WO2014117953A1 - Unité de reformage pour système de pile à combustible - Google Patents

Unité de reformage pour système de pile à combustible Download PDF

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Publication number
WO2014117953A1
WO2014117953A1 PCT/EP2014/000291 EP2014000291W WO2014117953A1 WO 2014117953 A1 WO2014117953 A1 WO 2014117953A1 EP 2014000291 W EP2014000291 W EP 2014000291W WO 2014117953 A1 WO2014117953 A1 WO 2014117953A1
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WO
WIPO (PCT)
Prior art keywords
reformer
burner
line
longitudinal axis
central longitudinal
Prior art date
Application number
PCT/EP2014/000291
Other languages
German (de)
English (en)
Inventor
Michael Reissig
Juergen Rechberger
Arthur Kliment
Original Assignee
Avl List Gmbh
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 Avl List Gmbh filed Critical Avl List Gmbh
Priority to DE112014000673.4T priority Critical patent/DE112014000673A5/de
Publication of WO2014117953A1 publication Critical patent/WO2014117953A1/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
    • 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
    • B01J8/0242—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 flow within the bed being predominantly vertical
    • B01J8/025—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 flow within the bed being predominantly vertical in a cylindrical shaped bed
    • 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
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/0285—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
    • C01B3/02—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
    • 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
    • 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
    • B01J2208/00212—Plates; Jackets; Cylinders
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—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
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • 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
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
    • 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
    • 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
    • C01B2203/1288—Evaporation of one or more of the different feed components
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • 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
    • C01B2203/1604—Starting up the process
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04097—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with recycling of the reactants
    • 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
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • 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 invention relates to a reformer unit, in particular for a fuel cell system, with a burner, which has a combustion chamber, a reformer, which at least partially in the
  • Combustion chamber is arranged and a first line, the
  • Reformer with process gas which in particular recirculated
  • Anode exhaust gas and hydrocarbons has supplied.
  • Such a reformer unit can, for example, in a
  • Energy generating unit are used with a fuel cell, which with hydrocarbons and not with pure
  • Such fuel cell systems form a compact and efficient energy source, in particular for
  • Multimedia technology such as radio, TV and
  • the low efficiency is not only energy
  • Reaction energy of a continuously supplied fuel and an oxidizing agent is converted directly into electrical energy, without energy losses caused by a coupling
  • Methanol formic acid, methane or the like as a fuel.
  • DE 10 2007 039 594 A1 therefore discloses on the one hand, the reformer and other elements that are necessary for reforming, and to arrange a fuel cell stack in a compact design in a common external insulation. Furthermore, this document proposes to recycle anode exhaust gas into the reformer in order to utilize the heat energy contained in the exhaust gas and to use the chemical substances contained therein for reforming.
  • the reformer is this purpose in a cylindrical combustion chamber of a
  • Flame burner arranged to heat the reformer in the starting phase. By applying the reformer wall with hot gas, this is heated and the reformer is a homogeneous
  • the present invention has for its object to provide a reformer unit with such a reformer, which is compact, universally applicable and energy-efficient.
  • a burner according to the invention is a device for
  • a combustion chamber in the context of the invention is used for combustion and / or mixing of fuel and oxidant.
  • Reforming or reforming for the production of a synthesis gas which contains at least hydrogen, in particular
  • a reformer is accordingly an apparatus for reforming.
  • a manifold according to the invention is a part of the housing of the reformer.
  • the manifold serves, in particular, to conduct a process gas to a reforming catalyst, to mix it and / or to distribute it homogeneously over the surface of a reforming catalyst.
  • the manifold is designed as a connection piece and can be referred to as distributor or process gas distributor.
  • a fuel cell according to the invention is a galvanic cell, which converts the chemical reaction energy of a continuously supplied fuel and an oxidizing agent into electrical energy.
  • a galvanic cell which converts the chemical reaction energy of a continuously supplied fuel and an oxidizing agent into electrical energy.
  • usually several cells are connected in series to a stack (engl., For 'stack').
  • a flow direction in the context of the invention is the
  • a longitudinal axis in the sense of the invention is that axis of a
  • Body corresponding to the direction of its greatest extent and / or its axis of symmetry.
  • a central longitudinal axis is
  • the longitudinal axis in the center of a body corresponds to a cylinder of
  • Deflection means in the sense of the invention are means for interrupting or swirling a fluid flow.
  • An overlap in the sense of the invention is a projection in a defined direction.
  • a flow volume is the volume which is available to a fluid as it flows through a device.
  • a process temperature in the sense of the invention is the temperature which in a device when executing a respective
  • Isolation in the sense of the invention is any type of
  • Adiabatic in the sense of the invention means that in the overall process of the power generation unit, both exothermic and endothermic reactions take place in parallel, so that the overall process in the power generation unit
  • Hydrocarbon-containing energy is converted into electrical energy.
  • the reformer unit according to the invention has a
  • Manifold in which a first line with process gas for the reformer opens.
  • downstream arranged inflow surface of the reforming catalyst achieved.
  • the at least one outer surface of the manifold is spaced from the respective opposite surface of the combustion chamber.
  • Reformer unit to a starting burner, the exhaust gas is inserted into the burner.
  • the starting burner provides during the starting phase of the
  • a flame tube of the starting burner protrudes into the combustion chamber.
  • the hot exhaust gas of the starting burner can be aimed at the reformer during the starting phase.
  • Anode exhaust gas and / or cathode exhaust air of the fuel cell of a fuel cell system which during the start-up phase does not yet have the temperatures required to bring about the reforming, however, are forced into the outer regions of the combustion chamber, where they essentially come into contact with the walls of the combustion chamber, but not with the manifold and / or other surfaces of the reformer.
  • the burner and / or the starting burner are arranged in such a way that a central longitudinal axis of the reformer, a central longitudinal axis of the burner and / or a central longitudinal axis of the starting burner aligned substantially parallel and in particular identical are.
  • the reformer is optimally flows around during the start phase of the exhaust gases of the starting burner, thereby enabling a speedy achievement of the operating temperature of the reformer.
  • baffles cause turbulence of the exhaust stream from the starting burner, so that the manifold or other walls of the reformer are heated excessively uniformly and not an upstream surface of the reformer.
  • the manifold of the reformer at least partially on the shape of a cone or a truncated cone.
  • the conical or truncated cone shape further leads to a
  • the reformer is optimally flown inside with educt gas or reformer process gas.
  • Entry point into the reformer substantially 45 ° to 135 °, preferably 70 ° to 110 °, more preferably 80 ° to 100 °, and most preferably 90 °.
  • a tangent to the flow direction of the first line divides at one
  • Ratio 4 1, preferably 3: 1, more preferably 2: 1,
  • a second line supplies the burner with air, in particular cathode exhaust air
  • a third line supplies the burner with fuel gas, in particular substantially anode exhaust gas, wherein the third line opens downstream of the second line in the combustion chamber or the third
  • both gas streams are ideally mixed.
  • the third line may also be previously in the second line, whereby the fuel of the burner with the Oxidizing agent or the air is already mixed before the gases are introduced into the combustion chamber.
  • the angle between each of the flow direction of the second conduit and / or the third conduit and a central longitudinal axis of the burner at an entry point into the burner is substantially 45 ° to 135 °, preferably 70 ° to 110 °, more preferably 80 ° to 100 °, and most preferably 90 °.
  • the burner has a burner catalyst which is arranged in a thermally conductive manner around the reformer and / or the reformer has a reforming catalyst.
  • the improved heat dissipation prevents particularly hot zones (hot spots) in the two catalysts. This is particularly advantageous for heating the reforming catalyst.
  • sealing means such as a sealing mat, can be dispensed with, which additionally hinder the heat exchange.
  • a substrate of the burner catalyst carries the reformer.
  • the reforming catalyst overlaps with the burner catalyst in the axial direction a quarter, preferably one third, more preferably three quarters and most preferably completely or the overlap of the reformer is variable.
  • Reformer catalyst controls significantly the thermal conduction between the burner and the reformer.
  • Burner catalyst substantially 1: 1, preferably 1: 1.5,
  • the burner catalyst is then in relation to the
  • Reformer catalyst sized large enough, so that in the case of the maximum possible power, in particular a load shedding, no damage to the system caused by overheating.
  • the burner is at least partially disposed in an exhaust gas chamber and preferably has a central longitudinal axis, which is coaxial with the central longitudinal axis of the combustion chamber and / or the Manifolds.
  • the arrangement of the reformer unit in the exhaust chamber allows further isolation from the environment.
  • the reformer unit preferably comes in one
  • Power generation unit with a fuel cell a so-called fuel row system, in particular for a vehicle used.
  • Hydrocarbons which are already present in many vehicles in the form of diesel or gasoline, to operate a
  • Fuel cell can be used.
  • the reformer unit according to the invention is not limited to use in vehicles, but can also be used in purely stationary applications such as cogeneration plants in buildings.
  • FIG. 1 is a partially schematic process picture of a
  • Figure 2 shows a partially schematic cross section of
  • Fuel cell system with a first embodiment of a reformer unit according to the invention Fuel cell system with a first embodiment of a reformer unit according to the invention.
  • FIG. 3 shows a partially schematic, perspective cross-section of the first embodiment of the invention
  • FIG. 4 shows a partially schematic, perspective cross section of a second embodiment of the reformer unit according to the invention.
  • FIG. 5 shows a partially schematic, perspective cross section of a third embodiment of the reformer unit according to the invention.
  • Figure 6 shows a schematic representation of the geometric
  • FIG. 7 shows a partially schematic cross section through the second embodiment of the reformer unit according to FIG. 4.
  • the functional principle of the reformer unit 1 according to the invention is explained as follows in an application in a fuel cell system 2 or a power generation unit with a fuel cell on the basis of the process picture according to FIG.
  • Hydrocarbon is supplied. Furthermore, with the air blower 29 via the air connection 33, the fuel cell system. 2
  • Air and the hydrocarbons are preferably in the
  • Start burner 11 heated and ignited. This heats the
  • the exhaust gas of the starting burner 11, which flows out of the combustion chamber 4 of the burner 3, is preferably passed through a heat exchanger 28 to the exhaust port 34, which is preferably an exhaust. Air is heated in the heat exchanger 28 and subsequently flows to the cathode K of the fuel cell stack 22a, 22b.
  • air is conveyed to the recirculation fan 30 in the reformer 5, where this by the exhaust gas of the
  • Start burner 11 is heated and then by a preferably present first distributor plate 20 and a preferably existing second distributor plate 27 to the anode A of the
  • Fuel cell stack 22a, 22b is passed.
  • the gas flows into the evaporator 26.
  • hydrocarbons are also pumped via the hydrocarbon pump 35a to the evaporator, which evaporate through the heated anode exhaust gas in the evaporator 26.
  • This gas mixture is preferably mixed with air in the recirculation blower 30 to reformer process gas, the educt gas, and introduced into the reformer 5 via a first line 6 through the combustion chamber 4, in which the process gas is further heated.
  • the reformer 5 is now preferably heated by the starting burner 11 so far that a reforming of the reformer process gas to hydrogen and by-products, the product gas, takes place.
  • This reformate is in turn passed via the distributor plate 27 to the anode of the fuel cell 2, where now the conversion of substantially hydrogen and oxygen to water and
  • the heated cathode exhaust air is passed into the combustion chamber 4 of the burner 3. A portion of the heated anode exhaust gas is preferably returned to the evaporator 26. Another part of the
  • Anode exhaust gas is passed into the combustion chamber 4 of the burner 3.
  • this anode exhaust gas is mixed with the cathode exhaust air and preferably reacted by means of a catalyst in an exothermic reaction.
  • Heat energy is used to heat the reformer 5.
  • the starting burner 11 may preferably now be turned off.
  • Reformer catalyst 21 is heated solely by the heat of the exothermic reaction in the fuel cell stack 22a, 22b and the exotherm Reaction in the burner 3 is activated, so that the overall process in the power generation unit is substantially adiabatic.
  • Fuel cell system 2 preferably has the burner 3 with the combustion chamber 4, the reformer 5 with the Manifold 7, the
  • the starting burner 11 with flame tube 12th is the starting burner 11 with flame tube 12th
  • a bypass line (not shown) may be provided from the starting burner 11 directly into the heat exchanger 28.
  • a bypass line (not shown) may be provided from the starting burner 11 directly into the heat exchanger 28.
  • Fig. 2 shows the structure of an embodiment of a
  • Reformer unit 1 by a plane containing the central longitudinal axis ZF of the flame tube 12 (Strich Louist), central longitudinal axis ZB of the burner 3 (dotted) and central longitudinal axis ZR of the reformer 5 (dashed).
  • the fuel cell system 2 has primarily facilities that serve for media supply, for interrupting the media supply or regulation of the media supply and / or for the preparation of the media. Exemplary of this are the
  • Hydrocarbon pumps 35a, 35b Preferably is also a
  • Heat exchanger 28 is present, which heats the intake air, before being supplied to the cathode K of the fuel cell stacks 22a, 22b.
  • the reformer unit 1 is arranged in the center of the fuel cell system 2. This essentially comprises the means for reforming or converting the hydrocarbons into reformate or process gas for the fuel cell stack 22a, 22b.
  • the reformer is preferably arranged in the combustion chamber 4 of the burner 3.
  • the burner 3 is in turn preferably arranged in an exhaust gas chamber 23, in which the exhaust gas of the burner 3 and / or the exhaust gas of the starting burner 11 is conducted to the heat exchanger 28.
  • the start burner 11 is used in particular to the
  • the evaporator 26 is arranged, which hydrocarbons in the of the
  • Fuel cell 2 recirculated anode exhaust gas evaporates before it is introduced into the reformer 5.
  • the starting burner 11 and / or the burner 3 serve to heat the reformer 5.
  • the exhaust gas chamber 23 in turn heats the outer wall of the burner 3 or additionally insulates the burner from the environment.
  • Exhaust gas chamber 23 simultaneously provides heat energy for vaporization of the hydrocarbons in evaporator 26.
  • Embodiment are from the reformer unit 1 on the
  • Fuel cell stacks 22a, 22b are preferably via the Distributor plate 20, 27 connected to the respective terminals of the reformer unit.
  • the reformer 5 preferably has a reforming catalyst 21 and the burner 3 has a burner catalytic converter 19.
  • the combustion chamber 4 and the exhaust chamber 23 is bounded by a wall 10b, which is at the same time a fixing plate.
  • a wall 10b which is at the same time a fixing plate.
  • these extend only to the wall and have another, separate
  • the walls of the combustion chamber 4 and / or the exhaust chamber 23 may also be arranged at a distance from a fixing plate.
  • the fuel cell system (2) of the illustrated embodiment has two fuel cell stacks 22a, 22b.
  • the fixation of these two fuel cell stacks 22a, 22b and / or the distribution of the process gas and the other media or removal of the cathode exhaust air and the anode exhaust gas is preferably carried out via the second distributor plate 27, which is connected to the distributor plate 20 to communicate in a fluid-communicating manner.
  • the fuel cell stacks 22a, 22b are preferably made of SOFC fuel cells, but others may be
  • Fuel cell types are used, such. Alkaline fuel cells, polymer electrolyte fuel cells, direct methanol fuel cells, formic acid fuel cells,
  • Phosphoric acid fuel cells Phosphoric acid fuel cells, molten carbonate fuel cells, direct carbon fuel cells and / or magnesium air fuel cells or a combination thereof.
  • the fuel cell system 2 for power generation is preferably surrounded by insulation, which is not shown in FIG.
  • a first embodiment of the reformer unit 1 according to the invention will now be described with reference to FIG. In this
  • both the reformer 5, the burner 3 and the starting burner 11 with its flame tube 12 have a cylindrical shape.
  • the respective central longitudinal axes ZR, ZB, ZF of the three components lie in this embodiment on each other or are coaxial. This leads to a concentric arrangement of the three components.
  • each of the three components may have a shape other than the cylindrical shape and the three components may
  • the hot exhaust gas of the starting burner 11 leaves it via the flame tube 12 and heats the combustion chamber 4 of the burner 3.
  • Reformers flows directly from the exhaust gas jet of the starting burner 11 and thereby heated.
  • the manifold 7 of the reformer 5 on this upstream surface 8 is preferably in the shape of a truncated cone or a cone to the exhaust gas flow from the starting burner 11 to the
  • Burner catalyst 19 evenly distribute, which the
  • Reformer 5 preferably surrounds.
  • unreacted hydrocarbons can be post-combusted and / or harmful exhaust gas substances are converted.
  • the exhaust gas flow preferably flows via exhaust gas openings 37 into the exhaust gas chamber 23 (not in FIG. 3)
  • the reformer 5 consists essentially of two
  • the manifold 7 with the upstream surface 8 and at least one lateral surface 9 forms a hollow body, in which via the first conduit 6, a process gas is introduced, which is to be reformed.
  • An upstream surface 8 and a lateral surface 9 can in this case also the respective
  • Section of the reformer 5 is essentially of this
  • Reforming catalyst 20 is formed. In the reforming catalyst 20, the catalytic reforming takes place. On the side facing away from the Manifold 7 leaves the reformed process gas, the
  • reformate the reformer 5 preferably on the
  • Homogeneity of the current flow of the surface of the reforming catalyst 20 depends largely on the geometry of the arrangement of the first conduit 6, which leads the process gas in the reformer 5, and the manifold 7 from.
  • this geometry is on the one hand on the solid angle ⁇ between a flow direction SR and the
  • this geometry is over a second solid angle in a plane perpendicular to the respective central longitudinal axis ZR; For example, lies, defined.
  • this solid angle ß at a Entry point 14; 17; 18 are determined.
  • FIG. 7 shows such a solid angle with respect to the flow direction SR2 of the second line 15. It has been found to be particularly advantageous to choose the solid angle ⁇ in a range of about 90 ° to 130 °, preferably between 100 ° and 120 ° and on
  • the ratio Sa: Sb is given as a parameter in which the flow direction SR or a tangent to this flow direction SR at the entry point 14; 17; 18 divides a distance S, which on the one hand between the central longitudinal axis ZR;
  • it is arranged.
  • flow direction SRI of the first line 6 intersects the longitudinal axis ZR of the reformer 5 or, in the case of a cylindrical reformer 5 or manifold 7, corresponds to the flow direction SRI of the tangent to the manifold 7 in the direction of rotation, as is pure
  • controlled introduction of the process gases into the burner 3 is also advantageous for thorough mixing and uniform distribution of the gas to be converted to the burner catalyst 19.
  • Ratios of the sections S2a, S2b; S3a, S3b of the S2, S3 routes such as those providing good results with respect to the reformer.
  • Anode exhaust gas substantially tangential to the surface of
  • Combustion chamber 4 i. S2a >> S2b and S3a >> S3b, above the respective ones
  • the substrate of the burner catalyst 19 is preferably made
  • Such substrates have a significantly higher
  • the substrate of the reforming catalyst 21 may be made of metal. Preferably, however, this is made of ceramic. For one thing is such a substrate is more favorable than a metal substrate and good thermal conductivity is less important in this reforming catalyst 21. On the other hand, the ceramic substrate has a better sulfur compatibility and can be used at process temperatures of up to 1000 ° C, which can be significant in extreme operating conditions of the reformer unit 1.
  • the outer shell of the reformer 5 is preferably also made of metal and is preferably connected to the substrate of
  • the reformer 5 is fixed at other locations.
  • other types of attachment for example with a press fit or an additional swelling mat.
  • the reformer 5 is fixed at other locations.
  • Thermal conductivity of the temperature profile (axial and radial) of the reformer and burner catalyst can be homogenized.
  • the degree of overlap may be fixed to a quarter, preferably to one third, more preferably to three quarters and most preferably to a complete overlap of the
  • Reforming catalyst 21 may be set by the burner catalyst.
  • the degree of overlap is variable and changeable during operation of the fuel cell system to adjust the heat exchange to the respective modes of operation.
  • Burner catalyst 19 can be ensured that the
  • Burner catalyst 21 is designed to burn the reformate in the event of a sudden load shedding without causing irreversible damage to the fuel cell system.
  • the ratio is substantially 1: 1, preferably 1: 1.5, more preferably 1: 2, even more preferably 1: 3, and most preferably 1: 3.7.
  • Embodiment a volume of 95,000ccm, the burner catalyst 21 of 358,000ccm on.
  • the reformer unit according to the invention in a partially schematic, perspective cross-sectional view of the reformer unit 1
  • the flame tube 12 of the starting burner 11, the reformer 5 and the Reformermanifold 7 and the combustion chamber 4 of the burner 3 are cylindrical and more preferably concentric with coaxial centric
  • the air supply but also perpendicular to the surface for e'ine particularly good
  • Mixing be introduced into the mixture formation space.
  • a difference from the first embodiment is that the surface 10 b of the combustion chamber is formed or reinforced by a fixing plate used in the fuel cell system 2 for
  • the flame tube can also be flush on the surface 10b of the combustion chamber 4 with the surface 10b of the combustion chamber 4
  • the process gas via the first line 6 as long as possible in the burner chamber 4 is performed in order to transfer the heat energy present in the burner 3 also on this gas
  • the reforming catalyst 21 is not shown.
  • the third line 16 which directs anode exhaust gas into the burner, preferably not directly into the combustion chamber 4 but in the second line 15 opens, which air, preferably cathode exhaust air, into the burner chamber 4 leads. This allows an even better mixing of the
  • preferably cylindrical combustion chamber 4 is the
  • Flow direction SR2 then perpendicular to the surface of the combustion chamber 4.
  • the gas mixture occurs with a
  • FIG. 5 The embodiment illustrated in FIG. 5 in a partially schematic perspective cross-sectional view is shown in FIG.
  • Embodiment can be combined with the embodiments of the first and second embodiments in any way.
  • this embodiment differs from the second embodiment in that between the flame tube 12 of the burner 11 and the upstream surface 8 of the burner
  • Manifolds 7 of the burner 5 deflection means 13, are provided.
  • the deflection means 13 are held in position by a fixing means 31 in the combustion chamber 4 of the burner 3.
  • the deflection means 13 is a metal sheet, which is preferably formed as a ball cap, as shown in Figure 5.
  • the deflection means 13 may be formed as any other two- or three-dimensional structure, such as a plate or as a pyramid and / or consist of other refractory materials.
  • the deflection means 13 recesses, through which a fluid, in particular the exhaust gas of the starting burner 11 can flow. These recesses are preferably, as shown in Figure 5, formed as holes.
  • the deflection means 13 serve to ensure that the outer walls of the manifold 7, in particular the upstream surface 8 and the at least one lateral surface 9, be heated evenly.
  • the deflection means does not cause overheating in this area and the exhaust gas is distributed homogeneously over the burner catalyst 19.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Sustainable Energy (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Electrochemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Manufacturing & Machinery (AREA)
  • Fuel Cell (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

Unité de reformage (1), en particulier pour un système de pile à combustible (2), qui comporte un brûleur (3) pourvu d'une chambre de combustion (4), un reformeur (5) situé au moins en partie dans la chambre de combustion (4), et un premier conduit (6) qui alimente le reformeur (5) en gaz de travail constitué en particulier du gaz d'échappement d'anode recirculé et d'hydrocarbures. Selon l'invention, le reformeur (5) comporte un collecteur (7) dans lequel débouche le premier conduit (6).
PCT/EP2014/000291 2013-02-04 2014-02-04 Unité de reformage pour système de pile à combustible WO2014117953A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
DE112014000673.4T DE112014000673A5 (de) 2013-02-04 2014-02-04 Reformereinheit für Brennstoffzellensystem

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA81/2013A AT513931B1 (de) 2013-02-04 2013-02-04 Reformereinheit für Brennstoffzellensystem
ATA81/2013 2013-02-04

Publications (1)

Publication Number Publication Date
WO2014117953A1 true WO2014117953A1 (fr) 2014-08-07

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AT (1) AT513931B1 (fr)
DE (1) DE112014000673A5 (fr)
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0214432A1 (fr) * 1985-09-11 1987-03-18 Uhde GmbH Appareil pour la production de gaz de synthèse
WO2000027518A1 (fr) * 1998-11-10 2000-05-18 International Fuel Cells, Llc Installation de reformage de gaz combustible d'hydrocarbure pour centrale a piles a combustible
WO2000041804A1 (fr) * 1999-01-19 2000-07-20 International Fuel Cells, Llc Ensemble reformeur compact pour gaz combustible
US20040187386A1 (en) * 2003-03-26 2004-09-30 Wangerow James R. Simplified three-stage fuel processor
DE102007039594A1 (de) * 2006-10-03 2008-04-10 Avl List Gmbh Energieerzeugungseinheit mit zumindest einer Hochtemperaturbrennstoffzelle
US20110067303A1 (en) * 2008-03-24 2011-03-24 Sanyo Electric Co., Ltd. Reforming device

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2003244012A1 (en) * 2003-06-27 2005-01-13 Ebara Ballard Corporation Fuel reformer

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0214432A1 (fr) * 1985-09-11 1987-03-18 Uhde GmbH Appareil pour la production de gaz de synthèse
WO2000027518A1 (fr) * 1998-11-10 2000-05-18 International Fuel Cells, Llc Installation de reformage de gaz combustible d'hydrocarbure pour centrale a piles a combustible
WO2000041804A1 (fr) * 1999-01-19 2000-07-20 International Fuel Cells, Llc Ensemble reformeur compact pour gaz combustible
US20040187386A1 (en) * 2003-03-26 2004-09-30 Wangerow James R. Simplified three-stage fuel processor
DE102007039594A1 (de) * 2006-10-03 2008-04-10 Avl List Gmbh Energieerzeugungseinheit mit zumindest einer Hochtemperaturbrennstoffzelle
US20110067303A1 (en) * 2008-03-24 2011-03-24 Sanyo Electric Co., Ltd. Reforming device

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DE112014000673A5 (de) 2015-10-29
AT513931A1 (de) 2014-08-15
AT513931B1 (de) 2017-03-15

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