[go: up one dir, main page]

GB2172011A - Thermal reforming of gaseous hydrocarbon - Google Patents

Thermal reforming of gaseous hydrocarbon Download PDF

Info

Publication number
GB2172011A
GB2172011A GB08604844A GB8604844A GB2172011A GB 2172011 A GB2172011 A GB 2172011A GB 08604844 A GB08604844 A GB 08604844A GB 8604844 A GB8604844 A GB 8604844A GB 2172011 A GB2172011 A GB 2172011A
Authority
GB
United Kingdom
Prior art keywords
gas
plasma generator
water vapour
reforming
partially
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.)
Granted
Application number
GB08604844A
Other versions
GB8604844D0 (en
GB2172011B (en
Inventor
Sven Santen
Lars Bentell
Bjorn Hammarskog
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.)
SKF Steel Engineering AB
Original Assignee
SKF Steel Engineering AB
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 SKF Steel Engineering AB filed Critical SKF Steel Engineering AB
Publication of GB8604844D0 publication Critical patent/GB8604844D0/en
Publication of GB2172011A publication Critical patent/GB2172011A/en
Application granted granted Critical
Publication of GB2172011B publication Critical patent/GB2172011B/en
Expired legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
    • B01J12/002—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor carried out in the plasma state
    • 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
    • C01B3/342—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 with the aid of electrical means, electromagnetic or mechanical vibrations, or particle radiations
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0894—Processes carried out in the presence of a plasma
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
    • C01B2203/0222—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic carbon dioxide reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/049—Composition of the impurity the impurity being carbon
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0861—Methods of heating the process for making hydrogen or synthesis gas by plasma
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Health & Medical Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Electromagnetism (AREA)
  • Mechanical Engineering (AREA)
  • Toxicology (AREA)
  • Plasma & Fusion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

In a method for manufacturing a gas containing primarily CO + H2 through thermal reforming of gaseous hydrocarbon, gaseous hydrocarbon and water vapour are supplied, separately or mixed and in almost stoichiometric proportion, to a reforming reactor (1). The gas is heated entirely or partially with the aid of plasma generator(s) (5) to a temperature exceeding 1200 DEG C. <IMAGE>

Description

SPECIFICATION Thermal reforming of gaseous hydrocarbon The present invention relates to a method of manufacturing a gas containing primarily CO + H2 through thermal reforming of gaseous hydrocarbon, e.g. CH4, with water vapour in almost stoichiometric proportion and to a means for performing the method according to the invention.
The known method of reforming gaseous hydrocarbon such as CH4 for the production of a gas containing CO + H2 is through catalytic reforming at temperatures below about 1000"C. To produce reduction gas by what is known as one-step reforming, reforming is performed with an almost stoichiometric proportion between H20 and C. High temperatures are favoured for this process but the temperature is limited by the strength of the material in the reformer tubes.
A drawback with this known process is that the catalyst is extremely sensitive to sulphur and the hydrocarbon must therefore be freed from sulphur prior to reforming.
It is known per se that hydrocarbon can be reformed without using catalysts at temperatures above 1200 -1300 C. However, no suitable method or means for performing this process is known.
The object of the present invention is thus to effect a method and a means for thermal reforming of hydrocarbon without the use of reformer tubes or catalysts.
The method according to the invention comprises supplying gaseous hydrocarbon and water vapour, separately or mixed and in almost stoichiometric proportion, to a reforming reactor and heating the gas entirely or partially with the aid of a plasma generator so that the temperature of the gas mixture exeeds 1 200 C.
Besides enabling external energy to be supplied via plasma generators, the thermal reforming process according to the invention also gives a very low CO2 + H2O content right from the start, i.e. below 10%.
According to a suitable embodiment of the method according to the invention, hydrocarbon and/or water vapour is/are caused to pass entirely or partially through the plasma generator while the remaining gas is injected directly into the reactor.
The plasma generator may be provided with two annular electrodes or it may be of the transferred arc type.
According to another suitable embodiment of the method according to the invention, the heat loss in the process and/or the physical heat in the generated gas mixture is/are utilized at least partially to produce water vapour used in the princess.
According to another suitable embodiment of the method according to the invention, the physical heat in the generated gas mixture is utilized at least partially to desulphurize the gas produced. The desulphurizing is performed by injecting a sulphur acceptor, such as pulverized limestone or dolomite, into the reactor, after which most of the sulphur is separated off together with the consumed lime in solid and/or liquid form.
According to yet another suitable embodiment of the method according to the invention, the physical heat in the gas mixture generated is utilized at least partially to carburize the gas produced. This is preferablyachieved by injecting pulverized, reactive carbon carrier, usually coke, into the reactor, after which the ash remaining is separated in solid and/or liquid form. The remaining content of CO2 + H20 can thus be further reduced, theoretically down to 0%.
It is also per se feasible to perform desulphurizing and/or carburization in separate reactors through which the hot gas produced is passed after the reforming.
The invention is thus performed in an empty, heat-insulated reactor in which the temperature exceeds 1200"C, preferably reaching 1300"C. The pressure in the gas mixture inside the reactor is adjusted to the proposed purpose for which the gas is to be used. if it is to be used as reduction gas, the pressure should suitably be approximately 2 - 3 bar (a) and for use as synthetic gas, it should normally exceed about 20 bar (a). The temperature of the gas produced is controlled in a manner suitable for the purpose, such as by heat-exchanging and/or cooling.
The means for performing the method according to the invention comprises at least one reaction chamber, at least one plasma generator for the supply of external energy to the reaction chamber, supply means for hydrocarbon and water vapour to be heated by plasma generator, gas outlets and outlets for slag and ash.
According to a preferred embodiment of the means according to the invention, it also comprises supply means for reactive carbon carrier and sulphur acceptor.
The plasma generator may be provided with cylindrical electrodes between which an electric arc is produced or it may be of the transferred arc type.
According to another suitable embodiment of the means according to the invention, this comprises a vertical, cylindrical shaft separated into zones for reforming and carburizing, possibly having a constriction between the zones, and provided with an outlet for liquid slag at the bottom of the shaft, and a gas outlet arranged in the lower part of the shaft and communicating with a subsequent separator provided in its lower part with an outlet for solid slag and unvaporized material, and a gas outlet arranged in its upper part. Supply means for reactive carbon carrier and sulphur acceptor are arranged at one or more points in the shaft and in conjunction with the gas outlet from the shaft. According to another suitable embodiment of the means according to the invention, the plasma generators(s) is/are arranged at the top of the vertical shaft.
According to yet another suitable embodiment of the means according to the invention, the separator is designed as a cyclone in order to facilitate separation of solid particles.
According to still another embodiment of the means according the invention a heat-exchanger is provided in the gas outlet from the vertical shaft and/or from the separator.
Further features, advantages and embodiments of the invention will be revealed in the following detailed description, with reference to the accompanying drawing in which The figure shows a diagrammatic sketch of a means for performing the thermal reforming process according to the invention.
The means comprises a vertical, cylindrical shaft 1 composed of a reforming zone 2 and a carburizing zone 3. The two zones are shown partially separated by a constriction 4 but are in direct communication with each other.
At least one plasma generator 5 is arranged at the top of the shaft. Hydrncarbon can be injected entirely or partially directly into the shaft through the pipe 6, or be introduced through the pipe 7 to a mixer 8. In the embodiment shown in the-drawing, water exchanges heat with the generated gas and water vapour can be introduced into the mixer through the pipe 9 or be injected entirely or partially into the reforming zone through the pipe 10. A gas mixture can be generated in the mixer 8 which can be entirely or partially conveyed through the pipe 11 and caused to pass the plasma generator5, or å portion of the gas mixture can be injected directly into the reforming zonethrough the pipe 12.
The embodiment also permits only hydrocarbon orwatervapourto be supplied to the plasma generator via the mixer 8.
The carburizing zone 3 below the gasification zone 2 is in communication with a separator 14 via a gas pipe 13, thus ensuring a sufficiently long residence time for the gas to enable carburization to the desired remaining content of H2O and CO2. The separator preferably consists of a cyclone in orderto facilitate separation of pollutants in particle form from the gas, such as drops of slag and ungasified material.
Most of the slag from the gasification zone 2 is removed through a slag outlet 15 in the cylindrical gasification zone in the shaft 1, while particles accompanying the gas are removed through the slag outlet 16 at the bottom of the separator.
Functionally the gas pipe 13 forms a part of the carburizing zone 3. Nozzles 17,18, 19 for the supply of reactive carbon carrier and/or sulphur acceptor are arranged in the gasification zone, the carburizing zone and said gas pipe. Slag former may also possibly be injected through these nozzles.
In the drawing a heat-exchanger 21 is shown in the gas outlet 20 from the separator 14. This is utilized for heat-exchanging or cooling the gas generated.
As mentioned above, the heat-exchanger can preferably be used to generate watervapourforthe reforming process. Said heat-exchanging or cooling of the gas mixture generated may alternatively or also be carried out in the gas pipe 13connecting the carburizing zone to the separator.

Claims (18)

1. A method of manufacturing a gas containing primarily CO + H2throughthermal reforming of gaseous hydrocarbon, with water vapour in approximately stoichiometric proportion, comprising supplying gaseous hydrocarbon and water vapour, separately or mixed and in approximately stoichiometric proportion, to a reforming reactor and heating the gas entirely or partially with the aid of a plasma generator so that the temperature of the gas mixture exceeds 1 200 C.
2. A method according to Claim 1, wherein hydrocarbon and/or water vapour is/are caused to pass entirely or partially through the plasma generatorwhile the remaining gas, if any, is injected directly into the reactor
3. A method according to Claim 1 or 2, wherein the plasma generator is provided with two annularelectrodes.
4. A method according to Claim 1 or 2, wherein the plasma generator is of the transferred arc type.
5. A method according to any one of Claims 1 to 4, wherein the heat loss in the process and/or the physical heat in the generated gas mixture is/are utilized at least partially in the production of water vapour used in the process.
6. A method according to any one of Claims 1 to 5, wherein the physical heat in the generated gas mixture is utilized at least partiajlyto desulphurize the gas produced.
7. A method according to Claim 6, wherein the desulphurizing is performed by injecting a sulphur acceptor into the reactor, after which most of the sulphur is separated off together with the consumed sulphur acceptor in solid and/or liquid form.
8. A method according to any one of Claims 1 to 7, wherein the physical heat in the gas mixture generated is utilized at least partially to carburize the gas produced.
9. A method according to Claim 8, wherein the carburization-is achieved by injecting pulverized, reactive carbon carrier into the reactor, after which the ash remaining is separated in solid and/or liquid form.
10. A method according to Claim 9, wherein the COz + H2O content remaining after carburization of the gas mixture is below 10%.
11. A method according to Claim 1 substantially as hereinbefore described with reference to the accompanying drawing.
12. A means suitable for performing the method according to any one of Claims 1 to 11, comprising at least one reaction chamber, at least one plasma generator-for the supply of external energy to the reaction chamber, supply means for hydrocarbon and water vapour to be heated by plasma generator, and outlets for slag and ash.
13. A means according to Claim 12, comprising supply means for reactive carbon carrier and/or sulphur acceptor.
14. A means according to Claim 12 or 13, comprising a substantially vertical, cylindrical shaft separated into zones for reforming and carburizing, optionally with a constriction between the zones, and provided with an outlet for liquid slag at the bottom of the shaft, and agas outlet arranged in the lower part of the shaft and communicating with a subsequent separator provided in its lower part with an outlet for solid slag and unvaporized material, and a gas outlet arranged in the upper part of the separator.
15. a means according to any one of Claims 12 to 14, wherein the plasma generator(s) is/are arranged at the top of the substantially vertical shaft.
16. A means according to any-one of Claims 12 to 15, wherein the separator is designed as a cyclone.
17. A means according to any one of Claims 12 to 16, comprising a heat-exchanger in the gas outlet from the vertical shaft and/or in the gas outlet from the separator.
18. A means according to Claim 12 constructed and arranged to operate substantially as hereinbefore described with reference to the accompanying drawing.
GB8604844A 1985-03-01 1986-02-27 Thermal reforming of gaseous hydrocarbon Expired GB2172011B (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
SE8501005A SE8501005L (en) 1985-03-01 1985-03-01 THERMAL REFORM OF THE GAS SHOULDER

Publications (3)

Publication Number Publication Date
GB8604844D0 GB8604844D0 (en) 1986-04-03
GB2172011A true GB2172011A (en) 1986-09-10
GB2172011B GB2172011B (en) 1989-06-14

Family

ID=20359323

Family Applications (1)

Application Number Title Priority Date Filing Date
GB8604844A Expired GB2172011B (en) 1985-03-01 1986-02-27 Thermal reforming of gaseous hydrocarbon

Country Status (8)

Country Link
CN (1) CN86101235A (en)
AU (1) AU5400886A (en)
DE (1) DE3606108A1 (en)
FR (1) FR2578237B1 (en)
GB (1) GB2172011B (en)
NL (1) NL8600429A (en)
NO (1) NO860746L (en)
SE (1) SE8501005L (en)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2655330A1 (en) * 1989-12-01 1991-06-07 Shell Int Research PREPARATION OF HYDROCARBONS CONTAINING ONE OR MORE HETERO-ATOM (S).
FR2724806A1 (en) * 1994-09-16 1996-03-22 Pompes Maupu Entreprise Novel method for the non-catalytic vapour cracking of hydrocarbon(s) and halogen-organic cpds.
FR2802522A1 (en) * 1999-12-20 2001-06-22 Air Liquide Hydrogen production process from hydrocarbons comprises using a reactive element and a pressure of 1-10 bar
WO2003035545A1 (en) * 2001-10-26 2003-05-01 Renault S.A.S Method and device for generating hydrogen by high temperature conversion with water vapour
CN1316055C (en) * 2002-05-22 2007-05-16 光洋热系统株式会社 Atmosphere gas producer and method for carburising
FR2899597A1 (en) * 2006-04-05 2007-10-12 Commissariat Energie Atomique Production of fuel gas from organic/organo-halogen product in a form of liquid, gas/powder useful as energy source, comprises mixing the product with water to provide stoichiometric ratios between carbon atoms and oxygen mixtures
US7417385B2 (en) 2000-11-27 2008-08-26 Ceramatec, Inc. Systems and method for ignition and reignition of unstable electrical discharges
US8350190B2 (en) 2007-02-23 2013-01-08 Ceramatec, Inc. Ceramic electrode for gliding electric arc
US8618436B2 (en) 2006-07-14 2013-12-31 Ceramatec, Inc. Apparatus and method of oxidation utilizing a gliding electric arc
US8826834B2 (en) 2006-07-14 2014-09-09 Ceramatec, Inc. Apparatus and method of electric arc incineration
DE102015218098A1 (en) * 2015-09-21 2017-03-23 Deutsche Lufthansa Ag Process for the thermal decomposition of hydrocarbons and corresponding device
US20180327260A1 (en) * 2015-10-30 2018-11-15 CCP Technology GmbH Apparatus and process for production of synthesis gas

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001009031A1 (en) * 1999-07-29 2001-02-08 David Systems Technology, S.L. Plasma transformer for the transformation of fossil fuels into hydrogen-rich gas
ES2168040B1 (en) * 1999-07-29 2003-06-01 David Systems Technology Sl PLASMA CONVERTER OF FOSSIL FUELS IN A GAS RICH IN HYDROGEN.
DE102013020375A1 (en) * 2013-12-06 2015-06-11 CCP Technology GmbH PLASMA REACTOR FOR COLLIDING A HYDROCARBON FLUID
CN111186816B (en) * 2020-01-17 2022-04-01 西安交通大学 Plasma carbon sequestration system and method

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1354642A (en) * 1971-06-29 1974-06-05 Centre Rech Metallurgique Production of high temperature reformed gases
GB1475731A (en) * 1973-03-26 1977-06-01 Skf Ind Trading & Dev Method of producing reduction gas
GB2010901A (en) * 1977-08-19 1979-07-04 Boc Ltd Gaseous Atmospheres
EP0021601A1 (en) * 1979-05-25 1981-01-07 Westinghouse Electric Corporation Process for regenerating a reducing gas mixture from spent gas evolved in the production of sponge iron
GB2138458A (en) * 1983-04-21 1984-10-24 Skf Steel Eng Ab The recovery of chemicals from pulp waste liquor
GB2150590A (en) * 1983-12-02 1985-07-03 Skf Steel Eng Ab Method and plant for reducing oxidic material

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE427542C (en) * 1925-04-05 1926-04-10 Emil Edwin Production of gas mixtures consisting of nitrogen and hydrogen
SE371453C (en) * 1973-03-26 1978-01-23 Skf Ind Trading & Dev KIT FOR PRODUCTION OF REDUCTION GAS
BE814899A (en) * 1974-05-10 1974-11-12 PROCESS FOR MANUFACTURING HOT REDUCING GAS.
DE3120699A1 (en) * 1980-05-29 1982-02-11 USS Engineers and Consultants, Inc., 15230 Pittsburgh, Pa. METHOD FOR PRODUCING A HOT, REDUCING GAS WITH LOW SULFUR CONTENT
AT384007B (en) * 1984-04-02 1987-09-25 Voest Alpine Ag METHOD FOR PRODUCING SYNTHESIS GAS AND DEVICE FOR IMPLEMENTING THE METHOD

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1354642A (en) * 1971-06-29 1974-06-05 Centre Rech Metallurgique Production of high temperature reformed gases
GB1475731A (en) * 1973-03-26 1977-06-01 Skf Ind Trading & Dev Method of producing reduction gas
GB2010901A (en) * 1977-08-19 1979-07-04 Boc Ltd Gaseous Atmospheres
EP0021601A1 (en) * 1979-05-25 1981-01-07 Westinghouse Electric Corporation Process for regenerating a reducing gas mixture from spent gas evolved in the production of sponge iron
GB2138458A (en) * 1983-04-21 1984-10-24 Skf Steel Eng Ab The recovery of chemicals from pulp waste liquor
GB2150590A (en) * 1983-12-02 1985-07-03 Skf Steel Eng Ab Method and plant for reducing oxidic material

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1991008047A1 (en) * 1989-12-01 1991-06-13 Shell Internationale Research Maatschappij B.V. Preparation of hetero-atoms(s) containing hydrocarbons
US5105028A (en) * 1989-12-01 1992-04-14 Shell Oil Company Separation of hetero-atom(s) containing hydrocarbons
AU643724B2 (en) * 1989-12-01 1993-11-25 Shell Internationale Research Maatschappij B.V. Preparation of hetero-atoms(s) containing hydrocarbons
FR2655330A1 (en) * 1989-12-01 1991-06-07 Shell Int Research PREPARATION OF HYDROCARBONS CONTAINING ONE OR MORE HETERO-ATOM (S).
FR2724806A1 (en) * 1994-09-16 1996-03-22 Pompes Maupu Entreprise Novel method for the non-catalytic vapour cracking of hydrocarbon(s) and halogen-organic cpds.
FR2802522A1 (en) * 1999-12-20 2001-06-22 Air Liquide Hydrogen production process from hydrocarbons comprises using a reactive element and a pressure of 1-10 bar
US7417385B2 (en) 2000-11-27 2008-08-26 Ceramatec, Inc. Systems and method for ignition and reignition of unstable electrical discharges
WO2003035545A1 (en) * 2001-10-26 2003-05-01 Renault S.A.S Method and device for generating hydrogen by high temperature conversion with water vapour
FR2831532A1 (en) * 2001-10-26 2003-05-02 Armines Ass Pour La Rech Et Le METHOD AND DEVICE FOR GENERATING HYDROGEN BY HIGH TEMPERATURE CONVERSION WITH WATER VAPOR
CN1316055C (en) * 2002-05-22 2007-05-16 光洋热系统株式会社 Atmosphere gas producer and method for carburising
FR2899597A1 (en) * 2006-04-05 2007-10-12 Commissariat Energie Atomique Production of fuel gas from organic/organo-halogen product in a form of liquid, gas/powder useful as energy source, comprises mixing the product with water to provide stoichiometric ratios between carbon atoms and oxygen mixtures
US8618436B2 (en) 2006-07-14 2013-12-31 Ceramatec, Inc. Apparatus and method of oxidation utilizing a gliding electric arc
US8742285B2 (en) 2006-07-14 2014-06-03 Ceramatec, Inc. Method of oxidation utilizing a gliding electric arc
US8826834B2 (en) 2006-07-14 2014-09-09 Ceramatec, Inc. Apparatus and method of electric arc incineration
US8350190B2 (en) 2007-02-23 2013-01-08 Ceramatec, Inc. Ceramic electrode for gliding electric arc
DE102015218098A1 (en) * 2015-09-21 2017-03-23 Deutsche Lufthansa Ag Process for the thermal decomposition of hydrocarbons and corresponding device
US20180327260A1 (en) * 2015-10-30 2018-11-15 CCP Technology GmbH Apparatus and process for production of synthesis gas

Also Published As

Publication number Publication date
SE8501005L (en) 1986-09-02
CN86101235A (en) 1986-10-01
NL8600429A (en) 1986-10-01
GB8604844D0 (en) 1986-04-03
DE3606108A1 (en) 1986-09-04
FR2578237A1 (en) 1986-09-05
FR2578237B1 (en) 1990-07-13
GB2172011B (en) 1989-06-14
AU5400886A (en) 1986-09-04
SE8501005D0 (en) 1985-03-01
NO860746L (en) 1986-09-02

Similar Documents

Publication Publication Date Title
US4606799A (en) Method, and an arrangement, for producing synthesis gases
GB2172011A (en) Thermal reforming of gaseous hydrocarbon
EP0227807B1 (en) Production of synthesis gas using convective reforming
FI68075C (en) SAETTING OVER ANORDING FOR FRAMSTAELLNING AV EN HUVUDSAKLIGEN COOKS OCH VAETGAS INNEHAOLLANDE GAS UR KOL- OCH / ELLER KOLV AEEHALTIGT UTGAONGSMATERIAL
KR19980701311A (en) METHOD FOR CO-PRODUCING FUEL AND IRON
CN108474048B (en) Method and system for producing high carbon DRI by using syngas
JPS61222904A (en) Heat exchange reformation and reactor
JPH04214001A (en) Manufacture of hydrogen-containing gas stream
GB2239261A (en) A process for the direct reduction of metal oxides
TWI864000B (en) Method for operating a blast furnace
CA1309589C (en) Method of producing a clean gas containing carbon monoxide and hydrogen
GB2169310A (en) Gas production
CA1265340A (en) Carbon gasification
JPS5818963B2 (en) Method for reducing granular iron ore to sponge iron particles
SE453920B (en) SET AND DEVICE FOR GASING OF FOSSIL FUEL AND REFORM OF GAS FUEL
US20190048429A1 (en) Method and system for the production of porous iron
EP0209861B1 (en) Melt-reductive iron making method from iron ore
JPH0257134B2 (en)
JP2024522088A (en) Blast furnace operation method
KR20230075410A (en) How to operate blast furnace equipment
GB2150590A (en) Method and plant for reducing oxidic material
JPS5641306A (en) Iron making method by direct reduction of iron oxide
RU2062287C1 (en) Method and aggregate for coal gasification
JP3094435B2 (en) Insulated reformer
GB2150592A (en) Method and plant for reducing oxidic material

Legal Events

Date Code Title Description
PCNP Patent ceased through non-payment of renewal fee