US3798005A - Apparatus for obtaining hydrogen - Google Patents

Apparatus for obtaining hydrogen Download PDF

Info

Publication number
US3798005A
US3798005A US00098264A US3798005DA US3798005A US 3798005 A US3798005 A US 3798005A US 00098264 A US00098264 A US 00098264A US 3798005D A US3798005D A US 3798005DA US 3798005 A US3798005 A US 3798005A
Authority
US
United States
Prior art keywords
catalyst
block
sintered
sinter
sintered block
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00098264A
Other languages
English (en)
Inventor
C Koch
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.)
Siemens AG
Original Assignee
Siemens AG
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 Siemens AG filed Critical Siemens AG
Application granted granted Critical
Publication of US3798005A publication Critical patent/US3798005A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • C01B3/38—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 catalysts
    • C01B3/386—Catalytic partial combustion
    • 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
    • C01B3/48—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 followed by reaction of water vapour with carbon monoxide
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • 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
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C01B2203/0294—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing three or more CO-shift steps
    • 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
    • C01B2203/0415—Purification by absorption in liquids
    • 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
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • 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
    • C01B2203/0872—Methods of cooling
    • C01B2203/0877—Methods of cooling by direct injection of fluid
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1064—Platinum group metal catalysts
    • C01B2203/107—Platinum catalysts
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1076—Copper or zinc-based catalysts
    • 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
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • 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
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the thus obtained gas mixture which consists. mainly of CO and H is brought by means of at least one quenching with 11 0 down to temperatures of 500 to 150C and subsequently reacted with the formed water vapor in sinter blocks which are highly porous. contain conversion catalysts and are provided with preferably parallel passage openings.
  • a process is known, from my application Ser. No. 56,885, filed July 2], i970, for flameless combustion of gases in porous sinter blocks, wherein a mixture of hydrocarbons and oxygen or a hydrocarbon and air mixture is burned in a highly porous sinter block, provided with passage openings.
  • said sinter block containing nickel or platinum.
  • sinter blocks containing nickel may reach temperatures of 900 to l,400C
  • sinter blocks containing platinum may reach temperatures up to l.650C.
  • the hydrocarbons employed may easily be evaporated by preheating.
  • Particularly suitable are hydrocarbons of formula C H to C,,H that is those hydrocarbons which are liquid at room temperature.
  • the original materials are installed when nickel catalysts are used, preferably in a stoichiometric ratio, for example. according to the equation:
  • the sinter blocks used for flameless combustion comprise a highly porous material which is essentially open-pored, for example a sintered magnesium aluminum oxide. They comprise additional, preferably parallel positioned passage openings.
  • the passage openings may have a pore radius of approximately 0.5 mm, whereby about 40 passageopenings are provided per 1 cm of sinter block area.
  • the entire pore volume should be at least 50 volume-percent, but is preferably about 65 volume-percent.
  • the additional passage openings first ofall. prevent clogging of the sinter block by contamination and, secondly, facilitate and increase the throughput of the gas mixture considerably.
  • the installation of the nickel or platinum catalyst is carried out in a known fashion through impregnation of the sinter block with a nickel salt solution, or a platinum salt solution, or with a platinum acid solution.
  • Suitable nickel salts are, for example, nickel acetate, nickel carbonate, nickel formate, etc.
  • the platinum is preferably inserted into the sinter block in form of an aqueous solution of H [PtCI Other platinum com pounds may also be used in lieu of H [PtCl,,].
  • nickel in the sinter block may amount to l mg/cm to 200 mg/cm, but may also be higher. An increase in sinter block load capacity could no longer be observed with nickel quantities of 500 mg/cm, 800 mg/cm and above. Particularly suitable were found to be nickel quantities of 10 to mg/cm.
  • the platinum content is about 0.] to mg/cm but preferably 5 to 10 mg/cm. It is essential for the selection of the catalyst salt that the salt be easy to dissociate thermally. After drying in air or, if necessary, with heat, the sinter block may immediately be installed as a radiation surface into an appropriate heating chamber.
  • a mixture of benzenevapor and air in a stoichiometric ratio is combusted in a sinter block wherein 50 mg/cm nickel are uniformly distributed, one obtains, depending on the radiation ratio and gas mixture, a surface temperature of about l,lOOC to 1,450C and when combustion takes place in a sinter block containing 5 to 10 mg/cm platinum, a surface temperature of up to l,600C is obtained according to the higher reaction.
  • the nickel salts used for forming catalysts can also be doped with uranium compounds in order to increase the stability.
  • the gas mixture which is obtained during the incomplete and flameless combustion of hydrocarbons may be employed particularly expediently for obtaining hydrogen. This is of advantage especially when a small construction is indicated for the hydrogen producing system, which is frequently the case in fuel cell plants.
  • the reaction proceeds even without the addition of water vapor without soot, which is important for the practical execution of the method. It occurs mainly in the sinter block impregnated with nickel or platinum.
  • the gases formed during the incomplete combustion (CO, H, and slight amounts By quenching, we mean here, the injection of water the sinter of CO are reacted catalytically with water vapor, according to the equation:
  • the catalysts may be any of the known conversion catalysts. such as for example. mixtures of zinc and copper or iron and chromium. Particularly effective were the mixtures of zinc. copper. chromium and slight amounts of ironsThe indicated catalysts may also be employed in oxidized form or in mixtures, with oxides.
  • a temperature gradient occurs along blocks 13 to 16. so that conversion takes place in sinter blocks 13 and l4, at temperatures of about 350 to-500C and in sinter blocks 15 and 16, at temperatures from 200 to 280C.
  • the supply of water into the injection chambers 9 to 12 is effected via the ribbed pipe system 17, the collecting pipe 18 and the branch pipes 19, 20, 21 and 22. The water is simultaneously being preheated in the tubular system 17.
  • the resulting raw gas leaves the hydrogen producing installation, according to the invention, via line 23 and comprises carbon dioxide and hydrogen.
  • the carbon dioxide is removed from the gas by means of suitable absorbants in known manner.
  • the numeral 24 denotes the housing, 25 the interior lining and 26 the housing insulation. while 27 represents the outer insulation of the suction channel 2.
  • the dimensions of the hydrogen producing installation were 844 mm. 131 mm width and 155 mm height.
  • the device for producing hydrogen by means of sootfree conversion of hydrocarbons with oxygen or air and water vapor is characterized primarily through its low space requirement and is therefore particularly suitable for such installations which are supposed .to be small in size such as, for example, for hydrogen producing installations of portable fuel cell batteries.
  • the device shown in the FIGURE is suitable. however, not only for producing hydrogen but also for the production of inert gas. for example, nitrogen.
  • nitrogen is obtained from air, it is preferable to employ the benzene and air mixture in a stoichiometric ratio so that only CO is ensuing catalytical combustion in sinter block 7, which present in a raw gas mixture, in addition to nitrogen.
  • the CO may be washed out, in a known manner, with the aid of an absorption liquid.
  • the method according to the invention can also be used for converting carbon monoxide contained in the exhaust gases of motor vehicles, whereby the injection 1 claim:
  • a device for obtaining a gas mixture containing hydrogen and carbon dioxide by incomplete, catalytic combustion of a hydrocarbon and oxygen containing gas mixture and subsequent catalytic conversion of the obtained gas mixture. containing CO and H by adding water. which comprises a common housing with inlet ducts for hydrocarbons andoxygen and an outlet duct for the gas mixture containing hydrocarbon and carbon dioxide. at least two highly porous sintered blocks with parallel openings between said inletand outlet ducts, said sintered blocks being positioned in flow direction, one behind another. at such spacing that a free space is formed therebetween. the first of said sintered blocks. in flow direction, being provided with a catalyst for incomplete flameless combustion of the hydrocarbon and oxygen containing gas mixture and at least the last of said sintered blocks. in flow direction, being provided with a catalyst for converting the CO and H, containing gas mixture and means for injecting liquid water into the free space positioned ahead of the sintered blocks provided with converting catalyst.
  • a catalyst-free sintered block provided with passage openings is arranged in the oxygen inlet duct in flow direction ahead of the first sintered block, a free space is formed between the catalyst-free block and the first sintered block and the inlet duct for hydrocarbons ending in said free space.
  • preheating at least one of the hydrocarbons, the water and the oxygen are provided behind the last sintered block in flow direction provided with converting catalyst.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Catalysts (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
US00098264A 1969-12-24 1970-12-15 Apparatus for obtaining hydrogen Expired - Lifetime US3798005A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE1964810A DE1964810C3 (de) 1969-12-24 1969-12-24 Vorrichtung zur Gewinnung von Wasserstoff

Publications (1)

Publication Number Publication Date
US3798005A true US3798005A (en) 1974-03-19

Family

ID=5754928

Family Applications (1)

Application Number Title Priority Date Filing Date
US00098264A Expired - Lifetime US3798005A (en) 1969-12-24 1970-12-15 Apparatus for obtaining hydrogen

Country Status (12)

Country Link
US (1) US3798005A (fr)
JP (1) JPS5023675B1 (fr)
AT (1) AT311920B (fr)
BE (1) BE760829A (fr)
CA (1) CA924079A (fr)
CH (1) CH555294A (fr)
DE (1) DE1964810C3 (fr)
FR (1) FR2074176A5 (fr)
GB (1) GB1332829A (fr)
NL (1) NL7017470A (fr)
SE (1) SE362861B (fr)
ZA (1) ZA708583B (fr)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3897225A (en) * 1972-07-03 1975-07-29 Siemens Ag Method and apparatus for generating a gas mixture to be formed through catalytic conversion of fuel and a gas serving as an oxygen carrier
US3954423A (en) * 1973-02-07 1976-05-04 Siemens Ag Quick start device for reformed-gas generators
US3957962A (en) * 1973-04-17 1976-05-18 Shell Oil Company Process for the preparation of hydrogen-rich gas
US3963000A (en) * 1974-03-06 1976-06-15 Nissan Motor Co., Ltd. System for reforming engine fuel into hydrogen gas-containing mixture by catalytic reaction
US4131086A (en) * 1974-07-20 1978-12-26 Nippon Soken, Inc. Fuel reforming apparatus for use with internal combustion engine
US4138220A (en) * 1978-02-13 1979-02-06 Colonial Metals, Inc. Apparatus for catalytic oxidation of grease and fats in low temperature fumes
US4270896A (en) * 1975-08-26 1981-06-02 Engelhard Minerals & Chemicals Corporation Catalyst system
US4302292A (en) * 1978-03-03 1981-11-24 GHT, Gesellschaft fur Hochtemperatur-Technik mbH Apparatus for the catalytic cracking of gases
US4371500A (en) * 1979-06-30 1983-02-01 Unique Energy Systems, Inc. Apparatus for generating hydrogen
US4419329A (en) * 1980-07-09 1983-12-06 Heller Charles H Device for producing hydrogen and oxygen gases
WO1984002857A1 (fr) * 1983-01-26 1984-08-02 Unique Energy Systems Inc Procede et appareil pour produire de l'hydrogene
EP0878442A1 (fr) * 1997-05-15 1998-11-18 dbb fuel cell engines GmbH Réacteur de réformage et son procédé de mise en oeuvre
DE19836289A1 (de) * 1998-08-11 2000-02-17 Opel Adam Ag Reformer
US6287529B1 (en) * 1995-12-01 2001-09-11 Daimlerchrysler Ag Method for selective catalytic oxidation of carbon monoxide
US20060130462A1 (en) * 2003-07-14 2006-06-22 Herbert Wancura Process for the catalytic NOx reduction of a thermal engine, and device for said purpose
US20080229662A1 (en) * 2005-10-10 2008-09-25 Thomas Aicher Method for vaporising and reforming liquid fuels
US20120216501A1 (en) * 2009-11-04 2012-08-30 Siemens Aktiengellsschaft Chemical reactor featuring heat extraction

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19719997A1 (de) * 1997-05-13 1998-05-28 Daimler Benz Ag Reformierungsreaktoranlage und Betriebsverfahren hierfür
JP4810749B2 (ja) * 2000-06-08 2011-11-09 トヨタ自動車株式会社 燃料改質装置
JP4356198B2 (ja) * 2000-06-14 2009-11-04 トヨタ自動車株式会社 燃料改質装置
BRPI1009577B1 (pt) * 2009-03-19 2020-04-28 Air Prod & Chem processo para preparar uma mistura de gás rica em hidrogênio
JP2016103366A (ja) * 2014-11-27 2016-06-02 アイシン精機株式会社 燃料電池システム

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB265989A (en) * 1926-02-11 1927-09-22 Ig Farbenindustrie Ag Improvements in the decomposition of gaseous or vapourous hydrocarbons by means of water vapour
US1904908A (en) * 1930-08-07 1933-04-18 Standard Oil Co Hydrogen preparation
US1967665A (en) * 1930-06-17 1934-07-24 Ig Farbenindustrie Ag Conversion of hydrocarbons
US2465235A (en) * 1949-03-22 Production of hydrogen
US2482866A (en) * 1944-11-01 1949-09-27 Stanolind Oil & Gas Co Production of carbon monoxide and hydrogen
US2934407A (en) * 1955-12-27 1960-04-26 Simonek Jiri Method for the arrangement of thermodynamic relations
US2956864A (en) * 1955-01-10 1960-10-18 Wulff Process Company Furnace assemblies and combination of such furnaces
US3010807A (en) * 1958-09-10 1961-11-28 Chemical Construction Corp Multi-stage catalytic conversion
DE1152385B (de) * 1954-06-22 1963-08-08 Basf Ag Verfahren zur flammenlosen Umsetzung von gasfoermigen Kohlenwasserstoffen
US3172251A (en) * 1963-01-14 1965-03-09 Minnesota Mining & Mfg Afterburner system
US3441359A (en) * 1967-04-26 1969-04-29 Engelhard Ind Inc Catalytic radiant heater
GB1193202A (en) * 1967-05-02 1970-05-28 Texaco Development Corp Process for the Production of Synthesis Gas.
US3679372A (en) * 1969-04-09 1972-07-25 Gen Electric Off-gas burner system

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2465235A (en) * 1949-03-22 Production of hydrogen
GB265989A (en) * 1926-02-11 1927-09-22 Ig Farbenindustrie Ag Improvements in the decomposition of gaseous or vapourous hydrocarbons by means of water vapour
US1967665A (en) * 1930-06-17 1934-07-24 Ig Farbenindustrie Ag Conversion of hydrocarbons
US1904908A (en) * 1930-08-07 1933-04-18 Standard Oil Co Hydrogen preparation
US2482866A (en) * 1944-11-01 1949-09-27 Stanolind Oil & Gas Co Production of carbon monoxide and hydrogen
DE1152385B (de) * 1954-06-22 1963-08-08 Basf Ag Verfahren zur flammenlosen Umsetzung von gasfoermigen Kohlenwasserstoffen
US2956864A (en) * 1955-01-10 1960-10-18 Wulff Process Company Furnace assemblies and combination of such furnaces
US2934407A (en) * 1955-12-27 1960-04-26 Simonek Jiri Method for the arrangement of thermodynamic relations
US3010807A (en) * 1958-09-10 1961-11-28 Chemical Construction Corp Multi-stage catalytic conversion
US3172251A (en) * 1963-01-14 1965-03-09 Minnesota Mining & Mfg Afterburner system
US3441359A (en) * 1967-04-26 1969-04-29 Engelhard Ind Inc Catalytic radiant heater
GB1193202A (en) * 1967-05-02 1970-05-28 Texaco Development Corp Process for the Production of Synthesis Gas.
US3679372A (en) * 1969-04-09 1972-07-25 Gen Electric Off-gas burner system

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3897225A (en) * 1972-07-03 1975-07-29 Siemens Ag Method and apparatus for generating a gas mixture to be formed through catalytic conversion of fuel and a gas serving as an oxygen carrier
US3954423A (en) * 1973-02-07 1976-05-04 Siemens Ag Quick start device for reformed-gas generators
US3957962A (en) * 1973-04-17 1976-05-18 Shell Oil Company Process for the preparation of hydrogen-rich gas
US3963000A (en) * 1974-03-06 1976-06-15 Nissan Motor Co., Ltd. System for reforming engine fuel into hydrogen gas-containing mixture by catalytic reaction
US4131086A (en) * 1974-07-20 1978-12-26 Nippon Soken, Inc. Fuel reforming apparatus for use with internal combustion engine
US4270896A (en) * 1975-08-26 1981-06-02 Engelhard Minerals & Chemicals Corporation Catalyst system
US4138220A (en) * 1978-02-13 1979-02-06 Colonial Metals, Inc. Apparatus for catalytic oxidation of grease and fats in low temperature fumes
US4302292A (en) * 1978-03-03 1981-11-24 GHT, Gesellschaft fur Hochtemperatur-Technik mbH Apparatus for the catalytic cracking of gases
US4371500A (en) * 1979-06-30 1983-02-01 Unique Energy Systems, Inc. Apparatus for generating hydrogen
US4419329A (en) * 1980-07-09 1983-12-06 Heller Charles H Device for producing hydrogen and oxygen gases
WO1984002857A1 (fr) * 1983-01-26 1984-08-02 Unique Energy Systems Inc Procede et appareil pour produire de l'hydrogene
US6287529B1 (en) * 1995-12-01 2001-09-11 Daimlerchrysler Ag Method for selective catalytic oxidation of carbon monoxide
EP0878442A1 (fr) * 1997-05-15 1998-11-18 dbb fuel cell engines GmbH Réacteur de réformage et son procédé de mise en oeuvre
US6428758B1 (en) 1997-05-15 2002-08-06 Xcellsis Gmbh Reformation reactor and operating method
DE19836289A1 (de) * 1998-08-11 2000-02-17 Opel Adam Ag Reformer
US20060130462A1 (en) * 2003-07-14 2006-06-22 Herbert Wancura Process for the catalytic NOx reduction of a thermal engine, and device for said purpose
US20080229662A1 (en) * 2005-10-10 2008-09-25 Thomas Aicher Method for vaporising and reforming liquid fuels
US20120216501A1 (en) * 2009-11-04 2012-08-30 Siemens Aktiengellsschaft Chemical reactor featuring heat extraction

Also Published As

Publication number Publication date
CH555294A (de) 1974-10-31
ZA708583B (en) 1971-09-29
DE1964810C3 (de) 1979-04-05
GB1332829A (en) 1973-10-03
NL7017470A (fr) 1971-06-28
SE362861B (fr) 1973-12-27
DE1964810A1 (de) 1971-07-15
DE1964810B2 (de) 1978-07-20
CA924079A (en) 1973-04-10
AT311920B (de) 1973-12-10
JPS5023675B1 (fr) 1975-08-09
FR2074176A5 (fr) 1971-10-01
BE760829A (fr) 1971-06-24

Similar Documents

Publication Publication Date Title
US3798005A (en) Apparatus for obtaining hydrogen
US4214867A (en) Method and apparatus for catalytic heat exchange
US3453146A (en) Method and apparatus for reforming carbonaceous fuels and operating fuel cell
SU491238A3 (ru) Способ питани двигател внутреннего сгорани
KR100801861B1 (ko) 탄화수소의 자기발열 접촉 증기 개질법
CN100352760C (zh) 由甲醇生成氢气和二氧化碳的一步转化
US3885020A (en) Method of oxidizing hydrocarbons and oxygenated hydrocarbons to carbon dioxide and water
US3897225A (en) Method and apparatus for generating a gas mixture to be formed through catalytic conversion of fuel and a gas serving as an oxygen carrier
GB1057328A (en) Hydrogen generator
GB798741A (en) Process for the production of combustible gas enriched with methane
RU2010127266A (ru) Набор для анализа клеток и способ
KR100908401B1 (ko) 알코올의 촉매적 자열 스팀 개질을 위한 방법
US3857668A (en) Flameless catalytic combustion of hydrocarbon in porous sintered stones
US1124347A (en) Process of effecting dissociative reactions upon carbon compounds.
US4288346A (en) Catalyst for catalytic heat exchange
US3499797A (en) Water gas shift converter and fuel cell system therewith
US4407238A (en) Methanol dissociation using a copper-chromium-manganese catalyst
JP2003503295A (ja) エタノール改質用触媒および改質方法ならびにそれらを用いる燃料電池システム
AU679868B2 (en) Photocatalyst, method for preparing the same, and production of hydrogen using the same
US3410661A (en) Liquid phase reforming process
Arutyunov et al. A generator of synthesis gas and hydrogen based on a radiation burner
RU113729U1 (ru) Процессор для конверсии углеводородных топлив в синтез-газ для применения в твердооксидных топливных элементах
US6649562B2 (en) Methanol-decomposing catalyst and methanol-decomposing apparatus comprising same
JP3520367B2 (ja) 白金ニトロアンミン系錯体の製造方法
US3442618A (en) Method for producing hydrogen from hydrogen-containing feedstocks