CN116770336B - Bipolar plate and proton exchange film electrolytic tank - Google Patents
Bipolar plate and proton exchange film electrolytic tank Download PDFInfo
- Publication number
- CN116770336B CN116770336B CN202310994173.9A CN202310994173A CN116770336B CN 116770336 B CN116770336 B CN 116770336B CN 202310994173 A CN202310994173 A CN 202310994173A CN 116770336 B CN116770336 B CN 116770336B
- Authority
- CN
- China
- Prior art keywords
- plate
- cathode
- anode
- bipolar
- bipolar plate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000012528 membrane Substances 0.000 claims abstract description 57
- 238000007789 sealing Methods 0.000 claims description 72
- 239000001257 hydrogen Substances 0.000 claims description 52
- 229910052739 hydrogen Inorganic materials 0.000 claims description 52
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 51
- 238000009826 distribution Methods 0.000 claims description 49
- 238000009792 diffusion process Methods 0.000 claims description 47
- 238000005868 electrolysis reaction Methods 0.000 claims description 31
- 230000000712 assembly Effects 0.000 claims description 2
- 238000000429 assembly Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 15
- 230000008859 change Effects 0.000 abstract description 6
- 238000012546 transfer Methods 0.000 abstract description 6
- 239000007791 liquid phase Substances 0.000 abstract description 3
- 238000012545 processing Methods 0.000 abstract description 3
- 239000002609 medium Substances 0.000 description 50
- 239000007789 gas Substances 0.000 description 27
- 238000004519 manufacturing process Methods 0.000 description 14
- 238000013461 design Methods 0.000 description 13
- 239000012530 fluid Substances 0.000 description 11
- 238000005457 optimization Methods 0.000 description 11
- 238000004088 simulation Methods 0.000 description 9
- 230000005540 biological transmission Effects 0.000 description 6
- 239000003570 air Substances 0.000 description 5
- 229910001220 stainless steel Inorganic materials 0.000 description 5
- 239000010935 stainless steel Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000005520 cutting process Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007769 metal material Substances 0.000 description 3
- 240000000233 Melia azedarach Species 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012212 insulator Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005315 distribution function Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000003754 machining Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000006163 transport media Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
- C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/60—Constructional parts of cells
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention discloses a bipolar plate and a proton exchange membrane electrolytic cell, wherein the bipolar plate comprises a bipolar plate anode plate and a bipolar plate cathode plate which are connected back to back; the surface of the bipolar plate anode plate is provided with an anode flow field, and the surface of the bipolar plate cathode plate is provided with a cathode flow field; the anode flow field and the cathode flow field are provided with a plurality of flow channels; the medium of the anode flow field and/or the cathode flow field enters from the flow channel positioned in the middle and sequentially enters into the flow channels positioned at two sides, and the width of each flow channel on the anode flow field and/or the cathode flow field increases from the middle to the two sides in a linear way. The gradual change type flow field provided by the invention can improve the mass transfer problem of gas and liquid phases, ensure that liquid water flows more smoothly, ensure that media are distributed more uniformly, prevent the risk of uneven water transfer under high current density, and has the advantages of simple and compact structure, fewer system accessories, simple processing and small stress concentration, and can also ensure the strength of polar plates.
Description
Technical Field
The invention relates to the technical field of hydrogen production by water electrolysis, in particular to a bipolar plate and a proton exchange membrane electrolytic cell.
Background
Proton Exchange Membrane (PEM) electrolysers have fast dynamic response and strong load capacity, and can realize direct coupling with renewable energy sources, so the development of proton exchange membrane water electrolysis technology is urgent.
However, the cost of the PEM electrolyzer is still higher and is more than 4 times that of alkali liquor hydrogen production, thus limiting the large-scale popularization of PEM electrolyzer. Therefore, there is an urgent need to explore the application scenario advantages of PEM electrolysers. For example, PEM stacks can directly produce high pressure hydrogen in a high pressure (> 5 MPa) scenario, thereby reducing the hydrogen compression process from the hydrogen production side to the hydrogen addition station and reducing the standing hydrogen production cost. Secondly, in the fields of aerospace and deep sea applications, the importance of lightweight high-voltage PEM electrolysers is highlighted due to the limitations of volume, weight and hydrogen production.
The bipolar plate is used for the electrolytic tank of the water electrolysis hydrogen production system, and the bipolar plate can distribute fluid and gas, but because the flow rates of the fluid in the flow channels on the bipolar plate are different, the widths of the flow channels are generally the same, so that the stacking of the fluid is easy to occur at the place with high flow rate, and the quantity of the fluid passing through the place with low flow rate is small, and the risk of uneven water transmission under high current density is easy to occur.
Disclosure of Invention
Therefore, the invention aims to overcome the defect that the existing bipolar plate is easy to generate uneven water transmission under high current density, thereby providing a bipolar plate and a proton exchange membrane electrolytic cell, and ensuring the uniformity of medium transmission by improving the flow passage of the bipolar plate.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
a bipolar plate comprising an anode plate and a cathode plate of the bipolar plate connected opposite each other; the surface of the bipolar plate anode plate is provided with an anode flow field, and the surface of the bipolar plate cathode plate is provided with a cathode flow field; the anode flow field and the cathode flow field are provided with a plurality of flow channels; the medium of the anode flow field and/or the cathode flow field enters from the flow channel positioned in the middle and sequentially enters into the flow channels positioned at two sides, and the width of each flow channel on the anode flow field and/or the cathode flow field increases from the middle to the two sides in a linear way.
According to the further optimized technical scheme, a water inlet and a water outlet are formed in the bipolar plate anode plate; the medium flow direction of each flow channel is the X direction, the medium inlet of each flow channel is respectively communicated with the water inlet, and the medium outlet of each flow channel is respectively communicated with the water outlet.
According to a further optimized technical scheme, a first annular distribution runner suitable for pre-distributing a medium is arranged on the outer surface of the bipolar plate anode plate, and each runner on the bipolar plate anode plate is arranged on the inner side of the first annular distribution runner;
one side of the water inlet is communicated with a first annular distribution runner, and the other side of the first annular distribution runner is communicated with the water outlet; one side of the first annular distribution runner is suitable for pre-distributing media to each runner on the bipolar plate anode plate, each runner on the bipolar plate anode plate is suitable for conveying media and converging and conveying the media to the other side of the first annular distribution runner, and the other side of the first annular distribution runner is suitable for converging and inputting the media to the water outlet.
According to a further optimized technical scheme, a hydrogen outlet is formed in the bipolar plate cathode plate; the medium flow direction of each flow channel is in the Y direction, and the medium outlet of each flow channel is respectively communicated with the hydrogen outlet.
According to a further optimized technical scheme, second annular distribution flow passages suitable for collecting media are arranged on the outer surface of the bipolar plate cathode plate, and all flow passages on the bipolar plate cathode plate are arranged on the inner side of the second annular distribution flow passages.
According to the further optimized technical scheme, the surface of the bipolar plate anode plate and/or the surface of the bipolar plate cathode plate are provided with sealing ring grooves which are suitable for positioning sealing rings.
A proton exchange membrane electrolyzer comprising:
an electrolytic single cell anode plate is internally provided with a flow field, a second water inlet and a second water outlet;
a flow field and an air outlet are arranged in the electrolytic single cell cathode polar plate;
one or more bipolar plates, wherein a bipolar plate cathode plate positioned at the outermost side is arranged opposite to an electrolytic cell anode plate and forms a first electrolytic cell with the electrolytic cell anode plate, and a bipolar plate anode plate positioned at the outermost side is arranged opposite to an electrolytic cell cathode plate and forms a second electrolytic cell with the electrolytic cell cathode plate; when a plurality of bipolar plates are arranged, two adjacent bipolar plates are connected in series through an anode-cathode mode, and a third electrolytic cell is respectively formed between every two adjacent bipolar plates;
the proton exchange membrane assemblies are arranged between the anode plate and the cathode plate of the electrolysis cell and between the anode plate and the cathode plate of the electrolysis cell; when a plurality of bipolar plates are arranged, the proton exchange membrane assembly is also arranged between two adjacent bipolar plates.
Further optimizing technical scheme, proton exchange membrane subassembly includes:
the first diffusion laminate is arranged opposite to the flow field of the anode plate of the electrolytic cell or the anode flow field of the bipolar plate;
a first gasket in contact with the first diffusion layer plate;
the second sealing gasket is contacted with the cathode plate or the cathode plate of the bipolar plate of the electrolytic cell;
the second diffusion laminate is arranged between the first sealing gasket and the second sealing gasket and is opposite to the cathode flow field of the bipolar plate or the flow field of the cathode plate of the electrolytic cell;
and the proton exchange membrane is arranged between the first diffusion layer plate and the second diffusion layer plate.
According to the further optimized technical scheme, an anode end plate is arranged on the outer side of the anode plate of the electrolytic cell, and a cathode end plate is arranged on the outer side of the cathode plate of the electrolytic cell; an anode insulating pad is arranged between the anode end plate and the anode plate of the electrolysis cell, and a cathode insulating pad is arranged between the cathode end plate and the cathode plate of the electrolysis cell; the anode end plate and the cathode end plate are connected by a connecting assembly.
Further optimizing the technical scheme, cutting the edge positions of the anode end plate and the cathode end plate;
and/or the anode end plate and the cathode end plate are respectively provided with a lightening hole.
Further optimizing the technical scheme, still include:
the sealing rings are arranged between the anode plate and the cathode plate of the electrolysis cell and between the anode plate and the cathode plate of the electrolysis cell; when a plurality of bipolar plates are arranged, the sealing rings are also arranged between two adjacent bipolar plates.
The technical scheme of the invention has the following advantages:
1. the bipolar plate provided by the invention has the advantages that the flow field is directly designed on the cathode end plate, the anode end plate and the bipolar plate, and a design mode of a gradual change type flow channel is adopted. On the premise of ensuring that the wall height of the flow channel is unchanged, the width of the flow channel is linearly increased from the middle to the two sides, more specifically, the width of the flow channel positioned in the middle is narrower, the width of the flow channel positioned at the two sides is wider, the amount of fluid passing through the flow channel with low flow velocity before optimization is increased, the amount of fluid passing through the flow channel with high flow velocity before optimization is reduced, and the flow velocity of the medium in the middle is also reduced. The gradual flow field can improve the mass transfer problem of gas and liquid phases, so that the liquid water flows more smoothly, the distribution of media is ensured to be more uniform, the risk of uneven water transfer under high current density is prevented, and the gradual flow field has the advantages of simple and compact structure, fewer system accessories, simple processing and small stress concentration, and the strength of the polar plate can be ensured.
2. According to the bipolar plate provided by the invention, the first annular distribution flow channel is a circular flow channel, and the second annular distribution flow channel is a circular flow channel, so that the uniformity of pre-distribution of media can be ensured.
3. According to the bipolar plate provided by the invention, the flow channels arranged on the outer surface of the cathode plate of the bipolar plate are respectively arranged at intervals along the X direction, the medium flow direction of each flow channel is the Y direction, the medium outlet of each flow channel is respectively communicated with the hydrogen outlet, hydrogen can flow upwards through the flow channel in the Y direction after being generated at the cathode plate of the bipolar plate, the hydrogen outlet is arranged above each flow channel, and then each flow channel can collect hydrogen at the hydrogen connecting channel, so that the hydrogen can be conveniently transmitted to the hydrogen outlet and discharged.
4. The proton exchange membrane electrolytic cell provided by the invention realizes gas and liquid sealing of high-pressure (5-50 MPa) hydrogen production by adopting a bipolar plate design of one plate and two poles, a gradual change flow field configuration and a special shape end plate design, has a simple structure and greatly reduces the system quality. The invention adopts the design of two unipolar plates and bipolar plates, two electrolytic cells Chi Lian are combined together, and electrolytic cells can be continuously increased by adding bipolar plates, so that the hydrogen production efficiency and the hydrogen production scale of the system are improved. The bipolar plate, the anode plate of the electrolytic cell and the cathode plate of the electrolytic cell respectively form the electrolytic cell, the arranged bipolar plate is simpler in structure relative to the isolated design of the cathode and anode unipolar plates, unnecessary structures are reduced, the arranged bipolar plate can be used for arranging the cathode and the anode on one plate, the number of accessories is greatly reduced relative to the existing electrolytic cell, the impedance is effectively reduced, the energy consumption is reduced, and the gas/liquid leakage risk is reduced.
5. The proton exchange membrane electrolytic tank provided by the invention has the advantages that the sealing rings are arranged between the anode plate and the cathode plate of the electrolytic single cell and between the anode plate and the cathode plate of the electrolytic single cell, and the sealing rings are adopted for sealing, so that the overall sealing performance of the electrolytic tank is effectively ensured, and the problem of liquid leakage under a high-pressure environment is avoided.
6. The anode end plate of the proton exchange membrane electrolytic cell provided by the invention is made of stainless steel, so that in-plane support is provided for the electrolytic cell, and axial pressure is uniformly distributed. The cathode end plate is made of stainless steel, provides in-plane support for the electrolytic tank, and evenly distributes axial pressure.
7. According to the proton exchange membrane electrolytic cell provided by the invention, the edge positions of the anode end plate and the cathode end plate are cut, so that the weight of the proton exchange membrane electrolytic cell can be reduced, and the weight of the whole electrolytic cell is further reduced. The edges of the anode end plate and the cathode end plate are cut into a plurality of arc-shaped grooves which are distributed at intervals. And the anode end plate and the cathode end plate are respectively provided with lightening holes which are circumferentially arranged at intervals, so that the weight of the anode end plate and the cathode end plate is further reduced. The invention has the advantages that the grooves with specific shapes and the cutting at the edge positions are arranged on the cathode end plate and the anode end plate, so that the volume of the end plate is reduced as much as possible on the premise of ensuring the bearing of the system and not influencing the matching, thereby reducing the weight of the system.
8. According to the proton exchange membrane electrolytic tank provided by the invention, two single electrolytic cells are formed by adding one bipolar plate into two unipolar plates, the same bipolar plate structure can be adopted for superposition on the basis, and one single electrolytic cell can be added after adding one bipolar plate, the corresponding sealing gasket and the diffusion layer, so that the power and the hydrogen yield of the system are greatly improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present invention, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 is an axial exploded view of a proton exchange membrane electrolyzer provided by the invention;
fig. 2 is a schematic structural diagram of a bipolar plate anode plate of a bipolar plate according to the present invention;
fig. 3 is a schematic view of a bipolar plate cathode plate of a bipolar plate according to the present invention;
fig. 4 is a cross-sectional view of a bipolar plate provided by the present invention;
FIG. 5 is a front view of an anode end plate of a proton exchange membrane electrolyzer provided by the invention;
FIG. 6 is a reverse side view of an anode end plate of a proton exchange membrane electrolyzer provided by the invention;
FIG. 7 is a front view of a cathode end plate of a proton exchange membrane electrolyzer provided by the invention;
FIG. 8 is a reverse side view of a cathode end plate of a proton exchange membrane electrolyzer provided by the invention;
FIG. 9 is an overall assembly view of a proton exchange membrane electrolyzer provided by the invention;
FIG. 10 is a graph of simulation results of the flow rate of the medium for each flow channel of a bipolar plate prior to optimization;
FIG. 11 is a graph comparing the performance of the bipolar plate before and after optimization for each flow channel medium flow rate.
Reference numerals: 1. the nut, 2, anode end plate, 3, anode insulating pad, 4, electrolytic cell anode plate, 5, anode seal ring, 6, first tab, 7, first anode diffusion layer, 8, first anode seal pad, 9, first cathode diffusion layer, 10, first cathode seal pad, 11, first cathode seal ring, 12, second electrolytic cell anode seal ring, 13, bipolar plate, 14, second electrolytic cell anode diffusion layer, 15, second anode seal pad, 16, second cathode diffusion layer, 17, second cathode seal pad, 18, second cathode seal ring, 19, electrolytic cell cathode plate, 20, second tab, 21, cathode insulating pad, 22, cathode end plate, 23, locating bolts, 24, water inlet, 25, first locating pin grooves, 26, water outlet, 27, anode flow field, 28, seal ring grooves, 29, second locating pin grooves, 30, hydrogen outlet, 31, locating bolt holes, 32.
Detailed Description
The following description of the embodiments of the present invention will be made apparent and fully in view of the accompanying drawings, in which some, but not all embodiments of the invention are shown. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the description of the present invention, it should be noted that the directions or positional relationships indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
In addition, the technical features of the different embodiments of the present invention described below may be combined with each other as long as they do not collide with each other.
Example 1
As shown in fig. 2-4, the present invention discloses a bipolar plate comprising an oppositely connected bipolar plate anode plate and bipolar plate cathode plate. The bipolar plate is internally provided with a flow field, a water inlet, a water outlet and an air outlet, and is connected with the diffusion layer to play a role in conducting electricity and provide a water/air transmission channel. The surface of the anode plate of the bipolar plate is provided with an anode flow field 27, and the surface of the cathode plate of the bipolar plate is provided with a cathode flow field 32. The anode flow field 27 and the cathode flow field each have a number of flow channels. The medium of the anode flow field 27 and/or the cathode flow field preferentially enters from the flow channel positioned in the middle and sequentially enters into the flow channels positioned at two sides, and the width of each flow channel on the anode flow field 27 and/or the cathode flow field increases linearly from the middle to the two sides.
In the present invention, the "medium" may be a gas or a liquid. Wherein the gas is hydrogen or oxygen, but is not limited to hydrogen or oxygen; the liquid is water, but is not limited to water. If the application scene of the bipolar plate changes, the type of medium will also change correspondingly.
Before optimizing, the bipolar plate is preferably arranged such that the medium in the anode flow field 27 and/or the cathode flow field enters the flow channels on the two sides from the flow channels on the middle, the medium in the flow channels on the middle has a high flow rate, and the medium in the flow channels on the two sides has a low flow rate. The flow field is directly designed on the cathode end plate, the anode end plate and the bipolar plate, and a design mode of a gradual change type flow channel is adopted, as shown in figure 2. On the premise of ensuring that the wall height of the flow channel is unchanged, the width of the flow channel is linearly increased from the middle to the two sides, and more specifically, the invention sets the width of the flow channel positioned in the middle to be narrower, sets the width of the flow channel positioned at the two sides to be wider, further increases the amount of fluid passing through the flow channel with low flow velocity before optimization, decreases the amount of fluid passing through the flow channel with high flow velocity before optimization, and also decreases the flow velocity of the medium of the flow channel positioned in the middle. The gradual flow field can improve the mass transfer problem of gas and liquid phases, so that the liquid water flows more smoothly, the distribution of media is ensured to be more uniform, the risk of uneven water transfer under high current density is prevented, and the gradual flow field has the advantages of simple and compact structure, fewer system accessories, simple processing and small stress concentration, and the strength of the polar plate can be ensured.
The manner in which the progressive flow channel is designed will now be described with particular reference to the examples. As shown in fig. 10, the widths of the flow channels before optimization are the same, and the flow velocity of the medium in the middle flow channel is high, while the flow velocity of the medium in the two flow channels is low as shown by fluid mechanics simulation. As shown in FIG. 11, the graph is a graph comparing the performance of the medium flow rates of each flow channel before and after optimization. As can be seen from FIG. 11, before optimization, the medium flow rate of the medium in the middle flow channel is about 0.35-0.4 m/s; after optimization, the medium flow rate of the medium in the middle flow channel is about 0.2 m/s.
After optimization, the flow channels are designed in a mode that the width of each flow channel increases linearly from the middle to the two sides, the medium flow velocity of each flow channel is more uniform, and the medium flow velocity distribution of each flow channel is obviously improved.
The flow channel design of the bipolar plate is designed based on the fluid mechanics simulation result. The simulation model is established as follows: establishing a simulation model, wherein the simulation model corresponds to the flow channel setting form on the bipolar plate one by one; a water inlet and a water outlet are arranged; simultaneously giving parameters of water, wherein the parameters comprise flow rate, conductivity, salinity coefficient and the like; performing fluid mechanics simulation, and mainly observing the flow rate of water; setting the flow channels to be the same in width, and carrying out simulation, wherein the flow velocity distribution of the flow channels is observed to be that the flow velocity of the middle flow channel is high, and the flow velocity of the flow channels at two sides is low; and redesigning the model, redesigning the width of the flow channels, arranging the flow channels in a mode that the width of each flow channel linearly increases from the middle to the two sides, and carrying out simulation again to observe the flow velocity of water, wherein the result shows that the medium flow velocity of each flow channel is more uniform.
As a preferred embodiment, the width of the middle flow channel is 1.2-1.8 mm, the width of the outermost flow channel is 2.2-2.5 mm, and under the parameter, the flow velocity distribution of the medium in the flow channel is more uniform.
As a specific embodiment, the bipolar plate anode plate is provided with a water inlet 24 and a water outlet 26. The anode side is supplied with pure water by taking the water inlet 24 as an inlet; the water outlet 26 is used as an outlet to discharge oxygen and surplus pure water. The flow channels arranged on the outer surface of the bipolar plate anode plate are respectively arranged at intervals along the Y direction, the medium flow direction of each flow channel is the X direction, the medium inlet of each flow channel is respectively communicated with the water inlet 24, and the medium outlet of each flow channel is respectively communicated with the water outlet 26.
As a further improved embodiment, the outer surface of the bipolar plate anode plate is provided with a first annular distribution runner adapted for pre-distributing the medium, and each runner on the bipolar plate anode plate is arranged inside the first annular distribution runner. One side of the water inlet 24 is communicated with a first annular distribution flow passage through a first connecting flow passage, and the other side of the first annular distribution flow passage is communicated with the water outlet 26 through a second connecting flow passage. One side of the first annular distribution flow channel is adapted to pre-distribute media to each flow channel on the bipolar plate anode plate. Each flow channel on the bipolar plate anode plate is adapted to transport media and confluence the media to the other side of the first annular distribution flow channel, which is adapted to confluence the media to the water outlet 26.
The water inlet 24 is a pure water inlet, and the inside is of a pipe thread design and is used for connecting a quick connector. The inside of the water-gas outlet is designed into a pipe thread for connecting the quick connector.
The first annular distribution flow channel is a circular flow channel, so that uniformity of pre-distribution of the medium can be guaranteed. The first connecting flow channel and the second connecting flow channel are flow channels distributed along the X direction. Since each flow channel on the bipolar plate anode plate is arranged inside the first annular distribution flow channel and the first annular distribution flow channel is a circular flow channel, the length of each flow channel gradually decreases from the middle to the Y direction and the-Y direction. When the circular first annular distribution flow channel distributes the medium, the flow channels positioned at the middle part are firstly distributed with the medium, then the flow channels positioned in the Y direction and the Y direction are distributed with the medium, the length of the flow channels positioned at the two sides of the middle flow channel is set to be shorter, the time that the medium passes through each flow channel and flows to the second connection flow channel is consistent, and the uniformity of the distribution of the medium on the outer surface of the anode plate of the bipolar plate is enhanced.
As a further improved embodiment, the bipolar plate cathode plate is provided with a hydrogen outlet 30, the hydrogen outlet 30 is used for discharging hydrogen generated by cathode electrolytic water, reactants on the cathode side are protons provided by the PEM, and therefore, a water inlet and a water outlet are not required, and only the hydrogen outlet 30 is required to discharge generated high-pressure hydrogen. The channels arranged on the outer surface of the bipolar plate cathode plate are respectively arranged at intervals along the X direction, the medium flow direction of each channel is the Y direction, and the medium outlet of each channel is respectively communicated with the hydrogen outlet 30. In this embodiment, hydrogen generated at the cathode plate of the bipolar plate can flow upward through the channels in the Y direction, and the hydrogen outlet 30 is disposed above each channel, so that each channel can collect hydrogen at the hydrogen connecting channel and then transmit the hydrogen to the hydrogen outlet 30. It should be noted that the hydrogen connecting channel is set as a U-shaped channel, and a middle connecting channel is further provided in the middle of the U-shaped channel, and both the U-shaped channel and the middle connecting channel are communicated with each flow channel.
The outer surface of the bipolar plate cathode plate is provided with a second annular distribution runner which is suitable for collecting media, and each runner on the bipolar plate cathode plate is arranged on the inner side of the second annular distribution runner. Since each flow channel on the bipolar plate cathode plate is arranged inside the second annular distribution flow channel, and the second annular distribution flow channel is a circular flow channel, the length of each flow channel gradually decreases from the middle to the X direction and the-X direction. The circular second annular distribution flow channel can ensure the uniformity of the pre-distribution of the medium. When the circular second annular distribution flow channel distributes the medium, the flow channels positioned at the middle part are firstly distributed with the medium, then the flow channels positioned in the X direction and the-X direction are distributed with the medium, the length of the flow channels positioned at the two sides of the middle flow channel is set to be shorter, the time that the medium passes through each flow channel and flows to the second connection flow channel is consistent, and the uniformity of the distribution of the medium on the outer surface of the cathode plate of the bipolar plate is enhanced.
As a further improved embodiment, the surface of the anode plate and/or the cathode plate of the bipolar plate is provided with a sealing ring groove 28 for placing an O-ring and a retainer ring, so as to realize the sealing and close fit of the system under high pressure. More specifically, the outer edges of the flow fields of the anode plate and the bipolar plate are provided with sealing ring grooves. The seal ring groove is adapted to locate the seal ring. The seal ring grooves on the anode plate and the cathode plate of the bipolar plate are all elliptical, and it is required to be noted that the elliptical long axes of the seal ring grooves on the anode plate of the bipolar plate are arranged along the X direction, and the elliptical long axes of the seal ring grooves on the cathode plate of the bipolar plate are arranged along the Y direction. Under high pressure conditions (5-50 MPa), the risk of gas/liquid leakage increases because the pure water and gas pressures within the PEM cell stack are much greater than ambient air pressure. An O-shaped sealing ring and a check ring are arranged in the groove, so that the close fit of the system can be ensured, and water and gas leakage can be isolated.
The bipolar plate can be applied to an electrolytic cell, but is not limited to an electrolytic cell, and can also be applied to a fuel cell.
Example 2
The conventional PEM electrolytic stack system has excessively complex design of the cathode and anode unipolar plates, can obviously increase the system impedance, increase the energy consumption and increase the gas/liquid leakage risk in the electrolytic stack system with high power and multiple electrolytic cells connected in series. The above problems are caused by the fact that the above system uses more components and more metal materials, each metal material itself has resistance, and the resistance generated by the accumulation of the resistance of all the metal materials is larger. And the more parts, the accuracy of the machining size of each part cannot be ensured, and the problem of gas or liquid leakage easily occurs.
In order to solve the technical problems, the embodiment discloses a proton exchange membrane electrolyzer, the application scene is high-pressure (5-50 MPa) PEM water electrolysis hydrogen production, and the special application scene has higher requirements on the quality, volume and hydrogen production scale of an electrolytic stack.
Referring to fig. 1 to 9, the present invention proposes a proton exchange membrane electrolyzer based on the above application scenario, comprising an electrolysis cell anode plate 4, an electrolysis cell cathode plate 19, a bipolar plate and a proton exchange membrane assembly.
The electrolytic single cell anode plate 4 is internally provided with a flow field, a second water inlet and a second water outlet which are connected with the diffusion layer to play a role in conducting electricity and provide a water/gas transmission channel. The electrolytic cell anode plate 4 is provided with a first lug 6 connected with a power supply.
The cathode plate 19 of the electrolytic cell is internally provided with a flow field and an air outlet, and is connected with the diffusion layer to play a role in conducting electricity and provide a water/air transmission channel. The electrolytic cell cathode plate 19 is provided with a second lug 20 connected with a power supply.
In this embodiment, a bipolar plate of embodiment 1 is disposed opposite to the electrolytic cell anode plate 4 and forms a first electrolytic cell with the electrolytic cell anode plate 4, and a bipolar plate anode plate is disposed opposite to the electrolytic cell cathode plate 19 and forms a second electrolytic cell with the electrolytic cell cathode plate 19.
The proton exchange membrane components are arranged between the electrolytic single cell anode plate 4 and the bipolar plate cathode plate and between the bipolar plate anode plate and the electrolytic single cell cathode plate 19.
The proton exchange membrane electrolyzer has the advantages that the bipolar plates, the electrolysis unit cell anode plates 4 and the electrolysis unit cell cathode plates 19 respectively form the electrolysis unit cell, the arranged bipolar plates are simpler in structure relative to the isolated design of the cathode and anode unipolar plates, unnecessary structures are reduced, the arranged bipolar plates can be used for arranging the cathode and the anode on one plate, the number of accessories is greatly reduced relative to the existing electrolyzer, the impedance is effectively reduced, the energy consumption is reduced, and the gas/liquid leakage risk is reduced.
As a specific embodiment, a proton exchange membrane assembly includes a first diffusion layer, a first gasket, a second diffusion layer, and a proton exchange membrane. The first diffusion layer plate is disposed opposite the flow field of the electrolytic cell anode plate 4 or the anode flow field 27 of the bipolar plate. The first gasket is in contact with the first diffusion layer plate. The second gasket is in contact with the electrolytic cell cathode plate 19 or bipolar plate cathode plate. The second diffusion layer plate is disposed between the first and second gaskets and is disposed opposite the cathode flow field of the bipolar plate or the flow field of the electrolytic cell cathode plate 19. The proton exchange membrane is arranged between the first diffusion layer plate and the second diffusion layer plate, the shape of the proton exchange membrane is the same as that of the first diffusion layer plate and the second diffusion layer plate, and the proton exchange membrane is used for transferring protons (namely hydrogen atoms).
In this embodiment, taking a proton exchange membrane assembly between the electrolytic cell anode plate 4 and the bipolar plate as an example, a first anode diffusion layer 7, a first anode sealing pad, a proton exchange membrane, a first cathode diffusion layer 9 and a first cathode sealing pad 10 are sequentially arranged from left to right. Wherein the first anode diffusion layer 7 is connected with the polar plate and the membrane electrode as a porous supporting structure to provide the electric conduction and water/gas distribution functions. The first anode sealing gasket supports the anode diffusion layer and the membrane electrode, and plays a role in sealing to prevent water/gas leakage. The first cathode diffusion layer 9 is connected to the plate and membrane electrode as a porous support structure providing an electrically conductive, water/gas distribution effect. The first cathode sealing gasket 10 is used for supporting the first cathode diffusion layer 9, the first anode diffusion layer 7 and the membrane electrode, and plays a role of sealing to prevent water/gas leakage.
In this embodiment, taking a proton exchange membrane assembly between a bipolar plate and an electrolytic cell cathode plate 19 as an example, a second electrolytic cell anode diffusion layer 14, a second anode gasket 15, a second cathode diffusion layer 16, and a second cathode gasket 17 are sequentially disposed from left to right. Wherein the second electrolytic cell anode diffusion layer 14 is connected to the plate and membrane electrode as a porous support structure providing electrical conductivity, water/gas distribution. The second anode gasket 15 is used for supporting the second electrolytic cell anode diffusion layer 14 and the membrane electrode, and plays a role of sealing to prevent water/gas leakage. The second cathode diffusion layer 16 is connected to the plate and membrane electrode as a porous support structure providing a conductive, water/gas distribution effect. The second cathode sealing gasket 17 is used for supporting the second cathode diffusion layer and the membrane electrode, and has a sealing function to prevent water/gas leakage.
The cathode diffusion layer in the present invention functions as: the cathode diffusion layer in PEM electrolysers is typically a titanium fiber felt or titanium powder sintered felt, which functions primarily for mass transfer-electrical conduction and moisture transport, corresponding to the cathode being primarily hydrogen transport.
However, in the conventional PEM electrolytic stack system, the sealing function is realized only through the sealing gasket, and the problem of liquid leakage cannot be solved in a high-pressure environment. In order to solve the above technical problem, as a further improved embodiment, the present invention further comprises a plurality of sealing rings, wherein the sealing rings are arranged between the electrolytic cell anode plate 4 and the bipolar plate cathode plate and between the bipolar plate anode plate and the electrolytic cell cathode plate 19. An anode sealing ring 5 and a first cathode sealing ring 11 are arranged between the electrolytic cell anode plate 4 and the bipolar plate cathode plate, the anode sealing ring 5 is embedded on the electrolytic cell anode plate 4, and the first cathode sealing ring 11 is embedded in a sealing ring groove of the bipolar plate cathode plate. A second electrolysis cell anode sealing ring 12 and a second cathode sealing ring 18 are arranged between the bipolar plate anode plate and the electrolysis cell cathode plate 19, the second electrolysis cell anode sealing ring 12 is embedded in a sealing ring groove of the bipolar plate anode plate, and the second cathode sealing ring 18 is embedded in a sealing ring groove of the bipolar plate anode plate. The embodiment adopts the multiple sealing rings to seal, effectively ensures the overall sealing performance of the electrolytic tank, and avoids the problem of liquid leakage in a high-pressure environment.
Wherein, the anode sealing ring 5 and the second electrolysis cell anode sealing ring 12 are O-shaped sealing rings and check rings which are used in combination and are connected with the anode plate to play a role in sealing and prevent water/gas leakage. The first cathode sealing ring 11 and the second cathode sealing ring 18 are O-shaped sealing rings and check rings which are used in combination and are connected with a cathode polar plate to play a role in sealing and prevent water/gas leakage.
It should be noted that, the elliptical long axis of the seal ring groove formed on the bipolar plate cathode plate is arranged along the Y direction, and the elliptical long axis of the seal ring groove formed on the electrolytic cell anode plate 4 is arranged along the X direction, so that the seal ring on the bipolar plate cathode plate is mutually perpendicular to the seal ring on the electrolytic cell anode plate 4. The elliptic long axis of the sealing ring groove arranged on the anode plate of the bipolar plate is arranged along the X direction, and the elliptic long axis of the sealing ring groove arranged on the cathode plate 19 of the electrolytic cell is arranged along the Y direction, so that the sealing ring on the anode plate of the bipolar plate is mutually perpendicular to the sealing ring on the cathode plate 19 of the electrolytic cell. The reason for this arrangement is that the water inlet and the water outlet on the anode plate are arranged along the X direction, so that the elliptical long axis of the sealing ring groove on the anode plate is arranged along the X direction to enclose the water inlet and the water outlet inside. Since the hydrogen outlet on the cathode plate is arranged along the Y direction, the elliptical long axis of the seal ring groove on the cathode plate is arranged along the Y direction to enclose the hydrogen outlet inside.
As a further improved embodiment, the outside of the electrolytic cell anode plate 4 is provided with an anode end plate 2, and the outside of the electrolytic cell cathode plate 19 is provided with a cathode end plate 22. The anode end plate 2 and the cathode end plate 22 are previously connected by a connection assembly. The anode end plate 2 is made of stainless steel, provides in-plane support for the electrolytic cell, and evenly distributes axial pressure. The cathode end plate 22 is made of stainless steel, provides in-plane support for the electrolyzer, and distributes axial pressure evenly.
The connection assembly comprises a positioning bolt 23 and a nut 1, the positioning bolt 23 and the nut 1 providing an axial compression force to fix the electrolytic cell, as shown in fig. 9.
An anode insulating pad 3 is arranged between the anode end plate 2 and the electrolysis cell anode plate 4, and a cathode insulating pad 21 is arranged between the cathode end plate 22 and the electrolysis cell cathode plate 19. The cathode insulator 21 serves as an insulator for insulating the plates from the cathode end plate 22. The anode insulating pad 3 serves as an insulation for insulating the plates from the anode end plate 2.
The current PEM electrolyser end plates are thicker and made of stainless steel materials, so that the weight of the PEM electrolyser end plates is larger, and the PEM electrolyser end plates are not beneficial to special application occasions requiring weight and volume. In order to solve this technical problem, as a further improved embodiment, the end plates are the heaviest components in the electrolytic cell, and the edge positions of the anode end plate 2 and the cathode end plate 22 are cut, so that the weight thereof can be reduced, and thus the weight of the entire electrolytic cell can be reduced. The edges of the anode end plate 2 and the cathode end plate 22 are cut into a plurality of arc-shaped grooves arranged at intervals. And the anode end plate 2 and the cathode end plate 22 are respectively provided with lightening holes which are circumferentially arranged at intervals, so that the weight of the anode end plate 2 and the cathode end plate 22 is further reduced. The invention has the advantages that the grooves with specific shapes and the cutting at the edge positions are arranged on the cathode end plate and the anode end plate, so that the volume of the end plate is reduced as much as possible on the premise of ensuring the bearing of the system and not influencing the matching, thereby reducing the weight of the system.
The invention aims to provide a lightweight high-voltage-resistant PEM electrolytic stack structure. By adopting a bipolar plate design with one plate and two poles, a gradual change type flow field configuration and a special shape end plate design, gas and liquid sealing of high-pressure (5-50 MPa) hydrogen production is realized, the structure is simplified, and the system quality is greatly reduced.
The invention adopts the design of two unipolar plates and bipolar plates, two electrolytic cells Chi Lian are combined together, and electrolytic cells can be continuously increased by adding bipolar plates, so that the hydrogen production efficiency and the hydrogen production scale of the system are improved.
When the proton exchange membrane electrolytic cell is assembled and positioned, a plurality of positioning bolt holes 31 are respectively formed on the anode end plate 2 and the cathode insulating pad 21 at intervals in the circumferential direction. A plurality of locating pin grooves are formed in the side wall of the bipolar plate, and two locating pin grooves are formed in the locating pin groove in the embodiment, namely a first locating pin groove 25 and a second locating pin groove 29 which are oppositely arranged, as shown in fig. 2 and 3. Correspondingly, the cathode end plate 22 and the anode end plate 2 are also provided with a first detent groove 25 and a second detent groove 29, respectively. And the positioning pins sequentially penetrate through the grooves of the positioning pins, so that the alignment and calibration of all parts are ensured, and the system is initially assembled.
In the invention, when the electrolytic cell anode plate 2, the anode insulating pad 3, the electrolytic cell anode plate 4, the anode sealing ring 5, the first anode diffusion layer 7, the first anode sealing pad 8, the first cathode diffusion layer 9, the first cathode sealing pad 10, the bipolar plate 13, the second electrolytic cell anode diffusion layer 14, the second anode sealing pad 15, the second cathode diffusion layer 16, the second cathode sealing pad 17, the electrolytic cell cathode plate 19, the cathode insulating pad 21 and the cathode end plate 22 are assembled in sequence, and before the assembly, the sealing rings are positioned in the sealing ring grooves. The positioning pins sequentially penetrate through the positioning pin grooves to perform preliminary assembly on the system, the positioning bolts 23 sequentially penetrate through the positioning bolt holes 31, and the positioning bolts are positioned through the nuts 1 to realize integral assembly.
The proton exchange membrane electrolyzer is divided into two electrolytic cells from left to right by an electrolytic cell anode plate 4, a bipolar plate 13 (left cathode and right anode) and an electrolytic cell cathode plate 19 in a serial working mode. When the electrolytic cell works, pure water flows in from the water inlet of the anode, is transferred to the anode plate of the electrolytic cell through the anode flow field plate, and oxygen generated by reaction flows into the water outlet along with the pure water and is discharged. Protons in the pure water are transferred to the cathode through the proton exchange membrane, hydrogen is generated by reaction, and the hydrogen flows into a hydrogen outlet through a cathode flow field and is discharged.
Example 3
The present embodiment discloses a proton exchange membrane electrolyzer, which is based on embodiment 2, wherein a plurality of bipolar plates are arranged between an electrolysis cell anode plate 4 and an electrolysis cell cathode plate 19. Adjacent bipolar plates are connected in series through anode-cathode, and a third electrolytic cell is respectively formed between every two adjacent bipolar plates. The term "plurality" means two or more.
Because the bipolar plates in the embodiment are arranged in a plurality, the proton exchange membrane assembly is also arranged between two adjacent bipolar plates, so that water electrolysis can be carried out between the two bipolar plates.
And a sealing ring is also arranged between the two bipolar plates, and the bipolar plates are sealed through the sealing ring, so that the water/gas leakage is prevented.
The invention discloses a method for increasing power of an electrolytic stack, which comprises the following steps: two bipolar plates are added to form two electrolytic cells, the same bipolar plate structure can be adopted to carry out superposition on the basis, and one electrolytic cell can be added every time one bipolar plate, a corresponding sealing gasket and a diffusion layer are added, so that the power and the hydrogen yield of the system are greatly improved.
It is apparent that the above examples are given by way of illustration only and are not limiting of the embodiments. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention.
Claims (9)
1. A bipolar plate comprising an anode plate and a cathode plate of the bipolar plate connected opposite each other; the bipolar plate anode plate is characterized in that an anode flow field (27) is arranged on the surface of the bipolar plate anode plate, and a cathode flow field is arranged on the surface of the bipolar plate cathode plate; the anode flow field (27) and the cathode flow field are provided with a plurality of flow channels; the width of each flow channel on the anode flow field (27) and/or the cathode flow field increases linearly from the middle to the two sides along the direction perpendicular to the medium flow;
a water inlet (24) and a water outlet (26) are formed in the bipolar plate anode plate; the medium flow direction of each flow channel is in the X direction, the medium inlet of each flow channel is respectively communicated with the water inlet (24), and the medium outlet of each flow channel is respectively communicated with the water outlet (26);
the outer surface of the bipolar plate anode plate is provided with a first annular distribution runner which is suitable for pre-distributing a medium, and each runner on the bipolar plate anode plate is arranged at the inner side of the first annular distribution runner;
one side of the water inlet (24) is communicated with a first annular distribution flow passage, and the other side of the first annular distribution flow passage is communicated with the water outlet (26); one side of the first annular distribution runner is suitable for pre-distributing medium to each runner on the bipolar plate anode plate, each runner on the bipolar plate anode plate is suitable for conveying medium and converging and conveying the medium to the other side of the first annular distribution runner, and the other side of the first annular distribution runner is suitable for converging and inputting the medium to a water outlet (26).
2. Bipolar plate according to claim 1, characterized in that a hydrogen outlet (30) is provided on the bipolar plate cathode plate; the flow channels arranged on the outer surface of the bipolar plate cathode plate are respectively arranged at intervals along the X direction, the medium flow direction of each flow channel is the Y direction, and the medium outlet of each flow channel is respectively communicated with the hydrogen outlet (30).
3. The bipolar plate of claim 2 wherein the outer surface of the bipolar plate cathode plate is provided with second annular distribution channels adapted to collect media, each channel on the bipolar plate cathode plate being disposed inside the second annular distribution channel.
4. A bipolar plate according to any one of claims 1-3, characterized in that the surface of the bipolar plate anode plate and/or bipolar plate cathode plate is provided with seal ring grooves adapted for positioning seal rings.
5. A proton exchange membrane electrolyzer comprising:
an electrolytic single cell anode polar plate (4) is internally provided with a flow field, a second water inlet and a second water outlet;
a flow field and an air outlet are arranged in the electrolytic single cell cathode polar plate (19);
one or more bipolar plates according to any one of claims 1-4, wherein the bipolar plate cathode plate positioned at the outermost side is arranged opposite to the electrolytic cell anode plate (4) and forms a first electrolytic cell with the electrolytic cell anode plate (4), and the bipolar plate anode plate positioned at the outermost side is arranged opposite to the electrolytic cell cathode plate (19) and forms a second electrolytic cell with the electrolytic cell cathode plate (19); when a plurality of bipolar plates are arranged, two adjacent bipolar plates are connected in series through an anode-cathode mode, and a third electrolytic cell is respectively formed between every two adjacent bipolar plates;
the proton exchange membrane assemblies are arranged between the anode plate (4) of the electrolysis cell and the cathode plate of the bipolar plate and between the anode plate of the bipolar plate and the cathode plate (19) of the electrolysis cell; when a plurality of bipolar plates are arranged, the proton exchange membrane assembly is also arranged between two adjacent bipolar plates.
6. The proton exchange membrane electrolyzer of claim 5 wherein the proton exchange membrane module comprises:
the first diffusion laminate is arranged opposite to a flow field of the electrolytic single cell anode plate (4) or an anode flow field (27) of the bipolar plate;
a first gasket in contact with the first diffusion layer plate;
the second sealing gasket is contacted with the cathode plate (19) or the cathode plate of the bipolar plate of the electrolysis cell;
the second diffusion laminate is arranged between the first sealing gasket and the second sealing gasket and is opposite to a cathode flow field of the bipolar plate or a flow field of the electrolytic cell cathode plate (19);
and the proton exchange membrane is arranged between the first diffusion layer plate and the second diffusion layer plate.
7. The proton exchange membrane electrolyzer of claim 5 characterized in that the outside of the electrolysis cell anode plate (4) is provided with an anode end plate (2) and the outside of the electrolysis cell cathode plate (19) is provided with a cathode end plate (22); an anode insulating pad (3) is arranged between the anode end plate (2) and the electrolysis cell anode plate (4), and a cathode insulating pad (21) is arranged between the cathode end plate (22) and the electrolysis cell cathode plate (19); the anode end plate (2) and the cathode end plate (22) are connected by a connecting assembly.
8. Proton exchange membrane electrolyzer according to claim 7, characterized in that the edge locations of the anode end plate (2) and cathode end plate (22) are cut;
and/or the anode end plate (2) and the cathode end plate (22) are respectively provided with a lightening hole.
9. The proton exchange membrane electrolyzer of claim 5 further comprising:
the sealing rings are arranged between the electrolytic cell anode plate (4) and the bipolar plate cathode plate and between the bipolar plate anode plate and the electrolytic cell cathode plate (19); when a plurality of bipolar plates are arranged, the sealing rings are also arranged between two adjacent bipolar plates.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310994173.9A CN116770336B (en) | 2023-08-08 | 2023-08-08 | Bipolar plate and proton exchange film electrolytic tank |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310994173.9A CN116770336B (en) | 2023-08-08 | 2023-08-08 | Bipolar plate and proton exchange film electrolytic tank |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN116770336A CN116770336A (en) | 2023-09-19 |
| CN116770336B true CN116770336B (en) | 2023-12-26 |
Family
ID=87986100
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310994173.9A Active CN116770336B (en) | 2023-08-08 | 2023-08-08 | Bipolar plate and proton exchange film electrolytic tank |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116770336B (en) |
Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101656320A (en) * | 2009-09-04 | 2010-02-24 | 新奥科技发展有限公司 | Flow-field plate for electrochemical cell |
| KR20110087123A (en) * | 2010-01-25 | 2011-08-02 | 인제대학교 산학협력단 | Bipolar plate for fuel cell comprising sub channel |
| CN202523795U (en) * | 2012-04-27 | 2012-11-07 | 中国东方电气集团有限公司 | Bipolar plate, cooling plate and fuel cell stack |
| CN103806014A (en) * | 2014-01-24 | 2014-05-21 | 北京科技大学 | Proton exchange membrane water electrolysis device |
| CN208189743U (en) * | 2018-04-26 | 2018-12-04 | 苏州库宁换热系统科技有限公司 | A kind of battery water-cooled plate |
| CN110085886A (en) * | 2019-05-21 | 2019-08-02 | 吉林大学 | A kind of fuel battery double plates and its method in bionical flow field |
| CN110129818A (en) * | 2019-05-30 | 2019-08-16 | 武汉理工大学 | Proton exchange membrane water electrolyzer slot |
| CN209487611U (en) * | 2019-04-04 | 2019-10-11 | 深圳市致远动力科技有限公司 | A kind of bipolar plates and its fuel cell with micro-nano rank airflow channel |
| CN110813393A (en) * | 2018-08-08 | 2020-02-21 | 苏州含光微纳科技有限公司 | Structure for improving low-flow-speed liquid flow interface and immune micro-fluidic chip |
| CN216597644U (en) * | 2021-11-24 | 2022-05-24 | 广州仑擎能源科技有限公司 | Fuel cell with flow field and flow channel for enhancing gas mass transfer |
| CN114551921A (en) * | 2020-11-26 | 2022-05-27 | 中国科学院大连化学物理研究所 | High-temperature proton exchange membrane fuel cell flow field structure |
| CN217788456U (en) * | 2022-06-17 | 2022-11-11 | 嘉庚创新实验室 | Circular bipolar plate runner structure and electrolytic cell |
| CN115513486A (en) * | 2022-10-27 | 2022-12-23 | 中汽创智科技有限公司 | Unipolar plate, bipolar plate, electric pile and fuel cell |
| CN115986160A (en) * | 2022-12-27 | 2023-04-18 | 上海骥翀氢能科技有限公司 | Bipolar plate flow field, bipolar plate and fuel cell |
| KR20230082450A (en) * | 2021-12-01 | 2023-06-08 | 서울시립대학교 산학협력단 | concentric circular flow field with increasing oxygen emission for polymer electrolyte membrane water electrolysis stack with the same |
| CN116397250A (en) * | 2023-03-30 | 2023-07-07 | 同济大学 | Asymmetric metal mesh flow field for alkaline electrolytic tank and alkaline electrolytic tank |
| CN116960083A (en) * | 2023-07-06 | 2023-10-27 | 大连理工大学 | Multichannel radiator with coolant distributor |
-
2023
- 2023-08-08 CN CN202310994173.9A patent/CN116770336B/en active Active
Patent Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101656320A (en) * | 2009-09-04 | 2010-02-24 | 新奥科技发展有限公司 | Flow-field plate for electrochemical cell |
| KR20110087123A (en) * | 2010-01-25 | 2011-08-02 | 인제대학교 산학협력단 | Bipolar plate for fuel cell comprising sub channel |
| CN202523795U (en) * | 2012-04-27 | 2012-11-07 | 中国东方电气集团有限公司 | Bipolar plate, cooling plate and fuel cell stack |
| CN103806014A (en) * | 2014-01-24 | 2014-05-21 | 北京科技大学 | Proton exchange membrane water electrolysis device |
| CN208189743U (en) * | 2018-04-26 | 2018-12-04 | 苏州库宁换热系统科技有限公司 | A kind of battery water-cooled plate |
| CN110813393A (en) * | 2018-08-08 | 2020-02-21 | 苏州含光微纳科技有限公司 | Structure for improving low-flow-speed liquid flow interface and immune micro-fluidic chip |
| CN209487611U (en) * | 2019-04-04 | 2019-10-11 | 深圳市致远动力科技有限公司 | A kind of bipolar plates and its fuel cell with micro-nano rank airflow channel |
| CN110085886A (en) * | 2019-05-21 | 2019-08-02 | 吉林大学 | A kind of fuel battery double plates and its method in bionical flow field |
| CN110129818A (en) * | 2019-05-30 | 2019-08-16 | 武汉理工大学 | Proton exchange membrane water electrolyzer slot |
| CN114551921A (en) * | 2020-11-26 | 2022-05-27 | 中国科学院大连化学物理研究所 | High-temperature proton exchange membrane fuel cell flow field structure |
| CN216597644U (en) * | 2021-11-24 | 2022-05-24 | 广州仑擎能源科技有限公司 | Fuel cell with flow field and flow channel for enhancing gas mass transfer |
| KR20230082450A (en) * | 2021-12-01 | 2023-06-08 | 서울시립대학교 산학협력단 | concentric circular flow field with increasing oxygen emission for polymer electrolyte membrane water electrolysis stack with the same |
| CN217788456U (en) * | 2022-06-17 | 2022-11-11 | 嘉庚创新实验室 | Circular bipolar plate runner structure and electrolytic cell |
| CN115513486A (en) * | 2022-10-27 | 2022-12-23 | 中汽创智科技有限公司 | Unipolar plate, bipolar plate, electric pile and fuel cell |
| CN115986160A (en) * | 2022-12-27 | 2023-04-18 | 上海骥翀氢能科技有限公司 | Bipolar plate flow field, bipolar plate and fuel cell |
| CN116397250A (en) * | 2023-03-30 | 2023-07-07 | 同济大学 | Asymmetric metal mesh flow field for alkaline electrolytic tank and alkaline electrolytic tank |
| CN116960083A (en) * | 2023-07-06 | 2023-10-27 | 大连理工大学 | Multichannel radiator with coolant distributor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN116770336A (en) | 2023-09-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6500580B1 (en) | Fuel cell fluid flow plate for promoting fluid service | |
| US8617361B2 (en) | PEM water electrolyser module | |
| Ressel et al. | Performance of a vanadium redox flow battery with tubular cell design | |
| CN213804006U (en) | Water electrolysis bath with novel channel arrangement mode | |
| CN103806014A (en) | Proton exchange membrane water electrolysis device | |
| US9187833B2 (en) | Internally-reinforced water electrolyser module | |
| WO2003075379A2 (en) | Electrochemical spefc hydrogen compressor | |
| CN104157895B (en) | The light-duty pile of polymer dielectric film fuel cell and manufacture method thereof | |
| CN111244496B (en) | Fuel cell and flow distribution device | |
| US7432008B2 (en) | Gas diffusion layer for an electrochemical cell | |
| CN216039848U (en) | Electrolytic cell | |
| CN115976553A (en) | Water electrolysis hydrogen production device with turbulence strengthening module and method | |
| CN215266375U (en) | Single-plate three-cavity fuel cell bipolar plate and fuel cell stack | |
| CN102110838B (en) | Proton exchange membrane fuel cell stack | |
| CN219653143U (en) | Electrolytic tank, hydrogen production device and new energy hydrogen production system | |
| CN116770336B (en) | Bipolar plate and proton exchange film electrolytic tank | |
| CN217788456U (en) | Circular bipolar plate runner structure and electrolytic cell | |
| CN114622230B (en) | Electrochemical reaction apparatus and electrochemical device thereof | |
| CN112838238B (en) | Flow battery stack and heat insulation plate thereof | |
| CN113206269A (en) | Single-plate three-cavity fuel cell bipolar plate and fuel cell stack | |
| GB2505693A (en) | A proton exchange membrane fuel cell with open pore cellular foam | |
| EP3590144B1 (en) | Novel modular electrochemical cell and stack design | |
| CN217499434U (en) | Water electrolytic tank with long service life and short assembly period | |
| CN219696491U (en) | Integrated sintered bipolar plate | |
| CN115839990B (en) | Water electrolysis observation and electrochemical performance testing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |