CN1622377A - Proton exchange film fuel cell flow field structure - Google Patents
Proton exchange film fuel cell flow field structure Download PDFInfo
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- CN1622377A CN1622377A CNA2003101052024A CN200310105202A CN1622377A CN 1622377 A CN1622377 A CN 1622377A CN A2003101052024 A CNA2003101052024 A CN A2003101052024A CN 200310105202 A CN200310105202 A CN 200310105202A CN 1622377 A CN1622377 A CN 1622377A
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- 239000000446 fuel Substances 0.000 title claims abstract description 40
- 239000012528 membrane Substances 0.000 claims abstract description 15
- 238000007789 sealing Methods 0.000 claims abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 18
- 229910052751 metal Inorganic materials 0.000 claims description 15
- 239000002184 metal Substances 0.000 claims description 15
- 229910002804 graphite Inorganic materials 0.000 claims description 14
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 239000011148 porous material Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 2
- 239000007770 graphite material Substances 0.000 claims description 2
- 239000007769 metal material Substances 0.000 claims description 2
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- 238000005245 sintering Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 15
- 230000008901 benefit Effects 0.000 abstract description 10
- 238000003487 electrochemical reaction Methods 0.000 abstract description 4
- 230000008030 elimination Effects 0.000 abstract description 2
- 238000003379 elimination reaction Methods 0.000 abstract description 2
- 230000002349 favourable effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 56
- 239000010439 graphite Substances 0.000 description 12
- 239000012495 reaction gas Substances 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- 238000009792 diffusion process Methods 0.000 description 7
- 230000010287 polarization Effects 0.000 description 7
- 239000000376 reactant Substances 0.000 description 7
- 230000007547 defect Effects 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 239000007800 oxidant agent Substances 0.000 description 5
- 230000001590 oxidative effect Effects 0.000 description 5
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- 239000002131 composite material Substances 0.000 description 3
- 238000003411 electrode reaction Methods 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 239000011261 inert gas Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- -1 hydrogen ions Chemical class 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 239000011435 rock Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
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- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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- 239000010411 electrocatalyst Substances 0.000 description 1
- UQSQSQZYBQSBJZ-UHFFFAOYSA-N fluorosulfonic acid Chemical compound OS(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 125000001967 indiganyl group Chemical group [H][In]([H])[*] 0.000 description 1
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- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 1
- CFQCIHVMOFOCGH-UHFFFAOYSA-N platinum ruthenium Chemical compound [Ru].[Pt] CFQCIHVMOFOCGH-UHFFFAOYSA-N 0.000 description 1
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- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 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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Abstract
The present invention relates to proton exchange membrane fuel cell. The flow field structure of proton exchange membrane fuel cell consists of netted flow field and deflecting stripes. The deflecting stripes are set inside the netted flow field and parallel to one group of sealing side walls, and have width equal to the height of the netted flow field. Each of the deflecting stripes has one end connected perpendicularly to the side wall and the other end constituting the gas channel. The gas channel has width not smaller than that of the gas inlet. The present invention has the advantages of high pole area utilization, being favorable to the exhaust of water produced in the electrochemical reaction and the elimination of inertial component, no dead arean of gas flow, and stable operation of the cell under low pressure and normal pressure.
Description
Technical Field
The invention relates to a proton exchange membrane fuel cell, in particular to a flow field structure of the proton exchange membrane fuel cell.
Background
The Proton Exchange Membrane Fuel Cell (PEMFC) takes perfluorosulfonic acid solid polymer as electrolyte, platinum/carbon or platinum-ruthenium/carbon as electrocatalyst, hydrogen or purified reformed gas as fuel, air or pure oxygen as oxidant, and graphite or surface modified metal plate with gas flow channels as bipolar plate; FIG. 1 is a schematic diagram of the operating principle of a PEMFC.
The electrode reactions in PEMFCs are analogous to other acid electrolyte fuel cells. The hydrogen in the anode catalyst layer is subjected to electrode reaction under the action of a catalyst The electrons generated by the electrode reaction reach the cathode through an external circuit, and the hydrogen ions reach the cathode through a proton exchange membrane; oxygen reacts with hydrogen ions and electrons at the cathode to generate water The generated water does not dilute the electrolyte, but is discharged with the reaction off-gas through the electrode.
The core of PEMFCs are membrane electrodes and bipolar plates. The membrane electrode is the site of electrochemical reaction; the bipolar plate provides gas distribution and current collection, and in order to accomplish both gas distribution and current collection, the bipolar plate is usually electrically conductive and has a concave-convex surface, wherein the convex portion (current collection ridge) is used to contact the electrode and collect the current; the recessed portion (flow channel) provides a channel for gas delivery to the electrode surface. The part of the bipolar plate containing the concave-convex structure is called a flow field, and the flow field can be integrated with the bipolar plate or can be separated.
The bipolar plates for the current PEMFC mainly include graphite (including pure graphite plates and graphite and polymer composite plates), metal bipolar plates, and metal and graphite composite bipolar plates. The flow field of a graphite bipolar plate is generally integrated with the bipolar plate; the metal bipolar plate and the composite bipolar plate mostly adopt a flow field and a flow collecting part of the bipolar plate as a split structure. Conventional flow field structures such as those of fig. 2(a), 2(b), 2(c) and 2(d) have serpentine, rectilinear, forked, and reticulated or porous structures.
In the PEMFC, the flow type is generally laminar flow, and the reynolds number (Re) is in the range of 100 to 1000, so the design of the flow field should satisfy the requirements of having smaller resistance drop (reducing the auxiliary power consumption of gas compression) and ensuring the uniform transfer of gas to the catalyst surface through the diffusion layer, and the performance reduction caused by the uneven distribution of reaction components in the fuel cell experiment is often occurred. At H2In PEMFCs, the reaction is usually controlled by cathode kinetics, and if the hydrogen is not diluted to a large extent, the anode activation overpotential is negligible; at a current density of 1A/cm2The cathode overpotential is 0.4-0.5V, and the anode overpotential is only 20-30 mV. Since the typical oxidant is air, significant concentration polarization can also occur if the flow rate and flow field configuration are not properly designed.
Fig. 2(a) shows a serpentine flow channel flow field [ document 1: watkins; david s.; dircks; keneth w.; epp, respectively; danny g., "Fuel cell flow field plate", [ P]US5,108,849; document 2: griffith; kimr.; rock; jeffrey Allan, "Flow channels for fuel cell", [ P]US6,358,642; document 3: margiott; "Hybrid fuel cell reactivator flows" [ P]US6,472,095], the flow path being a continuous path from the inlet to the outlet. The snake-shaped flow passage has the advantages that barriers such as water drops in the passage can not block the flow of gas, if one snake-shaped flow passage is blocked, the gas is forced to bypass the electrode to enter the adjacent flow passage; the result is an increased pressure drop without a decrease in the active area of the cell. In contrast, in the flow field of the parallel structure (fig. 2b), blocking one flow channel affects the gas distribution downstream, forming a dead zone in which the gas supply to the electrodes is insufficient, resulting in large concentration polarization, and degrading the cell performance. The snake-shaped flow field has the defects that the pressure drop is larger than that of a parallel flow field, the concentration of reaction gas is greatly reduced and the concentration polarization is increased due to the overlong flow channel and the gradual consumption of gas along the flowing direction. Under the same stoichiometric condition of chemical reaction, the mass flow rate of the parallel flow channel is low, the resistance is reduced, and the components are uniformly distributed. Since the hydrogen reaction is not usually a rate control step, water droplet obstruction due to humidification is generated at the anode, and a serpentine flow field is used at the anode in a small PEMFC. For a larger electrode area, a structure combining a snake-shaped flow field and a parallel flow field is adopted.
The third flow field configuration is an Interdigitated (fig. 2c) configuration [ document 3; document 4: rock; jeffrey A, "stacked Bipolar plate for PEM Fuel cell stack" [ P]US 6,503,653]In interdigitated flow fields, the ends of the flow channels are blind and the gas is forced to enter the adjacent flow channels through a diffusion layer beneath the collecting current spine. The main advantage of the flow field is that the gas is forced to convect instead of the molecule diffusion to pass through the surface of the catalyst layer, which can greatly improve the transfer speed and reduce the concentration polarization when the current density is high; another advantage of this structure is that drainage of the catalyst surface is enhanced; the electrode active area under the spine for collecting current is increased; the main disadvantages of such flow fields are the large resistance drop and the possible breakage of the electrodes, depending on the porosity of the diffusion layer and the diffusion coefficient of the components. Because concentration polarization is easily formed at the cathode, water accumulation of a water flooded electrode can also happen, and the electrode area under the bottom of some current collecting spines cannot be applied, so that the interdigitated flow field is most suitable for the cathode with low stoichiometric coefficient or high current density. In serpentine flow channels, long flow channels can result in high pressure drops, in addition to which the consumption of reactants can lead to additional pressure drops. If the design is not reasonable, some channels with higher local resistance may be adjacent to a low pressure channel, in which case the mismatch of the reactant gases may cause a reactant gas bypass, i.e. the reactant gas passes from one channel to another channel from the bottom of the electrode in an undesired manner. This is conceptually similar to the flow of an interdigitated flow field, except that the flow channel resistance is not intentionally increased. Bypass of reactant gas is undesirable because of the dilution of the fuel (e.g., containing CO)2Or N2Reformed hydrogen) or an oxidant (e.g., air) and the fuel cell performance is drastically reduced because the electrode in the downstream portion of the bypass path is severely deficient in the reactant gas.
To address the problems of increased resistance and the risk of bypass in the serpentine flow field and the inefficient use of the electrode area under the current collection ridge, wilson et al [ document 5: wilson; mahlon s.; zawodzinski; christine, "Fuel cell with metal screen flow-field", [ P]. US6,207,310]uses a metal mesh as the flow field. The metal net flow field has the advantages of even gas distribution on the whole electrode surface, high effective utilization rate of the electrode area, simple preparation of the bipolar plate and low cost. The biggest defect is that if the difference of the electrode thickness or water accumulation in the flow field causes short circuit of gas, water or inert gas in part of the flow field is retained, the electrode corresponding to the part of the flow field is seriously lack of reaction gas, especially low-pressure operation is performed, or the aspect ratio of the electrode is not designed reasonably, the phenomenon is more obvious, and the fuel cell can not operate stably.
In order to reduce the disadvantage of the increase in resistance of the interdigitated flow field, Wilson [ document 6: wilson; mahlon S, "Fuel cell with interleaved porous flow-field", and [ P]. US5,641,586]propose to use porous material as flow field material, part of the gas flowing from one channel to the next channel not through the electrode diffusion layer, but through porous current collecting spines, to flow from one channel to the adjacent channel, in order to reduce the drag drop of the whole gas through the pore-limited diffusion layer. The disadvantage of this flow field is that, despite the reduced resistance drop, the problems of gas short-circuiting due to differences in resistance of the individual channels, resulting in uneven gas distribution, or the occurrence of dead zones, are not fundamentally solved.
Disclosure of Invention
In order to solve the defects of the flow fields, the invention draws the advantages of the reticular flow field, eliminates the defects of the reticular flow field and provides a flow field structure of the proton exchange membrane fuel cell; the advantages of even gas distribution in the net flow field and high electrode utilization rate are kept, and the defects of gas short circuit and dead zone are eliminated; the flowing direction of the gas in the flow field can be controlled.
In order to achieve the purpose, the invention adopts the technical scheme that:
a proton exchange membrane fuel cell flow field structure, is formed by netted flow field and baffling one, the baffling one is placed inside netted flow field, the width of baffling one is the same as height of the netted flow field, the baffling one is parallel to a pack of sealed sidewall surfaces of the netted flow field, one end of the baffling one is connected with another pack of sealed sidewall surfaces vertically alternately, another end of the baffling one is the gas channel; the width of the gas channel formed by the deflection strips, the deflection strips and the sealing side wall surface of the reticular flow field is not less than the width of the gas inlet.
The width of the gas channel formed by the deflecting strips and the vertical side wall surface of the reticular flow field is usually 1/3-5, preferably 1/3-4, of the length of the side wall surface of the reticular flow field parallel to the deflecting strips.
The reticular flow field can be a metal net, porous carbon paper, porous carbon cloth or porous sintered material and the like; the aperture ratio of the metal mesh or the porous material is generally 30-90%, preferably 40-70%, the aperture ratio is too small, the gas flow resistance is large, and the reaction gas generates a large pressure drop in the fuel cell; the current collection is problematic due to the overlarge aperture ratio, and the contact resistance is increased; when the reaction gas flows in the net-shaped or porous structure and is uniformly transferred to the surface of the catalyst through the surface of the electrode, the baffling strips have the function of limiting the flow direction of the gas, can be made of plastic, rubber, graphite or metal materials, have the height as high as that of a flow field, generally have the width of 1-5 mm, preferably 2-4 mm, ensure that the gas does not bypass from the lower part of the baffling strips, and do not occupy the large area of the flow field (or the electrode); the flow speed and the resistance drop of the gas in the flow field can be controlled by adjusting the opening rate of the reticular flow field and the distance between the baffle strips. The specific size of the deflection strips depends on the length-width ratio of the flow field, the flow field with large length-width ratio has more deflection strips, the flow field with small length-width ratio has fewer deflection strips, and the formed gas channel is preferably the same as the gas inlet channel in width; the width of the gas channel remaining in the baffle strip is generally the same as the width of the gas inlet channel.
The invention has the following advantages:
1. the electrode has high area utilization rate, and is beneficial to the removal of electrochemical generated water and the elimination of the accumulation of inert components; the gas of the electrode part under the spine for collecting current in the flow field can be prevented from being transferred, and water or other inert gases are accumulated at the position, so that the area utilization rate of the electrode is low.
2. By adopting the mesh-shaped baffling flow field structure, gas flows in the flow field to be baffled, short circuit and dead zones are avoided, and the fuel cell can be stably operated under low pressure or normal pressure.
3. By adopting the invention, the flow in the gas flow field is interfered by the net structure, thereby realizing turbulent flow, being beneficial to reducing the thickness of a boundary layer of reaction gas transferred from the flow field to the surfaces of the electrode and the catalyst, improving the mass transfer speed and reducing the concentration polarization.
4. The invention has simple and short structure and easy realization, integrates the advantages of the traditional snake-shaped flow field and the reticular flow field and abandons the defects of the traditional snake-shaped flow field and the reticular flow field; by adopting the invention, the flowing speed of the gas in the flow field is higher than that of the traditional reticular and parallel groove flow field and lower than that of the snake-shaped flow field, therefore, the resistance is reduced moderately, and the gas is favorably and uniformly distributed among all single cells.
Drawings
FIG. 1 is a schematic diagram of the operating principle of a PEMFC.
Fig. 2a is a schematic view of a serpentine flow field structure.
Fig. 2b is a schematic view of a parallel groove flow field structure.
Fig. 2c is a schematic view of an interdigitated flow field structure.
Fig. 2d is a schematic view of a reticulated flow field structure.
Fig. 3 is a schematic diagram comparing the structure of the proton exchange membrane fuel cell flow field and the structure of the mesh flow field.
Fig. 4 is a schematic diagram of the volt-ampere performance result of the pem fuel cell under different flow fields and different pressures.
Fig. 5 is a schematic diagram of stability experiment results of proton exchange membrane fuel cells with different flow field structures.
Detailed Description
Example 1
As shown in fig. 3, in one flow field embodiment, a 100-mesh and 40-mesh stainless steel metal mesh is used as the reticular flow field, flexible graphite is used as the deflection strips, the flexible graphite deflection strips are sandwiched between the two metal meshes, and the graphite strips and the metal mesh are flattened and fixed by an oil press; the distance between the graphite strips is 20 mm, and a gas channel reserved on the side surface of each graphite strip accounts for one fourth to one third of the length of the whole graphite strip; the flow field is composed of a reticular flow field and a deflecting strip, the reaction gas enters the flow field of the fuel cell from the gas inlet, under the limitation of the deflecting strip, the gas is deflected and uniformly passes through the whole flow field, so that the gas is uniformly distributed on the surface of the whole electrode, the problem of short circuit of the gas is avoided, the purpose of controllable gas flow is achieved, the utilization efficiency of the electrode is improved, the current is uniformly distributed, and the accumulation of water generated by electrochemical reaction in the cell is avoided.
The baffling strips in the net-shaped folding flow field have the following functions:
1) compared with a pure reticular flow field, the gas flow cross section is reduced, and the flow speed of gas in the flow field is improved, so that a mass transfer boundary layer is thinned, the transfer speed of reaction gas to the surface of a catalyst is improved, and the performance of a fuel cell is improved; meanwhile, the discharge of condensed water brought into the cell by electrochemical reaction or humidification is promoted, and partial electrodes are prevented from being flooded by water.
2) The baffle strips are adopted to lead the reaction gas to flow away and deflect in the limited flow field, so that the baffle strips have the advantage of a snake-shaped flow field, and the phenomenon that the gas flow speed at the position of the flow field where part of electrodes are positioned is too low and the speed of transferring reactants to the surface of the catalyst is reduced to form large concentration polarization caused by the short circuit of the reaction gas is avoided.
Because the gas is deflected in the flow field, and the distance between the deflection strips can be adjusted, the speed and resistance drop of the reaction gas in the flow channel can be controlled, and the phenomenon that inert gas (such as nitrogen in oxidant air) and liquid water are accumulated in the electrode to cause partial electrode of the electrode to lose effect is avoided.
Comparative example
As shown in fig. 4 and 5, they are the volt-ampere curve and stability curve of the proton exchange membrane fuel cell under the same operation conditions of the flow field structure of the present invention and the reticular flow field disclosed in the document [5]; the fuel is pure hydrogen, and the oxidant is air; as can be seen from fig. 4, the cell performance of the flow field of the present invention is significantly higher than that of the mesh-like flow field structure reported in the literature; as can be seen from fig. 5, with the conventional mesh flow field, no baffle bars are added, and the cell cannot be used at all under normal pressure.
Claims (10)
1. A proton exchange membrane fuel cell flow field structure is characterized in that: the gas flow field baffle is composed of a reticular flow field and baffle strips, wherein the baffle strips are arranged in the reticular flow field, the width of the baffle strips is the same as the height of the reticular flow field, the baffle strips are parallel to one group of sealing side wall surfaces of the reticular flow field, one end of each baffle strip is alternately and vertically connected with the other group of sealing side wall surfaces, and the other end of each baffle strip is a gas channel; the width of the gas channel formed by the deflection strips, the deflection strips and the sealing side wall surface of the reticular flow field is not less than the width of the gas inlet.
2. The pem fuel cell flow-field structure of claim 1 wherein: the width of a gas channel formed by the deflecting strips and the vertical side wall surfaces of the reticular flow field is 1/3-5 of the length of the side wall surfaces of the reticular flow field parallel to the deflecting strips.
3. The pem fuel cell flow-field structure of claim 1 wherein: the width of a gas channel formed by the deflecting strips and the vertical side wall surfaces of the reticular flow field is 1/3-4 of the length of the side wall surfaces of the reticular flow field parallel to the deflecting strips.
4. The pem fuel cell flow-field structure of claim 1 wherein: the gas channel is the same width as the gas inlet channel.
5. The pem fuel cell flow-field structure of claim 1 wherein: the width of the baffling strip is 1-5 mm.
6. The pem fuel cell flow-field structure of claim 1 wherein: the width of the baffling strip is 2-4 mm.
7. The pem fuel cell flow-field structure of claim 1 wherein: the reticular flow field is a metal net, porous carbon paper, porous carbon cloth or a porous sintering material.
8. A pem fuel cell flow-field configuration according to claim 7, wherein: the aperture ratio of the metal net or the porous material is 30-90%.
9. A pem fuel cell flow-field configuration according to claim 7, wherein: the aperture ratio of the metal net or the porous material is 40-70%.
10. The pem fuel cell flow-field structure of claim 1 wherein: the baffle strips are made of plastic, rubber, graphite or metal materials.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101052024A CN1305158C (en) | 2003-11-26 | 2003-11-26 | Proton exchange film fuel cell flow field structure |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101052024A CN1305158C (en) | 2003-11-26 | 2003-11-26 | Proton exchange film fuel cell flow field structure |
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| Publication Number | Publication Date |
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| CN1622377A true CN1622377A (en) | 2005-06-01 |
| CN1305158C CN1305158C (en) | 2007-03-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB2003101052024A Expired - Lifetime CN1305158C (en) | 2003-11-26 | 2003-11-26 | Proton exchange film fuel cell flow field structure |
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| CN (1) | CN1305158C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100449833C (en) * | 2005-08-26 | 2009-01-07 | 比亚迪股份有限公司 | Flow field plate for fuel battery |
| CN104360271A (en) * | 2014-10-24 | 2015-02-18 | 沈阳建筑大学 | Flow field plate used for assembling and testing fuel cells of different flow fields at one step and testing method |
| CN109921056A (en) * | 2017-12-13 | 2019-06-21 | 中国科学院大连化学物理研究所 | A kind of grid flow field |
| CN111640960A (en) * | 2020-06-02 | 2020-09-08 | 浙江锋源氢能科技有限公司 | Single cell assembly and fuel cell stack |
| CN112687907A (en) * | 2019-10-17 | 2021-04-20 | 未势能源科技有限公司 | Polar plate and fuel cell |
| CN112909286A (en) * | 2019-12-03 | 2021-06-04 | 未势能源科技有限公司 | Polar plate and fuel cell |
| CN114318386A (en) * | 2022-01-20 | 2022-04-12 | 氢鸿(杭州)科技有限公司 | Proton exchange membrane water electrolyzer, system and method |
| CN114759208A (en) * | 2022-05-09 | 2022-07-15 | 中国第一汽车股份有限公司 | Fuel cell bipolar plate and fuel cell with same |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5798187A (en) * | 1996-09-27 | 1998-08-25 | The Regents Of The University Of California | Fuel cell with metal screen flow-field |
| US6037073A (en) * | 1996-10-15 | 2000-03-14 | Lockheed Martin Energy Research Corporation | Bipolar plate/diffuser for a proton exchange membrane fuel cell |
| US6306530B1 (en) * | 1998-08-27 | 2001-10-23 | International Fuel Cells Llc | System for preventing gas pocket formation in a PEM coolant flow field |
| CN2418587Y (en) * | 2000-04-03 | 2001-02-07 | 信息产业部电子第十八研究所 | Two-Polar plate in grid flow-field distribution structure |
| US6544681B2 (en) * | 2000-12-26 | 2003-04-08 | Ballard Power Systems, Inc. | Corrugated flow field plate assembly for a fuel cell |
-
2003
- 2003-11-26 CN CNB2003101052024A patent/CN1305158C/en not_active Expired - Lifetime
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100449833C (en) * | 2005-08-26 | 2009-01-07 | 比亚迪股份有限公司 | Flow field plate for fuel battery |
| CN104360271A (en) * | 2014-10-24 | 2015-02-18 | 沈阳建筑大学 | Flow field plate used for assembling and testing fuel cells of different flow fields at one step and testing method |
| CN104360271B (en) * | 2014-10-24 | 2017-08-15 | 沈阳建筑大学 | Flow-field plate and method of testing for the different flow field fuel cells of an assembling test |
| CN109921056B (en) * | 2017-12-13 | 2021-12-14 | 中国科学院大连化学物理研究所 | Grid flow field |
| CN109921056A (en) * | 2017-12-13 | 2019-06-21 | 中国科学院大连化学物理研究所 | A kind of grid flow field |
| CN112687907B (en) * | 2019-10-17 | 2022-05-10 | 未势能源科技有限公司 | Polar plate and fuel cell |
| CN112687907A (en) * | 2019-10-17 | 2021-04-20 | 未势能源科技有限公司 | Polar plate and fuel cell |
| CN112909286A (en) * | 2019-12-03 | 2021-06-04 | 未势能源科技有限公司 | Polar plate and fuel cell |
| CN112909286B (en) * | 2019-12-03 | 2023-01-24 | 未势能源科技有限公司 | Polar plate and fuel cell |
| CN111640960A (en) * | 2020-06-02 | 2020-09-08 | 浙江锋源氢能科技有限公司 | Single cell assembly and fuel cell stack |
| CN114318386A (en) * | 2022-01-20 | 2022-04-12 | 氢鸿(杭州)科技有限公司 | Proton exchange membrane water electrolyzer, system and method |
| CN114759208A (en) * | 2022-05-09 | 2022-07-15 | 中国第一汽车股份有限公司 | Fuel cell bipolar plate and fuel cell with same |
| CN114759208B (en) * | 2022-05-09 | 2024-03-19 | 中国第一汽车股份有限公司 | Fuel cell bipolar plate and fuel cell with same |
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| CN1305158C (en) | 2007-03-14 |
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