CN118292007A - Alkaline electrolytic tank structure - Google Patents
Alkaline electrolytic tank structure Download PDFInfo
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- CN118292007A CN118292007A CN202410307769.1A CN202410307769A CN118292007A CN 118292007 A CN118292007 A CN 118292007A CN 202410307769 A CN202410307769 A CN 202410307769A CN 118292007 A CN118292007 A CN 118292007A
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- 239000003054 catalyst Substances 0.000 claims abstract description 60
- 239000012528 membrane Substances 0.000 claims abstract description 47
- 239000011148 porous material Substances 0.000 claims abstract description 23
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 118
- 229910052759 nickel Inorganic materials 0.000 claims description 56
- 238000005868 electrolysis reaction Methods 0.000 claims description 27
- 230000007704 transition Effects 0.000 claims description 19
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- 239000010935 stainless steel Substances 0.000 claims description 9
- 229910001220 stainless steel Inorganic materials 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 229910003460 diamond Inorganic materials 0.000 claims description 8
- 229920002492 poly(sulfone) Polymers 0.000 claims description 7
- -1 polytetrafluoroethylene Polymers 0.000 claims description 7
- 229910000990 Ni alloy Inorganic materials 0.000 claims description 6
- 239000004696 Poly ether ether ketone Substances 0.000 claims description 6
- 239000004734 Polyphenylene sulfide Substances 0.000 claims description 6
- 229910000831 Steel Inorganic materials 0.000 claims description 6
- 229920002530 polyetherether ketone Polymers 0.000 claims description 6
- 229920000069 polyphenylene sulfide Polymers 0.000 claims description 6
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- 150000002739 metals Chemical group 0.000 claims description 4
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- 239000004695 Polyether sulfone Substances 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- UQSQSQZYBQSBJZ-UHFFFAOYSA-N fluorosulfonic acid Chemical compound OS(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-N 0.000 claims description 3
- 229910044991 metal oxide Inorganic materials 0.000 claims description 3
- 150000004706 metal oxides Chemical class 0.000 claims description 3
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- 229920006393 polyether sulfone Polymers 0.000 claims description 3
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- 239000004800 polyvinyl chloride Substances 0.000 claims description 3
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 3
- 229920000181 Ethylene propylene rubber Polymers 0.000 claims description 2
- 230000005540 biological transmission Effects 0.000 abstract description 9
- 230000010354 integration Effects 0.000 abstract description 4
- 210000004027 cell Anatomy 0.000 description 39
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- 239000003513 alkali Substances 0.000 description 8
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- 229910000564 Raney nickel Inorganic materials 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910001030 Iron–nickel alloy Inorganic materials 0.000 description 1
- 239000007868 Raney catalyst Substances 0.000 description 1
- NPXOKRUENSOPAO-UHFFFAOYSA-N Raney nickel Chemical compound [Al].[Ni] NPXOKRUENSOPAO-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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- DMTIXTXDJGWVCO-UHFFFAOYSA-N iron(2+) nickel(2+) oxygen(2-) Chemical compound [O--].[O--].[Fe++].[Ni++] DMTIXTXDJGWVCO-UHFFFAOYSA-N 0.000 description 1
- 210000001595 mastoid Anatomy 0.000 description 1
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Abstract
The invention discloses an alkaline electrolytic tank structure, which comprises an electrolytic unit and a polar frame arranged around the electrolytic unit, wherein the electrolytic unit comprises an electrolytic cell, and the electrolytic cell comprises a bipolar plate, an anode porous layer, a membrane electrode, a cathode porous layer and a bipolar plate which are sequentially stacked; the membrane electrode comprises a porous membrane, and an anode catalyst layer and a cathode catalyst layer which are respectively supported on the two side surfaces of the membrane; the anode porous layer or the cathode porous layer comprises at least two layers of stacked structures with different opening pore diameters, and the opening pore diameters gradually decrease towards the direction of the membrane electrode. The invention realizes the integration of the electrode and the membrane, greatly reduces the ion transmission resistance between the cathode and the anode, and reduces the internal resistance.
Description
Technical Field
The invention relates to the technical field of electrolytic devices, in particular to an alkaline electrolytic tank structure.
Background
At present, three electrolytic tanks are generally used for producing hydrogen by pure water electrolysis, namely an alkaline electrolytic tank, a solid oxide electrolytic tank and a polymer electrolytic tank, wherein the alkaline electrolytic tank is the electrolytic tank with the longest development time and the most mature technology, and has the characteristics of simple operation and low cost.
The alkaline electrolytic tank in the prior art generally adopts a bipolar plate and a polar frame which are plated with nickel by carbon steel, then uses a nickel catalyst thermally sprayed on a metal nickel net as an electrode, and separates the positive electrode from the negative electrode by a porous diaphragm, but has two problems: 1) Gaps exist between the electrodes and the diaphragm all the time, so that the hydroxyl transmission distance is long, and the ion resistance is large; 2) The whole frame has large weight and large hot melting, so that the assembly and installation processes of the electrolytic tank are laborious, and the temperature response speed is low.
Disclosure of Invention
In order to solve the defects in the prior art, the main purpose of the invention is to provide an alkaline electrolytic tank structure, which realizes the integration of electrodes and membranes, greatly reduces the ion transmission resistance between the anode and the cathode and reduces the internal resistance.
In order to achieve the above object, the present invention provides an alkaline electrolytic cell structure, comprising an electrolytic unit and a polar frame arranged around the electrolytic unit, wherein the electrolytic unit comprises an electrolytic cell, and the electrolytic cell comprises a bipolar plate, an anode porous layer, a membrane electrode, a cathode porous layer and a bipolar plate which are stacked in sequence;
The membrane electrode comprises a diaphragm, and an anode catalyst layer and a cathode catalyst layer which are respectively supported on the two side surfaces of the diaphragm; the membrane is a porous membrane, the anode porous layer and/or the cathode porous layer comprises at least two layers of stacked structures with different pore diameters, and the pore diameters gradually decrease towards the direction of the membrane electrode.
In the invention, near the anode catalyst layer or the cathode catalyst layer, the pore diameter of the open pores is smaller, the compact structure is favorable for electric contact, the interface conductivity is improved, and then the pore diameter of the open pores is increased towards the direction of the bipolar plate, so that bubbles generated on the surface of the anode catalyst layer or the cathode catalyst layer and combined bubbles are discharged from the open pores.
Further, the anode porous layer and/or the cathode porous layer comprises a three-layer stacked structure with different opening diameters, and a flow field net layer, a transition mesh layer and a microporous layer are sequentially arranged towards the direction of the membrane electrode.
Further, the aperture size of the flow field mesh layer is 0.2-10mm, preferably 0.5-1mm, and the thickness is 0.5-5mm, preferably 1-3mm.
Further, the mesh number of the openings of the transition mesh layer is 50-400, preferably 100-300 mesh, and the thickness is 0.1-0.5mm, preferably 0.2-0.3mm.
Further, the microporous layer has a porosity of 50 to 80%, preferably 60 to 70%, and a thickness of 0.1 to 0.5mm, preferably 0.2 to 0.3mm.
Further, the flow field mesh layer or the transition mesh layer is selected from nickel mesh, nickel alloy mesh, steel mesh with Kong Nieban, nickel plating, nickel plated perforated steel plate, or stainless steel mesh, perforated stainless steel plate.
Further, the microporous layer is selected from nickel felt, punched nickel plate, woven nickel mesh, porous nickel or carbon paper, preferably punched nickel plate.
Further, the flow field net layer is a diamond punching stretching net, an included angle exists between the plane where the diamond holes are located and the plane where the bipolar plate is located, and the included angle ranges from 10 degrees to 60 degrees, preferably from 30 degrees to 45 degrees.
Further, the transition net layer is a plain weave net.
Further, the punching body of the microporous layer is round, square or diamond, the punched edge is preferably in a sawtooth structure, the punching diameter is in the range of 50-1000 μm, preferably 300-500 μm when cathode hydrogen is separated out, and the punching diameter is in the range of 100-2000 μm, preferably 500-800 μm, and the sawtooth depth is 10-30 μm, preferably 15-25 μm when anode hydrogen is separated out.
Further, the punched holes of the microporous layer are arranged in an array, and are square or hexagonal, preferably hexagonal.
Further, the porous membrane is made of one or more selected from polyethersulfone, polysulfone, polyphenylene sulfide, polytetrafluoroethylene, polyvinylidene fluoride, polyvinyl chloride and non-woven fabric.
Further, the thickness of the anode catalyst layer or the cathode catalyst layer is 1 to 200 micrometers, preferably 30 to 50 micrometers.
Further, the anode catalyst layer or the cathode catalyst layer comprises an anode or a cathode catalyst, and a binder, wherein the anode catalyst is selected from one or more of metals including nickel element and platinum element and metal oxides including nickel element and platinum element; the cathode catalyst is selected from metals including nickel element and platinum element; the binder is selected from one or more of perfluorosulfonic acid resin, polyether-ether-ketone and polyacrylonitrile.
Further, the bipolar plate is a nickel plate, a nickel alloy plate, a stainless steel plate or a nickel plated plate, and the thickness is 0.1mm-2mm, preferably 0.5-1mm. The bipolar plate may be a flat plate or a plate with flow channels after stamping or etching.
Further, the cathode electrode frame and the anode electrode frame are provided with sealing gaskets, the sealing gaskets are made of fluoroethylene, ethylene propylene rubber and the like, and the thickness of the sealing gaskets is 0.1-1mm, preferably 0.2-0.5mm.
Further, the side opening of the polar frame is used for circulating alkali liquor, and the alkali liquor enters the electrolysis cell.
Further, the pole frame is made of resin, preferably, the resin is selected from polysulfone or polyether ether ketone.
Compared with the prior art, the invention has the following advantages:
The invention directly coats the anode catalyst or the cathode catalyst of the electrode reaction on the two sides of the diaphragm to form a coating, realizes the integration of the electrode and the membrane, and obtains the membrane electrode, thereby greatly reducing the ion transmission resistance between the cathode and the anode, reducing the internal resistance and improving the current density and the electrolysis performance. In addition, the anode porous layer or the cathode porous layer with at least two layers of stacked structures with different opening diameters is arranged in the area between the bipolar plate and the membrane electrode, so that the interface electron transmission enhancement and bubble transport of the catalytic layer can be smoother, and the interface resistance and the diffusion resistance can be reduced.
In addition, the invention can adopt the resin pole frame as the main body of the electrolytic tank, and has the advantages of light weight, small hot melting, high temperature response speed and the like.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic view of an alkaline cell structure according to the present invention.
Reference numerals illustrate: the electrode comprises electrode frames 1A and 1B, a bipolar plate 2, a diaphragm 3, an anode catalyst layer 4, a cathode catalyst 5, a flow field net layer 6, a transition mesh 7, a microporous layer 8 and a sealing gasket 9.
Detailed Description
The following describes specific embodiments of the present invention in detail. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit 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 the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. Wherein the terms "first position" and "second position" are two different positions.
Unless specifically stated or limited otherwise, the terms "mounted," "connected," and "fixed" are to be construed broadly, and may be, for example, either fixed or removable; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The invention provides an alkaline electrolytic tank structure, which comprises an electrolytic unit and a polar frame arranged around the electrolytic unit, wherein the electrolytic unit comprises an electrolytic cell, and the electrolytic cell comprises a bipolar plate, an anode porous layer, a membrane electrode, a cathode porous layer and a bipolar plate which are sequentially stacked;
The membrane electrode comprises a diaphragm, and an anode catalyst layer and a cathode catalyst layer which are respectively supported on the two side surfaces of the diaphragm; the membrane is a porous membrane, the anode porous layer or the cathode porous layer comprises at least two layers of stacked structures with different pore diameters, and the pore diameters gradually decrease towards the direction of the membrane electrode.
The membrane electrode in the invention is of an integrated structure of anode catalyst layer-diaphragm-cathode catalyst layer. The membrane electrode takes a porous membrane as a membrane, and anode catalyst layers and cathode catalyst layers are respectively loaded on the surfaces of two sides of the membrane; based on the specific membrane electrode, an electrolysis cell is assembled with the bipolar plate, the anode porous layer and the cathode porous layer, and then an electrolysis tank is assembled.
In the invention, near the anode catalyst layer or the cathode catalyst layer, the pore diameter of the open pores is smaller, the compact structure is beneficial to electric contact, the interface conductivity is improved, and then the pore diameter of the open pores is enlarged towards the direction of the bipolar plate, so that the bubbles generated on the surface of the anode catalyst layer or the cathode catalyst layer are discharged.
In some embodiments, the porous membrane is made of one or more selected from polyethersulfone, polysulfone, polyphenylene sulfide, polytetrafluoroethylene, polyvinylidene fluoride, polyvinyl chloride, and non-woven fabric.
In some embodiments, the anode catalyst layer or the cathode catalyst layer has a thickness of 1-200 micrometers, and the catalyst layer with the thickness range is beneficial to improving the electrode reaction specific surface and reducing the ion transmission distance so as to improve the electrolysis performance; preferably 30-50 microns.
In some embodiments, the anode catalyst layer or the cathode catalyst layer comprises an anode or cathode catalyst, a binder, the anode catalyst selected from one or more of a metal comprising elemental nickel, elemental platinum, and a metal oxide comprising elemental nickel, elemental platinum; the cathode catalyst is selected from metals including nickel element and platinum element; the binder is selected from one or more of perfluorosulfonic acid resin, polyether-ether-ketone and polyacrylonitrile.
In some embodiments, the anode porous layer or the cathode porous layer comprises a three-layer stacked structure with different opening pore diameters, and the three-layer stacked structure sequentially comprises a flow field net layer, a transition mesh layer and a microporous layer towards the direction of the membrane electrode.
Preferably, the aperture size of the flow field mesh layer is 0.2-10mm, preferably 0.5-1mm, and the thickness is 0.5-5mm, preferably 1-3mm.
Preferably, the mesh layer has an open mesh size of 50 to 400, preferably 100 to 300 mesh, and a thickness of 0.1 to 0.5mm, preferably 0.2 to 0.3mm.
Preferably, the microporous layer has a porosity of 50-80%, preferably 60-70%, and a thickness of 0.1-0.5mm, preferably 0.2-0.3mm.
In some embodiments, the flow field mesh layer or transition mesh layer is selected from nickel mesh, nickel alloy mesh, steel mesh with Kong Nieban, nickel plated perforated steel sheet, or from stainless steel mesh, perforated stainless steel sheet.
In some embodiments, the microporous layer is selected from nickel felt, punched nickel plate, woven nickel mesh, porous nickel or carbon paper, which may be porous metal prepared by sintering nickel particles or foam nickel like sponge.
In some embodiments, the flow field net layer is preferably a diamond punching stretching net, on one hand, enough alkali liquor transmission channels can be provided, on the other hand, because an included angle exists between the plane where the diamond holes are positioned and the plane where the bipolar plate is positioned, alkali liquor can be promoted to flow towards the direction of the diaphragm after entering the cavity, and the mass transfer exchange between the alkali liquor and reaction produced gas is enhanced, wherein the included angle ranges from 10 degrees to 60 degrees, preferably from 30 degrees to 45 degrees.
In some embodiments, the transition mesh layer is preferably a plain weave mesh, which has better flow-through and sufficient conductive contact with the flow field mesh layer due to the surface roughness after weaving.
In some embodiments, the open cell body of the microporous layer is circular, square, diamond or other repeatable structure, the punched edge is preferably a saw tooth structure, the punched diameter ranges from 50 μm to 1000 μm, preferably from 300 μm to 500 μm when cathode hydrogen is separated, the punched diameter ranges from 100 μm to 2000 μm, preferably from 500 μm to 800 μm when anode hydrogen is separated, the saw tooth depth is from 10 μm to 30 μm, preferably from 15 μm to 25 μm, the above dimension settings take into account the size of hydrogen bubbles and oxygen bubbles, and the saw tooth edge is favorable for rapid shedding of generated bubbles.
In some embodiments, the punched holes of the microporous layer are arranged according to an array, which can be square or hexagonal, preferably a more compact hexagonal array, and the aperture ratio of the microporous layer is not less than 30%, so that the contact area of the microporous layer and the catalytic layer is ensured to be enough to realize charge transmission, and enough gaps are reserved for air bubbles and alkali liquor transmission.
In some embodiments, the bipolar plate is a nickel plate, a nickel alloy plate, a stainless steel plate or a nickel plated plate, the thickness is 0.1mm-2mm, and the bipolar plate with the thickness range is beneficial to reducing the metal consumption, reducing the volume resistance and improving the performance of thermal response speed; preferably 0.5-1mm.
In some embodiments, the cathode electrode frame comprises a cathode electrode frame B, and the cathode electrode frame B is arranged on the cathode electrode frame B, wherein the cathode electrode frame B is arranged on the anode electrode frame B, and the cathode electrode frame B is arranged on the anode electrode frame B.
Further, the side opening of the polar frame is used for circulating alkali liquor, and the alkali liquor enters the electrolysis cell.
Further, the pole frame is made of resin, preferably, the resin is selected from polysulfone or polyether ether ketone.
In some embodiments, the electrolysis cell of the electrolysis cell comprises more than two of said electrolysis cells, for example two or more, a plurality of electrolysis cells being arranged in a repeated stack, the bipolar plates between adjacent two electrolysis cells being sharable.
The invention also provides a preparation method of the alkaline electrolytic cell, which specifically comprises the following steps: respectively arranging a pole frame around the electrolysis unit, fixing the pole frames, and assembling to obtain the alkaline electrolysis tank; the assembly of the cell of the present invention may be performed by those skilled in the art using conventional assembly operations, which will not be described in detail.
In some embodiments, the step of preparing the membrane electrode in the electrolysis cell comprises: and respectively loading and forming an anode catalyst layer and a cathode catalyst layer on the surfaces of two sides of the diaphragm by a physical vapor deposition method, a transfer printing method, a spray coating method or a pore-forming agent assisted direct coating method to obtain the membrane electrode.
The alkaline cell structure of the present invention will be described in detail by way of examples.
The electrolytic cell performance testing process comprises the following steps:
Introducing 30% KOH solution into inlets of a cathode and an anode, applying different currents to a cathode and an anode after the temperature of an electrolytic cell reaches a set temperature (generally 80 ℃), testing the voltage of the cathode and the anode, and reading the voltage value after running for at least 15 minutes and stabilizing the voltage at each set current and recording as the cell voltage at the current.
Example 1
Referring to fig. 1, in the electrolytic cell of the present embodiment, the bipolar plate-anode porous layer-membrane electrode-cathode porous layer-bipolar plate are assembled into an electrolytic cell in this order, and the electrolytic cell comprises a plurality of the electrolytic cells; and (3) placing and fixing a pole frame A and a pole frame B around the electrolysis unit, assembling the electrolysis unit into an electrolysis tank, enabling an alkaline solution to circulate through the side surface of the pole frame, and enabling the side surface of the alkaline solution to enter an electrolysis cell.
The anode porous layer or the cathode porous layer comprises a three-layer stacked structure with different opening diameters, and is sequentially provided with a flow field net layer, a transition mesh layer and a microporous layer towards the direction of the membrane electrode.
The thickness of the bipolar plate is 1mm, and the bipolar plate is made of nickel;
The thickness of the porous diaphragm is 500 micrometers, the material is a composite of polyphenylene sulfide and zirconium dioxide particles, and the porosity is 60%;
the flow field net layer is a diamond punching stretched nickel net, the thickness is 3mm, the size of the opening is 1mm, and the shape of the opening is a diamond with an included angle of 30 degrees with the bipolar plate surface;
the transition mesh layer is a plain weave nickel screen, the thickness is 0.2mm, and the size of the opening is 100 meshes;
the cathode microporous layer is a punched nickel plate, the thickness is 0.2mm, the porosity is 60%, the punched hole is round with a sawtooth edge, the round diameter is 300 mu m, and the sawtooth depth is 20 mu m;
The anode microporous layer is a punched nickel plate, the thickness is 0.2mm, the porosity is 60%, the punched hole is round with a sawtooth edge, the round diameter is 600 mu m, and the sawtooth depth is 25 mu m;
the punched holes of the cathode microporous layer and the anode microporous layer are arranged according to a hexagonal array;
The thickness of the anode catalyst layer or the cathode catalyst layer is 50 μm;
The anode catalyst is nickel-iron alloy 10mg/cm 2, the cathode catalyst is Raney nickel 10mg/cm 2, and the binder is polytetrafluoroethylene 1mg/cm 2.
The pole frame is made of polysulfone.
In this embodiment, the preparation steps of the membrane electrode include: the catalyst powder with preset loading and the binder are stirred with ethanol, water and isopropanol by ultrasonic to prepare uniform slurry, the solid content is controlled to be more than 50%, the catalytic layers with preset loading are formed on the two sides of the diaphragm by an ultrasonic spraying method, and then the slurry is dried for 12 hours under the vacuum condition of 80 ℃, and then the slurry is hot-pressed for 3 minutes at 140 ℃ and 2MPa, so that the required electrode is obtained.
The electrolytic cell realizes good electrolytic performance through integration, and when the electrolytic voltage is 2.0V at 90 ℃, the cell current density reaches 1.6A/cm 2, the current density is improved by 3 times compared with the conventional electrolytic cell, and the weight is reduced by 50%.
Example 2: the anode adopts nickel-iron oxide catalyst, and the other is unchanged, and the cell current density reaches 2A/cm 2 when the electrolysis voltage is 2.0V at 90 ℃.
Example 3: the polytetrafluoroethylene perfluorinated sulfonic acid resin is used as a binder, the other materials are unchanged, and the cell current density reaches 1.8A/cm 2 at 90 ℃ when the electrolysis voltage is 2.0V.
Example 4: the thickness of the anode catalyst layer or the cathode catalyst layer was 30 μm, and the cell current density reached 1.7A/cm 2 at 90 ℃ when the electrolysis voltage was 2.0V.
Example 5
Similar to example 1, the difference is that:
the thickness of the flow field net layer is 3mm, the material is nickel net, the open pore is square with an included angle of 10 degrees with the bipolar plate surface, and the size of the open pore is 1mm;
The thickness of the transition mesh layer is 0.2mm, the material is plain weave nickel screen, and the size of the opening is 100 meshes;
the thickness of the microporous layer is 0.2mm, the material is nickel felt, and the porosity is 60%;
at 90℃the cell current density reached 1.3A/cm 2 at an electrolysis voltage of 2.0V.
Comparative example 1 (conventional alkaline electrolyzer)
The difference between the present comparative example and the electrolytic cell of example 1 is the structure of the electrolytic cell comprising a bipolar plate, an anode electrode, a separator, a cathode electrode and a bipolar plate stacked in this order. Wherein, bipolar plate, positive electrode, diaphragm, negative electrode and bipolar plate are respectively: the bipolar plate is made of carbon steel nickel plating material, and is stamped with a mastoid flow field with the thickness of 2mm; the carbon steel nickel plating electrode frame with the thickness of 10mm is welded into a whole, a cathode electrode adopts a 60-mesh nickel screen sprayed with Raney nickel catalyst, an anode electrode adopts a 100-mesh nickel screen, a diaphragm is a polyphenylene sulfide fabric film with the thickness of 700 microns, and a sealing gasket is made of polytetrafluoroethylene and has the thickness of 1mm.
The performance data for this comparative example is as follows: at 90℃the cell current density reached 0.4A/cm 2 at an electrolysis voltage of 2.0V.
Comparative example 2
The difference between this comparative example and the cell of example 1 is that: the membrane is a composite membrane of polyphenylene sulfide and zirconium dioxide with the thickness of 500 micrometers, 50 mesh nickel screens sprayed with catalysts are used as electrodes, the nickel screens are fixed on two sides of the membrane through mechanical force, punching nickel plates with the thickness of 2mm are arranged between the electrodes and the bipolar plates, and the size of openings is 0.8mm.
The performance data for this comparative example is as follows: at 90℃the cell current density reached 0.5A/cm 2 at an electrolysis voltage of 2.0V.
In the embodiment 1 of the application, the catalyst is directly coated on two sides of the diaphragm, the reaction interface is larger, while in the comparative example 2, the catalyst is thermally sprayed on the nickel screen, more catalyst cannot be directly contacted with the diaphragm, and a gap exists in the middle, so that the reaction resistance is increased after the electrolyte is filled.
Comparative example 3
The difference from example 1 is that:
The thickness of the flow field net layer is 3mm, the material is nickel net, the opening is diamond-shaped with a 30-degree included angle with the bipolar plate, and the size of the opening is 0.5mm;
The thickness of the transition mesh layer is 0.2mm, the material is a woven nickel screen, and the size of the opening is 200 meshes;
the thickness of the microporous layer is 0.2mm, the material is nickel felt, and the porosity is 70%.
The performance data are as follows: at 90℃the cell current density reached 0.6A/cm 2 at an electrolysis voltage of 2.0V. In the comparative example, the openings of the flow field mesh layer, the transition mesh layer and the microporous layer are not gradually reduced, so that mass transfer is unsmooth, interface resistance is large, and the electrolytic performance is poor.
It is to be understood that the above examples of the present invention are provided by way of illustration only and not by way of limitation of the embodiments of the present invention. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. Not all embodiments are exhaustive. All obvious variations or modifications which come within the spirit of the invention are desired to be protected.
Claims (17)
1. An alkaline electrolytic tank structure comprises an electrolytic unit and a pole frame arranged around the electrolytic unit, wherein the electrolytic unit comprises an electrolytic cell, and is characterized in that the electrolytic cell comprises a bipolar plate, an anode porous layer, a membrane electrode, a cathode porous layer and a bipolar plate which are stacked in sequence; wherein,
The membrane electrode comprises a porous membrane, and an anode catalyst layer and a cathode catalyst layer which are respectively supported on the two side surfaces of the membrane; the anode porous layer and/or the cathode porous layer comprises at least two layers of stacked structures with different opening pore diameters, and the opening pore diameters gradually decrease towards the direction of the membrane electrode.
2. The alkaline cell structure of claim 1, wherein the anode porous layer comprises a three-layer stacked structure with different opening pore diameters, and a flow field mesh layer, a transition mesh layer and a microporous layer are arranged in sequence towards the membrane electrode.
3. The alkaline cell structure of claim 1, wherein the cathode porous layer comprises a three-layer stacked structure with different opening pore diameters, and a flow field mesh layer, a transition mesh layer and a microporous layer are arranged in sequence towards the membrane electrode.
4. The alkaline cell structure of claim 1, wherein the anode porous layer and the cathode porous layer each comprise a three-layer stacked structure with different pore diameters, and a flow field mesh layer, a transition mesh layer and a microporous layer are sequentially arranged in the direction of the membrane electrode.
5. The alkaline cell structure of any one of claims 2-4, wherein the open cell size of the flow field mesh layer is 0.2-10mm and the thickness is 0.5-5mm.
6. The alkaline cell structure of any one of claims 2 to 5, wherein the transition mesh layer has an open mesh size of 50 to 400 mesh and a thickness of 0.1 to 0.5mm.
7. An alkaline cell structure according to any one of claims 2 to 6, wherein the microporous layer has a porosity of not less than 30%, preferably 50 to 80% and a thickness of 0.1 to 0.5mm.
8. The alkaline cell structure of any one of claims 2-7, wherein the flow field mesh layer or transition mesh layer is selected from nickel mesh, nickel alloy mesh, steel mesh with Kong Nieban, nickel plated, perforated steel plate with nickel plated, or from stainless steel mesh, perforated stainless steel plate; and/or the number of the groups of groups,
The microporous layer is selected from nickel felt, punched nickel plate, woven nickel mesh, porous nickel or carbon paper, preferably punched nickel plate.
9. The alkaline cell structure of claim 8 wherein the flow field mesh layer is a diamond punched tensile mesh and the transition mesh layer is a plain weave mesh.
10. The alkaline cell structure of claim 8, wherein the punched hole body of the microporous layer is circular, square or diamond, the punched hole edge of the microporous layer is preferably saw tooth structure, the punched hole diameter is 50 μm-1000 μm, preferably 300-500 μm when cathode hydrogen gas is separated out, the punched hole diameter is 100 μm-2000 μm, preferably 500-800 μm when anode hydrogen gas is separated out, and the saw tooth depth is 10-30 μm, preferably 15-25 μm.
11. An alkaline cell structure as claimed in claim 10, wherein the perforations of the microporous layer are arranged in an array, either square or hexagonal, preferably hexagonal.
12. The alkaline cell structure of claim 1, wherein the porous membrane is made of one or more selected from polyethersulfone, polysulfone, polyphenylene sulfide, polytetrafluoroethylene, polyvinylidene fluoride, polyvinyl chloride, and non-woven fabric.
13. Alkaline cell structure according to claim 1, characterized in that the anode catalyst layer or cathode catalyst layer has a thickness of 1-200 micrometer, preferably 30-50 micrometer.
14. The alkaline cell structure of any one of claims 1 to 13, wherein the anode catalyst layer or cathode catalyst layer comprises an anode or cathode catalyst, a binder, the anode catalyst being selected from one or more of a metal comprising elemental nickel, elemental platinum, and a metal oxide comprising elemental nickel, elemental platinum; the cathode catalyst is selected from metals including nickel element and platinum element; the binder is selected from one or more of perfluorosulfonic acid resin, polyether-ether-ketone and polyacrylonitrile.
15. The alkaline cell structure of claim 1, wherein the bipolar plate is a nickel plate, nickel alloy plate, stainless steel plate or nickel plated plate, and has a thickness of 0.1mm to 3mm.
16. The alkaline cell structure of claim 1, further comprising a gasket disposed between the cathode frame and the anode frame, wherein the gasket is made of a material selected from the group consisting of ethylene-propylene-rubber and has a thickness of 0.1-1mm.
17. The alkaline cell structure of any one of claims 1-16, wherein the side openings of the pole frame are used for circulating alkaline liquor, which enters the electrolysis cell;
the pole frame is made of resin, and preferably the resin is selected from polysulfone or polyether-ether-ketone.
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| Publication Number | Publication Date |
|---|---|
| CN118292007A true CN118292007A (en) | 2024-07-05 |
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