WO2003035544A1 - Convertisseur compact - Google Patents

Convertisseur compact Download PDF

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Publication number
WO2003035544A1
WO2003035544A1 PCT/GB2002/004737 GB0204737W WO03035544A1 WO 2003035544 A1 WO2003035544 A1 WO 2003035544A1 GB 0204737 W GB0204737 W GB 0204737W WO 03035544 A1 WO03035544 A1 WO 03035544A1
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WO
WIPO (PCT)
Prior art keywords
channels
chamber
catalyst
temperature
shift
Prior art date
Application number
PCT/GB2002/004737
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English (en)
Inventor
Andrew Leslie Dicks
Kevin David Pointon
Stuart Leigh Jones
Angelika Siddle
Robert William Judd
Original Assignee
Lattice Intellectual Property Ltd
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Filing date
Publication date
Application filed by Lattice Intellectual Property Ltd filed Critical Lattice Intellectual Property Ltd
Publication of WO2003035544A1 publication Critical patent/WO2003035544A1/fr

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    • 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
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • 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
    • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
    • 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
    • B01J19/249—Plate-type 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
    • B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0008—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one medium being in heat conductive contact with the conduits for the other medium
    • F28D7/0025—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one medium being in heat conductive contact with the conduits for the other medium the conduits for one medium or the conduits for both media being flat tubes or arrays of 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
    • B01J2208/00194—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
    • B01J2208/00548—Flow
    • 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
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/021—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles comprising a plurality of beds with flow of reactants in parallel
    • B01J2208/022—Plate-type reactors filled with granular catalyst
    • 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
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00081—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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2453—Plates arranged in parallel
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B01J2219/2462—Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2479—Catalysts coated on the surface of plates or inserts
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2482—Catalytically active foils; Plates having catalytically activity on their own
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2498—Additional structures inserted in the channels, e.g. plates, catalyst holding meshes
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0215—Coating
    • 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
    • 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
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1035—Catalyst coated on equipment surfaces, e.g. reactor walls
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1082—Composition of support materials
    • 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
    • C01B2203/16—Controlling the process
    • 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
    • C01B2203/16—Controlling the process
    • C01B2203/1614—Controlling the temperature
    • C01B2203/1619—Measuring the temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F2275/00—Fastening; Joining
    • F28F2275/06—Fastening; Joining by welding
    • F28F2275/061—Fastening; Joining by welding by diffusion bonding

Definitions

  • This invention relates to water-gas shift reactors that reduce the concentration of carbon monoxide and increase the level of hydrogen in gas streams.
  • gas streams may be produced by partial oxidation or steam reforming of hydrocarbon fuels. Removal of carbon monoxide is required in applications where the carbon oxides can deactivate catalysts such as in the production of ammonia or in low temperature fuel cells.
  • PEM-FC polymer fuel cell
  • a typical high temperature shift (HTS) reactor operates at around 400°C.
  • the low temperature shift (LTS) reactors operate at the lowest possible inlet temperature to achieve the maximum carbon monoxide conversion based on the chemical equilibrium, hi practice, the lowest possible inlet temperature is dictated by
  • the catalyst could be divided into three beds with inter-cooling or a second shift reactor could be used.
  • the gas at the exit of the first catalyst bed will effectively reach equilibrium whenever throughput is low.
  • the inlet and exit temperature in each bed must be inside the temperature working range of the catalysts.
  • cooling of the gas stream between reactors is achieved by heat exchange, hi some cases, the temperature may be reduced, by injecting steam or condensate into the process gas.
  • Addition of quench water allows CO concentration to be lowered but problems can arise during start up and shut down. In such plants the life of the LTS catalyst may be shortened because of the damage from the entrained water droplets and because of the presence of catalyst poisons in the water itself. Excessive condensation of water on LTS catalyst is invariably detrimental causing catalyst fragmentation and generally must be avoided. High steam levels in process gas can be tolerated provided condensation does not take place.
  • the catalysts used for shift reactors are generally used in pellet form.
  • Such a method of performing a shift reaction using a diffusion bonded heat exchanger provides for very efficient cooling of the shift reactants such that a small reactor is required.
  • Catalyst is preferably provided in the first chamber or set of channels.
  • the catalyst may be provided as a layer on the chamber or set of channels.
  • the rate of flow of coolant through the second chamber or set of channels may be controlled to ensure satisfactory cooling of the shift reactants.
  • an apparatus for performing a shift reaction comprising a diffusion bonded heat exchanger having two chambers or sets of channels formed therein, with the diffusion bonded heat exchanger being arranged to transfer heat between the two chambers or sets of channels, the first chamber or set of channels being arranged to convey fluids performing the shift reaction, and the other chamber or set of channels being arranged to convey coolant to cool the fluids in the first set of channels.
  • Figure 1 shows a diffusion bonded heat exchanger suitable for performing the first aspect of the present invention
  • Figure 2 shows the shift reaction being performed adjacent to the catalyst layer of a diffusion bonded heat exchanger
  • Figure 3 illustrates the temperature profile and carbon monoxide concentration across a reactor of the second aspect of the present invention and a conventional shift reactor.
  • Figures 1 and 2 shows a water gas shift reactor balanced with a coolant stream in a heat exchanger.
  • the reactor consists of a diffusion bonded heat exchanger 10 as shown in Figure 1 with two chambers or sets of channels therein, separated by a diffusion bonded heat exchanger plate. In one chamber or set of channels 11, the shift reaction takes place, in the other chamber or set of channels 12 a coolant gas stream flows as illustrated in Figure 2.
  • a diffusion bonded heat exchanger is very compact and provides very good heat transfer between the two chambers or sets of channels.
  • the catalyst is in the form of a thin layer comprising catalytically active particles dispersed in an inactive matrix.
  • the catalyst consists of copper and zinc supported on alumina.
  • the catalyst layer is applied to the shift reactor side of the heat exchanger plate using wash-coat technology.
  • This catalyst arrangement allows good heat transfer from the shift reaction through the heat exchanger plate to the coolant stream.
  • the coolant stream could be any suitable liquid or gas stream such as another gas stream in a fuel cell arrangement which requires pre-heating.
  • the rate of flow of coolant is controlled to ensure an appropriate amount of cooling so that the shift reaction is performed under suitable temperature conditions.
  • the temperature of the shift reaction chamber or set of channels is measured and the rate of flow of coolant is set appropriately to ensure that the shift reaction is performed at a suitable temperature.
  • the temperature of the chamber or set of channels in which shift reaction takes place may be monitored and the rate of flow of coolant controlled appropriately.
  • the coolant flow rate is determined dependent upon the shift reaction temperature by a processor such as a microprocessor using a look-up table or suitable algorithm.
  • the flow of coolant may be produced by any suitable means such as a blower or pump.
  • This method of heat removal is preferable to the traditional method of reducing the temperature in the shift reactor by using quench water.
  • higher steam concentrations can be used to achieve higher conversion of CO.
  • the disadvantage of this is that the system is more complicated, it can lead to problems at start up and shut down and it is more important that condensation does not take place as excessive condensation of water on the LTS is detrimental causing fragmentation.
  • the LTS or HTS shift catalyst has an effectiveness factor of 100%
  • a reduction in volume of catalyst allows the reactor to be more compact.
  • the pressure drop through a bed of catalyst is determined by the bed geometry and voidage. Design catalyst volumes decrease as the pressure is increased, being approximately inversely proportional to the square root of pressure for a pore diffusion limited reaction. In a traditional shift reactor the pressure is typically 30bar. If thin film catalyst is used in the reactor the pressure drop will be very limited and lower operating pressures can be used. For example in the case of the polymer fuel cell system the pressure is 3bar. Operating at lower pressure means less expensive reactor construction materials can be used.
  • a major technical hurdle to commercialisation of solid polymer fuel cells is the need for a low cost and compact fuel processing system to convert hydrocarbon fuel into a hydrogen-rich gas.
  • the inability of the PEM to tolerate more than 20ppm of carbon monoxide means there is a need for purification of the gases.
  • the resulting gas purification plant required for a PEM fuel cell system is complicated, large and expensive.
  • the process will include a reforming or partial oxidation stage followed by high temperature shift and low temperature shift then preferential oxidation (PROx) reactor.
  • the requirement for the PROx reaction is a carbon monoxide concentration of ⁇ 1 %.
  • the PROx will selectively oxidise the carbon monoxide rather than hydrogen to carbon dioxide and provide the hydrogen rich fuel to the fuel cell.
  • a critical component of the fuel processor is the water-gas shift reactor.
  • Existing water gas shift reactors are cumbersome because of their large size and weight. This is particularly important for fuel cells for mobile applications.
  • a shift reactor as proposed in this invention will simphfy the balance of plant reducing the cost and size.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Catalysts (AREA)

Abstract

La présente invention concerne un procédé et un appareil permettant d'effectuer une conversion à l'aide d'un échangeur de chaleur soudé par diffusion (10). L'échangeur de chaleur soudé par diffusion (10) comprend deux chambres ou ensembles de canaux (11, 12), la première chambre ou le premier ensemble de canaux étant agencé(e) pour transporter les fluides destinés à la conversion (11) et la seconde chambre ou le second ensemble de canaux (12) étant agencé(e) pour transporter un réfrigérant destiné à refroidir le fluide dans le premier ensemble de canaux. Un catalyseur destiné à la conversion peut se présenter sous la forme d'une couche sur la première chambre ou le premier ensemble de canaux. On peut régler l'écoulement du réfrigérant à travers le second ensemble de canaux afin d'obtenir un niveau désiré de refroidissement de la conversion.
PCT/GB2002/004737 2001-10-22 2002-10-18 Convertisseur compact WO2003035544A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB0125295A GB0125295D0 (en) 2001-10-22 2001-10-22 Shift reaction
GB0125295.6 2001-10-22

Publications (1)

Publication Number Publication Date
WO2003035544A1 true WO2003035544A1 (fr) 2003-05-01

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ID=9924276

Family Applications (1)

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PCT/GB2002/004737 WO2003035544A1 (fr) 2001-10-22 2002-10-18 Convertisseur compact

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GB (2) GB0125295D0 (fr)
WO (1) WO2003035544A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008073696A1 (fr) * 2006-12-14 2008-06-19 Uop Llc Conception d'un échangeur thermique pour une liquéfaction de gaz naturel

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0529329A2 (fr) * 1991-08-09 1993-03-03 Ishikawajima-Harima Heavy Industries Co., Ltd. Assemblage sous forme de plaques d'un appareil pour la convertion de monoxide de carbone
WO2001010773A1 (fr) * 1999-08-07 2001-02-15 Lattice Intellectual Property Ltd. Reacteur compact
WO2001054807A1 (fr) * 2000-01-27 2001-08-02 Battelle Memorial Institute Procede et appareil permettant d'obtenir une vitesse de production amelioree de reactions chimiques thermiques

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB656560A (en) * 1947-02-05 1951-08-29 Kellogg M W Co Improvements in or relating to hydrogenation of carbon oxides
US6309768B1 (en) * 1999-07-02 2001-10-30 International Fuel Cells Llc Process for regenerating a carbon monoxide oxidation reactor
CA2413388C (fr) * 2000-06-29 2009-12-22 H2Gen Innovations Inc. Dispositif ameliore de production d'hydrogene par reformage a la vapeur d'hydrocarbures et reacteur chimique integre servant a la production d'hydrogene a partir d'hydrocarbures

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0529329A2 (fr) * 1991-08-09 1993-03-03 Ishikawajima-Harima Heavy Industries Co., Ltd. Assemblage sous forme de plaques d'un appareil pour la convertion de monoxide de carbone
WO2001010773A1 (fr) * 1999-08-07 2001-02-15 Lattice Intellectual Property Ltd. Reacteur compact
WO2001054807A1 (fr) * 2000-01-27 2001-08-02 Battelle Memorial Institute Procede et appareil permettant d'obtenir une vitesse de production amelioree de reactions chimiques thermiques

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008073696A1 (fr) * 2006-12-14 2008-06-19 Uop Llc Conception d'un échangeur thermique pour une liquéfaction de gaz naturel

Also Published As

Publication number Publication date
GB0224287D0 (en) 2002-11-27
GB0125295D0 (en) 2001-12-12
GB2384196A (en) 2003-07-23

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