Electrolyzer device based on proton exchange membrane and method for manufacturing such a device

Abstract

An electrolyzer based on a proton exchange membrane includes an anode, a cathode, and a proton exchange membrane, wherein the anode is on a first surface of the membrane, and the cathode is on a second opposing surface. The anode includes a parallel anode catalyst layer and an anode porous transport layer, the catalyst layer being located between the transport layer and the first surface. The cathode includes a parallel cathode catalyst layer and a cathode porous transport layer, the catalyst layer being located between the transport layer and the second surface. The electrolyzer includes conductive first and second meshes on the anode and cathode sides, wherein the surface of the first mesh covers the surface of the anode catalyst layer, and wherein the surface of the second mesh covers the surface of the cathode catalyst layer.

Description

Invention Field

[0001] This invention relates to an electrolyzer device based on a proton exchange membrane. Furthermore, this invention relates to a method for manufacturing such a device. Background Technology

[0002] Proton exchange membrane electrolyzers (PEMWEs) have been considered among the most promising devices for producing hydrogen from water and storing energy, especially when combined with sustainable energy sources such as wind and solar power. Typically, existing PEMWEs comprise components such as bipolar plates (BPPs), porous transport layers (PTLs), catalyst layers (CLs), and proton exchange membranes (PEMs). The catalyst layer is typically coated onto the PEM. The PTL is used to transport liquid material from the bipolar plates to the PEM. The catalyst on the anode side is typically composed of iridium (Ir) or ruthenium (Ru) or an Ir-Ru alloy. The catalyst on the cathode side is typically composed of platinum (Pt). Each metal has relatively low abundance in the Earth and is therefore only available at high cost.

[0003] Therefore, it is desirable to better utilize these catalyst materials in the electrolyzer (at lower amounts). However, by reducing the amount of catalyst metal in the electrolyzer (i.e., lower catalyst material loading), PEMWE suffers from low catalyst utilization and high ohmic resistance across the electrolyzer assembly, particularly within the CL. Discontinuity / interruption can occur within the catalyst layer by reducing the amount of catalyst forming the layer. Consequently, the region within the catalyst layer becomes non-uniform, accompanied by the formation of small catalyst patches / islands. Due to the reduced catalyst loading, these small catalyst patches / islands may become electrically disconnected / isolated from each other and from the PTL. Therefore, the separated catalyst particles will not effectively promote the PEMWE electrochemical reaction, resulting in poor catalyst utilization. Furthermore, the electrically disconnected catalyst layer / patches will lead to a significantly higher overall ohmic resistance in the PEMWE, with a relatively higher required PEMWE power and thus reduced efficiency.

[0004] Electrochimica Acta 316 (2019) 43-51 describes improving the performance of proton exchange membrane electrolyzer cells by introducing in-plane transport enhancement layers (PTLs). PTLs were implemented as perforated plates with through-holes formed on a thin titanium plate. These bilayers of PTLs were used in conjunction with a layer with larger pores (830 μm) stacked on top of a layer with smaller pore size (100 μm) to improve mass transfer. However, no changes in kinetics or catalyst utilization were reported. The transport enhancement is claimed to be due to up to a moderate current density (2 Amps / cm²). 2The mass transfer of the catalyst material beneath the pores is primarily in the direction perpendicular to the plane of the PTL, thus reducing ohmic resistance. While the catalyst material below the pores will experience enhanced mass transfer, the catalyst material beneath the PTL substrate relies on in-plane mass transfer, which is not ideal for catalysts in a CL with this design. Therefore, it is conceivable that at higher current densities, where mass transfer resistance also becomes dominant, these regions of the CL will be deprived of reactants, resulting in poor catalyst utilization. On the other hand, with the reduced catalyst loading and the presence of an inhomogeneous CL, the catalyst material beneath the pores is electrically disconnected from the PTL and therefore cannot effectively participate in the electrochemical reaction. The latter also leads to poor catalyst utilization.

[0005] Therefore, the aim is to reduce the high total ohmic and mass transfer resistance across components to minimize the electrical power required to operate PEMWE, while improving catalyst utilization and kinetics. With better utilization of catalyst materials, the use of ultra-low-loaded catalyst materials becomes feasible, which could further reduce the cost of PEMWE and improve the prospects for its widespread adoption in clean energy technologies. Invention Overview

[0007] The invention aims to achieve its objective through a proton exchange membrane-based electrolyzer, comprising an anode portion, a cathode portion, and a proton exchange membrane; the anode portion is disposed on a first surface side of the membrane, and the cathode portion is disposed on a second opposing surface side of the membrane; the anode portion includes an anode catalyst layer and an anode porous transport layer; the anode catalyst layer is disposed between the anode porous transport layer and the first surface side; the cathode portion includes a cathode catalyst layer and a cathode porous transport layer; the cathode catalyst layer is disposed between the cathode porous transport layer and the second surface side; wherein the electrolyzer includes a conductive first mesh foil and / or a conductive second mesh foil, the conductive first mesh foil being stacked on the anode catalyst layer such that the surface of the mesh foil covers the surface of the anode catalyst layer in a first coverage area, and a first conductive interface is provided between the mesh foil and the anode catalyst layer in the first coverage area; the conductive second mesh foil being stacked on the cathode catalyst layer such that the surface of the mesh foil covers the surface of the cathode catalyst layer in a second coverage area, and a second conductive interface is provided between the mesh foil and the cathode catalyst layer in the second coverage area. The corresponding mesh foil is arranged in one of four ways. First, the mesh can be arranged between the anode catalyst layer and the proton exchange membrane. Second, the mesh can be arranged between the cathode catalyst layer and the proton exchange membrane. Third, the mesh can be arranged between the anode catalyst layer and the porous transport layer. Fourth, the mesh can be arranged between the cathode catalyst layer and the porous transport layer.

[0008] Advantageously, the conductive first and / or second mesh foil provides lateral (in-plane) shunts to the associated catalyst layer. In a relatively thin catalyst layer, the catalyst layer can become discontinuous, where regions of the catalyst layer may not be electrically connected to each other. The conductive mesh foil attached to the catalyst layer provides conductive shunts that create electrical connections between regions within the catalyst layer. As a result, any disconnected regions that did not contribute to electrolysis are now electrically connected and become effective. Furthermore, the ohmic resistance is reduced, which in turn reduces the electrical energy required to drive the electrolyzer.

[0009] The present invention also relates to a method for manufacturing such a proton exchange membrane-based electrolyzer, the electrolyzer comprising an anode portion, a cathode portion, and a proton exchange membrane, the anode portion being disposed on a first surface side of the membrane, and the cathode portion being disposed on a second opposing surface side of the membrane; the method comprising: providing an anode catalyst layer and an anode porous transport layer in the anode portion, while disposing the anode catalyst layer between the anode porous transport layer and the first surface side; providing a cathode catalyst layer and a cathode porous transport layer in the cathode portion, while disposing a cathode catalyst layer between the cathode porous transport layer and the second surface side, wherein the method further comprises: providing a conductive first mesh foil on a side of the anode portion, and stacking the conductive first mesh foil on the anode catalyst layer to form A first overlap between the surface of the mesh foil and the surface of the anode catalyst layer, with a first conductive interface between the mesh foil and the anode catalyst layer across the first overlap, wherein the conductive first mesh foil is disposed between the anode catalyst layer and the proton exchange membrane or between the anode catalyst layer and the porous transport layer, and / or a conductive second mesh foil is provided on the side of the cathode portion, and the conductive second mesh foil is stacked on the cathode catalyst layer such that a second overlap is formed between the surface of the mesh foil and the surface of the cathode catalyst layer, with a second conductive interface between the mesh foil and the cathode catalyst layer across the second overlap, wherein the conductive second mesh foil is disposed between the cathode catalyst layer and the proton exchange membrane or between the cathode catalyst layer and the porous transport layer.

[0010] The advantageous implementation is further defined by the dependent claims. Attached Figure Description

[0011] The invention will now be explained in more detail with reference to the accompanying drawings, in which exemplary embodiments of the invention are illustrated. The drawings are for illustrative purposes only and are not intended to limit the scope of the invention, which encompasses all variations, equivalents, and substitutions falling within its scope. The scope of the invention is defined only by the definitions given in the appended claims.

[0012] Figure 1 An exploded view of a proton exchange membrane-based electrolyzer according to an embodiment of the present invention is shown schematically.

[0013] Figure 2 A schematic plan view of a conductive mesh foil for a proton exchange membrane-based electrolyzer according to an embodiment of the present invention is shown.

[0014] Figure 3A 3B schematically illustrates the arrangement of layers in a proton exchange membrane-based electrolyzer according to an embodiment of the present invention;

[0015] Figure 4 Experimental polarization curves of a proton exchange membrane-based electrolyzer according to one embodiment and a proton exchange membrane-based electrolyzer according to the prior art are shown; and

[0016] Figure 5 Experimental electrochemical impedance spectroscopy (EIS) spectra of a proton exchange membrane-based electrolyzer according to an embodiment and a proton exchange membrane-based electrolyzer according to the prior art are shown.

[0017] Description of the implementation plan

[0018] In an electrolyzer, a splitting reaction occurs, where molecules such as water undergo a splitting reaction. The splitting reaction consists of two half-reactions: one half-reaction occurs at the cathode electrode, where electrons are supplied (added) from the cathode, and the other half-reaction occurs at the anode electrode, where electrons are removed from the anode.

[0019] As an example, for the electrolysis of water, in an acidic environment, the anodic half-reaction is given as follows:

[0020] 2H₂O(l)→O₂(g)+4H + (aq)+4e - (eq.1)

[0021] l: liquid, g: gas; aq: in aqueous solution, and e - :electronic

[0022] The cathode half-reaction is given below:

[0023] 2H + (aq)+2e - →H2(g)(eq.2)

[0024] The overall reaction is given below:

[0025] 2H₂O(l)→O₂(g)+2H₂(g) (eq. 3)

[0026] According to the reactions (eq.1 to eq.3), oxygen is produced at the anode of the electrolyzer, hydrogen is produced at the cathode of the electrolyzer, and protons (H) are produced simultaneously. + It is transported from the anode to the cathode.

[0027] Figure 1An exploded view of a proton exchange membrane-based electrolyzer 1 according to an embodiment of the present invention is shown schematically.

[0028] The proton exchange membrane-based electrolyzer 1 is a stacked structure, comprising an anode portion 20, a cathode portion 40, a proton exchange membrane 30, a first bipolar plate 10, and a second bipolar plate 50. The anode portion 20, the cathode portion 40, and the proton exchange membrane 30 are arranged between the first bipolar plate 10 and the second bipolar plate 50.

[0029] The proton exchange membrane 30 is the central part of the electrolyzer, which allows protons (H+) to pass through. + It flows from the anode section (i.e., the volume where the anodic reaction occurs) to the cathode section (the volume where the cathodic reaction occurs).

[0030] The anode portion 20 is arranged between the first bipolar plate 10 and the first membrane surface 31 of the proton exchange membrane 30.

[0031] The cathode portion 40 is disposed between the second membrane surface 32, which is opposite to the first surface of the proton exchange membrane 30, and the second bipolar plate 50.

[0032] The first bipolar plate has an inlet 12 for water and an outlet 13 for oxygen and unreacted water at its outer surface 11. A channel structure 15 is provided at the inner surface 14 of the first bipolar plate 10 for conveying water to the anode portion 20 and outputting oxygen from the anode portion 20.

[0033] The second bipolar plate 50 has an outlet 53 for hydrogen gas at its outer surface 51. A second channel structure (not shown) is provided at the inner surface 52 of the second bipolar plate 50 for supplying hydrogen gas from the cathode portion. It should be understood that in some embodiments, the cathode 50 may also have a water inlet (not shown here).

[0034] The anode portion 20 includes a stack of an anode porous transport layer 22, an anode catalyst layer 24, and a conductive first mesh foil 26, wherein the anode porous transport layer 22 is disposed between the first bipolar plate 10 adjacent to the first channel structure 15 and the combination of the first mesh foil 26 and the anode catalyst layer 24. The combination of the first mesh foil 26 and the anode catalyst layer 24 is adjacent on the first membrane surface 31 of the proton exchange membrane 30. The anode catalyst layer 24 and the anode porous transport layer 22 may be parallel to each other or substantially parallel to each other.

[0035] Similarly, the cathode portion 40 includes a stack of a cathode porous transport layer 42, a cathode catalyst layer 44, and a conductive second mesh foil 46, wherein the cathode porous transport layer 42 is disposed between the second bipolar plate 50 adjacent to the second channel structure 54 and the combination of the second mesh foil 46 and the cathode catalyst layer 44. The combination of the second mesh foil 46 and the cathode catalyst layer 44 is adjacent on the second membrane surface 32 of the proton exchange membrane 30. The cathode catalyst layer 44 and the cathode porous transport layer 42 may be parallel to each other or substantially parallel to each other.

[0036] According to one embodiment, a conductive first mesh foil 26 is stacked on an anode catalyst layer 24, which creates a first coverage area in which the surface of the first mesh foil covers and contacts the surface of the anode catalyst layer. In this way, the first mesh foil provides lateral current shunting between regions of the anode catalyst layer, which, during use of the electrolyzer 1, can supply current to all shunted regions of the anode catalyst layer (moving electrons to an external current source, not shown here). Through lateral current shunting, breaks / interruptions in the anode catalyst layer between regions are connected, and the effective area of ​​the anode catalyst layer is increased.

[0037] Similarly, according to one embodiment, a conductive second mesh foil 46 is stacked on the cathode catalyst layer 44, creating a second coverage area in which the surface of the second mesh foil covers and contacts the surface of the cathode catalyst layer. Likewise, the second mesh foil provides lateral current shunting between regions of the cathode catalyst layer, which can supply current to all shunted regions of the cathode catalyst layer during use of the electrolyzer 1. The effective active area of ​​the cathode catalyst layer increases in the same manner as that of the anode catalyst layer explained above.

[0038] refer to Figure 3A and 3B The arrangement of the conductive mesh foils 26 and 46 is further discussed, as well as the associated catalyst layers 24 and 44 between the porous transport layers 22 and 42 and the proton exchange membrane 30.

[0039] Figure 2 A schematic plan view of a conductive mesh foil for use in a proton exchange membrane-based electrolyzer according to an embodiment of the present invention is shown. The conductive mesh foil shown can be used with both a cathode catalyst layer and an anode catalyst layer.

[0040] Foil 26; 46 is a conductive foil, typically made of metals selected from gold (Au), silver (Ag), chromium (Cr), niobium (Nb), zirconium (Zr), tantalum (Ta), vanadium (V), hafnium (Hf), and is usually a valve metal. Additionally, the metal can be selected from the platinum group (ruthenium, rhodium, palladium, osmium, iridium, and platinum).

[0041] Alternatively, the foil can be made of conductive compounds selected from the group consisting of conductive oxides, nitrides, borides, and carbides, including titanium nitride (TiN), niobium nitride (NbN), titanium carbide (TiC), tungsten carbide (WC), and titanium diboride (TiB2). Furthermore, the foil can be made from low-cost base materials, such as stainless steel (SS), and coated with one or more valve metals and their derivatives.

[0042] It should be understood that the foil can also be made of other metals or metal compounds that are compatible with the electrolysis process.

[0043] According to one implementation, the surface of the foil can be additionally configured or be capable of conducting protons.

[0044] According to one implementation scheme, the foil has the following characteristics: Figure 2 The layout is shown schematically in the diagram. Figure 2 As an example, a two-dimensional mesh array with orthogonal mesh distribution is shown.

[0045] The foil 26; 46 is a foil having a mesh formed by a plurality of mesh openings 61 with spacings 62 between the openings. The mesh openings are preferably arranged in an array such that both the openings and the spacing are aligned. Such an array is, for example, a two-dimensional array of mesh openings with a size of 1-30 μm and a density of approximately 500-3000 rows / inch (196 rows / cm-1181 rows / cm) of spacing 62. By using this relatively small spacing, a foil covering is achieved on the catalyst layer, bridging any interruptions / discontinuities in the catalyst layer of comparable or larger size, and correspondingly increasing the effective active area of ​​the catalyst layer.

[0046] According to another embodiment, the foil 26; 46 is provided with mesh openings 61 of about 0.5 to about 30 μm, preferably about 1 to about 30 μm, more preferably about 1 to about 20 μm, even more preferably about 5 to about 10 μm, or about 0.5 to about 10 μm. The width of the row 62 of the foil 26; 46 between adjacent mesh openings 61 can be about 1 to about 10 μm. The distance between any two adjacent mesh openings in the foil can be about 1 to about 10 μm.

[0047] According to one embodiment, the thickness of the foil 26;46 is about 50 nm to about 25 μm, and preferably 1 to 3 μm.

[0048] In one embodiment, the holes are distributed along two orthogonal directions, each with 1000 rows / inch (392 rows / cm), each hole having a width of approximately 18 μm and a row spacing of approximately 7 μm (row width 62).

[0049] In an alternative implementation, the holes are distributed along two orthogonal directions, with 2000 rows / inch (788 rows / cm), each opening having a width of approximately 8 μm 64, and the row spacing (row width 62) being approximately 5 μm.

[0050] Figure 3A 3B schematically illustrates the arrangement of layers in a proton exchange membrane-based electrolyzer according to an embodiment of the present invention.

[0051] Alternatively, the mesh foil and the catalyst layer 24; 44 between the porous transport layer 22; 42 and the proton exchange membrane 30 can be implemented. The electrolyzer may include one, two, three, or four mesh foils. One or two of the mesh foils 26; 46 can be arranged between the porous transport layer 22; 42 and the catalyst layer 24; 44. In this case, the catalyst layer 24; 44 can be directly disposed on the surface of the proton exchange membrane 30. One or two of the mesh foils 26; 46 can be disposed between the catalyst layer 24; 44 and the porous transport layer 22. In this case, one or two mesh foils 26; 46 can be directly disposed on the surface of the proton exchange membrane 30.

[0052] like Figure 3A As shown, the mesh foil 26; 46 is disposed between the porous transport layer 22; 42 and the catalyst layer 24; 44. The catalyst layer 24; 44 is disposed directly on the surface of the proton exchange membrane 30.

[0053] Figure 3B The schematic diagram shows an optional arrangement in which the foil 26; 46 is directly disposed on the surface of the proton exchange membrane 30, and the catalyst layer 24; 44 is disposed between the porous transport layer 22; 42 and the foil 26; 46.

[0054] like Figure 3A The illustrated structure has an additional advantage: the mesh structure, composed of thin metal foil, exhibits relatively high flexibility, where the foil material has less stiffness than the PTL material; in other words, the foil is more flexible and ductile than the PTL. Due to this difference in flexibility, the mesh can conform to the roughness of the PTL, thereby increasing the size and number of contact points. This, in turn, leads to a further reduction in contact resistance and ohmic losses, while simultaneously improving the overall PEMWE efficiency. Furthermore, the mesh 26;46 between the porous transport layers 22;42 and the catalyst layers 24;44 forms a protective layer on the membrane 30.

[0055] Figure 3B The configuration shown has the additional advantage that it can be produced using ultrathin films (<50 micrometers) to reduce the overall ohmic resistance in PEMWE cells and significantly improve efficiency.

[0056] The arrangement of the mesh and catalyst layer on the cathode side can be the same as that on the anode side: either the catalyst layer is directly on the proton exchange membrane, or the mesh is directly on the proton exchange membrane. It is also conceivable that the arrangement of the mesh and catalyst layer on the cathode side can be the opposite of that on the anode side.

[0057] Note that in another embodiment, the catalyst layer on the cathode side and / or anode side is sandwiched between two parallel mesh foils. One of the mesh foils is disposed directly on the proton exchange membrane, while the other of the two mesh foils is between the catalyst layer and the porous transport layer.

[0058] In some embodiments, the foil has a higher electronic conductivity value than the adjacent catalyst layer, for example, at least about 25% higher.

[0059] Figure 4 Experimental polarization curves of water electrolysis performed using a proton exchange membrane-based electrolyzer according to one embodiment and a proton exchange membrane-based electrolyzer according to the prior art are shown.

[0060] The proton exchange membrane-based electrolyzer according to an embodiment of the present invention is equipped with a gold mesh (one on the cathode and one on the anode) with 1000 rows per inch (392 rows / cm), and the mesh openings have a width of 18 μm and a linewidth of 7 μm. The active area of ​​the proton exchange membrane-based electrolyzer is 10 cm². 2 Iridium was used as the anode (2.5 mg / cm²). 2 Platinum was used as the cathode (0.5 mg / cm). 2 The proton exchange membrane is made of 'Nafion 117'.

[0061] BekaertTi fabric was used as the porous transport layer.

[0062] Existing proton exchange membrane-based electrolyzers have the same active area and the same areal density of the anode and cathode. The membrane is also made of 'Nafion 117'. The same porous transport layer Ti fabric is used.

[0063] Water with a neutral pH is used as the source. The electrolysis reaction is carried out at 60°C in each electrolyzer.

[0064] exist Figure 4 In the diagram, the polarization curve shows the potential difference between the cathode and anode as a function of current density (i.e., current divided by electrode area). The polarization curve 70 of a prior art electrolyzer cell is represented by a line carrying a cross. The polarization curve 72 of the proton exchange membrane-based electrolyzer cell according to the present invention is represented by a line carrying a circle.

[0065] It can be seen that the polarization curve 70 of the prior art electrolyzer battery is higher than the polarization curve 72 of the proton exchange membrane-based electrolyzer battery according to the present invention: at the same current density, the potential difference between the cathode and anode of the prior art electrolyzer is greater. For the battery equipped with a mesh foil, the potential U (volts) required to generate a specific current density (corresponding to the hydrogen production rate) is lower than that of the prior art battery. This, in turn, means lower power consumption and higher efficiency.

[0066] Figure 5 Experimental electrochemical impedance spectroscopy (EIS) plots for water electrolysis using a proton exchange membrane-based electrolyzer according to an embodiment and a proton exchange membrane-based electrolyzer according to the prior art are shown.

[0067] exist Figure 5 In the diagram, the EIS curve shows the electrical impedance of the corresponding electrolyzer cell in a complex plane. The EIS curve 80 of a prior art electrolyzer cell is represented by a line carrying a cross. The EIS curve 82 of the proton exchange membrane-based electrolyzer according to the present invention is represented by a line carrying a circle.

[0068] EIS measurements are in accordance with the above references. Figure 4 The experiment was conducted under the same conditions described.

[0069] exist Figure 5 In the figure, the intercept of the real part Re(z) axis at high frequencies (indicated by arrows 84 and 86) represents the "high-frequency resistance," which needs to be minimized to obtain better conductivity and efficiency. As shown, at a battery temperature of 60°C and 1.7V, the electrolyzer according to the invention has an HFR of 0.024 ohms (arrow 84), while the prior art electrolyzer has an HFR of 0.0276 ohms (arrow 86). Furthermore, when using the grid according to the invention, the low-frequency resistance (LFR) decreases from 0.033 ohms (arrow 87) to 0.0285 ohms (arrow 88).

[0070] Although electrolysis methods related to water separation have been mentioned in the preceding description, electrolysis and electrolyzers are not limited to water separation methods, but can also be used in connection with various electrochemical methods known to those skilled in the art, such as carbon dioxide (CO2) reduction, ammonia (NH3) generation, and hydrogen peroxide (H2O2) generation.

[0071] Furthermore, it should be noted that the experimental data of the electrolyzer according to the above embodiments are merely examples for illustrating the present invention.

[0072] The invention may be practiced in other specific forms without departing from its essential characteristics. The described embodiments are to be considered merely illustrative in all respects and not as limiting of the concept of the invention. Therefore, the scope of the invention is indicated by the appended claims rather than the foregoing description. It will be apparent to those skilled in the art that alternative and equivalent embodiments of the invention can be conceived and simplified into practice. Furthermore, many modifications can be made to adapt the specific structure or materials of the electrolyzer to the teachings of the invention without departing from its essential scope.

[0073] All modifications within the meaning and scope of the equivalents of the claims are included within their scope.

Claims

1. An electrolyzer based on a proton exchange membrane, comprising an anode section, a cathode section, and a proton exchange membrane; An anode portion disposed on the first surface side of the membrane and a cathode portion disposed on the second opposing surface side of the membrane; The anode portion includes an anode catalyst layer and an anode porous transport layer; the anode catalyst layer is disposed between the anode porous transport layer and the first surface side. The cathode portion includes a cathode catalyst layer and a cathode porous transport layer; the cathode catalyst layer is disposed between the cathode porous transport layer and the second opposing surface side. The electrolyzer comprises a conductive first foil and / or a conductive second foil. The conductive first mesh foil is stacked on the anode catalyst layer such that the surface of the mesh foil covers the surface of the anode catalyst layer in the first covered area, and a first conductive interface is provided between the mesh foil and the anode catalyst layer in the first covered area; The conductive second foil is stacked on the cathode catalyst layer such that the surface of the foil covers the surface of the cathode catalyst layer in the second covered region, and a second conductive interface is provided between the foil and the cathode catalyst layer in the second covered region. The corresponding mesh foil is disposed between the anode catalyst layer and the proton exchange membrane or between the cathode catalyst layer and the proton exchange membrane, or The corresponding mesh foil is disposed between the anode catalyst layer and the porous transport layer or between the cathode catalyst layer and the porous transport layer.

2. The proton exchange membrane-based electrolyzer according to claim 1, wherein the corresponding foil is provided with meshes arranged in a two-dimensional array, with a gap between each adjacent mesh.

3. The proton exchange membrane-based electrolyzer according to claim 1 or claim 2, wherein the corresponding foil is provided with mesh openings of 0.5-20 μm.

4. The proton exchange membrane-based electrolyzer according to claim 1 or claim 2, wherein the corresponding foil is provided with mesh openings of 0.5-10 μm.

5. The proton exchange membrane-based electrolyzer according to claim 2, wherein in the respective foil, the mesh spacing has a density of 500-3000 rows / inch and 196 rows / cm-1181 rows / cm.

6. The proton exchange membrane-based electrolyzer according to claim 5, wherein the width of the line between adjacent mesh openings of the corresponding foil is 0.5-10 μm.

7. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the corresponding mesh foil is capable of proton transport along the conductive interface.

8. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the corresponding foil comprises at least one layer of conductive material; The conductive material is selected from: A group of metals including gold, silver, chromium, niobium, zirconium, tantalum, hafnium and vanadium, and valve metals, or Metals from the platinum group, or A group of carbides, nitrides and borides of transition metals or mixtures / layers thereof.

9. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the mesh foil has a relatively higher electronic conductivity than the porous transport layer.

10. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the stiffness of the foil material is less than the stiffness of the PTL material.

11. The proton exchange membrane-based electrolyzer of claim 8, wherein the corresponding foil further comprises a substrate material layer, the substrate material being conductive or non-conductive, and the at least one conductive material layer is disposed on the surface of the substrate material layer.

12. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the respective foil further comprises a substrate material layer, the substrate material being conductive or non-conductive, and the substrate material layer being covered on each of its surfaces by the conductive material layer.

13. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the corresponding mesh foil is configured to laterally shunt the catalyst layer on which the mesh foil is disposed.

14. The proton exchange membrane-based electrolyzer according to claim 1 or 2, wherein the corresponding mesh foil has a thickness of 50 nm to 25 μm, more typically 1 to 10 μm.

15. A method for manufacturing a proton exchange membrane-based electrolyzer, the electrolyzer comprising an anode portion, a cathode portion and a proton exchange membrane, the anode portion being disposed on a first surface side of the membrane and the cathode portion being disposed on a second opposing surface side of the membrane; The method includes: An anode catalyst layer and an anode porous transport layer are provided in the anode portion, and the anode catalyst layer is disposed between the anode porous transport layer and the first surface side; A cathode catalyst layer and a cathode porous transport layer are provided in the cathode portion, and the cathode catalyst layer is disposed between the cathode porous transport layer and the second opposing surface side. The method further includes: A conductive first mesh foil is provided on the side of the anode portion, and the conductive first mesh foil is stacked on the anode catalyst layer such that there is a first overlap between the surface of the mesh foil and the surface of the anode catalyst layer, and a first conductive interface between the mesh foil and the anode catalyst layer is formed across the first overlap, wherein the conductive first mesh foil is disposed between the anode catalyst layer and the proton exchange membrane or between the anode catalyst layer and the porous transport layer, and / or A conductive second mesh foil is provided on the side of the cathode portion, and the conductive second mesh foil is stacked on the cathode catalyst layer such that a second overlap is formed between the surface of the mesh foil and the surface of the cathode catalyst layer, and a second conductive interface is formed between the mesh foil and the cathode catalyst layer across the second overlap. The conductive second mesh foil is disposed between the cathode catalyst layer and the proton exchange membrane or between the cathode catalyst layer and the porous transport layer.

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