[go: up one dir, main page]

WO2000032513A1 - Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene - Google Patents

Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene Download PDF

Info

Publication number
WO2000032513A1
WO2000032513A1 PCT/GB1999/003958 GB9903958W WO0032513A1 WO 2000032513 A1 WO2000032513 A1 WO 2000032513A1 GB 9903958 W GB9903958 W GB 9903958W WO 0032513 A1 WO0032513 A1 WO 0032513A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
selective oxidation
feedstock
hydrogen
reactor according
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.)
Ceased
Application number
PCT/GB1999/003958
Other languages
English (en)
Inventor
Peter Geoffrey Gray
John Frederick Pignon
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.)
Johnson Matthey PLC
Original Assignee
Johnson Matthey PLC
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 Johnson Matthey PLC filed Critical Johnson Matthey PLC
Priority to CA002352776A priority Critical patent/CA2352776A1/fr
Priority to JP2000585163A priority patent/JP2002531247A/ja
Priority to EP99956238A priority patent/EP1144302A1/fr
Publication of WO2000032513A1 publication Critical patent/WO2000032513A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/2485—Monolithic reactors
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
    • B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • 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
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00194—Tubes
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • 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
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
    • 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
    • C01B2203/0435—Catalytic purification
    • C01B2203/044—Selective oxidation of 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
    • C01B2203/04—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
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide

Definitions

  • the present invention concerns an improved reactor, more particularly it concerns a reactor particularly adapted for and suitable for certain selective oxidation reactions.
  • the present invention provides a reactor for catalytic selective oxidation, comprising a reactor vessel with counter current cooling and at least one stage, each stage provided with an inlet for a first feedstock, e.g. CO contaminated hydrogen, an inlet for a second feedstock, e.g. oxygen-containing gas, gas mixing means and a catalytic reaction zone, preferably comprising a selective oxidation catalyst deposited on a substrate having good heat conduction properties.
  • a first feedstock e.g. CO contaminated hydrogen
  • a second feedstock e.g. oxygen-containing gas
  • gas mixing means e.g. oxygen-containing gas
  • the invention also provides a process for the removal of quantities of CO from a hydrogen feedstock by partial oxidation, comprising at least one step of admixing said feedstock with a quantity of oxygen, passing the resulting mixture over a selective oxidation catalyst in a selective oxidation zone and recovering a hydrogen product with reduced content of CO, whilst simultaneously cooling the selective oxidation zone, preferably to maintain the selective oxidation zone at a temperature in the range 100 to 250°C, by counter- current coolant flow.
  • the reactor in its most preferred embodiment, has four stages and this is effective to reduce a reformate having a CO content of 1 to 2% to below lOppm. In other embodiments, there may be 2 to 10 stages.
  • the reactor is suitably in the form of a vessel in which the reaction zones are generally annular in shape, and provided with internal and/or external liquid cooling. Cooling is preferably provided by internal cooling using water, which is suitably under pressure to prevent boiling at the temperatures generated. Other liquid coolants, or forced air cooling may be used if desired. According to specific reactor designs, heat removal may be enhanced by increasing heat exchange surface areas by corrugation or other established means. Heat removal may be altered by altering the flow of coolant and/or altering the quantity of heat removed from the coolant by means of a heat exchanger.
  • Each reaction zone suitably comprises a metallic catalyst support (“monolith”) of generally honeycomb construction, as is in common use in automobile exhaust gas catalysis. These may have 50 to 1200 cells per square in cell density, preferably 200 to 600 cpsi, and may be of a variety of types of stainless steel. In general, the present invention does not result in the reaction stages reaching the higher temperatures generally met with in exhaust gas catalysis (e.g. 500-900°C), but the material should be capable of resisting temperature excursions.
  • An alternative reaction zone design utilises what has become known as "static mixers" which combine a very high degree of gas agitation and mixing, resulting in non- laminar flow, with relatively low pressure drop. Such static mixers may be manufactured from a variety of metals and are commercially available. However, it is presently preferred to use a honeycomb monolith.
  • the reaction zone desirably carries a selective oxidation catalyst comprising a platinum group metal, especially comprising platinum and/or rhodium, carried on a high surface area metal oxide support, such as alumina.
  • a selective oxidation catalyst comprising a platinum group metal, especially comprising platinum and/or rhodium, carried on a high surface area metal oxide support, such as alumina.
  • the metallic catalyst support may be coated by generally known methods with a slurry of oxide support, dried and fired, and then impregnated with the catalytically active components, before a final firing. Such procedures are in themselves known, and do not form part of this invention.
  • An essentially cylindrical metal vessel made by pressing two halves and seam-welding, has a main gas inlet, 2, for reformate gas, and an outlet, 3, for cleaned gas.
  • the vessel has a number of annular reaction zones, 4, each consisting of an annular wound corrugated catalyst support.
  • the vessel further has an internal water jacket, 5, between a spacer and the shell and this is supplied with cooling water by means of a water circuit comprising a circulating pump, 6, and a heat exchanger, 7.
  • the heat exchanger is desirably used to recover heat in an integrated system e.g. in an integrated combined heat and power system.
  • the vessel further is provided with four air inlets, 8, each providing pre-determined (for a steady-state operation) levels of air (that is reaction oxygen; air is generally suitable).
  • controlled amounts of oxygen may be used downstream of each air inlet.
  • Zone 9a is suitably a static mixer, but zones 9b, 9c and 9d are preferably alternating annular mixing vanes, 10, and discs, 11, having gas flow holes, as illustrated in Figs 2 and 3. It should be noted that for simplicity only four vanes and four holes are shown, but more, e.g. six or eight, may be used.
  • vanes and discs may be manufactured by pressing to form a sleeve which may be fitted and brazed or welded onto the jacket 5 with the intention that each gas mixing zone also serves to remove hear from the reaction gases leaving each reaction zone.
  • each reaction zone may incorporate different and/or different loadings, of catalyst.
  • Each metal catalyst support monolith suitably has 300-400 cells per sq.in. and is coated with a washcoat comprising ⁇ 36wt% alumina solids of D50 of approx 5 ⁇ m and D90 of approx 16 ⁇ m, to deposit approx 3g/m 3 . After drying and firing, the coated monolith was impregnated with a platinum salt solution to result in 5% by wt of Pt deposited on the alumina. The resulting coated monolith was again dried and fired before being assembled into the reactor.
  • the reactor of the invention is compact and exhibits relatively low pressure drop. Manufacturing costs are relatively low.
  • the reactor is believed to be suitable for mobile or automobile uses as well as stationery uses. It is presently envisaged that the reactor shell will be lagged to control heat loss and prevent injury.
  • the reactor can be manufactured simply and inexpensively, using pressed and welded parts. It is desirably operated to achieve low pressure drop, and the particular embodiment illustrated is designed for a gas hourly space velocity of approx. 30,000h " ' gas throughput.
  • the reactor as described may be altered in a variety of ways without departing from the central inventive concept.
  • the invention is now illustrated below in a working example of a two-stage reactor, fed with a synthetic reformate gas mixture containing N 2 , H 2 , CO, CO 2 and H O.
  • Each of the two stages consists of a mixing zone with three off-set spiral vanes, followed by air injection accomplished through a number of apertures in an annular ring, producing a swirling, mixing gas.
  • the thus mixed hydrogen and air mixture passes through an annular metal honeycomb support mounted on a central cooling jacket.
  • the cooling jacket is fed counter-current to the flow of hydrogen with a heat transfer fluid, conveniently water under pressure, and the metal honeycomb support is mounted in good heat exchange contact with the cooling jacket.
  • the metal honeycomb carries a selective oxidation catalyst.
  • Gas may be extracted for analysis between the two stages and/or after the second stage.
  • the test two-stage reactor can model a three or four stage reactor.
  • the detailed operating conditions and other experimental detail for one typical run of the above reactor now follow. It was remarkable that the pressure drop across the whole of the est reactor was about the measurement limit of the gauges being used, and was of the order of 1.5-3mbar (150-300Pa), at the two throughputs tested. This indicates that the reactor is very efficient, compact and requires very little energy to operate.
  • Each catalyst support was an annular of internal diameter 3.85in (9.78cm), external diameter 5.85in (14,86cm) and 3.0in(7.62cm) length, made from "Fecralloy" steel and having 500 cells per sq in.
  • Each support had been washcoated with alumina washcoat as used in exhaust gas catalytic convertors, followed by loading with 5% by wt of the alumina of Pt. Conventional manufacturing techniques were used.
  • the synthetic reformate had the compositions: 48%N 2 (dry), 40%H 2 (dry), 10%CO 2 (dry), 0.5-1.5%CO (dry) and 13% H 2 O (of total flow).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne une cuve de réaction (1) à un ou plusieurs étages d'oxydation sélective, avec refroidissement en contre-courant (5, 6, 7), chaque étage ayant une admission pour charge du type hydrogène contaminé par CO (2), une admission pour seconde charge du type oxygène ou air (8) un système de mélange de gaz (9a, 9b) et une zone de réaction catalytique (4), renfermant de préférence un support métallique à catalyseur d'oxydation sélective. Ce type de reformeur compact à chute de pression très basse est approprié à la production d'hydrogène pour une pile à combustible.
PCT/GB1999/003958 1998-12-01 1999-11-29 Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene Ceased WO2000032513A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CA002352776A CA2352776A1 (fr) 1998-12-01 1999-11-29 Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene
JP2000585163A JP2002531247A (ja) 1998-12-01 1999-11-29 水素から一酸化炭素を除去するための反応器および方法
EP99956238A EP1144302A1 (fr) 1998-12-01 1999-11-29 Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GBGB9826222.3A GB9826222D0 (en) 1998-12-01 1998-12-01 Improved reactor
GB9826222.3 1998-12-01

Publications (1)

Publication Number Publication Date
WO2000032513A1 true WO2000032513A1 (fr) 2000-06-08

Family

ID=10843323

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB1999/003958 Ceased WO2000032513A1 (fr) 1998-12-01 1999-11-29 Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene

Country Status (5)

Country Link
EP (1) EP1144302A1 (fr)
JP (1) JP2002531247A (fr)
CA (1) CA2352776A1 (fr)
GB (1) GB9826222D0 (fr)
WO (1) WO2000032513A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002293509A (ja) * 2001-03-30 2002-10-09 Tokyo Gas Co Ltd Ｃｏ除去器
JP2003081606A (ja) * 2001-09-10 2003-03-19 Toyota Motor Corp 改質ガスの流路交換装置またはガス混合部を備えた燃料改質装置
WO2003033401A1 (fr) * 2001-10-15 2003-04-24 Ballard Generation Systems Inc. Appareil d'oxydation selective de monoxyde de carbone dans un melange gazeux contenant de l'hydrogene
EP1349226A1 (fr) 2002-03-27 2003-10-01 Nissan Motor Co., Ltd. Dispositif d'oxydation du monoxyde de carbone
DE10240953A1 (de) * 2002-09-02 2004-03-18 Viessmann Werke Gmbh & Co Kg Apparat zur Erzeugung von Wasserstoff
EP2281776A4 (fr) * 2008-05-30 2012-06-13 Panasonic Corp Convertisseur de combustible
WO2015018961A1 (fr) * 2013-08-07 2015-02-12 Abengoa Hidrógeno, S.A. Réacteur d'oxydation préférentielle de monoxyde de carbone

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5047548B2 (ja) 2006-07-06 2012-10-10 ユニ・チャーム株式会社 着用物品の止着構造
JP7130743B2 (ja) * 2017-06-27 2022-09-05 シジジー プラズモニクス インコーポレーティッド 複数の光触媒リアクタセルを有する光触媒リアクタ

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2075859A (en) * 1980-04-29 1981-11-25 Humphreys & Glasgow Ltd Catalytic reactor with internal heat exchanger
EP0305203A2 (fr) * 1987-08-27 1989-03-01 Haldor Topsoe A/S Procédé pour exécuter des réactions chimiques hétérogènes catalytiques
US4988431A (en) * 1986-09-17 1991-01-29 Linde Aktiengesellschaft Process for performing catalytic reactions
WO1993019005A1 (fr) * 1992-03-19 1993-09-30 International Fuel Cells Corporation Procede et appareil d'elimination du monoxyde de carbone contenu dans des milieux gazeux
DE4334981A1 (de) * 1993-10-14 1995-04-20 Daimler Benz Ag Reaktor zur katalytischen Entfernung von CO in H¶2¶-reichem Gas
DE19544895C1 (de) * 1995-12-01 1997-02-27 Daimler Benz Ag Verfahren und Vorrichtung zur selektiven katalytischen Oxidation von Kohlenmonoxid

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2075859A (en) * 1980-04-29 1981-11-25 Humphreys & Glasgow Ltd Catalytic reactor with internal heat exchanger
US4988431A (en) * 1986-09-17 1991-01-29 Linde Aktiengesellschaft Process for performing catalytic reactions
EP0305203A2 (fr) * 1987-08-27 1989-03-01 Haldor Topsoe A/S Procédé pour exécuter des réactions chimiques hétérogènes catalytiques
WO1993019005A1 (fr) * 1992-03-19 1993-09-30 International Fuel Cells Corporation Procede et appareil d'elimination du monoxyde de carbone contenu dans des milieux gazeux
DE4334981A1 (de) * 1993-10-14 1995-04-20 Daimler Benz Ag Reaktor zur katalytischen Entfernung von CO in H¶2¶-reichem Gas
DE19544895C1 (de) * 1995-12-01 1997-02-27 Daimler Benz Ag Verfahren und Vorrichtung zur selektiven katalytischen Oxidation von Kohlenmonoxid

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002293509A (ja) * 2001-03-30 2002-10-09 Tokyo Gas Co Ltd Ｃｏ除去器
JP2003081606A (ja) * 2001-09-10 2003-03-19 Toyota Motor Corp 改質ガスの流路交換装置またはガス混合部を備えた燃料改質装置
WO2003033401A1 (fr) * 2001-10-15 2003-04-24 Ballard Generation Systems Inc. Appareil d'oxydation selective de monoxyde de carbone dans un melange gazeux contenant de l'hydrogene
EP1349226A1 (fr) 2002-03-27 2003-10-01 Nissan Motor Co., Ltd. Dispositif d'oxydation du monoxyde de carbone
DE10240953A1 (de) * 2002-09-02 2004-03-18 Viessmann Werke Gmbh & Co Kg Apparat zur Erzeugung von Wasserstoff
EP2281776A4 (fr) * 2008-05-30 2012-06-13 Panasonic Corp Convertisseur de combustible
US8398731B2 (en) 2008-05-30 2013-03-19 Panasonic Corporation Fuel treatment device with gas supply and diffusion regions
WO2015018961A1 (fr) * 2013-08-07 2015-02-12 Abengoa Hidrógeno, S.A. Réacteur d'oxydation préférentielle de monoxyde de carbone

Also Published As

Publication number Publication date
JP2002531247A (ja) 2002-09-24
CA2352776A1 (fr) 2000-06-08
GB9826222D0 (en) 1999-01-20
EP1144302A1 (fr) 2001-10-17

Similar Documents

Publication Publication Date Title
US6524550B1 (en) Process for converting carbon monoxide and water in a reformate stream
EP1345679B1 (fr) Module de reacteur s'utilisant dans un dispositif compact de traitement de combustible
EP1251949B1 (fr) Procede et appareil permettant d'obtenir une vitesse de production amelioree de reactions chimiques thermiques
DE69913037T2 (de) Reformierungsreaktor
US4863707A (en) Method of ammonia production
US6824577B2 (en) Nested compact fuel processor for producing hydrogen rich gas
EP0991465B1 (fr) Echangeur de chaleur actif a microcanaux
JP4718069B2 (ja) 小型軽量のメタノール燃料気体自熱式改質装置
KR100669311B1 (ko) 연료 전지 발전 장치에 사용하기 위한 소형 경량 촉매베드 및 이의 제조방법
JP4643027B2 (ja) 小型軽量の自熱式改質装置
EP1314688B1 (fr) Procédé catalytique de reformage autothermique à la vapeur des mélanges d'alcools supérieurs, spécialement l'éthanol avec des hydrocarbures
EP1286914A4 (fr) Production d'hydrogene par decomposition autothermique d'ammoniac
EP1412075A1 (fr) Reacteur catalytique
US20040005268A1 (en) Method and multi-stage shift reactor for reducing the carbon monoxide content in a hydrogen-containing gas stream, and reformer installation
WO2000032513A1 (fr) Cuve de reaction et procede permettant d'eliminer le monoxyde de carbone dans l'hydrogene
EP1977822B1 (fr) Récipient et dispositif de réaction
EP1253974A1 (fr) Processus chimique
US20040037757A1 (en) Hydrogen purification apparatus
EP1910222B1 (fr) Système d'oxydation préférentielle en deux étapes avec une seule injection d'air
KR100782125B1 (ko) 개질가스 정제용 촉매 및 이의 제조방법
US20120014864A1 (en) Hybrid foam/low-pressure autothermal reformer
de la Osa et al. The Development of Millistructured Reactors for High Temperature and Short Time Contact

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): CA JP US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
ENP Entry into the national phase

Ref document number: 2352776

Country of ref document: CA

Ref country code: CA

Ref document number: 2352776

Kind code of ref document: A

Format of ref document f/p: F

WWE Wipo information: entry into national phase

Ref document number: 1999956238

Country of ref document: EP

ENP Entry into the national phase

Ref country code: JP

Ref document number: 2000 585163

Kind code of ref document: A

Format of ref document f/p: F

WWE Wipo information: entry into national phase

Ref document number: 09857116

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 1999956238

Country of ref document: EP

WWW Wipo information: withdrawn in national office

Ref document number: 1999956238

Country of ref document: EP