WO2024045228A1 - 用于燃料电池的热管双极板、燃料电池电堆 - Google Patents

用于燃料电池的热管双极板、燃料电池电堆 Download PDF

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WO2024045228A1
WO2024045228A1 PCT/CN2022/119578 CN2022119578W WO2024045228A1 WO 2024045228 A1 WO2024045228 A1 WO 2024045228A1 CN 2022119578 W CN2022119578 W CN 2022119578W WO 2024045228 A1 WO2024045228 A1 WO 2024045228A1
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Prior art keywords
plate
fuel cell
heat
capillary core
anode plate
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PCT/CN2022/119578
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English (en)
French (fr)
Inventor
诸葛伟林
韩雨麒
张扬军
彭杰
钱煜平
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清华大学
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Publication of WO2024045228A1 publication Critical patent/WO2024045228A1/zh

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    • 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
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • 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
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • H01M8/0258—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant
    • 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
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • H01M8/0267—Collectors; Separators, e.g. bipolar separators; Interconnectors having heating or cooling means, e.g. heaters or coolant flow channels
    • 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
    • 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
    • H01M8/04029—Heat exchange using liquids
    • 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
    • H01M8/04059—Evaporative processes for the cooling of a fuel cell
    • 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
    • H01M8/04067—Heat exchange or temperature measuring elements, thermal insulation, e.g. heat pipes, heat pumps, fins
    • H01M8/04074—Heat exchange unit structures specially adapted for fuel cell
    • 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
    • H01M8/1016—Fuel cells with solid electrolytes characterised by the electrolyte material
    • H01M8/1018—Polymeric electrolyte materials
    • 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
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • 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
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/2457—Grouping of fuel cells, e.g. stacking of fuel cells with both reactants being gaseous or vaporised
    • 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 present application relates to the technical field of fuel cells, and in particular to a heat pipe bipolar plate and a fuel cell stack for a fuel cell.
  • the proton exchange membrane fuel cell is an energy conversion device that converts chemical energy into electrical energy. It has the characteristics of environmental friendliness, quick start, low operating temperature, and high efficiency. It is considered to be one of the most potential next-generation power sources.
  • the operating temperature of proton exchange membrane fuel cells is 60 to 90°C. If the temperature is too low, the internal polarization of the fuel cell will increase and the performance will decrease; if the temperature is too high, the membrane will dry out and the proton conductivity will decrease, causing the stack performance to decrease. Too high will also lead to thermal degradation of the membrane electrode, significantly reducing the durability of the stack. Therefore, thermal management is crucial for fuel cell systems.
  • the power range of fuel cell systems for automobiles and aircraft usually ranges from tens to hundreds of kilowatts, and battery thermal management generally takes the form of liquid cooling.
  • the coolant channel of the liquid cooling device needs to be integrated with the reactant gas channel to improve the compactness of the structure, resulting in a contradiction between improving the heat dissipation performance of the stack and reducing the thickness of the single cell.
  • the liquid cooling device system is complex, has many accessories, and is large in size and weight, which has a great impact on the power density of the fuel cell system.
  • Heat pipes are high-performance heat transfer devices based on the phase change principle. They have high thermal conductivity and good temperature uniformity. They are light in weight and simple in structure. They have been widely used in various types of highly integrated electronic products.
  • the use of heat pipes to participate in the thermal management of fuel cells has great development potential. At present, most relevant research is still in its infancy, and most of them adopt the solution of embedding columnar heat pipes or flat heat pipes in graphite plates, which can meet the thermal management needs of fuel cells but increases the thickness of the plates greatly, resulting in a higher power density of the fuel cell stack. Low.
  • Patent application CN110416568A discloses a heat pipe metal bipolar plate air-cooled (single) battery stack, vehicle and electronic equipment.
  • the heat pipe metal bipolar plate includes: a power generation area and a heat dissipation area; the power generation area and the heat dissipation area are connected internally. A closed space is used for phase change heat transfer of the heat transfer medium.
  • CN110416568A does not provide a specific internal structure design of the metal bipolar plate. It does not consider the low heat transfer limit of the ultra-thin heat pipe. The external reaction gas flow field is not coupled with the internal capillary structure design. This internal structure will lead to volumetric power. Low density and lack of practicality.
  • Patent application CN108110276A provides a heat dissipation bipolar plate for fuel cells, which belongs to the field of thermal control.
  • the heat-dissipating bipolar plate includes an oxygen plate and a hydrogen plate.
  • the oxygen plate and the hydrogen plate are coupled to form a hollow structure for storing phase change media to dissipate heat through phase change.
  • the internal structure of CN108110276A is based on an idealized flat cube cavity. There is no specific description of the internal structure of the cavity, and the practicality is low.
  • Patent application CN114300704A discloses a fuel cell device with heat pipe enhanced heat transfer.
  • the fuel cell is composed of at least two battery cells stacked in series.
  • Each of the battery cells includes a bipolar plate and the A membrane electrode fitted with a bipolar plate, wherein the bipolar plate has a porous capillary structure and a closed inner cavity.
  • the implementation of CN114300704A does not take into account the fluidity and heat transfer performance of the heat exchange medium in the heat pipe, and does not provide a specific internal optimized structure of the bipolar plate.
  • This application is made in view of the state of the art described above.
  • the purpose of this application is to provide a heat pipe bipolar plate for a fuel cell, which can improve the heat dissipation performance of the fuel cell while reducing the volume and weight of the fuel cell thermal management system.
  • the present application also provides a fuel cell stack including the aforementioned heat pipe bipolar plate for a fuel cell.
  • An embodiment of the present application provides a heat pipe bipolar plate for a fuel cell.
  • the heat pipe bipolar plate includes an anode plate and a cathode plate arranged to overlap each other,
  • the anode plate and the cathode plate respectively include a plurality of protrusions with a rectangular or trapezoidal cross-section.
  • the anode plate and the cathode plate are arranged in such a manner that their protrusions are away from each other.
  • a heat exchange working fluid flow channel is defined between the cathode plate and the cathode plate, and the heat exchange working fluid flow channel is filled with a heat exchange working fluid
  • the heat exchange working fluid flow channel includes a capillary core structure and a steam chamber
  • the capillary core structure includes a support capillary core and a wall capillary core.
  • the support capillary core is disposed between the anode plate and the cathode plate so that the anode plate and the cathode plate support the anode plate and the cathode plate at intervals. anode plate and said cathode plate,
  • the wall capillary wick is disposed on the inner surfaces of the protrusions of the anode plate and the cathode plate,
  • the anode plate, the cathode plate and the capillary wick structure define the steam within the heat exchange medium flow channel. cavity.
  • the entire inner surface of the opposite protrusions of the anode plate and the cathode plate is covered with the wall capillary wick,
  • the supporting capillary cores are spaced between the anode plate and the cathode plate,
  • the supporting capillary wick connects two adjacent steam chambers and extends until its end is flush with the wall capillary wick.
  • the entire inner surface of the opposite protrusions of the anode plate and the cathode plate is covered with the wall capillary wick,
  • the supporting capillary core forms a continuous layer structure between the anode plate and the cathode plate,
  • Both sides of the supporting capillary core are connected to the anode plate, the cathode plate and the wall capillary core respectively.
  • the support capillary core includes a first support capillary core and a second support capillary core of different models, and the first support capillary core and the second support capillary core are alternately distributed at intervals,
  • the wall capillary core is only provided on the end surface and one side surface of the protruding inner surface
  • the first supporting capillary wick connects the adjacent sides of two adjacent steam chambers and is not connected to the wall surface of the capillary wick, and the end of the first supporting capillary wick is flush with the side of the steam chamber.
  • the second supporting capillary core is connected to the adjacent wall capillary core for communicating with the adjacent steam chamber and transporting the heat exchange medium.
  • the end of the second supporting capillary core is connected to the adjacent wall capillary core.
  • the wall capillary core is flush.
  • the anode plate is aligned with, or staggered by a certain distance from, the protrusions of the cathode plate that form the heat exchange medium flow channel.
  • the support capillary core is connected to or separated from the wall capillary core.
  • An embodiment of the present application also provides a fuel cell stack, including:
  • the membrane electrode assembly abuts the protrusion of the anode plate or the cathode plate.
  • At least one side of the membrane electrode assembly is connected to the anode plate of one of the heat pipe bipolar plates, and adjacent protrusions of the anode plate and the membrane electrode assembly define fuel channel,
  • the other side of the at least one membrane electrode assembly is connected to the cathode plate of the other heat pipe bipolar plate, and adjacent protrusions of the cathode plate and the membrane electrode assembly define an oxidant channel.
  • An embodiment of the present application also provides a fuel cell, which uses the aforementioned fuel cell stack,
  • the fuel cell includes:
  • One or more condensation heat sink zones are One or more condensation heat sink zones.
  • the heat pipe bipolar plate absorbs heat in the reaction heat absorption area and dissipates heat in the condensation heat dissipation area, thereby dissipating heat for the fuel cell.
  • the one or more condensation heat dissipation zones are connected to an external cooling device
  • the cooling device is an air cooling device or a liquid cooling device.
  • Figure 1 is a schematic structural diagram of a heat pipe bipolar plate according to an embodiment of the present application.
  • Figure 2 is a schematic structural diagram of a fuel cell stack according to an embodiment of the present application.
  • Figure 3 is a schematic diagram of the lower structure of a fuel cell stack according to an embodiment of the present application.
  • FIG. 4A is a schematic structural diagram of a heat pipe bipolar plate according to the second embodiment of the present application.
  • FIG. 4B is a schematic structural diagram of a heat pipe bipolar plate according to the third embodiment of the present application.
  • Figure 5 is a schematic layout diagram of a fuel cell according to an embodiment of the present application.
  • FIG. 6 is a partially enlarged schematic diagram of the heat pipe bipolar plate of the fuel cell shown in FIG. 5 .
  • FIG. 7 is a schematic structural diagram of the heat pipe bipolar plate of the fuel cell shown in FIG. 5 along cross section A-A.
  • the embodiment of the present application provides a heat pipe bipolar plate 100.
  • the heat pipe bipolar plate 100 of the present application may include an anode plate 110, a cathode plate 120, and a capillary core structure 130.
  • the anode plate 110 and the cathode plate 120 may respectively form a plurality of protrusions.
  • a fuel channel 220 for fuel (for example, hydrogen) to flow may be formed between adjacent protrusions of the anode plate 110 (and the membrane electrode assembly 210 to be described later), and between adjacent protrusions of the cathode plate 120 (and the membrane electrode assembly 210 to be described later).
  • An oxidant supply channel 230 for flowing oxidant eg, oxygen
  • oxidant eg, oxygen
  • the anode plate 110 and the cathode plate 120 respectively include a plurality of protrusions with a rectangular or trapezoidal cross-section.
  • the anode plate 110 and the cathode plate 120 are arranged in such a manner that their protrusions are away from each other and are defined between the anode plate 110 and the cathode plate 120 .
  • the heat exchange working fluid flow channel includes a capillary core structure 130 and a steam chamber 140.
  • the capillary wick structure 130 may include a support capillary wick 131 and a wall capillary wick 132 .
  • the supporting capillary core 131 may be located between the anode plate 110 and the cathode plate 120 so that the anode plate 110 and the cathode plate 120 are spaced apart to support the anode plate 110 and the cathode plate 120 .
  • the wall capillary core 132 may be disposed on the inner surface of the protrusion defined by the anode plate 110 and the cathode plate 120 and constituting the heat exchange medium flow channel.
  • the supporting capillary core 131 can be connected to or separated from the wall capillary core 132 .
  • the anode plate 110, the cathode plate 120 and the capillary core structure 130 define a vapor chamber 140 within the heat exchange medium flow channel.
  • the supporting capillary core 131 and the anode plate are flush with the wall capillary core 132 inside the heat exchange medium flow channel defined by the cathode plate, so as to make the side of the steam chamber 140 smooth.
  • the channels for the oxidant or fuel flow of the anode plate 110 and the cathode plate 120 can be aligned, as shown in Figure 1; or along the extending direction of the supporting capillary wick 131 (left and right direction in Figure 1, up and down in Figure 7 direction) staggered by a certain distance, as shown in Figure 6 and Figure 7.
  • the materials of the anode plate 110 and the cathode plate 120 can be metal plates, non-porous graphite plates, composite graphite plates, etc.
  • the heat exchange medium flow channel can be filled with heat exchange medium.
  • the channel through which the heat exchange working fluid flows is composed of a plurality of steam chambers 140 and a capillary core structure 130 (that is, forming a heat pipe structure).
  • the membrane electrode assembly 210 is the main source of heat, and the heat exchange medium can absorb the heat generated when the fuel cell is operating at the wall capillary core 132 in the heat exchange medium flow channel.
  • the steam chamber 140 is the main flow channel of the gaseous heat exchange working medium
  • the capillary wick structure 130 is the main flow channel of the liquid heat exchange working medium.
  • the heat exchange working medium is mainly in the wall capillary wick adjacent to the membrane electrode assembly 210. 132 absorbs heat and evaporates, but this does not rule out that the heat exchange medium may undergo phase change at any position in its flow channel.
  • the heat exchange medium absorbs heat at the gas-liquid phase interface, evaporates, and then enters the evaporation chamber 140 .
  • the gaseous heat exchange working fluid flows to the condensation and heat dissipation area 310 of the fuel cell under the action of the pressure gradient of thermal diffusion.
  • the gaseous heat exchange medium releases heat in the condensation heat dissipation zone 310 and condenses into a liquid state.
  • the liquid heat exchange medium then flows back through the capillary action of the capillary core structure 130 and absorbs heat to evaporate to the steam chamber 140 .
  • the heat exchange medium continuously circulates in its flow channel (heat pipe) and repeats the above-mentioned phase change heat transfer process of the heat exchange medium.
  • the heat exchange working fluid can be water, acetone and other materials.
  • the supporting capillary core 131 and the wall capillary core 132 in the capillary core structure 130 are only divided for convenience of explanation, and are not based on functional or structural divisions.
  • the supporting capillary core 131 and the wall capillary core 132 can both support the fuel cell and transfer the heat exchange medium.
  • the supporting capillary core 131 and the wall capillary core 132 can be of the same or different capillary core types, for example, groove, wire mesh, braided mesh, powder sintered particles and other capillary core types.
  • the supporting capillary core 131 can be replaced by a supporting structure with smaller void ratio or a solid supporting structure.
  • the thickness, structure, cross-sectional shape, mixing pore size, gradient, wettability treatment, etc. of the supporting capillary core 131 and the wall capillary core 132 can be determined based on the parameters of the flow channel of the heat exchange medium.
  • An embodiment of the present application also provides a fuel cell stack 200, including the above-mentioned heat pipe bipolar plate 100 and membrane electrode assembly 210.
  • the heat pipe bipolar plates 100 can be connected to both sides of the membrane electrode assembly 210 respectively.
  • the lower side of the membrane electrode assembly 210 is connected to the anode plate 110 of a heat pipe bipolar plate 100, and the upper side of the membrane electrode assembly 210 is connected to another heat pipe.
  • Cathode plate 120 of bipolar plate 100 is connected to the channel structure formed on the upper surface of the anode plate 110 .
  • the channel structure formed on the upper surface of the anode plate 110 is combined with the membrane electrode assembly 210 to form a fuel (eg, hydrogen) channel 220 .
  • the channel structure formed on the lower surface of the cathode plate 120 is combined with the membrane electrode assembly 210 to form an oxidant (eg, oxygen) channel 230 . It is understood that the positions of the anode plate 110 and the cathode plate 120 relative to the membrane electrode assembly 210 may be interchanged. It can be understood that this application does not limit the usage direction or posture of the fuel cell stack 200 or the fuel cell 300
  • a plurality of the above fuel cell stacks 200 are repeatedly stacked to form a fuel cell stack.
  • the uppermost and lowermost heat pipe bipolar plates of the fuel cell stack 200 only retain the anode plate 110 or the cathode plate 120 .
  • the lowermost structure of the fuel cell stack is shown.
  • the supporting capillary core 131 of the heat pipe bipolar plate 100 on the lower side is no longer connected to the cathode plate 120 , but is connected to the fuel cell housing 240 .
  • the gas flow channel type of the heat pipe bipolar plate 100 can be a parallel channel flow field, a multi-channel serpentine flow field, an interdigitated flow field, etc., and the anode plate 110 and the cathode plate 120 can use the same or different flow channel types. .
  • the wall capillary core 132 can cover the entire inner surface of the protrusions of the anode plate 110 and the cathode plate 120 .
  • the supporting capillary core 131 is located between the anode plate 110 and the cathode plate 120 and is distributed at intervals, and is connected to the wall capillary core 132 inside the heat exchange medium flow channel. The end of the supporting capillary core 131 can be flush with the wall capillary core 132 .
  • the capillary core structure 130 composed of the supporting capillary core 131 and the wall capillary core 132 arranged in this way is evenly distributed between the anode plate 110 and the cathode plate 120, forming a heat exchange working fluid flow channel with good fluidity but simple structure. (heat pipe), suitable for most fuel cell bipolar plates.
  • the supporting capillary wick 131 can form a continuous layer of capillary wick between the anode plate 110 and the cathode plate 120 to divide the steam chamber 140 into upper and lower parts. Two parts.
  • the wall capillary wick 132 may cover the entire inner surface of the protrusions of the anode plate 110 and the cathode plate 120 and be connected to the support capillary wick 131 .
  • the heat pipe bipolar plate 100 provided in this embodiment uses a continuous supporting capillary core 131, which reduces the contact resistance compared to the first embodiment, thereby reducing the ohmic polarization effect.
  • the flow resistance of the liquid heat exchange working medium in this embodiment is small, while the flow resistance of the gaseous heat exchange working medium is large, which is suitable for application in flow channel structures with a large aspect ratio.
  • the wall capillary core 132 may be disposed only inside the protrusions of the anode plate 110 and the cathode plate 120 close to the end surfaces of the membrane electrode assembly 210 and One side, and capillary core selection with larger cross-section (thickness) can be used.
  • the supporting capillary cores 132 in this embodiment can be distributed at intervals, and two different types of supporting capillary cores 1311 and 1312 can be used.
  • the porosity of the first supporting capillary wick 1311 that is not connected to the wall capillary wick 132 may be smaller, and its end is connected to two adjacent steam chambers 140 and is flush with the side of the steam chamber 140 .
  • the first supporting capillary core 1311 is mainly responsible for supporting the heat pipe bipolar plate 100 .
  • the second supporting capillary core 1312 connecting the two adjacent wall capillary cores 132 can have a larger porosity and a lower flow resistance of the liquid heat exchange medium, and it plays a supporting and mass transfer role in the heat pipe bipolar plate 100 at the same time.
  • the end of the second supporting capillary wick 1312 may be flush with the wall capillary wick 132 .
  • Embodiments of the present application also provide a fuel cell 300 that uses the above-mentioned heat pipe bipolar plate 100 or fuel cell stack 200.
  • the fuel cell 300 may include a condensation heat dissipation area 310 , a reaction heat absorption area 320 , a fuel inlet 330 , an oxidant inlet 340 , a fuel outlet 350 , and an oxidant outlet 360 .
  • the fuel cell 300 of the present application uses the above-mentioned heat pipe bipolar plate 100 or fuel cell stack 200.
  • the heat exchange medium flows through phase changes inside the structure, and there is no need to set up a coolant inlet and cooling system. liquid outlet.
  • the fuel cell stack 200 is disposed in the reaction heat absorption area 320.
  • an electrochemical reaction occurs to release heat, causing the heat exchange medium to absorb heat and vaporize in the steam chamber 140.
  • the gaseous heat exchange working fluid enters the condensation and heat dissipation zone 310 along with the pressure gradient, where it releases heat and is condensed and liquefied.
  • the liquefied heat exchange working fluid flows back to the reaction endothermic zone 320 due to the capillary action of the capillary core structure 130 .
  • the heat exchange medium continuously repeats the above process in the heat pipe bipolar plate 100 of the fuel cell, and flows through phase change between the reaction heat absorption area 320 and the condensation heat dissipation area 310, thereby achieving a better cooling and heat dissipation effect for the fuel cell 300.
  • FIG. 6 shows the structure of a heat pipe bipolar plate 100 in the fuel cell stack 200
  • FIG. 7 shows a possible structural diagram of the heat pipe bipolar plate 100
  • the cavity of the heat exchange working fluid flow channel on the lower side is connected to the condensation heat dissipation area 310 .
  • the protrusions of the anode plate 110 and the cathode plate 120 used to form the heat exchange fluid flow channel may be aligned or not completely aligned and staggered by a certain distance.
  • the condensation heat dissipation areas 310 are arranged on both sides perpendicular to the flow direction of the fuel and oxidant, and the structure of the heat pipe bipolar plate 100 of the first and second embodiments can be adopted.
  • the condensation heat dissipation areas 310 can also be arranged on both sides of the flow direction of the fuel and oxidant, and can adopt the structure of the heat pipe bipolar plate 100 of the third embodiment. It can be understood that when the cooling and heat dissipation requirements of the fuel cell 300 are not high, the condensation heat dissipation area 310 can also be provided only on one side of the reaction heat absorption area 320 .
  • the condensation heat dissipation area 310 can be connected to an external cooling device, which can be an air cooling or liquid cooling device.
  • the fuel cell 300 may be provided with multiple condensation heat dissipation areas 310 .
  • the structure of the condensation heat dissipation area 310 may be plate type, wave type, plate fin type, etc.
  • the condensation heat dissipation area 310 can be distributed on one or more sides of the reaction heat absorption area 320, and a microchannel structure that enhances convection heat transfer can be arranged on its surface.
  • the heat pipe bipolar plate, fuel cell stack and fuel cell used in this application adopt a heat pipe thermal management system.
  • the thermal management system based on the heat pipe bipolar plate is The management system has a simple structure and no accessories such as water pumps and water tanks, which can greatly increase the power density of the fuel cell system.
  • the heat pipe bipolar plate, fuel cell stack and fuel cell used in this application integrate the heat pipe and the bipolar plate and specifically provide several possible internal structures of the heat pipe bipolar plate. Compared with the existing heat pipe embedded bipolar plate, the thickness and stack volume of the fuel cell stack can be further reduced, and the heat dissipation performance of the fuel cell can be improved.
  • the heat pipe bipolar plate, fuel cell stack and fuel cell used in this application can be designed in a small way in terms of the specific support capillary core and wall capillary core structure design.
  • the thickness of the electrode plate is increased (about 0.1 ⁇ 0.4mm)
  • the flow area of the liquid and gaseous heat exchange working fluids is greatly increased, thereby reducing the fluid pressure drop and preventing the steam chamber size from being smaller than the critical value for the sharp increase in pressure drop (about 0.3 mm), which increases the ultimate heat transfer capacity of ultra-thin heat pipes to meet the growing heat dissipation needs of fuel cells.

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Abstract

提供了用于燃料电池的热管双极板，其包括彼此重叠设置的阳极板和阴极板，阳极板和阴极板分别包括多个横截面为矩形或梯形的凸起，阳极板和阴极板以它们的凸起彼此远离的方式设置，在阳极板和阴极板之间限定出换热工质流动通道，换热工质流动通道内填充换热工质，换热工质流动通道包括毛细芯结构、蒸汽腔，毛细芯结构包括支撑毛细芯和壁面毛细芯，支撑毛细芯设置在阳极板和阴极板之间以使阳极板和阴极板隔开间隔地支撑阳极板和阴极板，壁面毛细芯设置于阳极板和阴极板的凸起的内表面，在阳极板和阴极板的相对的凸起之间，阳极板、阴极板、毛细芯结构在换热工质流动通道内限定出蒸汽腔。还提供了燃料电池电堆和燃料电池。

Description

用于燃料电池的热管双极板、燃料电池电堆
相关申请的引用
本申请要求申请日为2022年9月1日、申请号为202211066893.0，发明名称为“用于燃料电池的热管双极板、燃料电池电堆”的在中国递交的在先发明专利申请的优先权，该在先申请的全部内容通过引用合并于此。
技术领域
本申请涉及燃料电池技术领域，且特别涉及一种用于燃料电池的热管双极板、燃料电池电堆。
背景技术
质子交换膜燃料电池是一种将化学能转化为电能的能量转化装置，具有环境友好、快速启动、低工作温度、高效率等特点，被认为是最具潜力的下一代动力源之一。质子交换膜燃料电池的工作温度为60～90℃，温度过低会造成燃料电池内部极化增大，性能下降；温度过高会引发膜干，质子传导率降低，使电堆性能下降，温度过高还会导致膜电极热降解，使电堆耐久性大幅下降。因此，热管理对于燃料电池***至关重要。
近年来，汽车、航空等行业对燃料电池***功率密度的要求持续提高，要求燃料电池单电池厚度不断减小、电流密度不断提高、***附件体积重量不断减小，对热管理***性能提出了越来越高的要求。汽车和航空器用燃料电池***的功率范围通常在几十到几百千瓦，其电池热管理一般采取液冷形式。液冷装置的冷却液通道需要与反应气通道集成以提高结构紧凑性，导致提高电堆散热性能与减小单电池厚度之间存在矛盾。此外，液冷装置***复杂、附件多，体积重量大，对燃料电池***功率密度影响较大。
热管是基于相变原理的高性能传热装置，具有较高的导热率和良好的均温性，且其重量轻、结构简单，已广泛应用于各类高集成度电子产品。采用热管参与燃料电池的热管理极具发展潜力。目前相关的研究大多仍处于起步阶段，多采用在石墨极板中嵌入柱状热管或平板热管的方案，可满足燃料电池热管理需求但使极板厚度增大较多，导致燃料电池堆功率密度较低。
专利申请CN110416568A公开了一种热管金属双极板风冷(单)电池堆、交通工具及电子设备，其中，热管金属双极板包括：发电区和散热区；发电区和散热区内部为连通的密闭空间，空间用于传热介质相变传热。CN110416568A未给出具体的金属双极板内部结构设计，未考虑超薄热管的传热极限较低的问题，外部反应气体流场也未与内部毛细结构设计耦合，这种内部结构会导致体积功率密度低，缺乏实用性。
专利申请CN108110276A提供了一种燃料电池用散热双极板，属于热控领域。所述散热双极板包括氧板和氢板，所述氧板和氢板扣合形成中空结构，用于储存相变介质以通过相变散热。CN108110276A的内部结构基于理想化的平整方体空腔，没有对腔体内部结构给出具体说明，实用性较低。
专利申请CN114300704A公开了一种热管强化传热的燃料电池装置，所述燃料电池由至少两个电池单体以串联方式层叠组合而成，每个所述电池单体包括双极板及与所述双极板贴合的膜电极，其中所述双极板具有多孔道毛细结构和密闭内腔。CN114300704A的实施方式没有考虑到热管中换热工质的流动性及传热性能，没有给出具体的双极板内部优化结构。
发明内容
鉴于上述现有技术的状态而做出本申请。本申请的目的在于提供一种用于燃料电池的热管双极板，可以在提高燃料电池散热性能的同时减小燃料电池热管理***的体积和重量。
本申请还提供一种包括前述用于燃料电池的热管双极板的燃料电池电堆。
本申请的实施方式提供一种用于燃料电池的热管双极板，所述热管双极板包括彼此重叠设置的阳极板和阴极板，
所述阳极板和所述阴极板分别包括多个横截面为矩形或梯形的凸起，所述阳极板和所述阴极板以它们的所述凸起彼此远离的方式设置，在所述阳极板和所述阴极板之间限定出换热工质流动通道，所述换热工质流动通道内填充换热工质，
所述换热工质流动通道包括毛细芯结构、蒸汽腔，
所述毛细芯结构包括支撑毛细芯和壁面毛细芯，所述支撑毛细芯设置在所述阳极板和所述阴极板之间以使所述阳极板和所述阴极板隔开间隔地支撑所述阳极板和所述阴极板，
所述壁面毛细芯设置于所述阳极板和所述阴极板的所述凸起的内表面，
在所述阳极板和所述阴极板的相对的所述凸起之间，所述阳极板、所述阴极板和所述毛细芯结构在所述换热工质流动通道内限定出所述蒸汽腔。
在至少一个可能的实施方式中，在所述阳极板和所述阴极板的相对的所述凸起的整个内表面都覆盖有所述壁面毛细芯，
所述支撑毛细芯间隔分布于所述阳极板与所述阴极板之间，
所述支撑毛细芯连接相邻两个所述蒸汽腔且延伸至其端部与所述壁面毛细芯平齐。
在至少一个可能的实施方式中，在所述阳极板和所述阴极板的相对的所述凸起的整个内表面都覆盖有所述壁面毛细芯，
所述支撑毛细芯在所述阳极板与所述阴极板之间形成连续的一层结构，
所述支撑毛细芯的两侧分别连接到所述阳极板、所述阴极板以及所述壁面毛细芯。
在至少一个可能的实施方式中，所述支撑毛细芯包括型号不同的第一支 撑毛细芯和第二支撑毛细芯，所述第一支撑毛细芯与所述第二支撑毛细芯间隔交替分布，
所述壁面毛细芯仅设置于所述凸起的内表面的端面与一个侧面，
所述第一支撑毛细芯连接相邻两个所述蒸汽腔的相邻近且不连接所述壁面毛细芯的侧面，所述第一支撑毛细芯的端部与所述蒸汽腔的侧面平齐，
所述第二支撑毛细芯连接相邻近的所述壁面毛细芯，用于连通相邻的所述蒸汽腔并输送所述换热工质，所述第二支撑毛细芯的端部与所述壁面毛细芯平齐。
在至少一个可能的实施方式中，所述阳极板与所述阴极板的形成所述换热工质流动通道的所述凸起对齐，或者错开一定距离。
在至少一个可能的实施方式中，所述支撑毛细芯与所述壁面毛细芯连接或者分开。
本申请的实施方式还提供一种燃料电池电堆，包括：
膜电极组件；以及
前述的热管双极板，所述膜电极组件抵靠所述阳极板或所述阴极板的所述凸起。
在至少一个可能的实施方式中，至少一个所述膜电极组件的一侧连接到一个所述热管双极板的所述阳极板，所述阳极板的相邻凸起及该膜电极组件限定出燃料通道，
所述至少一个膜电极组件的另一侧连接到另一个所述热管双极板的所述阴极板，所述阴极板的相邻凸起及该膜电极组件限定出氧化剂通道。
本申请的实施方式还提供一种燃料电池，其使用前述的燃料电池电堆，
所述燃料电池包括：
一个或多个冷凝散热区；以及
反应吸热区、燃料入口、氧化剂入口、燃料出口、氧化剂出口，
所述热管双极板在所述反应吸热区吸热在所述冷凝散热区散热，从而为所述燃料电池散热。
在至少一个可能的实施方式中，所述一个或多个冷凝散热区连接到外置的冷却装置，
所述冷却装置为风冷装置或者液冷装置。
附图说明
图1为根据本申请的一个实施方式的热管双极板的结构示意图。
图2为根据本申请的一个实施方式的燃料电池电堆的结构示意图。
图3为根据本申请的一个实施方式的燃料电池电堆的下层结构示意图。
图4A为根据本申请的第二实施方式的热管双极板的结构示意图。
图4B为根据本申请的第三实施方式的热管双极板的结构示意图。
图5为根据本申请的一个实施方式的燃料电池的布局示意图。
图6为图5所示的燃料电池的热管双极板的局部放大示意图。
图7为图5所示的燃料电池的热管双极板的在A-A截面的结构示意图。
附图标记说明
100 热管双极板
110 阳极板
120 阴极板
130 毛细芯结构
131 支撑毛细芯
1311 第一支撑毛细芯
1312 第二支撑毛细芯
132 壁面毛细芯
140 蒸汽腔
200 燃料电池电堆
210 膜电极组件
220 燃料通道
230 氧化剂通道
240 燃料电池壳体
300 燃料电池
310 冷凝散热区
320 反应吸热区
330 燃料入口
340 氧化剂入口
350 燃料出口
360 氧化剂出口
具体实施方式
下面参照附图描述本申请的示例性实施方式。应当理解，这些具体的说明仅用于示教本领域技术人员如何实施本申请，而不用于穷举本申请的所有可行的方式，也不用于限制本申请的范围。
本申请的实施方式提供一种热管双极板100，如图1所示，本申请的热管双极板100可以包括阳极板110、阴极板120、毛细芯结构130。
具体的，如图1所示，阳极板110、阴极板120可以分别形成多个凸起。阳极板110的相邻凸起(及后述的膜电极组件210)之间可以形成供燃料(例如，氢气)流动的燃料通道220，阴极板120的相邻凸起(及后述的膜电极组件210)之间可以形成供氧化剂(例如，氧气)流动的供氧化剂通道230。
阳极板110和阴极板120分别包括多个横截面为矩形或梯形的凸起，阳极板110和阴极板120以它们的凸起彼此远离的方式设置，在阳极板110和阴极板120之间限定出换热工质流动通道。换热工质流动通道包括毛细芯结构130、蒸汽腔140。
毛细芯结构130可以包括支撑毛细芯131和壁面毛细芯132。支撑毛细芯131可以位于阳极板110与阴极板120之间，使阳极板110和阴极板120隔开间隔地支撑阳极板110和阴极板120。壁面毛细芯132可以布置在阳极板110与阴极板120限定出的组成换热工质流动通道的凸起的内表面。支撑毛细芯131可以与壁面毛细芯132相连接或者分开。
在阳极板110和阴极板120的相对的凸起之间，阳极板110、阴极板120和毛细芯结构130在换热工质流动通道内限定出蒸汽腔140。
优选的，支撑毛细芯131和阳极板与阴极板限定出的换热工质流动通道内部的壁面毛细芯132平齐，以使蒸汽腔140的侧面平滑。
可选的，阳极板110与阴极板120的供氧化剂或燃料流动的通道可以对齐，如图1所示；或者沿支撑毛细芯131的延伸方向(图1中的左右方向、图7中的上下方向)错开一定距离，如图6、图7所示。
优选的，阳极板110与阴极板120的材料可以选用金属板、无孔石墨板、复合石墨板等。
进一步的，换热工质流动通道内可以填充换热工质。换热工质流动的通道由多个蒸汽腔140与毛细芯结构130组成(即形成热管结构)。燃料电池工作时，膜电极组件210是主要的热量来源，换热工质可以在换热工质流动通道内的壁面毛细芯132处吸收燃料电池工作时产生的热量。可以理解，蒸汽腔140是主要的气态换热工质流动通道，毛细芯结构130是主要的液态换热工质流动通道，换热工质主要在与膜电极组件210相邻近的壁面毛细芯132处吸热并蒸发汽化，但这并不排除换热工质在其流动通道内任意位置均可能发生相变。
如图5所示，利用热传导原理，换热工质在气液相界面吸热蒸发汽化后进入蒸发腔140内。气态的换热工质，在热扩散的压力梯度作用下流向燃料电池的冷凝散热区310。气态的换热工质在冷凝散热区310放出热量并冷凝为 液态，液态的换热工质再依靠毛细芯结构130的毛细作用回流并吸热蒸发至蒸汽腔140。换热工质在其流动通道(热管)内不断循环重复上述的换热工质的相变传热过程。
优选的，换热工质可以选用水、丙酮等材料。
可以理解，毛细芯结构130中支撑毛细芯131和壁面毛细芯132只是为方便说明而作的划分，而非基于功能性或者结构性的划分。支撑毛细芯131与壁面毛细芯132均可以承担支撑燃料电池和传递换热工质的作用。
优选的，支撑毛细芯131与壁面毛细芯132可以选用相同或者不同的毛细芯类型，例如，沟槽、丝网、编织网、粉末烧结颗粒等毛细芯类型。
可选的，在一些情况下，支撑毛细芯131可以由空隙率较小或者实心的支撑结构代替。
优选的，支撑毛细芯131与壁面毛细芯132的厚度、结构、截面形状、混合孔径、梯度、润湿性处理等可以依据换热工质的流动通道的参数等确定。
本申请的实施方式还提供一种燃料电池电堆200，包括上述的热管双极板100及膜电极组件210。
具体的，如图2、图3所示，膜电极组件210的两侧可以分别连接热管双极板100。示例性的，在一个燃料电池电堆200中的一个单电池中，膜电极组件210的下侧连接到一个热管双极板100的阳极板110，膜电极组件210的上侧连接到另一个热管双极板100的阴极板120。阳极板110上表面形成的通道结构与膜电极组件210结合形成燃料(例如，氢气)通道220。阴极板120的下表面形成的通道结构与膜电极组件210结合形成氧化剂(例如，氧气)通道230。可以理解，阳极板110和阴极板120相对于膜电极组件210的位置可以互换。可以理解，本申请不限制燃料电池电堆200或者燃料电池300的使用方向或姿态
氢气与氧气在膜电极组件210处发生化学反应，将化学能转化为电能。 多个上述燃料电池电堆200重复堆叠形成燃料电池电堆。
特别的，燃料电池电堆200的最上层与最下层的热管双极板仅保留阳极板110或者阴极板120。示例性的，如图3所示为燃料电池电堆的最下层结构，下侧的热管双极板100的支撑毛细芯131不再连接到阴极板120，而是连接到燃料电池壳体240。
优选地，热管双极板100的气体流道类型可为平行通道流场、多通道蛇形流场和交指型流场等，阳极板110和阴极板120可以选用相同或不同的流道类型。
示例性的，下面提供三种可能的热管双极板100及燃料电池电堆200的具体结构的实施方式。
第一实施方式
在本申请的热管双极板100的第一实施方式中，如图1、图2、图3所示，壁面毛细芯132可以覆盖于阳极板110和阴极板120的凸起的整个内表面。支撑毛细芯131位于阳极板110与阴极板120之间，且间隔分布，并连接换热工质流动通道内部的壁面毛细芯132。支撑毛细芯131端部可以与壁面毛细芯132平齐。
这种布置方式的支撑毛细芯131及壁面毛细芯132组成的毛细芯结构130，较均匀的分布于阳极板110与阴极板120之间，形成流动性好但结构简单的换热工质流动通道(热管)，适用于大部分的燃料电池双极板。
第二实施方式
在本申请的热管双极板100的第二实施方式中，如图4A所示，支撑毛细芯131可以在阳极板110与阴极板120中间形成连续的一层毛细芯，将蒸汽腔140分成上下两部分。壁面毛细芯132可以覆盖于阳极板110和阴极板120的凸起的整个内表面，并且连接到支撑毛细芯131。
本实施方式提供的热管双极板100使用连续的支撑毛细芯131，相比于第 一实施方式减小了接触电阻，故而降低了欧姆极化效应。该实施方式中的液态换热工质的流阻较小，而气态换热工质的流阻较大，适合应用于纵横比较大的流道结构。
第三实施方式
在本申请的热管双极板100的第三实施方式中，如图4B所示，壁面毛细芯132可以仅设置于阳极板110和阴极板120的凸起的内部靠近膜电极组件210的端面与一个侧面，并且可以采用横截面(厚度)较大的毛细芯选型。本实施方式中的支撑毛细芯132可以间隔分布，并且可以使用两种不同类型支撑毛细芯1311、1312。
与壁面毛细芯132不连接的第一支撑毛细芯1311的孔隙率可以较小，其端部连接相邻两个蒸汽腔140并且与蒸汽腔140的侧面平齐。第一支撑毛细芯1311主要承担支撑热管双极板100的作用。
连接相邻的两个壁面毛细芯132的第二支撑毛细芯1312孔隙率可以较大、液态换热工质流阻较低，其在热管双极板100中同时起支撑和传质作用。第二支撑毛细芯1312端部可以与壁面毛细芯132平齐。
应当理解，上述实施方式、实施例或示例及其部分方面或特征可以适当地组合。
本申请的实施方式还提供一种燃料电池300，其使用上述的热管双极板100或者燃料电池电堆200。
如图5所示，燃料电池300可以包括冷凝散热区310、反应吸热区320、燃料入口330、氧化剂入口340、燃料出口350、氧化剂出口360。
特别的，区别于传统的燃料电池，本申请的燃料电池300采用上述的热管双极板100或者燃料电池电堆200，换热工质在结构内部相变流动，不需要设置冷却液入口和冷却液出口。
具体的，燃料电池电堆200设置在反应吸热区320，燃料电池电堆在工作 时发生电化学反应释放热量使换热工质在蒸汽腔140内吸热汽化。气态换热工质随压力梯度进入冷凝散热区310，并在此释放热量冷凝液化。液化后的换热工质由于毛细芯结构130的毛细作用回流到反应吸热区320。换热工质在燃料电池的热管双极板100内不断重复上述过程，在反应吸热区320及冷凝散热区310之间相变流动，实现对燃料电池300较好的冷却散热效果。
图6示出了燃料电池电堆200中的一层热管双极板100的结构，图7给出了该热管双极板100的一种可能的结构图。图7中，下侧的换热工质流动通道的腔体连接到冷凝散热区310。可选的，如图6、图7所示，阳极板110和阴极板120的用于形成换热工质流动通道的凸起可以对齐或者不完全对齐并错开一定距离。
示例性的，图5中冷凝散热区310布置在垂直于燃料及氧化剂流动方向的两侧，可以采用上述第一实施方式和第二实施方式的热管双极板100的结构。冷凝散热区310还可以布置在燃料及氧化剂的流动方向的两侧，可以采用上述第三实施方式的热管双极板100的结构。可以理解，当燃料电池300的冷却散热要求不高时，也可以仅在反应吸热区320的一侧设置冷凝散热区310。
优选的，冷凝散热区310可以连接到外置的冷却装置，该冷却装置可以为风冷或者液冷装置。
优选的，燃料电池300可以设置有多个冷凝散热区310。冷凝散热区310的结构可为板式、波浪式、板翅式等。冷凝散热区310可分布于反应吸热区320的一侧或多侧，其表面可以布置强化对流换热的微通道结构。
下面简单说明本申请的上述实施方式的部分有益效果。
(i)本申请的用于燃料电池的热管双极板、燃料电池电堆及燃料电池采用热管式的热管理***，与液冷式燃料电池热管理***相比，基于热管双极板的热管理***结构简单，无水泵、水箱等附件，可大幅提高燃料电池***的功率密度。
(ii)本申请的用于燃料电池的热管双极板、燃料电池电堆及燃料电池，将热管与双极板一体化设计并具体给出了热管双极板的几种可能的内部结构，相比于现有的热管嵌入式双极板，可以进一步降低燃料电池电堆的厚度和电堆体积，并提高燃料电池的散热性能。
(iii)本申请的用于燃料电池的热管双极板、燃料电池电堆及燃料电池，相比现有的热管双极板技术，其具体的支撑毛细芯与壁面毛细芯结构设计可以在小幅增加极板厚度的情况下(大约0.1～0.4mm)，大幅增加液态和气态换热工质的通流面积，从而降低流体压降，避免蒸汽腔尺寸小于压降剧增的临界值(约0.3mm)，使得超薄热管的极限传热能力增加，满足日益增长的燃料电池散热需求。
可以理解，在本申请中，未特别限定部件或构件的数量时，其数量可以是一个或多个，这里的多个是指两个或更多个。对于附图中示出和/或说明书描述了部件或构件的数量为例如两个、三个、四个等的具体数量的情况，该具体数量通常是示例性的而非限制性的，可以将其理解为多个，即两个或更多个，但是，这不意味着本申请排除了一个的情况。
应当理解，上述实施方式仅是示例性的，不用于限制本申请。本领域技术人员可以在本申请的教导下对上述实施方式做出各种变型和改变，而不脱离本申请的范围。

Claims (10)

  1. 一种用于燃料电池的热管双极板，其特征在于，所述热管双极板(100)包括彼此重叠设置的阳极板(110)和阴极板(120)，
    所述阳极板(110)和所述阴极板(120)分别包括多个横截面为矩形或梯形的凸起，所述阳极板(110)和所述阴极板(120)以它们的所述凸起彼此远离的方式设置，在所述阳极板(110)和所述阴极板(120)之间限定出换热工质流动通道，所述换热工质流动通道内填充换热工质，
    所述换热工质流动通道包括毛细芯结构(130)、蒸汽腔(140)，
    所述毛细芯结构(130)包括支撑毛细芯(131)和壁面毛细芯(132)，所述支撑毛细芯(131)设置在所述阳极板(110)和所述阴极板(120)之间以使所述阳极板(110)和所述阴极板(120)隔开间隔地支撑所述阳极板(110)和所述阴极板(120)，
    所述壁面毛细芯(132)设置于所述阳极板(110)和所述阴极板(120)的所述凸起的内表面，
    在所述阳极板(110)和所述阴极板(120)的相对的所述凸起之间，所述阳极板(110)、所述阴极板(120)和所述毛细芯结构(130)在所述换热工质流动通道内限定出所述蒸汽腔(140)。
  2. 根据权利要求1所述的热管双极板，其特征在于，
    在所述阳极板(110)和所述阴极板(120)的相对的所述凸起的整个内表面都覆盖有所述壁面毛细芯(132)，
    所述支撑毛细芯(131)间隔分布于所述阳极板(110)与所述阴极板(120)之间，
    所述支撑毛细芯(131)连接相邻两个所述蒸汽腔(140)且延伸至其端部与所述壁面毛细芯(132)平齐。
  3. 根据权利要求1所述的热管双极板，其特征在于，
    在所述阳极板(110)和所述阴极板(120)的相对的所述凸起的整个内 表面都覆盖有所述壁面毛细芯(132)，
    所述支撑毛细芯(131)在所述阳极板(110)与所述阴极板(120)之间形成连续的一层结构，
    所述支撑毛细芯(131)的两侧分别连接到所述阳极板(110)、所述阴极板(120)以及所述壁面毛细芯(132)。
  4. 根据权利要求1所述的热管双极板，其特征在于，
    所述支撑毛细芯(131)包括型号不同的第一支撑毛细芯(1311)和第二支撑毛细芯(1312)，所述第一支撑毛细芯(1311)与所述第二支撑毛细芯(1312)间隔交替分布，
    所述壁面毛细芯(132)仅设置于所述凸起的内表面的端面与一个侧面，
    所述第一支撑毛细芯(1311)连接相邻两个所述蒸汽腔(140)的相邻近且不连接所述壁面毛细芯(132)的侧面，所述第一支撑毛细芯(1311)的端部与所述蒸汽腔(140)的侧面平齐，
    所述第二支撑毛细芯(1312)连接相邻近的所述壁面毛细芯(132)，用于连通相邻的所述蒸汽腔(140)并输送所述换热工质，所述第二支撑毛细芯(1312)的端部与所述壁面毛细芯(132)平齐。
  5. 根据权利要求1至4中任一项所述的热管双极板，其特征在于，所述阳极板(110)与所述阴极板(120)的形成所述换热工质流动通道的所述凸起对齐，或者错开一定距离。
  6. 根据权利要求1至4中任一项所述的热管双极板，其特征在于，所述支撑毛细芯(131)与所述壁面毛细芯(132)连接或者分开。
  7. 一种燃料电池电堆，其特征在于，包括：
    膜电极组件(210)；以及
    权利要求1至6中任一项所述的热管双极板(100)，所述膜电极组件(210)抵靠所述阳极板(110)或所述阴极板(120)的所述凸起。
  8. 根据权利要求7所述的燃料电池电堆，其特征在于，
    至少一个所述膜电极组件(210)的一侧连接到一个所述热管双极板(100)的所述阳极板(110)，所述阳极板(110)的相邻凸起及该膜电极组件(210)限定出燃料通道(220)，
    所述至少一个膜电极组件(210)的另一侧连接到另一个所述热管双极板(100)的所述阴极板(120)，所述阴极板(120)的相邻凸起及该膜电极组件(210)限定出氧化剂通道(230)。
  9. 一种燃料电池，其特征在于，其使用权利要求7或8所述的燃料电池电堆，
    所述燃料电池(300)包括：
    一个或多个冷凝散热区(310)；以及
    反应吸热区(320)、燃料入口(330)、氧化剂入口(340)、燃料出口(350)、氧化剂出口，
    所述热管双极板在所述反应吸热区(320)吸热在所述冷凝散热区(310)散热，从而为所述燃料电池散热。
  10. 根据权利要求9所述的燃料电池，其特征在于，所述一个或多个冷凝散热区(310)连接到外置的冷却装置，
    所述冷却装置为风冷装置或者液冷装置。
PCT/CN2022/119578 2022-09-01 2022-09-19 用于燃料电池的热管双极板、燃料电池电堆 WO2024045228A1 (zh)

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