CN220364597U - Electrochemical electrolytic tank with diffusion flow channel - Google Patents
Electrochemical electrolytic tank with diffusion flow channel Download PDFInfo
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- CN220364597U CN220364597U CN202320627861.7U CN202320627861U CN220364597U CN 220364597 U CN220364597 U CN 220364597U CN 202320627861 U CN202320627861 U CN 202320627861U CN 220364597 U CN220364597 U CN 220364597U
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- solid electrolyte
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- electrolyte layer
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- 238000009792 diffusion process Methods 0.000 title claims abstract description 59
- 239000007784 solid electrolyte Substances 0.000 claims abstract description 89
- 239000002245 particle Substances 0.000 claims abstract description 22
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 13
- 238000005341 cation exchange Methods 0.000 claims abstract description 12
- 239000012528 membrane Substances 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims description 47
- 239000007788 liquid Substances 0.000 claims description 24
- 239000004793 Polystyrene Substances 0.000 claims description 4
- 229920002223 polystyrene Polymers 0.000 claims description 4
- 229920003053 polystyrene-divinylbenzene Polymers 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 45
- 150000002500 ions Chemical class 0.000 abstract description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 24
- -1 hydrogen ions Chemical class 0.000 description 10
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000010411 electrocatalyst Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 4
- 125000003277 amino group Chemical group 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 125000000542 sulfonic acid group Chemical group 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 239000003792 electrolyte Substances 0.000 description 2
- 125000000524 functional group Chemical group 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000008151 electrolyte solution Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000002688 persistence Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Abstract
The utility model provides an electrochemical cell with a diffusion channel, comprising: an anode, a cathode, and a porous solid electrolyte layer disposed between the anode and the cathode; wherein, the anode comprises an anode current collecting plate, an anode electrocatalytic layer and a cation exchange membrane which are sequentially arranged; the cathode comprises a cathode current collecting plate, a gas diffusion layer, a cathode electrocatalytic layer and an anion exchange membrane which are sequentially arranged; the porous solid electrolyte layer is arranged between the cation exchange membrane and the anion exchange membrane, and a diffusion runner is arranged in the porous solid electrolyte layer. According to the electrochemical electrolytic tank with the diffusion flow channel, the diffusion flow channel is arranged in the porous solid electrolyte layer, so that the water flow speed in the porous solid electrolyte layer and the water content of solid electrolyte particles can be effectively improved, the ion conductivity is improved, and the tank voltage of the electrolytic tank is further reduced.
Description
Technical Field
The utility model relates to the technical field of environmental engineering and energy utilization, in particular to an electrochemical electrolytic cell with a diffusion runner.
Background
In current hydrogen peroxide generating devices, there are typically three key elements, namely anode, cathode and electrolyte. The electrodes are placed in electrolyte solution with a certain concentration for electrolysis, and the electrolyte is usually inert salt, so that the generated hydrogen peroxide contains a large amount of inert salt, which is unfavorable for the subsequent separation process.
For this reason, researchers have proposed a hydrogen peroxide generating apparatus using a porous solid electrolyte layer in which rectangular reaction through holes are filled with a solid electrolyte, so that an inert salt is not present in the produced hydrogen peroxide. In the production process, a liquid inlet device is required to be arranged to introduce water flow into the anode so as to generate hydrogen ions at the anode, and air is introduced into the cathode so as to generate peroxy hydrogen ions at the cathode. And another group of liquid inlet devices are arranged at the same time, and water flow is introduced into the porous solid electrolyte layer from bottom to top. The hydrogen ions generated at the anode and the hydrogen peroxide ions generated at the cathode combine in the water stream passing through the porous solid electrolyte layer to produce hydrogen peroxide. After the device is amplified, because only one point of water flow is introduced into the porous solid electrolyte layer, when the water flow crosses the solid electrolyte, the water flow gradually diffuses to the solid electrolyte, the water flow is unevenly distributed, the solid electrolyte cannot fully absorb water, the conductivity of each part is inconsistent, and the cell voltage is higher.
Disclosure of Invention
In view of the above, the present utility model provides an electrochemical cell with a diffusion channel, which can improve the uniformity of water flow in a porous solid electrolyte layer and the water content of the solid electrolyte, further improve the ion conductivity and reduce the cell voltage.
In order to solve the technical problems, the utility model adopts the following technical scheme:
an electrochemical cell with a diffusion channel according to an embodiment of the present utility model includes: an anode, a cathode, and a porous solid electrolyte layer disposed between the anode and the cathode;
the anode comprises an anode current collecting plate, an anode electrocatalytic layer and a cation exchange membrane which are sequentially arranged;
the cathode comprises a cathode current collecting plate, a gas diffusion layer, a cathode electrocatalytic layer and an anion exchange membrane which are sequentially arranged;
the porous solid electrolyte layer is arranged between the cation exchange membrane and the anion exchange membrane, is respectively communicated with the cation exchange membrane and the anion exchange membrane, and is internally provided with a diffusion runner.
In one embodiment of the present utility model, a reaction chamber is provided in a porous solid electrolyte layer, the porous solid electrolyte layer comprising:
the flow channel plates are arranged at intervals and are respectively connected with the cavity wall of the reaction cavity to form diffusion flow channels, and the length of the flow channel plates is smaller than that of the reaction cavity.
In one embodiment of the present utility model, the reaction chamber is filled with spherical solid electrolyte particles.
In one embodiment of the utility model, the diffusion flow channels are serpentine flow channels or parallel flow channels.
In one embodiment of the present utility model, the porous solid electrolyte layer further includes:
the liquid inlet of the solid electrolyte layer is connected with the port of the diffusion flow channel;
the liquid outlet of the solid electrolyte layer is connected with the other port of one side of the diffusion runner, which is away from the liquid inlet of the solid electrolyte layer.
In one embodiment of the utility model, the ratio of the area of the reaction cavity to the area of the cross section of the junction of the flow channel plate and the reaction cavity is 1: (0.1-0.3).
In one embodiment of the present utility model, the solid electrolyte particles have a skeleton of polystyrene or polystyrene-divinylbenzene, and the functional group is a sulfonic acid group or a quaternary amine group.
In one embodiment of the utility model, a cathode reaction chamber is provided within the cathode collector plate, the cathode reaction chamber being provided with a cathode chamber inlet for air to pass in and a cathode chamber outlet for air to exit.
The technical scheme of the utility model has at least one of the following beneficial effects:
according to the electrochemical electrolytic tank with the diffusion flow channel, the diffusion flow channel is arranged in the reaction cavity of the porous solid electrolyte layer, so that the contact area between the solid electrolyte and water flow can be effectively increased, the distribution uniformity of the water flow is improved, the solid electrolyte can fully absorb water, the conductivity of each part is uniform, the ion conductivity is improved, and the tank voltage is reduced.
Drawings
FIG. 1 is a schematic side cross-sectional view of an electrochemical cell with a diffusion channel according to an embodiment of the present utility model;
FIG. 2 is a schematic side sectional view of a serpentine diffusion channel in an electrochemical cell with a diffusion channel according to an embodiment of the present utility model;
FIG. 3 is a schematic side sectional view of parallel diffusion channels in an electrochemical cell with diffusion channels according to an embodiment of the present utility model;
FIG. 4 is a plot of cell voltage versus cell voltage for an electrochemical cell with a diffusion channel according to an embodiment of the utility model.
Reference numerals: 100. an anode; 110. an anode current collecting plate; 111. an exhaust port; 120. an anode electrocatalyst layer; 130. a cation exchange membrane; 200. a cathode; 210. a cathode current collecting plate; 211. a cathode chamber inlet; 212. a cathode chamber outlet; 220. a gas diffusion layer; 230. a cathode electrocatalyst layer; 240. an anion exchange membrane; 300. a porous solid electrolyte layer; 301. a liquid inlet of the solid electrolyte layer; 302. a solid electrolyte layer liquid outlet; 310. a reaction chamber; 320. and a runner plate.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present utility model more clear, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present utility model. It will be apparent that the described embodiments are some, but not all, embodiments of the utility model. All other embodiments, which are obtained by a person skilled in the art based on the described embodiments of the utility model, fall within the scope of protection of the utility model.
Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this utility model belongs. The terms "first," "second," and the like, as used herein, do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. Likewise, the terms "a" or "an" and the like do not denote a limitation of quantity, but rather denote the presence of at least one. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate a relative positional relationship, which changes accordingly when the absolute position of the object to be described changes.
In order to facilitate understanding of the technical scheme of the present utility model, first, the technical problem to be solved by the present utility model will be described. In some aspects, the electrochemical cell communicates with the liquid inlet of the reaction chamber of the porous solid electrolyte layer via a liquid inlet device and provides a flow of water to the solid electrolyte particles filled in the reaction chamber. And a liquid outlet is formed in the other side of the reaction cavity, which is away from the liquid inlet, and the generated hydrogen peroxide can be carried out through the liquid outlet by water flow. In the process, the water flow can only contact with the solid electrolyte through the liquid inlet, so that the water flow contacted by the solid electrolyte particles far away from the liquid inlet is far smaller than the water flow contacted by the solid electrolyte particles near the liquid inlet, and the water content is lower. Therefore, when water flows across the solid electrolyte, the water flow distribution is uneven, the solid electrolyte cannot sufficiently absorb water, and the conductivity is not uniform everywhere, so that the cell voltage is high.
An electrochemical cell with a diffusion channel according to an embodiment of the present utility model will be described in detail with reference to the accompanying drawings.
Referring to fig. 1, fig. 1 is a schematic side sectional view of an electrochemical cell with a diffusion channel of the present utility model. As shown in fig. 1, an electrochemical cell with a diffusion channel includes: an anode 100, a cathode 200, and a porous solid electrolyte layer 300 disposed between the anode 100 and the cathode 200. Wherein the anode 100 includes an anode current collecting plate 110, an anode electrocatalyst layer 120, and a cation exchange membrane 130, which are sequentially disposed; the cathode 200 includes a cathode current collecting plate 210, a gas diffusion layer 220, a cathode electrocatalyst layer 230, and an anion exchange membrane 240, which are sequentially disposed; the porous solid electrolyte layer 300 is disposed between the cation exchange membrane 130 and the anion exchange membrane 240, and communicates with the cation exchange membrane 130 and the anion exchange membrane 240, respectively, and diffusion channels are provided in the porous solid electrolyte layer 300.
The electrochemical cell will be described below with respect to the production of hydrogen peroxide. Pure water may be introduced into the porous solid electrolyte layer 300 at the time of production, and air may be introduced into the cathode 200 to generate hydrogen peroxide ions. Pure water is introduced into the porous solid electrolyte layer 300, and the pure water can be sufficiently diffused in the diffusion flow channels provided in the porous solid electrolyte layer 300, thereby improving the ion conductivity of the porous solid electrolyte layer 300 and reducing the cell voltage.
As shown in fig. 2 and 3, in one embodiment of the present utility model, a reaction chamber 310 is provided in a porous solid electrolyte layer 300, and the porous solid electrolyte layer 300 includes a plurality of flow field plates 320. The plurality of flow channel plates 320 are disposed at intervals and are respectively connected with the chamber walls of the reaction chamber 310 to form diffusion channels, and the length of the flow channel plates 320 is smaller than that of the reaction chamber 310.
That is, a plurality of flow channel plates 320 are disposed at intervals in the chamber wall of the reaction chamber 310, and since the length of the flow channel plates 320 is smaller than that of the reaction chamber 310, spaces isolated by the respective flow channel plates 320 communicate with each other, thereby separating diffusion channels in the reaction chamber 310. Thus, the inner surface area of the reaction chamber 310 can be effectively increased, thereby improving the diffusion uniformity of the water flow.
In one embodiment of the present utility model, the reaction chamber 310 is filled with solid electrolyte particles. That is, the solid electrolyte particles are filled in the reaction chamber 310 provided with the diffusion flow path. By providing the diffusion flow channels, a large amount of solid electrolyte particles are filled in the reaction cavity 310, so that the contact area between the solid electrolyte particles and water flow can be effectively increased, and the water content of each part of solid electrolyte particles can be further improved. A large amount of solid electrolyte particles capable of absorbing water sufficiently can rapidly transfer anions and cations, so that the ion conductivity is effectively improved, and the cell voltage is further reduced. In addition, the cations generated by the anode 100 and the anions generated by the cathode 200 can be rapidly combined to generate a reactant, thereby improving the production efficiency.
In one embodiment of the present utility model, as shown in fig. 2 and 3, the diffusion flow channels are serpentine flow channels or parallel flow channels. Specifically, in the serpentine flow channel, the flow channel plate 320 is connected to the upper and lower chamber walls and the both side chamber walls of the reaction chamber 310 at intervals, respectively, and the water flow can flow in a serpentine shape since the length of the flow channel plate 320 is smaller than the length of the chamber walls of the reaction chamber 310. The flow channel plates are arranged in parallel, and in the parallel flow channels, the flow channel plates 320 are respectively connected with the cavity walls at two sides of the reaction cavity 310. Because a plurality of corners are arranged in the diffusion flow channel, the flow velocity of water flow can be effectively improved while the water flow distribution uniformity is increased, so that the ion conduction speed is effectively improved, and the reaction speed is improved.
As shown in fig. 1 to 3, in one embodiment of the present utility model, the porous solid electrolyte layer 300 further includes: a solid electrolyte layer liquid inlet 301 and a solid electrolyte layer liquid outlet 302. Wherein the solid electrolyte layer liquid inlet 301 is connected with the first port of the diffusion channel. The solid electrolyte layer liquid outlet 302 and the second port of the diffusion flow channel, the second port is away from the solid electrolyte layer liquid inlet 301.
Specifically, in the production of hydrogen peroxide, a water stream may be introduced into the porous solid electrolyte layer 300 through the solid electrolyte layer liquid inlet 301. The water stream may be sufficiently contacted with the solid electrolyte particles so that portions of the solid electrolyte particles may be sufficiently water-absorbing, and hydrogen ions and hydrogen peroxide ions combine to form hydrogen peroxide under the conduction of the sufficiently water-absorbing solid electrolyte particles, and then carried out of the solid electrolyte layer outlet 302 by the water stream.
In one embodiment of the present utility model, the ratio of the chamber area of the reaction chamber 310 to the cross-sectional area at the junction of the flow channel plate 320 and the reaction chamber 310 is 1: (0.05-0.5). In a preferred embodiment, the ratio of the area of the reaction chamber 310 to the cross-sectional area at the junction of the flow channel plate 320 and the reaction chamber 310 may be 1: (0.1-0.3). That is, the flow field plate 320 occupies an area smaller than that of the reaction chamber 310 provided with the diffusion flow field. Thereby, the contact area of the solid electrolyte particles with the water flow is further enlarged.
In one embodiment of the present utility model, the skeleton of the solid electrolyte particles may be polystyrene or polystyrene-divinylbenzene material, and the functional group is a sulfonic acid group or a quaternary amine group. The sulfonic acid group or the quaternary amine group is arranged on the polystyrene or the polystyrene-divinylbenzene skeleton, so that the ionic conduction speed can be effectively improved, and the reaction generation rate is improved. Further, the diameter of the solid electrolyte particles is 50-300 micrometers, that is, the volume of the single solid electrolyte particles is small, and when a large amount of solid electrolyte particles are filled, the contact area between water flow and the solid electrolyte can be effectively increased, so that the water flow is fully and uniformly distributed, the water content of each part of the solid electrolyte is increased, the ion conductivity of the solid electrolyte is further improved, and finally the cell voltage is reduced.
As shown in fig. 1, in one embodiment of the present utility model, a cathode reaction chamber is provided in a cathode collecting plate 210, and the cathode reaction chamber is provided with a cathode chamber inlet 211 for introducing air and a cathode chamber inlet 212 for discharging air.
Specifically, air may enter through the cathode chamber inlet 211 and diffuse through the gas diffusion layer 220 to reach the cathode electrocatalyst layer 230, where a two-electron oxygen reduction reaction occurs to generate peroxyhydride ions. The generated hydrogen peroxide ions cross the anion exchange membrane 240 and enter the porous solid electrolyte layer 300, and react with the hydrogen ions generated at the anode 100 to generate hydrogen peroxide.
In addition, an anode reaction chamber is provided in the anode current collecting plate 110; the anode reaction chamber is provided with an exhaust port 111, and when the anode electro-catalytic layer 120 electro-catalyzes water, hydrogen ions and oxygen gas are generated, and the oxygen gas generated by the anode 100 can be exhausted through the exhaust port 111. Thereby, the persistence of the reaction is ensured.
According to the electrochemical electrolytic tank with the diffusion runner, the reaction cavity of the porous solid electrolyte layer is internally provided with the plurality of runner plates to form the diffusion runner, so that the contact area between the solid electrolyte and water flow is effectively increased, the distribution uniformity of the water flow is improved, the solid electrolyte can fully absorb water, the conductivity of each part is uniform, and the tank voltage is lower.
Referring to fig. 4, fig. 4 shows a plot of cell voltage versus cell voltage for an electrochemical cell with a diffusion channel according to an embodiment of the present utility model. As shown in fig. 4, the cell voltage of an electrochemical cell with a diffusion channel is significantly lower than the cell voltage of the cell in some embodiments at the same current density. Obviously, the electrochemical electrolytic cell of the utility model improves the ion conductivity and effectively reduces the cell voltage compared with the electrolytic cell in the background technology.
The foregoing is a preferred embodiment of the present utility model and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present utility model and are intended to be comprehended within the scope of the present utility model.
Claims (7)
1. An electrochemical cell with a diffusion channel, comprising: an anode, a cathode, and a porous solid electrolyte layer disposed between the anode and the cathode;
the anode comprises an anode current collecting plate, an anode electrocatalytic layer and a cation exchange membrane which are sequentially arranged;
the cathode comprises a cathode current collecting plate, a gas diffusion layer, a cathode electrocatalytic layer and an anion exchange membrane which are sequentially arranged;
the porous solid electrolyte layer is arranged between the cation exchange membrane and the anion exchange membrane and is respectively communicated with the cation exchange membrane and the anion exchange membrane, a diffusion runner is arranged in the porous solid electrolyte layer, a reaction cavity is arranged in the porous solid electrolyte layer, the porous solid electrolyte layer further comprises a plurality of runner plates, the runner plates are arranged at intervals and are respectively connected with the cavity wall of the reaction cavity to form diffusion runners, and the length of the runner plates is smaller than that of the reaction cavity.
2. The electrochemical cell with diffusion channel of claim 1, wherein the reaction chamber is filled with solid electrolyte particles.
3. An electrochemical cell with a diffusion channel according to claim 2, wherein the diffusion channel is a serpentine channel or a parallel channel.
4. An electrochemical cell with a diffusion channel according to claim 3, wherein the porous solid electrolyte layer further comprises:
a liquid inlet of the solid electrolyte layer is connected with a first port of the diffusion flow channel;
and the liquid outlet of the solid electrolyte layer is connected with a second port of the diffusion flow channel, and the second port is away from the liquid inlet of the solid electrolyte layer.
5. The electrochemical cell with diffusion channel of claim 4, wherein the ratio of the reaction chamber cavity area to the cross-sectional area at the junction of the flow field plate and the reaction chamber is 1: (0.1-0.3).
6. The electrochemical cell with diffusion channel of claim 2, wherein the solid electrolyte particles have a skeleton of polystyrene or polystyrene-divinylbenzene material.
7. An electrochemical cell with a diffusion channel according to claim 1, characterized in that a cathode reaction chamber is provided in the cathode collector plate, the cathode reaction chamber being provided with a cathode chamber inlet for air inlet and a cathode chamber outlet for air exhaust.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320627861.7U CN220364597U (en) | 2023-03-27 | 2023-03-27 | Electrochemical electrolytic tank with diffusion flow channel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320627861.7U CN220364597U (en) | 2023-03-27 | 2023-03-27 | Electrochemical electrolytic tank with diffusion flow channel |
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| Publication Number | Publication Date |
|---|---|
| CN220364597U true CN220364597U (en) | 2024-01-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320627861.7U Active CN220364597U (en) | 2023-03-27 | 2023-03-27 | Electrochemical electrolytic tank with diffusion flow channel |
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| CN (1) | CN220364597U (en) |
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- 2023-03-27 CN CN202320627861.7U patent/CN220364597U/en active Active
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