WO2001094005A1 - Reacteur catalytique a plaques avec recuperation interne de la chaleur - Google Patents

Reacteur catalytique a plaques avec recuperation interne de la chaleur Download PDF

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Publication number
WO2001094005A1
WO2001094005A1 PCT/CH2001/000348 CH0100348W WO0194005A1 WO 2001094005 A1 WO2001094005 A1 WO 2001094005A1 CH 0100348 W CH0100348 W CH 0100348W WO 0194005 A1 WO0194005 A1 WO 0194005A1
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Prior art keywords
reactor
plate
reaction
wall
exothermic
Prior art date
Application number
PCT/CH2001/000348
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German (de)
English (en)
Inventor
Konrad Geissler
Tilman Schildhauer
Original Assignee
Paul Scherrer Institut
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Filing date
Publication date
Application filed by Paul Scherrer Institut filed Critical Paul Scherrer Institut
Priority to AU60009/01A priority Critical patent/AU6000901A/en
Publication of WO2001094005A1 publication Critical patent/WO2001094005A1/fr

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Classifications

    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H01M8/0625—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material in a modular combined reactor/fuel cell structure
    • H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
    • 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
    • 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
    • C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
    • 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
    • C01B3/384—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 the catalyst being continuously externally heated
    • 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
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • 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
    • B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
    • 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
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2458—Flat plates, i.e. plates which are not corrugated or otherwise structured, e.g. plates with cylindrical shape
    • 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
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2459—Corrugated 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
    • 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
    • B01J2219/2465—Two reactions in indirect heat exchange with each other
    • 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
    • B01J2219/2483—Construction materials of the plates
    • B01J2219/2485—Metals or alloys
    • 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
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells
    • 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
    • Y02P20/10—Process efficiency

Definitions

  • the present invention relates to a process for carrying out at least one exothermic and at least one endothermic reaction according to the preamble of claim 1 and to a catalytic plate reactor for carrying out the process.
  • Thermal control is an important factor for optimizing the reaction process.
  • conventional fixed bed reactions e.g. These reactions often cause an unbalanced temperature profile, i.e. For example, undesirable temperature peaks can occur or the reaction can be brought to a standstill locally or freeze due to excessively low temperatures.
  • the selectivity of the reactions is also influenced by the choice of a specific catalyst, the selectivity often being temperature-dependent. In other words, the selectivity is disturbed by an unbalanced temperature profile. A catalyst can also become unstable or damaged if the temperature is too high.
  • run away i.e. a rapid development of the reaction rate with an uncontrolled increase in the temperature level.
  • EP-0 885 653 proposes a compact fixed bed reactor for catalytic reactions with integrated heat exchange.
  • two fluid paths separated by a wall are provided in a reactor, in particular for an exothermic fluid and an endothermic fluid, the exothermic reaction supplying the heat required for the endothermic reaction.
  • US Pat. No. 3,860,535 describes the combination of an oxidation and a reduction reaction in the same reactor, the heat generated in one reaction being used for the conditioning of the other reaction.
  • the catalytic purification of exhaust gases is described in particular, wherein NO x constituents are reduced in the first pass through the reactor and hydrocarbons and carbon monoxide are oxidized in a second pass, which is conducted separately in countercurrent.
  • a water vapor reforming reactor is similarly described in EP 0 967 005, in which in one and the same reactor an oxidation stage for carrying out the catalytic oxidation reaction with the downstream reformer stage for carrying out the water vapor reforming reaction is thermally coupled, in that the two reactions are carried out by a thermally conductive partition are separated.
  • the reactions are carried out by means of conventional oxidation catalysts or reforming catalysts which are arranged in the form of a pellet bed or a conventional fixed bed.
  • the present invention has for its object to propose a further variant of a reaction control of catalytic reactions, in which the thermal control can be further optimized.
  • the task is the thermal coupling of an endothermic with an exothermic reaction, the reaction and the design of the reactor used for this should be as simple as possible and the most efficient heat exchange possible between the two reactions.
  • the tasks are solved by a method according to the wording of claim 1.
  • a process is proposed for carrying out at least one exothermic and at least one endothermic reaction in one and the same reactor housing, the exothermic and the endothermic reaction in the same fluid stream being at least partially locally separated.
  • a reactor is proposed for carrying out the method according to the invention, in which the fluid flows past a plate coated on both sides and is partially converted thereon. At the opposite end of the plate, the fluid is redirected so that it can then be converted further on the back of the plate. If the sign of the sum of the heat shades of the reactions taking place on the front side in a certain plate section is opposite to the sign of the sum of the heat shades of the reactions taking place on the corresponding plate section of the back side, the heat flow in the plate causes a temperature equalization between the two plate sides and thus achieved between the fluids. For example, an exothermic reaction on the front of the plate can be coupled with an endothermic reaction on the back of the plate. This reduces the temperature peak that occurs due to the exothermic reaction.
  • a feature of the present invention is that on the one hand both at least one exothermic and at least one endothermic reaction take place in one and the same fluid stream and in one and the same reactor, or the reactions are carried out in one and the same reaction space.
  • Both the exothermic and the endothermic reaction can be favored by different selection of the catalysts or else by a reaction partner participating in one reaction, the reaction of which is kinetically favored, at least almost completely used up, as a result In the absence of this reaction partner, the other kinetically less favored reaction, which has an opposite shade of heat, is promoted and leads to the implementation of further reaction partners.
  • the type of reactor suitable for the reaction according to the invention has the following properties:
  • FIG. 1 in perspective and schematic representation, a catalytic plate reactor defined according to the invention
  • Fig. 2 in perspective and schematic representation, one
  • Fig. 2a shows the section along the line I-I from FIG. 2,
  • FIG. 4a and 4b schematically depict the gas flow through the various plate reactors mentioned above,
  • Fig. 6 is a corrugated, catalytically coated plate on both sides, and
  • the reactor suitable for the invention is shown schematically and in perspective in FIG. 1, the reactor being particularly well suited for the production of hydrogen in mobile reactor systems, for example for the supply of fuel cells, so that the advantages are exemplified by autothermal methanol -Reformation can be best explained.
  • a plurality of catalytically coated plates 3 are arranged in a reactor housing 1, on which the catalytically favored exothermic and endothermic reactions take place along both sides.
  • reaction 1 can proceed according to the following scheme:
  • this reaction can be, for example, the following:
  • the working principle of the reactor will be explained in more detail with reference to FIG. 5, in which the structure of a catalytically coated plate is shown in section.
  • the working principle is based on the need to redistribute the heat in the reactor as well as possible when coupling exothermic and endothermic reactions, since the two reactions usually do not take place in the same place. Purely convective transport is often out of the question because of the low heat capacity of the gaseous reaction mixture, so the heat can essentially only be transferred by conduction.
  • Heat transport is optimal if the limiting heat transfer from gas to solid and vice versa can also be avoided. This is possible by using a metal plate 4 coated on both sides with a catalyst 6, since the heat of the exothermic reaction is thus conducted from the catalyst directly through the plate to the other side on which the endothermic reaction takes place. As can be seen in FIG. 1, the feed flows along the downstream side of the plate, the exothermic reaction 1 taking place until a limiting educt concentration has been reached completely (e.g. complete oxygen consumption in the autothermal reforming of methanol); The heat generated is then used for the endothermic reaction of the redirected fluid (e.g. steam reforming of methanol).
  • a limiting educt concentration e.g. complete oxygen consumption in the autothermal reforming of methanol
  • the reaction used for the explanation of the catalytically coated plate 3 for the production of hydrogen is of course only an example, which is particularly well suited. It is also not a requirement that the plate be made from sheet steel. Of course, other suitable materials can also be used for this, which allow good heat transfer. Again, it is not a requirement that the plate be coated on both sides with one and the same catalyst, for example it is also possible to use a catalyst responsible for carrying out the exothermic reaction and on the opposite side another catalyst which is responsible for favoring endothermic reaction. Again, it is possible to use a corrugated plate catalytically coated on both sides instead of a straight plate, as shown schematically for example with reference to FIG.
  • the plates 3 coated with the catalyst are to be arranged next to one another as parallel, flat plates, but the plates can also be formed, for example, as tubes arranged concentrically to one another, as to one another laterally displaced plates, sloping plates, etc.
  • reactor optimization how to arrange the individual plates coated with the catalyst inside the reactor. It is also quite possible that, for example, the exothermic reaction 1 is at least largely exhausted even before the deflection path 9 is reached and the endothermic reaction 2 already starts in the fluid flow before this deflection path 9 is reached. This does not play a role in itself, since due to the good thermal conductivity of the catalytically coated plate 3, it is of course also possible for heat to flow in the plane of the plate itself and not only perpendicular to the plane of the plate.
  • the plates coated with the catalyst can for example be corrugated, or can also be ribbed, folded or provided with any embossing.
  • the plates coated with the catalyst can be structured or provided with any embossing.
  • the reactor proposed according to the invention or the process carried out in this reactor is, for example, also generally suitable for the reaction or the degradation of hydrocarbon compounds, it being possible to work with the same catalyst on both sides of the plate and with different catalysts ,
  • the inventive principle is suitable for the catalytic afterburning of unreacted products of endothermic reactions.
  • Other possible applications include autothermal reactions, such as the production of synthesis gas by autothermal reforming of hydrocarbons or oxidative dehydrogenation.
  • the fluid can be both gases or gas mixtures as well as liquids or liquid mixtures.
  • the fluid can be both gases or gas mixtures as well as liquids or liquid mixtures.
  • Plates which can also be aligned at an angle, evenly distributed over the entire width of the plate, the length of the plates up to the fluid deflection is the only geometric parameter of the reaction design.
  • a scale-up is thus done by simply spreading the plates or by
  • FIGS. 2 and 2a Design variant of a reactor according to the invention, as shown in FIGS. 2 and 2a.
  • a significantly flatter temperature profile 51 could be measured in the plate reactor according to FIG. 2 despite complete air conversion shown in a tubular reactor in profile 52, in which the autothermal methanol reforming took place at the same catalyst load with stoichiometric air addition to 500 mg of catalyst.
  • a heterogeneous catalytic reactor is advantageously constructed in such a way that the catalyst can be changed without having to replace essential pressure-resistant parts. Therefore, the aim for the plate reactor described here is to install the plates as a replaceable insert in a pressure-resistant housing, this housing should ideally also contain the distribution of the fluid to the supply lines and the discharge lines of the product.
  • the interchangeable insert can now be carried out, for example, by connecting a plurality of catalytic plates via spacers which, as shown in FIGS. 2 and 2a, can be designed, for example, in a horseshoe shape and can contain parts of the feed and discharge lines of the fluid.
  • FIG. 3 Another possible construction is shown in FIG. 3 and consists in the use of plates 33 folded in a harmonic shape parallel to the direction of flow, as shown in FIG. 3.
  • a similar design is described in EP 0 885 653 A3, but for two different fluid flows and using spacers between the sheets, which have no rear contact with the opposite fluid flow and thus do not allow direct heat exchange between the two reaction zones. Due to the concertina folding, the inlet and outlet lines 35 and 43 can each be accommodated on separate sides of the reactor housing, and the number of sealing surfaces required is also reduced.
  • a further reduction in the number of sealing surfaces can be achieved by using both plate ends instead of one plate end for the diversion 39 of the fluid.
  • the supply and discharge 35 and 43 of the fluid must preferably take place in the middle of the plate length in the direction of flow.
  • 4a and 4b schematically illustrate the gas flow as it takes place in the various reactors shown in FIGS. 1 to 3 using schematic diagrams. 4a relates to the gas flow, for example through a reactor according to FIG. 1, where only a deflection 9 takes place at one end of the plate.
  • the reactors described are suitable for the production of hydrogen in mobile reactor systems, for example for the supply of fuel cells, so that the advantages are explained using the example of autothermal methanol reforming.
  • the previously known reactor concepts for on-board hydrogen production are either classic fixed bed reactors, as described in the article by Jenkins, W., Shut, E (1989) Platinum Metals Reviews 33 (3), 118, heat exchanger reactors with external heating, as described by Kohnke, HJ, development of a methanol reformer based on a plate concept, diss. University comprehensive college
  • a key advantage of the design compared to fixed bed reactors is the expected problem-free scaling up. This would be achieved by simply widening or increasing the number of plates. A change in the thermal behavior is not to be expected, since the ratio of catalyst mass and heat exchange area does not change.
  • At least one exothermic and one endothermic reaction is carried out in one and the same fluid stream for carrying out the method proposed according to the invention, the reaction taking place largely on opposite sides of a plate-like wall which is at least in partial areas, for example in the form of a strip or is coated in spots with a catalyst.
  • the exothermic reaction is at least largely exhausted before reaching the deflection to the opposite side in the fluid flow and the endothermic reaction can already start on the same side of the plate-like wall on which the exothermic reaction takes place .
  • a heat flow takes place in the plate plane, specifically from the region of the exothermic reaction to the end region in which the endothermic reaction takes place.
  • the exothermic reaction it is possible for the exothermic reaction to extend beyond the deflection region to the opposite side of the plate-like wall before the endothermic reaction then begins.

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  • Engineering & Computer Science (AREA)
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  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
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  • Sustainable Energy (AREA)
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  • General Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Electrochemistry (AREA)
  • Sustainable Development (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un procédé de mise en oeuvre au moins d'une réaction exothermique et au moins d'une réaction endothermique dans un même et unique caisson de réacteur. Selon ledit procédé, la réaction exothermique et la réaction endothermique sont produites dans le même flux fluidique de façon localement séparée au moins partiellement. Ce flux fluidique est dirigé le long d'une paroi (3) sous forme de plaque dotée des deux côtés au moins partiellement d'un revêtement catalytique et mis en réaction au moins partiellement sur ladite paroi. Le fluide est alors dévié au niveau d'une extrémité (9) de la paroi puis mis à nouveau en réaction le long de la face arrière de cette paroi. De plus, le signe de la somme de la chaleur de réaction des réactions se produisant sur la face avant de la paroi est opposé au signe de la somme de la chaleur de réaction des réactions se produisant sur la face arrière.
PCT/CH2001/000348 2000-06-08 2001-06-06 Reacteur catalytique a plaques avec recuperation interne de la chaleur WO2001094005A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU60009/01A AU6000901A (en) 2000-06-08 2001-06-06 Catalytic plate reactor with internal heat recovery

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH1124/00 2000-06-08
CH11242000 2000-06-08

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WO2001094005A1 true WO2001094005A1 (fr) 2001-12-13

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1234612A2 (fr) * 2001-02-21 2002-08-28 DEG Intense Technologies & Services GmbH Réacteur pour des réactions catalytiques
DE10359205A1 (de) * 2003-12-17 2005-07-14 Webasto Ag Reformer und Verfahren zum Umsetzen von Brennstoff und Oxidationsmittel zu Reformat
US6936238B2 (en) * 2002-09-06 2005-08-30 General Motors Corporation Compact partial oxidation/steam reactor with integrated air preheater, fuel and water vaporizer
EP1681094A3 (fr) * 2005-01-17 2006-10-11 Basf Aktiengesellschaft Réacteur avec au moins deux chambres de réaction séparées
WO2007004888A1 (fr) * 2005-07-01 2007-01-11 Norsk Hydro Asa Reacteur destine au melange et a la reaction de deux ou plusieurs fluides, ainsi qu'au transfert de chaleur entre lesdits fluides, et procede permettant de faire fonctionner ledit reacteur
DE102006033441A1 (de) * 2006-06-29 2008-01-03 Webasto Ag Reformer für ein Brennstoffzellensystem
DE102007018311A1 (de) * 2007-04-18 2008-10-23 Enerday Gmbh Zweistufiger Reformer und Verfahren zum Betreiben eines Reformers
DE102007017787A1 (de) * 2007-04-16 2008-10-30 Enerday Gmbh Reformer mit einer Katalysatoreinrichtung und einem Wärmeübertrager sowie Verfahren zum Betreiben eines Reformers
WO2011051696A1 (fr) * 2009-10-26 2011-05-05 Compactgtl Plc Réacteur traversé de canaux
EP2520542A1 (fr) 2011-05-04 2012-11-07 Vaillant GmbH Réformateur
DE102014004264A1 (de) 2014-03-14 2015-09-17 Universität Stuttgart Wärmeintegrierte Hochtemperatur-Reaktoren für die autotherme partielle Oxidation
US20230008708A1 (en) * 2021-07-08 2023-01-12 U.S. Army DEVCOM, Army Research Laboratory Highly heat recirculating multiplexed reactors

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EP0885653A2 (fr) * 1997-06-16 1998-12-23 Gerhard Friedrich Réacteur à lit fixe avec échange de chaleur intégrée pour des réactions catalytiques
EP0887307A1 (fr) * 1997-06-28 1998-12-30 dbb fuel cell engines GmbH Dispositif pour la production d' un gaz riche en hydrogène et procédé pour sa mise en marche
WO1999053561A1 (fr) * 1998-04-16 1999-10-21 International Fuel Cells, Llc Reformeur de gaz combustible a paroi impregnee d'un complexe catalytique
EP0967005A2 (fr) * 1998-06-23 1999-12-29 dbb fuel cell engines GmbH Réacteur de reformage à vapeur d'eau, spécialement avec contrÔle d'un procédé autothermique

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US5846494A (en) * 1992-04-30 1998-12-08 Gaiser; Gerd Reactor for catalytically processing gaseous fluids
EP0885653A2 (fr) * 1997-06-16 1998-12-23 Gerhard Friedrich Réacteur à lit fixe avec échange de chaleur intégrée pour des réactions catalytiques
EP0887307A1 (fr) * 1997-06-28 1998-12-30 dbb fuel cell engines GmbH Dispositif pour la production d' un gaz riche en hydrogène et procédé pour sa mise en marche
WO1999053561A1 (fr) * 1998-04-16 1999-10-21 International Fuel Cells, Llc Reformeur de gaz combustible a paroi impregnee d'un complexe catalytique
EP0967005A2 (fr) * 1998-06-23 1999-12-29 dbb fuel cell engines GmbH Réacteur de reformage à vapeur d'eau, spécialement avec contrÔle d'un procédé autothermique

Cited By (19)

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Publication number Priority date Publication date Assignee Title
EP1234612A3 (fr) * 2001-02-21 2003-05-21 DEG Intense Technologies & Services GmbH Réacteur pour des réactions catalytiques
EP1234612A2 (fr) * 2001-02-21 2002-08-28 DEG Intense Technologies & Services GmbH Réacteur pour des réactions catalytiques
US6936238B2 (en) * 2002-09-06 2005-08-30 General Motors Corporation Compact partial oxidation/steam reactor with integrated air preheater, fuel and water vaporizer
DE10338240B4 (de) * 2002-09-06 2006-08-03 General Motors Corp., Detroit Kompakter Partialoxidations-/Wasserdampfreaktor mit integriertem Luftvorheizer und Brennstoff- und Wasserstoffverdampfer
DE10359205B4 (de) * 2003-12-17 2007-09-06 Webasto Ag Reformer und Verfahren zum Umsetzen von Brennstoff und Oxidationsmittel zu Reformat
DE10359205A1 (de) * 2003-12-17 2005-07-14 Webasto Ag Reformer und Verfahren zum Umsetzen von Brennstoff und Oxidationsmittel zu Reformat
EP1681094A3 (fr) * 2005-01-17 2006-10-11 Basf Aktiengesellschaft Réacteur avec au moins deux chambres de réaction séparées
JP2008544846A (ja) * 2005-07-01 2008-12-11 ノルスク・ヒドロ・アーエスアー ２つ以上の流体を混合及び反応させると共に当該流体間で熱を移動させる反応器、及び当該反応器を操作する方法
WO2007004888A1 (fr) * 2005-07-01 2007-01-11 Norsk Hydro Asa Reacteur destine au melange et a la reaction de deux ou plusieurs fluides, ainsi qu'au transfert de chaleur entre lesdits fluides, et procede permettant de faire fonctionner ledit reacteur
DE102006033441A1 (de) * 2006-06-29 2008-01-03 Webasto Ag Reformer für ein Brennstoffzellensystem
DE102006033441B4 (de) * 2006-06-29 2009-05-07 Enerday Gmbh Reformer für ein Brennstoffzellensystem
DE102007017787A1 (de) * 2007-04-16 2008-10-30 Enerday Gmbh Reformer mit einer Katalysatoreinrichtung und einem Wärmeübertrager sowie Verfahren zum Betreiben eines Reformers
DE102007018311A1 (de) * 2007-04-18 2008-10-23 Enerday Gmbh Zweistufiger Reformer und Verfahren zum Betreiben eines Reformers
DE102007018311B4 (de) * 2007-04-18 2008-12-04 Enerday Gmbh Zweistufiger Reformer und Verfahren zum Betreiben eines Reformers
WO2011051696A1 (fr) * 2009-10-26 2011-05-05 Compactgtl Plc Réacteur traversé de canaux
EP2520542A1 (fr) 2011-05-04 2012-11-07 Vaillant GmbH Réformateur
DE102011100417A1 (de) * 2011-05-04 2012-11-08 Vaillant Gmbh Reformer
DE102014004264A1 (de) 2014-03-14 2015-09-17 Universität Stuttgart Wärmeintegrierte Hochtemperatur-Reaktoren für die autotherme partielle Oxidation
US20230008708A1 (en) * 2021-07-08 2023-01-12 U.S. Army DEVCOM, Army Research Laboratory Highly heat recirculating multiplexed reactors

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