous reaction ~:
product has the following composition:
' . ' % vol.

, C2 0.01 - 20 CH4 0.01 - 20 ~, f N2 A 0.1 - 75 i~ H2S 0 - 4 ~.
The invention will now be further illustrated by means of the following Example to which it is by no means restricted.

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~ -6-1 .

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~, ;

lOS~Z71 EXAMPLE
As a feedstock coal was used having the following composition:
%wt C 73.7 H 5.1 8.8 S o.9 N 1.6 ~ -~
ash 9.
This coal contained 33.8%wt volatile components and 2.6~wt water; It was ground to a powder, 70% of which could pass a sieve of 200 mesh.
1028 kg of the coal were mixed with 858 kg of an oxidizing gas containing 98.9%wt 2 and 91 kg steam having a te~perature of 300C.
The coal/gas suspension was introduced at a linear velocity of 65 m/sec. in a first reaction zone.
; The reaction temperature in the first reaction zone was 1500C and the pressure was 40 kg/cm2 absolute.
The residence time of the reactants in the first reaction zone was 4 seconds.
.~ .
- After the coal had been converted, the reaction product was withdrawn from the first reaction zone and introduced into a second reaction zone together with 116 kg of the above-mentioned coal and 135 kg steam having a pressure of 50 kg/cm2 absolute and a temperature of 300C.

' .

.... . . ... .

~OSQ271 ~

In the second reaction zone the reaction product of the first reaction zone reacted with the coal and the steam. ;
The reaction conditions were: ;
tcmperaturc 1100C
pressure 39 kg/cm2 residence time 6 seconds After drying the ultimate product gas mixture had the following composition: .
%vol.
C0 62.5 :~
H2 33.8 -.
C2 1.2 N2 + A 0.9 H2S 0.3 .

I

', .

.

Claims (13)

THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the production of a hydrogen and carbon monoxide-containing gas from a carbonaceous fuel which comprises reacting diluted oxygen with the carbonaceous fuel in a first reaction zone which is kept at an average temperature in the range of from 1200 to 1700°C and introducing the effluent of the first reaction zone into a second reaction zone, the average temperature of which is at least 100°C lower than that of the first reaction zone.
2. A process as claimed in claim 1, in which the carbonaceous fuel is a powdered solid, 70% of which has a particle size smaller than 200 mesh.
3. A process as claimed in claim 1, in which the diluted oxygen is preheated to a temperature in the range of from 200 to 1300°C.
4. A process as claimed in claim 1, 2 or 3, in which the fuel is mixed with the diluted oxygen and the diluted oxygen/fuel mixture is intro-duced as a jet in the first reaction zone at a linear velocity in the range of from 10 to 200 m/sec.
5. A process as claimed in claim 1, 2 or 3, in which 50 to 95% of the total amount of fuel is introduced into the first reaction zone and the remaining part of the fuel is introduced into the effluent of the first reaction zone and/or the second reaction zone.
6. A process as claimed in claim 1, 2 or 3, in which the reaction in the first reaction zone is carried out at a pressure in the range of from 1 to 200 kg/cm2 and a residence time in the range of from 0.02 to 20 seconds.
7. A process as claimed in any one or more of claims 1, 2 or 3, in which the total fuel is introduced into the first reaction zone and the residence time therein is in the range of from 0.02 to 3 seconds.
8. A process as claimed in claim 1, 2 or 3, in which part of the fuel is introduced into the first reaction zone and the residence time there-in is in the range of from 0.5 - 20 seconds.
9. A process as claimed in claim 1, 2 or 3, in which part of the fuel is introduced into the reaction zone together with 1/10 to 2 m3 (NTP) per kg fuel of a diluent consisting of steam, nitrogen and/or CO2.
10. A process according to claim 1, 2 or 3, in which part of the fuel is introduced into the first reaction zone and the residence time there-in is in the range of from 0.5 - 20 seconds and part of the fuel is intro-duced into the second reaction zone together with 1/10 to 2 m3 (NTP) per kg fuel of a diluent consisting of steam, nitrogen and/or CO2.
11. A process as claimed in claim 1, 2 or 3, in which part of the fuel is introduced into the second reaction zone together with 1/10 to 2 m3 (NTP) per kg fuel of a diluent consisting of steam, nitrogen and/or CO2, and the diluent has a pressure in the range of from 2 to 210 kg/cm2 and a tem-perature in the range of from 100 to 700°C.
12. A process as claimed in claim 1, 2 or 3, in which the tempera-ture in the second reaction zone is in the range of from 600 to 1400°C.
13. A process as claimed in claim 1, 2 or 3, in which the reaction in the second reaction zone is carried out at a temperature in the range of from 600 to 1400°C, a pressure in the range of from 1 to 200 kg/cm2 absolute and a residence time in the range of from 0.5 to 40 seconds.
CA217,858A 1974-02-21 1975-01-14 Process for the production of hydrogen and carbon monoxide-containing gas Expired CA1050271A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB7903/74A GB1491465A (en) 1974-02-21 1974-02-21 Process for the production of hydrogen and carbon monoxide-containing gas

Publications (1)

Publication Number Publication Date
CA1050271A true CA1050271A (en) 1979-03-13

Family

ID=9842016

Family Applications (1)

Application Number Title Priority Date Filing Date
CA217,858A Expired CA1050271A (en) 1974-02-21 1975-01-14 Process for the production of hydrogen and carbon monoxide-containing gas

Country Status (7)

Country Link
JP (1) JPS5851036B2 (en)
CA (1) CA1050271A (en)
DE (1) DE2507124A1 (en)
FR (1) FR2261974B1 (en)
GB (1) GB1491465A (en)
NL (1) NL7501943A (en)
ZA (1) ZA751033B (en)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2442216A1 (en) * 1978-11-24 1980-06-20 Texaco Development Corp Prodn. of clean fuel gas and/or power from hydrocarbon fuels - by partial oxidation in free-flow, non-catalytic gas generator
US4278445A (en) * 1979-05-31 1981-07-14 Avco Everett Research Laboratory, Inc. Subsonic-velocity entrained-bed gasification of coal
JPS57182394A (en) * 1981-05-06 1982-11-10 Hitachi Ltd Jet bed gasification furnace
JPH0649874B2 (en) * 1982-08-25 1994-06-29 株式会社日立製作所 Coal spouted bed gasification method
JPS6026254U (en) * 1983-07-28 1985-02-22 川崎重工業株式会社 piston
DE4209549A1 (en) * 1992-03-24 1993-09-30 Vaw Ver Aluminium Werke Ag Processes for the thermal treatment of residues, e.g. for the separation and recycling of metal compounds with organic components, using a combination of pyrolysis and gasification
US5431703A (en) * 1993-05-13 1995-07-11 Shell Oil Company Method of quenching synthesis gas
DE19652770A1 (en) * 1996-12-18 1998-06-25 Metallgesellschaft Ag Process for gasifying solid fuels in the circulating fluidized bed
RU2408528C2 (en) * 2008-08-06 2011-01-10 Институт химии нефти Сибирского отделения Российской академии наук Method of producing hydrogen

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3746522A (en) * 1971-09-22 1973-07-17 Interior Gasification of carbonaceous solids

Also Published As

Publication number Publication date
AU7833875A (en) 1976-08-19
GB1491465A (en) 1977-11-09
ZA751033B (en) 1976-01-28
JPS50119006A (en) 1975-09-18
FR2261974A1 (en) 1975-09-19
NL7501943A (en) 1975-08-25
JPS5851036B2 (en) 1983-11-14
DE2507124A1 (en) 1975-08-28
FR2261974B1 (en) 1978-02-03

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