WO2019157549A1 - Wärmetauscher für ein brennstoffzellensystem und verfahren zum betreiben eines brennstoffzellensystems - Google Patents
Wärmetauscher für ein brennstoffzellensystem und verfahren zum betreiben eines brennstoffzellensystems Download PDFInfo
- Publication number
- WO2019157549A1 WO2019157549A1 PCT/AT2019/060057 AT2019060057W WO2019157549A1 WO 2019157549 A1 WO2019157549 A1 WO 2019157549A1 AT 2019060057 W AT2019060057 W AT 2019060057W WO 2019157549 A1 WO2019157549 A1 WO 2019157549A1
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- WIPO (PCT)
- Prior art keywords
- heat exchanger
- fuel
- fuel cell
- reforming
- region
- Prior art date
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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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
- H01M8/04022—Heating by combustion
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—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
-
- 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
- H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
-
- 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
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam 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
- C01B2203/067—Integration with other chemical processes with fuel cells the reforming process taking place in the fuel cell
-
- 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
- C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
-
- 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
- C01B2203/1294—Evaporation by heat exchange with hot process stream
-
- 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
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
- H01M2008/1293—Fuel cells with solid oxide electrolytes
-
- 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
Definitions
- the invention relates to heat exchangers for a fuel cell system, in particular an operated with a liquid fuel SOFC system, with several
- Energy between a system exhaust line and an anode supply line of a fuel cell system is transferable, comprising an evaporation region, an overheating region and a reforming region, which are flow-connected to each other.
- the invention relates to a use of such a heat exchanger.
- the invention relates to a fuel cell system, in particular SOFC system, with such a heat exchanger, comprising a fuel cell stack with an anode section and a cathode section.
- the invention relates to a method for operating a
- Fuel cell system in particular a SOFC system.
- Heat exchangers for fuel cell systems are known from the prior art. These are arranged at different locations in a fuel cell system, such as in an anode feed line. About the
- Anode supply line becomes fuel to an anode section of the
- Synthesis gas or hydrogen-rich gas is generated.
- a plurality of heat exchangers through which heat from system exhaust gas can be transferred to the fuel.
- a reformer of a fuel cell system at least heat-transmitting with a Fleizmantel to pair.
- Such a reformer is designed to perform a partial catalytic reaction, which is why it also includes a mixing space for admixing air.
- the object of the invention is to provide a heat exchanger of the type mentioned, with which a fuel cell system with as few components is efficiently operable.
- Another object is to provide a method of the type mentioned, with which a fuel cell system can be operated component low and efficient.
- Heat transfer elements of a heat exchanger of the type mentioned at least partially comprise a catalytic material.
- the heat exchanger according to the invention comprises an evaporator, a superheater and a reformer is within the scope of the invention
- Heat transfer elements are arranged distributed over an entire volume of the heat exchanger. Including that the heat exchanger in one
- Fuel cell system can be arranged and / or with lines thereof
- Strömungsverbindbar is within the scope of the invention to be understood that this for arrangement in a fuel cell system and the corresponding
- Heat exchanger in particular free of one and / or without mixing chamber
- the evaporation region, the overheating region and the reforming region of the heat exchanger are directly fluidly connected to each other. It is beneficial if each of the areas except the fluid connection in itself
- the heat exchanger is designed to flow through the fuel.
- a heat exchanger which in principle can be operated in the DC principle, countercurrent principle or cross-flow principle.
- the heat exchanger transmits thermal energy from a first fluid, in particular
- System exhaust to a second fluid, in particular fuel or fuel, preferably a water-fuel mixture.
- the fluids may be gaseous or liquid or partly gaseous or partly liquid.
- the second fluid in particular a water-containing fuel, upstream of the heat exchanger liquid and the system exhaust gas.
- the Anodenzumol technisch or the fuel and the system exhaust line or the system exhaust gas are thus coupled to each other heat transfer.
- a heat exchanger for a fuel cell system in particular for a SOFC system (SOFC stands for solid oxide fuel cell or solid oxide fuel cell) is provided.
- SOFC solid oxide fuel cell or solid oxide fuel cell
- Such a fuel cell system is operated in particular with liquid fuel, more preferably with a liquid fuel-water mixture such as an ethanol-water mixture.
- a liquid fuel-water mixture such as an ethanol-water mixture.
- the heat exchanger according to the invention in a motor assembly of a
- the heat transfer elements are coated with a catalytic material. It is advantageous if the evaporation region is smaller than the reforming region, that is, the evaporation region also comprises fewer heat transfer elements than the reforming region. Preferably, its volume is also smaller than the volume of
- the evaporation region is fluidic with the
- Overheating connected and the overheating area is fluidly connected to the reforming area.
- the anode supply line is flow-connected to the evaporation region, wherein fuel can be passed to an anode section of the fuel cell system via the anode supply line connected to a cold side of the heat exchanger.
- fuel supply line forming part of the Anodenzu classroom
- Koch liquid fuel to the evaporation region can be conducted, where it is converted into a gas.
- the fuel is thus passed over the cold side of the heat exchanger, wherein this is in particular evaporable by a heat of system exhaust gas.
- burned system exhaust over the warm side of the heat exchanger is feasible.
- hot or hot system exhaust gas in particular, the catalytic material of the reforming region to a predetermined operating temperature or
- Activation temperature can be brought. Due to the catalytic material are in the
- a downstream flow direction of the system exhaust gas is as follows: reforming area, overheating area, evaporation area.
- System exhaust is understood in the context of the invention, in particular anode exhaust gas and cathode exhaust gas.
- anode exhaust gas and cathode exhaust gas.
- the heat exchanger according to the invention is anode exhaust gas downstream of a
- air cathode exhaust gas
- system exhaust gas line for supplying system exhaust gas of the fuel cell system to the overheating region and / or the reforming region which can not be completely combusted system exhaust gas via the warm side of the heat exchanger. That is, in one
- Fuel cell system with the heat exchanger according to the invention, the downstream of a fuel cell stack of anode exhaust gas and cathode exhaust gas merged system exhaust gas in particular supplied directly to the heat exchanger. It can therefore be dispensed with a catalytic afterburner.
- the heat transfer elements therefore have a catalytic material or are coated with a catalytic material on that side, which is traversed by the system exhaust gas or can be flowed through. In doing so, all areas of the
- Heat exchangers may be catalytically coated on a side through which the system exhaust gas flows or only individual ones thereof. It is advantageous if at least the heat transfer elements of the reforming region both on the side, which is traversed by the fuel, as well as on the side which from
- System exhaust gas is flowed through, is catalytically coated. Due to the catalytic material arranged on the system exhaust side of the heat transfer elements, it is possible for one to have the system exhaust gas which is in the
- Fuel cell stack has not been completely burned, nachverbines completely catalytic in the heat exchanger and on the other hand enough heat is generated, whereby a heat transfer is further improved in a row.
- a heat exchanger formed in this way not only comprises an evaporation region, an overheating region and a reforming region, but also an afterburner region.
- the overheating region and the reforming region are designed as a common region. This is to say that the overheating and the reforming of the fuel in one step or at least very quickly in a row are feasible.
- the overheating area and the reforming region are designed as a common region. This is to say that the overheating and the reforming of the fuel in one step or at least very quickly in a row are feasible.
- Reforming area are not spatially separated.
- the evaporation area is so from the overheating area and / or
- the gaseous fuel can be heated to a temperature of about 300 ° C to about 400 ° C or more by a heat transfer from the system exhaust and thereby preconditionable for reforming.
- the superheated and preconditioned gas can be used and reformed directly in the reformer.
- the heat exchanger can be arbitrarily, for example, as a tube bundle heat exchanger, formed. Appropriately, however, this is designed as a plate heat exchanger. So here are the
- Heat transfer elements formed as plates or plate bundles, wherein the plates or plate bundles of the reforming region comprise a catalytic material or coated with a catalytic material.
- Plate heat exchanger formed heat exchanger is particularly advantageous if the plates with a small thickness of in the range of about 1 mm to 2 mm, in particular about 1, 2 mm to 1, 5 mm, more preferably about
- the evaporation area may comprise about 24 plates, whereas a common area for overheating and
- Reforming may comprise about 30 plates, which are at least partially catalytically coated or comprise a catalytic material. In principle, however, more or fewer plates can be provided. A number of the plates is dependent on a given space and / or pressure loss requirements.
- the plates of the plate-shaped heat exchanger are so non-positively or cohesively connected to each other, that in each successive spaces between individual plates once the fuel and then the system exhaust gas flows or out.
- the plates are advantageously each formed with a profile or profiled, so that a surface for the heat transfer is further increased. It is advantageous if the plates, which are arranged in the reforming region, are coated with a catalytic material. One side of each of the plates is catalytically coated, the
- the plates of the plate heat exchanger may also be at least partially coated on both sides, so that even those areas in which the system exhaust gas flows, are designed for catalytic reforming. This is particularly advantageous if the system exhaust immediately downstream of a fuel cell stack is fed to the heat exchanger via the system exhaust line without being previously completely burned in an afterburner. Such a heat exchanger then assumes the function of an afterburner or also contains this component.
- the catalytic coating is formed as a catalytic tissue or catalytically coated, in particular metallic, grid.
- the catalytic coating is designed to reform the vaporized and optionally superheated fuel.
- the reforming area and the overheating area are integrally formed, the evaporated fuel is overheated and reformed almost simultaneously.
- the reforming is advantageously carried out by steam reforming without supply of air or steam.
- a water-containing fuel such as an ethanol-water mixture no separate supply of (water) vapor is necessary.
- the amount of steam required for steam reforming is already provided by the vaporized fuel itself.
- the catalytic coating it can be provided within the scope of the invention for the catalytic coating to be in the form of a catalytically coated metallic grid
- the reforming region is designed and assigned to carry out a steam reforming. So there is an endothermic reaction.
- the energy required for this is according to the invention over the System exhaust, which is heat transfer coupled to the reforming area provided.
- a supply line of air to the evaporation area or overheating area is provided.
- air upstream of the evaporation zone is mixable with the fuel.
- the fuel and the air are fed separately from one another to the evaporation region of the heat exchanger. It may also be advantageous if the air downstream of the
- Evaporation area is supplied to the overheating area.
- an oxygen-containing fluid in particular a
- oxygen-containing gas particularly preferably ambient air, understood. This makes it possible, optionally next to or alternatively to steam reforming a
- Fuel cell stack is still cold and needs to be heated. By the supply of air at, in particular exclusively, a start phase of
- Fuel cell system is thus the fuel cell stack by catalytic partial oxidation can be reheated. If this has reached a predetermined temperature, the supply of air, in particular by a valve is switched off again. In addition, by the air supply at a starting phase of the
- an electric heater is provided. That is, the heat exchanger includes an electric heater.
- the heating device can also be non-electric. This is in particular to
- Heating the fuel or fuel-water mixture formed more preferably, the heating means is exclusively for heating,
- Evaporation and / or reforming of the fuel or fuel-water mixture formed and arranged at a warm-up phase of the fuel cell system At a start-up phase or warm-up phase of the fuel cell system is still no or insufficient or not enough warm system exhaust vorahnden to transfer the heat required to the heat exchanger.
- the electric heater may operate for a period of about 2 minutes to 10 minutes. It is favorable, if the
- Evaporation area and the reforming area and / or overheating area is arranged.
- the electrical support for evaporation and reforming can indeed be carried out in principle in an external component, but an integration of this function for reasons of space is desirable.
- a use of a heat exchanger according to the invention takes advantage of me to evaporate, overheated and reforming a liquid fuel in a SOFC system.
- the fuel cell system further includes a fuel stack having an anode portion and a cathode portion, and a start burner, an afterburner, and at least one other
- Heat exchanger on It is favorable, if the fuel cell system more valves for controlling various lines and a fan for conveying the
- the at least one further heat exchanger is with a cold side in a Kathodenzutubetechnisch
- the fuel cell system according to the invention is used in particular in a motor vehicle.
- a method of the type mentioned at the beginning comprises the following steps: - Passing a liquid fuel, in particular a liquid fuel-water mixture in the direction of one in a Anodenzumol
- Heat exchanger wherein the heat exchanger over, in particular completely burned, system exhaust gas is heated, wherein heat from in a
- the entire waste heat of the system exhaust gas is used to heat a single component.
- the heat of the system exhaust gas is advantageously transferred in the following order for carrying out the processes taking place in the heat exchanger: overheating and / or
- Fuel cell system have been described.
- heat exchanger comprises a catalytic material.
- the heat exchanger comprises a catalytic material.
- no air supply is necessary or provided.
- heat-conducting elements for example plates, with a
- the heat exchanger in DC principle or in
- Cross-flow principle are flowed through by the fuel and the system exhaust gas.
- a particularly efficient heat transfer from the system exhaust gas to the fuel is achieved when the heat exchanger flows through the fuel and the system exhaust gas in a countercurrent flow principle.
- the fuel or vaporized or superheated fuel is flowed past the system exhaust gas as being opposite in the respective region of the heat exchanger, heat being transferred from the system exhaust gas to the system exhaust gas
- System exhaust gas is flowed through, wherein the reforming region is flowed through upstream of an overheating region of the heat exchanger from the system exhaust gas.
- heat is transferred particularly efficiently. That is, the necessary and predetermined temperatures required for the respective processes (evaporation, superheating, reforming) are achieved in a short period of time.
- Heat exchanger is flowed through upstream of an overheating region of the heat exchanger by the fuel, wherein a reforming region of the
- Heat exchanger downstream of the overheating region is flowed through by the fuel in order to further optimize the heat transfer.
- Cathode section of the fuel cell system is passed. Under air is understood in the context of the invention, in particular ambient air, although air may also consist of a major portion of oxygen or pure oxygen. Downstream of the fuel cell stack, anode exhaust and cathode exhaust gas are mixed into the system exhaust gas, which provides the necessary heat for the system
- Fig. 1 a heat exchanger according to the invention
- Fig. 2 is a block diagram for illustrating an inventive
- Fig. 3 is a block diagram illustrating another inventive
- Fuel cell system according to an embodiment of the invention.
- Fig. 1 shows a heat exchanger according to the invention 1. This comprises a plurality of heat transfer elements 2, an evaporation region 5, a
- the plate heat exchanger designed as a heat exchanger 1 has a cold side 8 and a warm side 9.
- the heat exchanger 1 is with its cold side 8 in a
- Anodenzu111 decisively can be arranged and via a system exhaust line 3 heat from system exhaust gas can be transferred to a guided in the Anodenzu211 effet 4 aqueous fuel.
- the heat exchanger 1 is designed as a plate heat exchanger and comprises a plurality of plate-shaped heat transfer elements 2, which partially comprise a catalytic material. Both the
- Evaporation area 5, overheating area 6, and reforming area 7 include heat transfer element 2, these areas being fluidly connected to each other.
- the heat exchanger 1 is adapted to a
- the heat exchanger 1 can basically be designed for heat transfer in the DC principle, countercurrent principle or crossflow principle. It is a flow direction of the
- Heat exchanger 1 is operated in countercurrent principle. Should this be in
- FIG. 2 is a block diagram illustrating a device according to the invention
- Fuel cell system (100) according to an embodiment of the invention shown.
- this further includes a
- Cathode section 130 In addition, a start burner 140, an afterburner 150, another heat exchanger 160 and a fuel source 170 and an air source 180.
- the elements are connected via an anode feed line 4, a cathode feed line 12 and a system exhaust line 3.
- anode feed line 4 For switching these lines 3, 4, 12 different valves 13 are provided.
- a cathode blower 200 is provided, which is arranged in the cathode supply line 12 in the flow direction of the air downstream of the air source 180 and upstream of the further heat exchanger 160.
- the further heat exchanger 160 is arranged with its cold side in the Kathodenzuschreibtechnisch 12 and for heating the air which is supplied to the cathode portion 130 is formed. A warm side of the further heat exchanger 160 flows through the system exhaust gas upstream of the heat exchanger 1.
- Fig. 3 shows a preferred embodiment of the fuel cell system 100, wherein the heat exchanger 1 is flowed through in the countercurrent principle.
- Fuel cell system 100 of FIG. 3 is in regular operation, a liquid water-fuel mixture from the fuel source 170 through the
- Heat exchanger 1 the water-fuel mixture is completely evaporated in a first step in the evaporation region 5, wherein this at a discharge from the evaporation region 5 has a temperature of about 100 ° C, preferably above 1 10 ° C, in particular from about 120 ° C. , In a second, the
- the gaseous water-fuel mixture so for use in
- Synthesis gas present water-fuel mixture is downstream of the heat exchanger 1 in the Anodenzutechnisch 4 to the fuel cell stack 120, more precisely to the anode section 110, out.
- the anode exhaust gas and the cathode exhaust gas are combined to form the system exhaust gas, with the anode exhaust gas being burnt in admixture with the cathode exhaust gas in a catalytic afterburner 150. Downstream of the afterburner 150, the now completely burned system exhaust gas in the system exhaust line 3 is guided in the direction of the further heat exchanger 160. About the other heat exchanger 160 is
- Cathode feed line to the cathode section 130 is supplied. Downstream of the further heat exchanger 160, it is arranged heat exchanger 1, to which the system exhaust gas is supplied.
- the heat exchanger 1 is shown in FIG. 3 in
- Reforming area 7 and the overheating area 6 formed substantially as a common area. That is, the two steps of overheating and reforming in the heat exchanger 1 take place substantially at the same time or with a very short time interval from each other. Downstream of the
- Reforming area 7 or overheating area 6 the system exhaust gas is supplied to the evaporation region 5 connected thereto flow. The remaining heat of the system exhaust gas is thus used to evaporate the water-fuel mixture. The now cooled system exhaust gas is discharged downstream of the heat exchanger 1 in the environment 220.
- this and / or the elements disposed therein Prior to the regular operation of the fuel cell system 100 described above, this and / or the elements disposed therein must be heated to a predetermined temperature usually. This includes the
- Fuel cell system 100 a starting burner 140.
- About two sections 14 a, 14 b of the sub-line 14 is the starting burner 140 fuel from the fuel source 170th and air supplied from the air source 180.
- the first section 14a separates downstream of the fuel source 170 from the anode supply line 4, wherein a valve 13b is arranged in the first section.
- the second section 14 b separates downstream of the air source 180 from the cathode supply line 12, wherein the first section 14 a and the second section 14 b are merged upstream of the starting burner 140.
- the starting burner 140 is the
- fuel is burned while supplying air to a hot gas.
- the gas is downstream of the starting burner 140 at a warm-up of the
- Heat exchanger 160 and then fed to the heat exchanger 1, wherein the heat of the gas is transferred to this. Once the fuel cell system 100 or the individual elements thereof have reached the predetermined operating temperature, the heat transfer takes place on the heat exchanger 1, 160 as above
- Air or an oxygen-containing fluid to the evaporation region 5 can be supplied to warm up the fuel cell stack 120 via a catalytic partial oxidation during a heating operation of the fuel cell system 100. Once the fuel cell system 100 has reached an operating temperature, the air supply can be adjusted via a valve, not shown.
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- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
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Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201980012844.9A CN111712956B (zh) | 2018-02-16 | 2019-02-15 | 用于燃料电池系统的换热器和燃料电池系统的运行方法 |
BR112020016636-7A BR112020016636A2 (pt) | 2018-02-16 | 2019-02-15 | Trocador de calor para um sistema de célula de combustível e método para operar um sistema de célula de combustível |
DE112019000810.2T DE112019000810A5 (de) | 2018-02-16 | 2019-02-15 | Wärmetauscher für ein brennstoffzellensystem und verfahren zum betreiben eines brennstoffzellensystems |
RU2020130261A RU2782253C2 (ru) | 2018-02-16 | 2019-02-15 | Теплообменник для системы топливных элементов и способ работы системы топливных элементов |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ATA50153/2018 | 2018-02-16 | ||
ATA50153/2018A AT520976B1 (de) | 2018-02-16 | 2018-02-16 | Wärmetauscher für ein Brennstoffzellensystem und Verfahren zum Betreiben eines Brennstoffzellensystems |
Publications (1)
Publication Number | Publication Date |
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WO2019157549A1 true WO2019157549A1 (de) | 2019-08-22 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/AT2019/060057 WO2019157549A1 (de) | 2018-02-16 | 2019-02-15 | Wärmetauscher für ein brennstoffzellensystem und verfahren zum betreiben eines brennstoffzellensystems |
Country Status (5)
Country | Link |
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CN (1) | CN111712956B (de) |
AT (1) | AT520976B1 (de) |
BR (1) | BR112020016636A2 (de) |
DE (1) | DE112019000810A5 (de) |
WO (1) | WO2019157549A1 (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114631209A (zh) * | 2019-10-17 | 2022-06-14 | 蓝界科技控股公司 | 具多流热交换器的燃料电池系统、其用途以及其操作方法 |
WO2022256857A1 (de) * | 2021-06-11 | 2022-12-15 | Avl List Gmbh | Brennkraftsystem mit einem verbrennungsmotor |
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DE102007018264A1 (de) * | 2007-04-11 | 2008-10-16 | Ebz Entwicklungs- Und Vertriebsgesellschaft Brennstoffzelle Mbh | Hochtemperaturbrennstoffzellensystem |
CA2984097A1 (en) * | 2015-04-28 | 2016-11-03 | Nissan Motor Co., Ltd. | Fuel cell system |
EP3136487A1 (de) * | 2015-08-28 | 2017-03-01 | Panasonic Intellectual Property Management Co., Ltd. | Vorrichtung zur wasserstoffproduktion und brennstoffzellensystem |
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- 2019-02-15 BR BR112020016636-7A patent/BR112020016636A2/pt unknown
- 2019-02-15 WO PCT/AT2019/060057 patent/WO2019157549A1/de active Application Filing
- 2019-02-15 DE DE112019000810.2T patent/DE112019000810A5/de active Pending
- 2019-02-15 CN CN201980012844.9A patent/CN111712956B/zh active Active
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CN114631209A (zh) * | 2019-10-17 | 2022-06-14 | 蓝界科技控股公司 | 具多流热交换器的燃料电池系统、其用途以及其操作方法 |
CN114631209B (zh) * | 2019-10-17 | 2022-11-22 | 蓝界科技控股公司 | 具多流热交换器的燃料电池系统、其用途以及其操作方法 |
WO2022256857A1 (de) * | 2021-06-11 | 2022-12-15 | Avl List Gmbh | Brennkraftsystem mit einem verbrennungsmotor |
Also Published As
Publication number | Publication date |
---|---|
AT520976B1 (de) | 2020-04-15 |
CN111712956A (zh) | 2020-09-25 |
AT520976A1 (de) | 2019-09-15 |
DE112019000810A5 (de) | 2020-11-05 |
BR112020016636A2 (pt) | 2020-12-15 |
CN111712956B (zh) | 2024-01-19 |
RU2020130261A (ru) | 2022-03-16 |
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