CN113178592A - Proton exchange membrane fuel cell - Google Patents
Proton exchange membrane fuel cell Download PDFInfo
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- CN113178592A CN113178592A CN202110386541.2A CN202110386541A CN113178592A CN 113178592 A CN113178592 A CN 113178592A CN 202110386541 A CN202110386541 A CN 202110386541A CN 113178592 A CN113178592 A CN 113178592A
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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
- 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
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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
- H01M8/04—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
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
- H01M8/04126—Humidifying
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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
- H01M8/04—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
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
- H01M8/04156—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal
- H01M8/04164—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal by condensers, gas-liquid separators or filters
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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
- H01M8/10—Fuel cells with solid electrolytes
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- 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
Abstract
The invention relates to a proton exchange membrane fuel cell, comprising: a battery reactor and a water diversion system; the battery reactor comprises a positive plate, a negative plate, a cathode flow field chamber, a plurality of anode flow field chambers, at least one anode partition plate and a tail exhaust electromagnetic valve, wherein a reactor reaction interval is formed between the positive plate and the negative plate, anode gas and cathode gas are respectively introduced into the reactor reaction interval from the positive plate and the negative plate, the cathode flow field chambers are positioned on one side inside the reactor reaction interval, the anode flow field chambers are correspondingly arranged on the other side inside the reactor reaction interval, the anode flow field chambers are sequentially arranged from front to back in the direction from the positive plate to the negative plate, every two adjacent anode flow field chambers are separated by the anode partition plate, and the tail exhaust electromagnetic valve is arranged at the rear end of the anode flow field chamber at the rearmost end; the water diversion system comprises at least one water diverter, and a water diverter is correspondingly arranged between every two adjacent anode flow field chambers.
Description
Technical Field
The invention relates to the technical field of fuel cells, in particular to a proton exchange membrane fuel cell.
Background
Proton exchange membrane fuel cells have been widely used in the fields of transportation vehicles, buses, ships, underwater vehicles, spacecraft, and the like. Compared to other power source type technologies, pem fuel cells have many advantages, including short start-up time, small system size, low pollutant emissions, relatively high system efficiency, and low noise levels. In a proton exchange membrane fuel cell system for a vehicle, pure hydrogen is generally used as a power generation fuel, and hydrogen gas that has not been sufficiently used will be discharged to the atmosphere together with impurity gases. However, in order to achieve maximum power generation efficiency of the fuel cell power system and to ensure safe use conditions of the fuel cell power system, it is required that the system should consume as little fuel as possible at a given output power, and should minimize the discharge of hydrogen to the outside environment.
The ratio of hydrogen consumed by the fuel cell to generate heat and electricity to hydrogen supplied to the fuel cell system is currently defined as the fuel hydrogen utilization. If the fuel cell system is operating at 100% utilization, the amount of hydrogen fed to the anode of the fuel cell will be the same as the stoichiometric flow of hydrogen required for the electrochemistry, referred to as dead-end operation. However, in dead-end operation, there is a risk of fuel starvation at the fuel cell outlet, which may lead to cell voltage instability and cell performance degradation. The main reasons for this effect are the accumulation of liquid water at the anode and the accumulation of impurity gases at the anode and nitriding at the cathode, resulting in hydrogen starvation or even starvation at the anode tail. Therefore, in the conventional electric pile, hydrogen is supplied to the pem fuel cell in an amount much larger than the stoichiometric flow rate during operation, so as to provide sufficient forced convection and excess gas, discharge accumulated product water from the anode, and reduce the concentration of impurity gas and nitrogen, generally, the fuel utilization rate of such a pem fuel cell system without a hydrogen circulation system is about 80-90%, and the excess hydrogen and impurity gas are discharged directly or intermittently to the external environment in an excess manner. In order to further improve the utilization rate of the fuel, technicians develop a hydrogen pump and a hydrogen ejector, hydrogen is sucked to an inlet from an outlet of the electric pile again, and the utilization rate of the fuel can be improved to more than 95%. However, such a circulation system still has the following problems: because of the accumulation effect of the impurity gas (mainly from the impurity gas contained in the nitrogen and hydrogen permeating from the cathode side to the anode), the closed hydrogen circulation system needs to continuously and intermittently discharge the gas to reach the balance of hydrogen concentration, at the moment, the pulse discharged gas contains a large amount of hydrogen, and the improvement of the fuel utilization rate is limited; secondly, the addition of a circulating pump additionally increases the components of the system, increases the complexity and cost of the system, reduces the reliability of the system and increases the power consumption; in addition, the hydrogen ejector has limited hydrogen consumption amount of the galvanic pile under the low-load working condition, so that enough ejection gas is difficult to generate to meet the full-power use requirement of the galvanic pile.
Disclosure of Invention
In view of the above, there is a need to provide a chemical immunoassay analyzer for solving the technical problem of large occupied space of the prior art immunoassay analyzer workbench.
The invention provides a proton exchange membrane fuel cell, comprising: a battery reactor and a water diversion system;
the battery reactor comprises a positive plate, a negative plate, a cathode flow field chamber, a plurality of anode flow field chambers, at least one anode separator plate and a tail exhaust electromagnetic valve, a reactor reaction zone is formed between the positive plate and the negative plate, anode gas and cathode gas are respectively introduced into the reactor reaction zone from the positive plate and the negative plate, the cathode flow field chambers are positioned on one side in the reactor reaction section, the plurality of anode flow field chambers are correspondingly arranged on the other side in the reactor reaction section, the plurality of anode flow field chambers are sequentially arranged from front to back in the direction from the positive plate to the negative plate, every two adjacent anode flow field chambers are separated by the anode partition plate, and the tail exhaust electromagnetic valve is arranged at the rear end of the anode flow field chamber at the rearmost end and used for exhausting reaction products at an anode exhaust port;
the water diversion system comprises at least one water diverter, and one water diverter is correspondingly arranged between every two adjacent anode flow field chambers; the water separator is used for separating anode gas and water of a gas-liquid mixed product in the anode flow field chamber at the front end, and introducing the separated anode gas into the anode flow field chamber at the rear end.
Furthermore, the water separator is provided with a feeding end, a water outlet end and an air outlet end, the feeding end of the water separator is communicated with the anode flow field cavity at the front end, the air outlet end of the water separator is communicated with the anode flow field cavity at the rear end, and the water outlet end of the water separator is arranged corresponding to the anode product water outlet.
Furthermore, the water diversion system further comprises a liquid level sensor and a drainage electromagnetic valve, wherein each liquid level sensor corresponds to one of the water distributors, and each water outlet end of each water distributor is provided with a drainage electromagnetic valve.
Furthermore, the number of the anode gas flow field chambers is 4, and the occupied space of the four anode gas flow field chambers is reduced from front to back in sequence.
The device further comprises a humidifying system, wherein the humidifying system is arranged outside the reactor reaction section and is used for humidifying anode gas and cathode gas.
Furthermore, the humidifying system comprises an anode gas humidifier, a cathode gas humidifier, a first humidifying membrane, a second humidifying membrane and a humid air chamber, the anode gas humidifier and the cathode gas humidifier are respectively arranged on two sides of the humid air chamber, the first humidifying membrane is arranged between the anode gas humidifier and the humid air chamber, the second humidifying membrane is arranged between the cathode gas humidifier and the humid air chamber, the side wall of the humid air chamber can leak moisture to the first humidifying membrane and the second humidifying membrane, the air inlet end of the humid air chamber is communicated with the air outlet of the cathode gas, and the air outlet end of the humid air chamber is connected with a gas silencer.
Further, the anode gas is air, and the cathode gas is hydrogen.
Further, still include air supply system, air supply system includes air cleaner and air compressor machine, air cleaner's the end of giving vent to anger with the inlet end of air compressor machine links to each other, the end of giving vent to anger of air compressor machine with the inlet end of cathode gas humidifier links to each other.
Further, the hydrogen humidifier also comprises a hydrogen supply system, wherein the hydrogen supply system comprises a hydrogen high-pressure storage tank and a hydrogen pressure reducing valve, and a gas outlet of the hydrogen high-pressure storage tank is connected with the anode gas humidifier through the hydrogen pressure reducing valve.
Furthermore, the anode separator plate is made of metal conductive materials.
The utility model provides a proton exchange membrane fuel cell, it sets up a plurality of positive pole flow field chambers that are separated by the positive pole division board in the pile reaction interval between positive plate and negative plate, guarantee the normal discharge of sufficient and reactant of positive pole reaction gas concentration, and because the gaseous consumption of positive pole in the one-level positive pole flow field chamber of back, can realize the siphon effect to preceding one-level, drive the gaseous passive suction of positive pole, and do not have the anode flow field chamber of siphon effect to last one-level, adopt the mode drive anode gas of pulse tail row to flow through the tail solenoid valve of arranging, and then guarantee that the battery generates electricity steadily, realize the gaseous high-efficient utilization of positive pole.
The foregoing is a summary of the present invention, and in order to provide a clear understanding of the technical means of the present invention and to be implemented in accordance with the present specification, the following is a detailed description of the preferred embodiments of the present invention.
Drawings
Fig. 1 is a schematic structural diagram of a proton exchange membrane fuel cell according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a cell reactor and a water diversion system according to an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a humidifying system in an embodiment of the present invention;
FIG. 4 is a schematic diagram of the flow of reactant gases in a PEM fuel cell according to an embodiment of the present invention.
Detailed Description
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate preferred embodiments of the invention and together with the description, serve to explain the principles of the invention and not to limit the scope of the invention.
As shown in fig. 1, an embodiment of the present invention provides a proton exchange membrane fuel cell, which includes a cell reactor 10, a water diversion system 20, and a humidification system 30.
As shown in fig. 2, the battery reactor includes a positive plate 11, a negative plate 12, a cathode flow field chamber 13, a plurality of anode flow field chambers, at least one anode separator 14, and a tail exhaust solenoid valve 15; in the preferred embodiment of the present application, the number of anode flow field chambers is 4, and the footprint of the four anode gas flow field chambers decreases from front to back in sequence. It will be appreciated that in other embodiments of the present application, other numbers of anode flow field chambers are possible.
Form the reactor reaction interval 1a between positive plate 11 and the negative plate 12, anode gas and cathode gas pass into the reactor reaction interval 1a from positive plate 11 and negative plate 12 respectively, cathode flow field chamber 13 is located the inside one side of reactor reaction interval 1a, 4 corresponding settings in the inside opposite side of reactor reaction interval 1a of positive pole flow field chamber, 4 positive pole flow field chambers arrange the setting in proper order from the front to the back according to the direction from positive plate 11 to negative plate 12, and every two adjacent positive pole flow field chambers are separated by anode splitter 14, tail discharge solenoid valve 15 is installed in the rear end of the positive pole flow field chamber of rearmost end, in order to be used for the discharge of anode exhaust mouth reaction product.
The water diversion system 20 comprises at least one water diverter, and a water diverter is correspondingly arranged between every two adjacent anode flow field chambers; the water separator is used for separating anode gas and water of a gas-liquid mixed product in the anode flow field chamber at the front end, and introducing the separated anode gas into the anode flow field chamber at the rear end.
As described above, the number of the water separators is equal to the number of the anode flow field chambers-1, so in the embodiment of the present application, the number of the water separators is 3, for convenience of description, 4 anode flow field chambers are sequentially a first-stage anode chamber 161, a second-stage anode chamber 162, a third-stage anode chamber 163, and a fourth-stage anode chamber 164, and 3 water separators are sequentially a first-stage water separator 211, a second-stage water separator 212, and a third-stage water separator 213.
In the embodiment of the application, 3 anode flow field chambers separated by an anode separator plate 14 are arranged in a pile reaction section 1a between an anode plate 11 and a cathode plate 12, so that 4-stage reaction is formed in the anode reaction section, anode gas required by the reaction of the next-stage anode flow field chamber needs to flow through the previous-stage anode flow field chamber, an excess coefficient is formed between the total amount of gas entering each-stage anode flow field chamber and the anode gas required by each-stage reaction, sufficient concentration of the anode reaction gas and normal discharge of reactants are ensured, siphon effect is realized on the previous stage due to consumption of the anode gas in the next-stage anode flow field chamber, passive suction of the anode gas is driven, and the anode gas is driven to flow by a tail discharge electromagnetic valve in a pulse tail discharge mode for the anode flow field chamber without siphon effect of the last stage, so as to ensure stable power generation of a battery, the efficient utilization of the anode gas is realized.
The water separators in the embodiment of the application are identical in structure, and take any water separator as an example, the water separator is provided with a feeding end, a water outlet end and an air outlet end, the feeding end of the water separator is communicated with the anode flow field cavity at the front end, the air outlet end of the water separator is communicated with the anode flow field cavity at the rear end, and the water outlet end of the water separator is arranged corresponding to the anode product water outlet.
Preferably, the water diversion system 20 further comprises liquid level sensors 22 and water drainage electromagnetic valves 23, each liquid level sensor 22 is arranged corresponding to a water diversion device, and a water drainage electromagnetic valve 23 is installed at the water outlet end of each water diversion device; and then each water separator is subjected to closed-loop control, so that automatic water separation and drainage are realized.
In the present embodiment, the anode gas is air and the cathode gas is hydrogen, unless otherwise specified.
The humidification system 30 is installed outside between the reactor reaction regions 1a and is used to humidify the anode gas and the cathode gas.
As shown in fig. 3, the humidification system 30 includes an anode gas humidifier 31, a cathode gas humidifier 32, a first humidification film 33, a second humidification film 34 and a moisture chamber 35, the anode gas humidifier 31 and the cathode gas humidifier 32 are respectively installed at two sides of the moisture chamber 35, the first humidification film 33 is disposed between the anode gas humidifier 31 and the moisture chamber 35, the second humidification film 34 is disposed between the cathode gas humidifier 32 and the moisture chamber 35, the side wall of the moisture chamber 35 can leak moisture onto the first humidification film 33 and the second humidification film 34, the air inlet end of the moisture chamber 35 is communicated with the air outlet of the cathode gas, and the air outlet end of the moisture chamber 35 is connected to a gas silencer 36.
The embodiment of the application utilizes a large amount of product water and wet steam existing in the cathode exhaust port, and dry air and dry hydrogen are effectively humidified through the membrane humidification principle, so that the reactant utilization rate of the fuel cell system is effectively improved.
Preferably, the embodiment of the present invention further includes an air supply system 40 and a hydrogen supply system 50, wherein the air supply system 40 includes an air filter 41 and an air compressor 42, an air outlet of the air filter 41 is connected to an air inlet of the air compressor 42, and an air outlet of the air compressor 42 is connected to an air inlet of the cathode humidifier 32.
The fresh and dry air passes through the air filter 41, so that the impurity and dust in the air can be effectively filtered; the clean air enters the air compressor 42 to raise the air pressure to operating pressure to facilitate efficient cathode reactant gas delivery to the cell reactor 10.
The hydrogen supply system 50 includes a hydrogen high-pressure storage tank 51 and a hydrogen pressure reducing valve 52, the outlet of the hydrogen high-pressure storage tank 51 is connected to the anode gas humidifier 32 via the hydrogen pressure reducing valve 52, and the hydrogen high-pressure storage tank 51 serves as a high-pressure hydrogen source, which is depressurized by the hydrogen pressure reducing valve 52 and then enters the anode gas humidifier 32 to be humidified.
In the embodiment of the present application, the anode separator 14 is made of a metal conductive material, such as a copper plate or an aluminum plate.
With reference to fig. 1 to 4, the specific using process of the embodiment of the present invention is as follows: the fresh and dry air passes through the air filter 41 to filter foreign dust in the air; the air raises the cathode air pressure to the working pressure through the air compressor 42, and enters the cathode flow field chamber 13 of the cell reactor 10 through the cathode gas humidifier 32; the hydrogen high-pressure storage tank 51 enters the anode gas humidifier 31 through a hydrogen pressure reducing valve 52, and then enters the anode of the galvanic pile to participate in electrochemical reaction; the cathode product water is taken out along with excess air and enters the humidifying cavity to provide humidifying water for the cathode humidifier and the anode humidifier; the humidified hydrogen firstly enters the first-stage anode chamber 161 to participate in the reaction, and at this time, the gas passing through the first-stage anode chamber 161 comprises gas required by the first-stage cell reaction, gas required by the second, third and fourth-stage cell reactions, air permeating through the membrane of the first-stage cell, humidified water vapor, impurity gas and the like; because the gases required by the second-stage battery reaction, the third-stage battery reaction and the fourth-stage battery reaction need to flow through the first-stage anode chamber, the total amount of the gases and the gases required by the first-stage battery reaction can form an excess coefficient, and further the sufficient concentration of the anode reaction hydrogen and the discharge of water can be ensured; hydrogen consumed by the second, third and fourth stages of continuous reaction can form a siphon effect on the first stage to drive the passive suction of gas; in the same principle, the second-stage anode chamber 162 forms an excess by using the third and fourth-stage siphon effects, so that the stable flow of hydrogen and the discharge of product water in the second-stage anode chamber 162 are realized; the third stage anode chamber 163 is similar in principle; the fourth-stage anode chamber 164 is the last stage of the pile, has no siphon effect, and needs to drive the anode gas of the fourth-stage battery to flow in a pulse tail discharge mode to ensure the stable power generation of the battery; at the moment, the gas discharged from the pulse tail is mainly impurity gas and water vapor accumulated after four-stage reaction, and contains a small amount of hydrogen, so that the method can realize the efficient utilization of anode hydrogen.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention.
Claims (10)
1. A proton exchange membrane fuel cell comprising: a battery reactor and a water diversion system;
the battery reactor comprises a positive plate, a negative plate, a cathode flow field chamber, a plurality of anode flow field chambers, at least one anode separator plate and a tail exhaust electromagnetic valve, a reactor reaction zone is formed between the positive plate and the negative plate, anode gas and cathode gas are respectively introduced into the reactor reaction zone from the positive plate and the negative plate, the cathode flow field chambers are positioned on one side in the reactor reaction section, the plurality of anode flow field chambers are correspondingly arranged on the other side in the reactor reaction section, the plurality of anode flow field chambers are sequentially arranged from front to back in the direction from the positive plate to the negative plate, every two adjacent anode flow field chambers are separated by the anode partition plate, and the tail exhaust electromagnetic valve is arranged at the rear end of the anode flow field chamber at the rearmost end and used for exhausting reaction products at an anode exhaust port;
the water diversion system comprises at least one water diverter, and one water diverter is correspondingly arranged between every two adjacent anode flow field chambers; the water separator is used for separating anode gas and water of a gas-liquid mixed product in the anode flow field chamber at the front end, and introducing the separated anode gas into the anode flow field chamber at the rear end.
2. The pem fuel cell of claim 1 wherein said water separator has a feed end, a discharge end and a discharge end, said feed end of said water separator being in communication with said anode flow field chamber at the front end and said discharge end of said water separator being in communication with said anode flow field chamber at the rear end, said discharge end of said water separator being disposed in correspondence with the anode product water discharge port.
3. The pem fuel cell of claim 2 wherein said water separator system further comprises liquid level sensors and water discharge solenoid valves, each of said liquid level sensors being disposed corresponding to one of said water separators, and a water discharge solenoid valve being mounted at the water outlet end of each of said water separators.
4. The pem fuel cell of claim 2 wherein said number of anode gas flow field chambers is 4, and the footprint of four of said anode gas flow field chambers decreases sequentially from front to back.
5. The pem fuel cell of claim 1 further comprising a humidification system mounted outside said stack reaction zone for humidifying anode and cathode gases.
6. The pem fuel cell of claim 5 wherein said humidification system comprises an anode gas humidifier, a cathode gas humidifier, a first humidification membrane, a second humidification membrane and a humidification gas chamber, wherein said anode gas humidifier and said cathode gas humidifier are respectively installed on both sides of said humidification gas chamber, said first humidification membrane is installed between said anode gas humidifier and said humidification gas chamber, said second humidification membrane is installed between said cathode gas humidifier and said humidification gas chamber, the side wall of said humidification gas chamber can leak moisture onto said first humidification membrane and said second humidification membrane, the inlet of said humidification gas chamber is connected to the outlet of the cathode gas, and the outlet of said humidification gas chamber is connected to a gas silencer.
7. The pem fuel cell of claim 6 wherein said anode gas is air and said cathode gas is hydrogen.
8. The pem fuel cell of claim 7 further comprising an air supply system, said air supply system comprising an air filter and an air compressor, said air filter having an outlet connected to an inlet of said air compressor, said air compressor having an outlet connected to an inlet of said cathode humidifier.
9. The pem fuel cell of claim 7 further comprising a hydrogen supply system, wherein said hydrogen supply system comprises a high-pressure hydrogen storage tank and a hydrogen pressure reducing valve, and the outlet of said high-pressure hydrogen storage tank is connected to said anode gas humidifier via said hydrogen pressure reducing valve.
10. The pem fuel cell of claim 1 wherein said anode separator plate is fabricated from a metallic conductive material.
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| CN202110386541.2A CN113178592B (en) | 2021-04-12 | 2021-04-12 | Proton exchange membrane fuel cell |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110386541.2A CN113178592B (en) | 2021-04-12 | 2021-04-12 | Proton exchange membrane fuel cell |
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| CN113178592A true CN113178592A (en) | 2021-07-27 |
| CN113178592B CN113178592B (en) | 2022-05-24 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113791355A (en) * | 2021-08-17 | 2021-12-14 | 南昌智能新能源汽车研究院 | Method and system for quantitatively evaluating quality of fuel cell flow field design |
| CN114976122A (en) * | 2022-06-07 | 2022-08-30 | 武汉氢能与燃料电池产业技术研究院有限公司 | Reaction gas pressure control system and method for fuel cell |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060240302A1 (en) * | 2005-04-25 | 2006-10-26 | Ralf Senner | Fuel cell operating method with improved hydrogen and oxygen utilization |
| CN101577342A (en) * | 2009-06-08 | 2009-11-11 | 清华大学 | Fuel cell with humidification zone of single cell |
| CN102800876A (en) * | 2012-09-06 | 2012-11-28 | 江苏冰城电材股份有限公司 | Self-humidifying fuel cell |
-
2021
- 2021-04-12 CN CN202110386541.2A patent/CN113178592B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060240302A1 (en) * | 2005-04-25 | 2006-10-26 | Ralf Senner | Fuel cell operating method with improved hydrogen and oxygen utilization |
| CN101577342A (en) * | 2009-06-08 | 2009-11-11 | 清华大学 | Fuel cell with humidification zone of single cell |
| CN102800876A (en) * | 2012-09-06 | 2012-11-28 | 江苏冰城电材股份有限公司 | Self-humidifying fuel cell |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113791355A (en) * | 2021-08-17 | 2021-12-14 | 南昌智能新能源汽车研究院 | Method and system for quantitatively evaluating quality of fuel cell flow field design |
| CN113791355B (en) * | 2021-08-17 | 2024-04-19 | 南昌智能新能源汽车研究院 | Method and system for quantitatively evaluating fuel cell flow field design quality |
| CN114976122A (en) * | 2022-06-07 | 2022-08-30 | 武汉氢能与燃料电池产业技术研究院有限公司 | Reaction gas pressure control system and method for fuel cell |
| CN114976122B (en) * | 2022-06-07 | 2024-03-12 | 武汉氢能与燃料电池产业技术研究院有限公司 | System and method for controlling reaction gas pressure of fuel cell |
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| CN113178592B (en) | 2022-05-24 |
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