CN216648371U - Internal humidifying liquid cooling fuel cell stack - Google Patents
Internal humidifying liquid cooling fuel cell stack Download PDFInfo
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- CN216648371U CN216648371U CN202123346845.0U CN202123346845U CN216648371U CN 216648371 U CN216648371 U CN 216648371U CN 202123346845 U CN202123346845 U CN 202123346845U CN 216648371 U CN216648371 U CN 216648371U
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- 239000000446 fuel Substances 0.000 title claims abstract description 48
- 239000007788 liquid Substances 0.000 title claims abstract description 14
- 238000001816 cooling Methods 0.000 title abstract description 5
- 239000012528 membrane Substances 0.000 claims abstract description 89
- 238000006243 chemical reaction Methods 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 35
- 238000003487 electrochemical reaction Methods 0.000 claims abstract description 10
- 239000001301 oxygen Substances 0.000 claims abstract description 4
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- 239000000110 cooling liquid Substances 0.000 claims description 6
- UQSQSQZYBQSBJZ-UHFFFAOYSA-N fluorosulfonic acid Chemical compound OS(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-N 0.000 claims description 5
- 238000005192 partition Methods 0.000 claims description 5
- 239000004695 Polyether sulfone Substances 0.000 claims description 4
- 229920006393 polyether sulfone Polymers 0.000 claims description 4
- 239000004696 Poly ether ether ketone Substances 0.000 claims description 2
- 239000004642 Polyimide Substances 0.000 claims description 2
- 229920000491 Polyphenylsulfone Polymers 0.000 claims description 2
- 229920002492 poly(sulfone) Polymers 0.000 claims description 2
- 229920002530 polyetherether ketone Polymers 0.000 claims description 2
- 229920001721 polyimide Polymers 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 42
- 230000000694 effects Effects 0.000 abstract description 10
- 238000000034 method Methods 0.000 abstract description 9
- 238000009826 distribution Methods 0.000 abstract description 6
- 238000009792 diffusion process Methods 0.000 abstract description 4
- 230000007774 longterm Effects 0.000 abstract description 4
- 230000010354 integration Effects 0.000 abstract description 3
- 239000002826 coolant Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000012510 hollow fiber Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 239000003792 electrolyte Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
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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
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- Fuel Cell (AREA)
Abstract
The utility model relates to an internal humidifying liquid cooling fuel cell pile, which is divided into two sections, wherein one section is a humidifying section for humidifying fresh dry air by wet air after reaction, the other section is a reaction section for generating electric energy by hydrogen-oxygen electrochemical reaction, and the humidifying section is positioned between the reaction section and an air inlet and outlet end plate of the pile; the method can promote the air to diffuse to the humidifying membrane by changing the sectional area of the flow channel of the flow field at the two sides of the humidifying membrane at the humidifying section, thereby improving the humidifying effect; the air flow field of the reaction section can also promote the diffusion of air to the membrane electrode by changing the sectional area of the flow channel, thereby improving the performance of the cell. The utility model cancels an external humidifier and a humidifying heat-insulating pipeline, simplifies the system structure, and improves the system integration level, the system volume specific power and the system weight specific power; the edge effect of performance attenuation of single cells at two ends of the fuel cell is reduced, the uniformity of gas and water distribution in each cell is kept, the consistency of the galvanic pile is improved, and the long-term stable operation of the fuel cell is further promoted.
Description
Technical Field
The utility model relates to the technical field of fuel cells, in particular to a humidifying technology suitable for a liquid-cooled fuel cell.
Background
Fuel cells are one of the most desirable ways to utilize hydrogen energy. The Proton Exchange Membrane Fuel Cell (PEMFC) is a low-noise high-energy conversion efficiency zero-emission power generation device which can be quickly started, can be widely applied to a power supply for vehicles, a fixed power station, an aviation power supply, an underwater power supply, a mobile power supply, a portable power supply and the like, meets the power consumption requirements of multiple fields, and is one of the fuel cells which is closest to practical application.
In a proton exchange membrane fuel cell, an electrolyte is a proton exchange membrane with proton transfer performance, and a perfluorosulfonic acid membrane is widely adopted at present. The transfer of protons in the electrolyte membrane relies on water molecules as the conductive carrier, so the water content in the proton exchange membrane has a great influence on the performance of the fuel cell, the membrane water is in a saturated state and has the best proton conductivity, and the fuel cell exerts the best power generation performance. Therefore, humidification or moisture retention of proton exchange membranes is a necessary choice in proton exchange membrane fuel cells.
Currently, the conventional humidification technology for proton exchange membrane fuel cells is an active humidification method, i.e., a water source is provided from the outside. The humidifying method comprises bubbling humidifying, spraying humidifying, membrane humidifying, dew point humidifying, direct water injection and the like, and can be divided into external humidifying and internal humidifying according to the integration tightness degree with the galvanic pile: the external humidification is to separate the humidification subsystem from the battery and carry out humidification before the reaction gas; the internal humidification is to integrate the humidification subsystem with the battery, and the humidification is carried out after the reaction gas enters the battery.
The humidification of the fuel cell stack is carried out by using an external water source, so that a waterway system is required to be constructed, at least relevant components of a water tank, a water circulation pipeline, a pump and a valve are required, the water level is required to be monitored, and water is supplemented when the water level of the water tank is insufficient. However, since the fuel cell generates water by the reaction of hydrogen and oxygen during operation, the generated water can be recycled to the water tank after steam-water separation, and the added water is humidified, which causes system complexity. For fuel cells, water acts to maintain membrane wettability to maintain good ionic conductivity. In reality, the water produced by the electrochemical reaction of the stack is sufficient to humidify the fresh air. It is important to recover the water vapor in the cathode exhaust of the fuel cell to humidify the fresh dry air. The water vapor in the recovered tail gas is used for humidifying the inlet air, so that the system is simplified, the power consumption of auxiliary machines in the system is reduced, and the power density of the whole system is provided.
Currently, membrane humidifiers are commonly used in the market to humidify dry air entering the battery by using tail gas containing water vapor. The membrane humidifier is internally provided with a hollow fiber tube, fresh dry air flows in the hollow fiber tube, and the cathode tail gas of the fuel cell flows out of the tube. The water vapor in the tail gas of the fuel cell is condensed on the outer pipe wall of the hollow fiber pipe to form a water film, and the water enters the pipe through the pipe wall to humidify the fresh dry air, so that the aim of humidifying is fulfilled. Fresh dry air is humidified and then is conveyed to the fuel cell through a heat insulation pipeline, so that the condensation of water vapor is avoided. And simultaneously, the humidified air enters a common pipeline of the galvanic pile and then enters a flow field through a distribution channel on each cell. Since the steam will partially condense in the gas distribution channels during the process of introducing the humidified fresh dry air from the common duct into the cell flow field, it is difficult to maintain the same humidity level of the gas introduced into each cell. Due to the non-uniformity of the gas distribution, differences in the performance of each cell are easily created, which can be amplified after long-term operation of the stack. Experiments prove that the probability and the amplitude of performance attenuation of the single cells at the two ends of the fuel cell are larger than those of the single cells in the middle of the fuel cell. Therefore, how to maintain the uniformity of gas and water distribution in each cell is a key issue to be solved for the long-term stable operation of fuel cells.
SUMMERY OF THE UTILITY MODEL
Aiming at the problems of insufficient humidification, low consistency, low battery performance and the like of a liquid cooling fuel cell in practical use, the utility model divides a galvanic pile into two sections, wherein the first section is a humidification section, and the second section is a reaction section. The method ensures the sufficiency of the humidification of the electric pile, maintains the humidification temperature to be consistent with the reaction temperature of the battery, and avoids the condensation of water vapor caused by temperature reduction, so that the manufacturing and subsequent assembly procedures are relatively simple, the method is very suitable for large-scale processing and manufacturing, reduces the cost and can be applied to large-scale practical application. The utility model simplifies the system structure and further improves the mass specific power and the volume specific power of the system.
The technical scheme of the utility model is as follows:
an inner humidification liquid cooling fuel cell pile is sequentially provided with an end plate I, a humidification section, a partition plate, a reaction section and an end plate II from one side to the other side, wherein the humidification section comprises one or more humidification units, and each humidification unit comprises a humidification plate back-surface flow field, a humidification membrane and a humidification plate front-surface flow field which are sequentially arranged; the back flow field of the humidifying plate is filled with reacted wet air, the front flow field of the humidifying plate is filled with unreacted dry air, and the humidifying membrane is a water-guiding air-blocking membrane and is used for transferring moisture in the wet air to the dry air; the reaction section comprises a current collecting plate, a repeating unit formed by alternately stacking a plurality of bipolar plates and a membrane electrode, and the current collecting plate on the other side, and generates electric energy through hydrogen-oxygen electrochemical reaction.
Based on the scheme, preferably, the air is promoted to diffuse to the humidifying membrane by changing the sectional area of the flow channel of the flow field at the two sides of the humidifying membrane at the humidifying section, so that the humidifying effect is improved; the air flow field of the reaction section can also promote the diffusion of air to the membrane electrode by changing the sectional area, thereby improving the performance of the cell.
Based on the above technical scheme, preferably, the method for changing the cross-sectional area of the flow channel of the flow field on both sides of the humidifying membrane at the humidifying section can be realized by changing the width of the flow channel and also by changing the depth of the flow channel. The width of the flow channel can be changed by repeatedly arranging a plurality of flow channel widening sections and flow channel narrowing sections, and meanwhile, the ridge and groove proportion of the flow field is considered, so that the shearing of the flow field on two sides of the membrane to the membrane is avoided; when the depth of the flow channel is changed, the convex points or the convex platforms are mainly added in the flow channel, and the height of the convex points or the convex platforms is based on the principle that the gas flow resistance is not excessively increased.
Based on the technical scheme, preferably, the flow channels in the front flow field and the reverse flow field of the humidifying plate are distributed in a one-time or multi-time turn-back type.
Based on the above technical solution, preferably, the gas in the flow channels on both sides of the humidifying membrane flows in a counter-current manner.
Based on the technical scheme, preferably, all the humidification units of the humidification section are connected in series or in parallel, or part of the humidification units are connected in series and then in parallel, the humidification effect is improved by connecting the humidification units in series, but the air transmission resistance is also increased by multiple times of turning back.
Based on the technical scheme, preferably, the reaction section and the humidification section share the humidified air pipeline and the reacted air pipeline, so that the transmission resistance is reduced; the humidified air pipeline transmits the humidified air of the humidifying section to the reaction section, and the reacted air pipeline transmits the reacted air of the reaction section to the humidifying section.
Based on the technical scheme, preferably, the gas common pipeline is in a double-plate type at two ends, a hydrogen inlet and a cooling liquid inlet are arranged on an end plate II, and a dry air inlet and a pile tail gas outlet are arranged on the end plate I; the gas common pipeline is arranged on the bipolar plate type at the periphery, and a hydrogen inlet, a cooling liquid inlet, a dry air inlet and a stack tail gas outlet can be arranged on the same end plate.
Based on the above technical solution, preferably, the water-conducting gas barrier membrane may be one or more of a perfluorosulfonic acid membrane, a sulfonated polyimide membrane, a sulfonated polysulfone membrane, a polyethersulfone membrane, a sulfonated polyphenylsulfone membrane, and a sulfonated polyetheretherketone membrane.
The utility model has the advantages that:
1. the utility model cancels an external humidifier and a humidifying heat-insulating pipeline, simplifies the system structure, and improves the system integration level, the system volume specific power and the system weight specific power;
2. the utility model reduces the edge effect of performance attenuation of single cells at two ends of the fuel cell, keeps the uniformity of gas and water distribution in each cell, improves the consistency of the galvanic pile and further promotes the long-term stable operation of the fuel cell;
3. the utility model adopts the method of changing the flow field flow passage section area to improve the humidifying effect and the battery performance.
Drawings
FIG. 1 is a schematic diagram of an internal humidification fuel cell stack;
FIG. 2 is a schematic view of a humidified flow field plate;
FIG. 3 is a schematic view of changing the depth of a flow channel of a flow field by adding bumps;
FIG. 4 is a schematic view of changing the width of a flow channel of a flow field;
FIG. 5 is a schematic view of changing the width of a flow channel of a flow field;
figure 6 is an internal humidification fuel cell stack performance;
FIG. 7 is a schematic view of an internal humidification fuel cell stack;
FIG. 8 is a schematic view of a humidified flow field plate;
figure 9 shows internal humidification fuel cell stack performance;
schematic illustration:
a, fresh dry air; b, galvanic pile tail gas; c, humidified air; d, wet air after reaction;
1. a humidifying section; 2. a reaction section; 3. an insulating end plate; 4. humidification plates (showing back flow field); 5. a humidifying membrane; 6. humidification plates (showing front flow field); 7. an insulating partition plate; 8. a collector plate; 9. a bipolar plate; 10. a membrane electrode; 11. a bipolar plate; 12. a collector plate; 13. and an insulating end plate.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples. In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, are only for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
Example 1
The two ends of the bipolar plate are plate-shaped of a gas common pipeline. The proton exchange membrane fuel cell stack is assembled according to the figure 1, the stack is composed of a humidifying section 1 and a reaction section 2, and the two ends of the stack are an insulating end plate 3 only provided with an air inlet and an air outlet and an insulating end plate 13 provided with a hydrogen inlet and a hydrogen outlet and a coolant inlet and an air outlet. The humidifying section 1 mainly comprises at least one humidifying membrane 5(m pieces) and humidifying plates 4 and 6(m +1 pieces) at two sides of the humidifying membrane; the reaction section 2 is mainly composed of at least one membrane electrode 10(n sheets), bipolar plates 9 and 11(n + 1) on both sides of the membrane electrode, and current collecting plates 8 and 12. The humidifying section 1 and the reaction section 2 are separated by an insulating partition plate 7.
Fresh dry air A enters the humidification section 1 of the electric pile through an air interface of an insulating end plate 3, and contacts with a humidification membrane 5 in a front flow field of a humidification plate 6, the front flow field of the humidification plate 6 is shown as figure 2-1 in figure 2, fresh dry air A flows into the flow field and contacts with the humidification membrane 5 to form humidified air C which enters a common pipeline shared by the humidification section 1 and the reaction section 2 to reach an air inlet of a bipolar plate 11 of the reaction section 2, the air C flows through the air flow field of the bipolar plate and simultaneously participates in electrochemical reaction to carry away more reaction generated water, the reacted air D enters the common pipeline shared by the reaction section 2 and the humidification section 1 to reach a back flow field of a humidification plate 4 of the humidification section 1 as shown as figure 2-2 in figure 2, and the reacted air D flows into the flow field and contacts with the humidification membrane 5 to form electric pile tail gas B which is discharged from the electric pile.
In the preparation process, flow fields are prepared on the front side and the back side of each humidifying plate, as 2-1 and 2-2 shown in fig. 2, a humidifying membrane is arranged between every two humidifying plates, namely, the flow fields on the two sides of the humidifying membrane are consistent with the flow fields on the front side and the back side of each humidifying plate, and the gas flow in the flow channels on the two sides is in a counter-current direction, so that the humidifying effect is improved.
After the electrochemical reaction, more reaction generated water forms reacted air D, the reacted air D flows through a back flow field (figure 2-2) of the humidifying plate 4, the water is transmitted to the humidifying membrane 5, the humidifying membrane 5 transmits the water to fresh dry air A flowing through a front flow field (figure 2-1) of an adjacent humidifying plate 6, and therefore the fresh air A is humidified to form humidified air C which enters a reaction section to participate in the electrochemical reaction. The humidifying membrane 5 is a gas-blocking water-guiding membrane, which prevents gas from flowing between two sides of the membrane and transmits water to the other side. The humidifying membrane used in this example was a sulfonated polyethersulfone membrane.
The sectional area of the flow channel is changed, the local resistance of the gas can be changed, the local pressure is further converted, the longitudinal diffusion of the gas to the surface of the membrane can be promoted, and the humidifying effect is improved. In fig. 3, the cross-sectional area is changed by changing the depth of the flow channel by adding bumps in the flow channel. In fig. 4 and 5, the cross-sectional area of the flow path is changed by changing the width of the flow path.
According to the technology of the utility model, the humidifying membrane is a 30-section parallel humidifying unit of the sulfonated polyether sulfone membrane, salient points (shown in figure 3) are added in a flow channel of a humidifying section flow field, the normal depth is 0.5mm, and the depth of the salient points is 0.25 mm; the reaction section is a 145-section fuel cell stack, and the effective area of an electrode is 300cm2. Hydrogen is used as fuel, air is used as oxidant, the operating pressure of hydrogen is 1.2bar, the air pressure is 1.0bar, and the stoichiometric ratio of air is 2; the cooling medium is deionized water, the inlet temperature is 65 ℃, the outlet temperature is 70 ℃, the battery performance is shown in figure 6, and the maximum output can be 40 kW.
Example 2
The periphery of the bipolar plate is a plate type of a gas common pipeline. According to the figure 7, the proton exchange membrane fuel cell stack is assembled, the stack is composed of a humidifying section 1 and a reaction section 2, one end of the stack is an insulating end plate 3 with an air inlet and outlet, a hydrogen inlet and outlet and a coolant inlet and outlet, and the other end is a plane insulating end plate 13. The humidifying section 1 mainly comprises at least one humidifying membrane 5(m pieces) and humidifying plates 4 and 6(m +1 pieces) at two sides of the humidifying membrane; the reaction section 2 is mainly composed of at least one membrane electrode 10(n pieces), bipolar plates 9, 11(n +1 pieces) at both sides of the membrane electrode, and current collecting plates 8, 12. The humidifying section 1 and the reaction section 2 are separated by an insulating partition plate 7.
Fresh dry air A enters the humidification section 1 of the electric pile through an air interface of the insulating end plate 3, contacts with a humidification membrane 5 in a back flow field of the humidification plate 4, the back flow field of the humidification plate 4 is shown as figure 8-1 in figure 8, fresh dry air A flows into the flow field and contacts with the humidification membrane 5 to form humidified air C, the humidified air C enters a common pipeline shared by the humidification section 1 and the reaction section 2 to reach an air inlet of a bipolar plate 11 of the reaction section 2, the air C flows through the air flow field of the bipolar plate and simultaneously participates in electrochemical reaction to carry away more reaction generated water, the reacted air D enters the common pipeline shared by the reaction section 2 and the humidification section 1 to reach a front flow field of a humidification plate 6 of the humidification section 1 as shown as figure 8-2 in figure 8, and the reacted air D flows into the flow field and contacts with the humidification membrane 5 to form electric pile tail gas B, and is discharged from the electric pile.
In the preparation process, flow fields are prepared on the front side and the back side of each humidifying plate, as 8-1 and 8-2 shown in fig. 8, a humidifying membrane is arranged between every two humidifying plates, namely, the flow fields on the two sides of the humidifying membrane are consistent with the flow fields on the front side and the back side of each humidifying plate, and the gas flow in the flow channels on the two sides is in a counter-current direction, so that the humidifying effect is improved.
After the electrochemical reaction, more reaction generated water forms reacted air D, the reacted air D flows through a front flow field (figure 8-2) of the humidifying plate 6, the water is transmitted to the humidifying membrane 5, the humidifying membrane 5 transmits the water to fresh dry air A flowing through a back flow field (figure 8-1) of the adjacent humidifying plate 4, and therefore the fresh air A is humidified to form humidified air C which enters a reaction section to participate in the electrochemical reaction. The humidifying membrane 5 is a gas-blocking water-guiding membrane, which prevents gas from flowing between two sides of the membrane and transmits water to the other side. The humidifying membrane used in this example was a perfluorosulfonic acid membrane.
The sectional area of the flow channel is changed, the local resistance of the gas can be changed, the local pressure is further converted, the longitudinal diffusion of the gas to the surface of the membrane can be promoted, and the humidifying effect is improved. In fig. 4 and 5, the cross-sectional area of the flow path is changed by changing the width of the flow path.
According to the technology of the utility model, 10 sections of humidification units with humidification membranes being perfluorosulfonic acid membranes are assembled in parallel, the sectional area (as shown in figure 4) is changed by changing the width of a flow channel of a flow field in a humidification section, the normal width is 1.0mm, the wide position is 1.2mm, and the narrow position is 0.8 mm; the reaction section is a 50-section fuel cell stack, and the effective area of an electrode is 300cm 2. Hydrogen is used as fuel, air is used as oxidant, the operating pressure of hydrogen is 1.2bar, the air pressure is 1.0bar, and the stoichiometric ratio of air is 2; the cooling medium is deionized water, the inlet temperature is 65 ℃, the outlet temperature is 70 ℃, the battery performance is shown in figure 9, and the maximum output can be 15 kW.
The present invention is not limited to the above-mentioned preferred embodiments, and any other products in various forms can be obtained by anyone in the light of the present invention, but any changes in the shape or structure thereof, which have the same or similar technical solutions as those of the present application, fall within the protection scope of the present invention.
Claims (9)
1. An internally humidified liquid cooled fuel cell stack, comprising: the galvanic pile is sequentially provided with an end plate I, a humidifying section, a partition plate, a reaction section and an end plate II from one side to the other side, wherein the humidifying section comprises one or more humidifying units, and each humidifying unit comprises a humidifying plate reverse flow field, a humidifying membrane and a humidifying plate front flow field which are sequentially arranged; the back flow field of the humidifying plate is filled with reacted wet air, the front flow field of the humidifying plate is filled with unreacted dry air, and the humidifying membrane is a water-guiding air-blocking membrane and is used for transferring moisture in the wet air to the dry air; the reaction section comprises a current collecting plate, a repeating unit formed by alternately stacking a plurality of bipolar plates and a membrane electrode, and the current collecting plate on the other side, and generates electric energy through hydrogen-oxygen electrochemical reaction.
2. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: the cross section of the flow channel is changed by changing the width or the depth of the flow channel in the front flow field and the back flow field of the humidifying plate.
3. The internally humidified, liquid cooled fuel cell stack of claim 2, wherein: the depth of the flow channel is changed by arranging bulges at intervals in the flow channel, and the width of the flow channel is changed by repeatedly arranging a plurality of flow channel widening sections and flow channel narrowing sections.
4. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: the flow channels in the front flow field and the reverse flow field of the humidifying plate are distributed in a one-time or multi-time turn-back type.
5. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: and the gas in the flow channels at the two sides of the humidifying membrane flows in a countercurrent manner.
6. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: all the humidifying units of the humidifying section are connected in series or in parallel, or part of the humidifying units are connected in series and then in parallel.
7. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: the reaction section and the humidifying section share a humidified air pipeline and a reacted air pipeline; the humidified air pipeline transmits the humidified air of the humidifying section to the reaction section, and the reacted air pipeline transmits the reacted air of the reaction section to the humidifying section.
8. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: the two ends of the bipolar plate are plate-shaped of a gas common pipeline, a hydrogen inlet, a hydrogen outlet, a cooling liquid inlet and a cooling liquid outlet are positioned on the end plate II, and a dry air inlet and a pile tail gas outlet are positioned on the end plate I; the periphery of the bipolar plate is a plate type of a gas common pipeline, and a hydrogen inlet, a hydrogen outlet, a cooling liquid inlet, a cooling liquid outlet, a dry air inlet and a stack tail gas outlet are distributed on the same end plate.
9. The internally humidified, liquid cooled fuel cell stack of claim 1, wherein: the humidifying membrane is one or more of a perfluorosulfonic acid membrane, a sulfonated polyimide membrane, a sulfonated polysulfone membrane, a polyether sulfone membrane, a sulfonated polyphenyl sulfone membrane and a sulfonated polyether ether ketone membrane.
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| CN202123346845.0U CN216648371U (en) | 2021-12-28 | 2021-12-28 | Internal humidifying liquid cooling fuel cell stack |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114243059A (en) * | 2021-12-28 | 2022-03-25 | 大连华氢动力有限公司 | Internal humidifying fuel cell stack |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114243059A (en) * | 2021-12-28 | 2022-03-25 | 大连华氢动力有限公司 | Internal humidifying fuel cell stack |
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Effective date of registration: 20240204 Address after: Room 2106, 4th Floor, No. 35 Congratulations Street, Zhongshan District, Dalian City, Liaoning Province, 116001 Patentee after: Liaoning Guokexin Energy Science Research Co.,Ltd. Country or region after: China Address before: 116000 No. 1-4, Huaihe West Road, Dalian Economic and Technological Development Zone, Liaoning Province Patentee before: Dalian huahydrogen Power Co.,Ltd. Country or region before: China |