CN111424287A - Electrolysis-electrodialysis cell for hydrogen iodide concentration - Google Patents
Electrolysis-electrodialysis cell for hydrogen iodide concentration Download PDFInfo
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- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
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Abstract
An electrolysis-electrodialysis cell for concentrating hydrogen iodide belongs to the technical field of electrochemistry. The electrolysis-electrodialysis cell comprises at least one single cell, wherein each single cell comprises a proton selective permeation membrane, a cathode side support body, an anode side support body, a sealing ring, an upper polar plate and a lower polar plate. The cathode side support body and the anode side support body adopt graphite felts; the upper polar plate and the lower polar plate adopt flat plate structures. The invention is characterized in that the graphite felt material with large porosity is adopted, which not only can provide good filling and supporting functions, but also can ensure that the HIx material can uniformly and quickly pass through the HIx material, and can be stably used for a long time under the conditions of HIx material liquid soaking and high-current electrochemical reaction, thereby further improving the efficiency of the electrochemical reaction in the electrolysis-electrodialysis pool. The upper and lower polar plates adopt a flat plate structure, so that the problems of high processing difficulty, high processing cost and the like caused by carving a flow channel are solved, and the device has the advantages of high efficiency, stability, compactness and low cost.
Description
Technical Field
The invention relates to an electrochemical treatment device, in particular to an electrolysis-electrodialysis cell which is suitable forIn iodine-containing hydrogen iodide solution (i.e. HI-I)2-H2O mixed solution) and the electrochemical preparation of HI or hydroiodic acid, belonging to the electrochemical technical field.
Background
Electrolysis-electrodialysis (EED, also known as ion exchange membrane electrolysis or membrane electrolysis) is a highly efficient electrochemical concentration method and can also be used for the electrochemical synthesis of specific chemicals. The electrolysis-electrodialysis cell (EED cell) can be used under the harsh conditions of high temperature, acid, alkali, strong oxidant and the like, and has practical value.
Electrolysis-electrodialysis has found application in the thermochemical iodine-sulfur cycle decomposition of water to produce hydrogen. The iodine sulfur cycle is an efficient, clean scale process for producing hydrogen, and it is particularly attractive to couple it with nuclear power heating (e.g., heating from a high temperature gas cooled reactor). The hydrogen in the process is from HI-I2-H2HI in O mixture (i.e. HIx) is decomposed, but due to HI and H2The molar ratio between O is 1:5, and thus when using direct distillation or rectification for HIx, although HI is available, a significant amount of heat energy is used for water evaporation and the economics of the process will be significantly reduced. In view of this situation, researchers at home and abroad propose: first subjecting the HIx to EED concentration to increase the HI concentration in the HIx above the constant boiling composition, i.e. HI: H2O>1:5, a large amount of HI IS distilled out in the distillation/rectification process, the distilled amount of water IS small, and even pure HI gas can be obtained after the process IS optimized, so that the improvement of the overall efficiency of the IS process IS facilitated.
The EED principle of HIx is as follows: when both cathode and anode have HIx material flowing through, H+Under the action of an electric field, the proton selectively penetrates through the membrane and enters the cathode region from the anode region, and the following electrode reactions occur on the two polar plates:
anode: 2I--2e→I2
Cathode: i is2+2e→2I-
As a result of the integration, the anode region H+、I-Reduction of I2Increased, cathode area I2Reduction of，H+、I-The increase, i.e. the concentration of HI in the cathode zone is obtained.
In addition, if the cathode material is still HIx and the anode material is a solution of sulfuric acid, hydrochloric acid or nitric acid, the following still occurs: 1) h+Under the action of electric field, the proton passes through the selective permeable membrane and enters the cathode region from the anode region, 2) cathode reaction I2+2e→2I-. And the anode side generates electrode reaction corresponding to acid radicals such as sulfuric acid, hydrochloric acid, nitric acid and the like, such as: the anolyte is sulfuric acid, the anode is oxygen evolution reaction, and H is consumed in the anode area+Cathode region I2Reduction of H+、I-Increased, corresponding to the synthesis of HI in the cathode region. Thus, the production of HI can be carried out by the method of EED.
The electrolysis-electrodialysis (EED) process needs to be carried out at the range of normal temperature to 130 ℃, operation under higher current density is required for improving equipment compactness and controlling cost, and meanwhile, due to the fact that HIx has extremely strong corrosivity, the structural design and material selection of the EED cell are very important.
The existing EED cell or EED cell stack is composed of a series of single cells with the same structure, the basic structure of the single cells is shown in FIG. 1, in a general EED cell, a cathode side support body and an anode side support body cannot be generally omitted, otherwise, a proton selective permeation membrane swings in a direction vertical to the surface of the membrane when a feed liquid flows, and when the area of the proton selective permeation membrane is large, the swing is particularly obvious, and is very unfavorable for operation stability. The cathode side and anode side support bodies are used for filling the space between the polar plate and the proton selective permeation membrane, and have the functions of supporting and fixing the proton selective permeation membrane to avoid the swinging. At present, PTFE net, carbon fiber cloth, graphite cloth and other materials are mostly adopted as cathode side and anode side support bodies in the EED cell. For example, in document 1, "Yoshida M, et al. concentration of HIx dissolution by electro-electrochemical-catalysis using Nafion117for thermal water-separation process. int J Hydrogen Energy,2008,33:6913-The internal resistance of (2) is relatively large, and thus the energy consumption is relatively high. Document 2 "Hong S D, et al. evaluation of the membrane properties with a changing iodine ratio in HIx (HI-I)2-H2O mix) solution to concentrated apparatus HI by electro-electrochemical Science 2007,291(1-2): 106-.
In the actual use process, carbon fiber cloth (including activated carbon fiber cloth) and graphite cloth are used as thin layer materials, are not easy to fix in the battery, and are easy to move, partially fold and the like in the battery under the washing of feed liquid, so that the performance of the battery is seriously influenced, and even the malfunction of the EED battery is caused. In addition, when the activated carbon fiber cloth is used as a cathode side support body and an anode side support body, the activated carbon fiber cloth is unstable in HIx soaking and electrochemical environments due to more non-carbonized and non-graphitized components, and is easy to be pulverized and peeled off, so that the activated carbon fiber cloth assembled in a pool is lost, the EED efficiency is reduced, and the peeled powder or velvet can gradually enter the feed liquid to cause the feed liquid pollution.
From the overall structure of the EED cell, in a general EED cell, when using PTFE net cathode side and anode side support bodies, in most cases, both sides of the upper and lower polar plates need to be grooved to make flow channels to optimize the flow of the feed liquid, especially when using carbon fiber cloth and graphite cloth, the flow channels need to be prefabricated, because the carbon fiber cloth and graphite cloth are very thin; if the plate pressed on the plate has no flow channel, the fluid resistance of the feed liquid is very large, and the feed liquid is difficult to flow smoothly and uniformly in the space between the plate and the proton selective permeable membrane, and especially the EED operation with large flow rate cannot be carried out. Under the condition of manufacturing a flow channel, the processing requirement is high, the manufacturing cost is high, particularly when a thin plate is grooved, due to deformation generated in the machining process, the consistency of the groove depth and the yield and reliability of a polar plate are difficult to ensure, the problems of the processing cost and the processing difficulty are more prominent, the multi-cell stacking of an EED cell is obviously restricted, and the light weight and the compactness of EED equipment are hindered.
Disclosure of Invention
The present invention aims to overcome the defects and shortcomings of the prior art, and provides an electrolysis-electrodialysis cell for hydrogen iodide concentration, aiming at solving the following problems of the prior electrolysis-electrodialysis cell: 1) the upper and lower polar plates need to be provided with flow channels engraved on two sides, so that the processing difficulty is high and the processing cost is high; 2) when the support bodies on the cathode side and the anode side adopt PTFE nets, the internal resistance of the cell is higher; 3) when the support bodies on the cathode side and the anode side adopt activated carbon fiber cloth, the support bodies are easy to be pulverized and lose efficacy under the use condition; 4) when the cathode side and the anode side support bodies adopt carbon fiber cloth (including activated carbon fiber cloth) and graphite cloth, the carbon fiber cloth and the graphite cloth are not easy to fix in the battery, and the problems of movement, folding and the like are easy to occur, so that the performance of the battery is seriously influenced.
The technical scheme of the invention is as follows:
an electrolysis-electrodialysis cell for hydrogen iodide concentration, which comprises one or more single cells arranged in sequence, wherein each single cell comprises a proton selective permeation membrane, a cathode side supporting body, an anode side supporting body, a sealing ring, an upper polar plate and a lower polar plate, and is characterized in that: the cathode side support body and the anode side support body adopt graphite felts; the upper polar plate and the lower polar plate adopt flat plate structures.
Preferably, a single-layer or multi-layer carbon fiber grid or metal grid is attached to the surface or the inner part of the graphite felt.
The invention has another technical characteristics that: the porosity of the graphite felt is more than or equal to 70%, the carbon content is more than or equal to 98%, and the thickness of the graphite felt is 0.5 mm-10 cm.
The technical scheme of the invention also comprises: the cathode-side support and the anode-side support carry a catalyst. The periphery of the cathode side supporting body is wrapped with a cathode sealing ring, and the periphery of the anode side supporting body is wrapped with an anode sealing ring. The upper polar plate and the lower polar plate are made of corrosion-resistant metal plates, rigid graphite plates or flexible graphite plates.
Compared with the prior art, the invention has the following advantages and prominent technical effects: the invention adopts the graphite felt with high porosity as the cathode side support body and the anode side support body, and fully utilizes the porosity, high conductivity and electrochemical corrosion resistance of the graphite felt with high porosity to achieve the high efficiency and low cost of the electrolysis-electrodialysis cell. This is because: 1) the graphite felt with large porosity has compressibility, can be firmly arranged in the battery under the auxiliary reinforcement of the carbon fiber grids or the metal grids, can provide good filling and supporting functions, and can realize uniform and rapid passing of HIx materials in the battery; 2) the graphite felt can enable the electrolysis-electrodialysis cell to have smaller internal resistance due to high conductivity, has high chemical stability, and can be stably used for a long time under the conditions of HIx liquid soaking and high-current electrochemical reaction. Because the graphite felt has porosity and a certain thickness, the graphite felt is easier to load the catalyst on the graphite felt, thereby further improving the efficiency of the electrochemical reaction in the electrolysis-electrodialysis cell. 3) The graphite felt with large porosity solves the problem that the HIx flows uniformly in the polar region of the electrolysis-electrodialysis cell, so that the electrolysis-electrodialysis cell can adopt a flat plate-shaped polar plate/bipolar plate, and the problems of high processing difficulty, high processing cost and the like caused by carving a flow channel on the graphite felt are avoided.
In conclusion, by adopting the technical scheme of the invention, the electrolysis-electrodialysis cell for concentrating hydrogen iodide, which is efficient, stable, compact and low in cost, can be constructed.
Drawings
Fig. 1 is a schematic view showing a typical structure of a prior art electrolysis-electrodialysis cell unit cell for hydrogen iodide concentration.
Fig. 2 is a schematic view showing the structure of a unit cell of an electrolysis-electrodialysis cell for hydrogen iodide concentration according to the present invention.
In the figure: 1-an upper polar plate; 2-cathode side support; 3-a cathode sealing ring; 4-proton permselective membranes; 5-anode side support; 6-anode sealing ring; 7-lower polar plate.
Detailed Description
The structure, principles and embodiments of the present invention are further described below in conjunction with the accompanying drawings and specific embodiments to enable those skilled in the art to understand and implement the present invention.
Fig. 1 is a schematic view showing a typical structure of a prior art electrolysis-electrodialysis cell unit cell for hydrogen iodide concentration. A cathode side supporting body 2 and an upper polar plate 1 with a flow channel are sequentially distributed on the cathode side by taking the proton selective permeable membrane 4 as the center; the cathode side is distributed with an anode side support body 5 and a lower polar plate 7 with a flow passage in turn; the peripheries of the cathode side supporting body 2 and the anode side supporting body 5 are respectively sealed by a cathode sealing ring 3 and an anode sealing ring 6, and the outer sides of the sealing rings are flush with the outer edge of the polar plate. The cathode sealing ring 3 is positioned between the upper polar plate 1 and the proton selective permeation membrane 4, and the center of the cathode sealing ring is wrapped by the cathode side supporting body 2; the anode sealing ring 6 is positioned between the lower polar plate 7 and the proton selective permeation membrane 4, and the center of the anode sealing ring is wrapped by the anode side supporting body 5, so that the separation between the cathode chamber and the anode chamber in the battery is realized, and the leakage of substances in the battery to the environment can be prevented.
Fig. 2 is an electrolysis-electrodialysis cell for hydrogen iodide concentration according to the present invention, which comprises one or more unit cells arranged in sequence, wherein each unit cell comprises a proton selective permeable membrane 4, a cathode side support body 2, an anode side support body 5, and an upper plate 1 and a lower plate 7; the periphery of the cathode side supporting body 2 is wrapped with a cathode sealing ring 3, and the periphery of the anode side supporting body 5 is wrapped with an anode sealing ring 6. The cathode-side support 2 and the anode-side support 5 carry a catalyst. The invention is technically characterized in that the cathode side support body 2 and the anode side support body 5 both adopt graphite felt materials; to enhance the ability of the graphite felt to retain shape, a single or multiple layers of carbon fiber mesh or metal mesh may also be attached to the surface or interior of the graphite felt. The porosity of the graphite felt in the cathode side support body 2 and the anode side support body 5 is more than or equal to 70%, the carbon content is more than or equal to 98%, and the thickness of the graphite felt is preferably 0.5 mm-10 cm.
The upper polar plate 1 and the lower polar plate 7 do not need to be provided with a flow passage and adopt a flat plate structure; the upper polar plate and the lower polar plate are preferably made of corrosion-resistant metal plates, rigid graphite plates or flexible graphite plates.
When the electrolysis-electrodialysis cell is stacked by adopting a plurality of single cells, the end plates are arranged on the outer sides of the single cells positioned on two sides, the electrolysis-electrodialysis cell is pressed to a set pressure by a press machine and then is fastened and molded, a pull rod penetrates through the end plates, and the pull rod is fastened by a nut.
The invention adopts the graphite felt with high porosity (the porosity is not less than 70%) as the cathode side support body and the anode side support body, fully utilizes and exerts the characteristics of porosity, compressibility, high conductivity, electrochemical corrosion resistance, low cost and the like of the graphite felt material with high porosity, and effectively solves various problems of the electrolysis-electrodialysis cell for concentrating hydrogen iodide at present.
In the following, specific examples are given to further understanding the present invention.
Example 1:
by adopting the scheme of the invention, the electrolysis-electrodialysis cell consisting of 10 single cells which are sequentially stacked and arranged is manufactured, the proton selective permeable membrane is a Nafion117 CS (DuPont company) proton exchange membrane, and the effective membrane area of each single cell is 36cm2The proton selective permeation membrane is provided with a cathode side support body, an upper polar plate, an anode side support body and a lower polar plate which are sequentially and symmetrically distributed on two sides. Both the cathode side support and the anode side support were 0.5mm graphite felt (porosity 70%, carbon content 98%). The upper polar plate and the lower polar plate are both tantalum metal flat plates with the thickness of 1 mm. And carbon fiber grids are additionally paved between the polar plate and the graphite felt on the cathode side and the anode side, so that the shape keeping capability of the graphite felt is enhanced.
The cathode side supporting body and the anode side supporting body are wrapped by a cathode sealing ring and an anode sealing ring, and the materials of the cathode side supporting body and the anode side supporting body are Viton fluororubber.
After the 10 single battery units are stacked and arranged, aluminum alloy end plates are arranged on the two outermost sides, pull rods penetrating through the end plates are arranged, and after the battery units and the end plates are pressed by a press machine, the whole electrolysis-electrodialysis cell is fastened by screwing pull rod nuts.
H at 60 ℃ in the above apparatus2O:I2Iodine-containing hydriodic acid solution (1: 6.3: 0.5) was subjected to electrolysis-electrodialysis treatment to measure the hydriodic acid concentration (i.e., [ HI]) At 5.48mol/l, iodine concentration (i.e. [ I ]2]) The solution was circulated on the cathode side at 2.74 mol/l.1500 m L, and another 4500m L the solution circularly flows on the anode side, the external direct current keeps the current constant at 7.2A, and after 1 hour of treatment, the catholyte [ HI]Increase to 6.56mol/l, and [ I2]The reduction was 2.22 mol/l. I.e. HI is concentrated on the cathode side, I2And is correspondingly reduced.
Example 2:
by adopting the scheme of the invention, the electrolysis-electrodialysis cell consisting of 10 single cells which are sequentially stacked and arranged is manufactured, the proton selective permeable membrane is a Nafion117 CS (DuPont company) proton exchange membrane, and the effective membrane area of each single cell is 1200cm2The proton selective permeation membrane is provided with a cathode side support body, an upper polar plate, an anode side support body and a lower polar plate which are sequentially and symmetrically distributed on two sides. The cathode side support and the anode side support were each 1.5cm graphite felt (porosity 92%, carbon content 99.8%). Before assembly, spraying Pt/C catalyst dispersed in Nafion solution on one surface of the graphite felt facing to the proton selective permeable membrane, and then drying at 120 ℃ for 5 hours to obtain the graphite felt support body loaded with the Pt catalyst.
Both the upper and lower plates were hard graphite plates (available from POCO, USA) of 3mm thickness.
And metal tantalum grids are additionally paved between the polar plate and the graphite felt on the cathode side and the anode side, so that the shape keeping capability of the graphite felt is enhanced.
The cathode side supporting body and the anode side supporting body are wrapped by a cathode sealing ring and an anode sealing ring, and the materials of the cathode side supporting body and the anode side supporting body are Viton A fluororubber.
After the 10 battery units are stacked and arranged, aluminum alloy end plates are arranged on the two outermost sides, pull rods penetrating through the end plates are arranged, and after the battery units and the end plates are pressurized by a press machine, the whole electrolysis-electrodialysis cell is fastened by screwing pull rod nuts.
Subjecting HI to H at 80 deg.C by using the above electrolysis-electrodialysis apparatus2O:I2Iodine-containing hydriodic acid solution was subjected to electrolysis-electrodialysis treatment under a condition of 1:5.36:1.5 to measure the hydriodic acid concentration (i.e., [ HI ]]) At 4.32mol/l, iodine concentration (i.e. [ I ]2]) 6.50 mol/l.100.0L the solution circulated on the cathode side and another 100.0L the solution circulated on the anode sideFlowing, maintaining constant at 600A with external direct current, treating for 1 hr, and collecting catholyte]Increase to 5.70mol/l, and [ I2]The reduction is 4.77mol/l, in which case HI is H2O:I21:4.42: 0.84. I.e. HI is concentrated on the cathode side, I2And is correspondingly reduced.
Example 3:
by adopting the scheme of the invention, the electrolysis-electrodialysis cell consisting of 50 single cells which are sequentially stacked and arranged is manufactured, the proton selective permeable membrane adopts a Nafion 115 (DuPont company) proton exchange membrane, and the effective membrane area of each single cell is 2000cm2The proton selective permeation membrane is provided with a cathode side support body, an upper polar plate, an anode side support body and a lower polar plate which are sequentially and symmetrically distributed on two sides. Both the cathode side support and the anode side support were 5.6mm graphite felt (porosity 92%, carbon content 99.8%). And coating a layer of carbon fiber mesh in the graphite felt, spraying a Pt/C catalyst dispersed in Nafion solution on one surface of the graphite felt facing to the proton selective permeation membrane before assembling, and drying at 120 ℃ for 5 hours to obtain the graphite felt support body loaded with the Pt catalyst.
Both the upper and lower plates were 2mm flexible graphite plates (available from siegri, germany).
The cathode side supporting body and the anode side supporting body are wrapped by a cathode sealing ring and an anode sealing ring, and the materials of the cathode side supporting body and the anode side supporting body are Viton A fluororubber.
After the 50 battery units are stacked and arranged, aluminum alloy end plates are arranged on the two outermost sides, pull rods penetrating through the end plates are arranged, and after the battery units and the end plates are pressurized by a press machine, the whole electrolysis-electrodialysis cell is fastened by screwing pull rod nuts.
Example 4:
by adopting the scheme of the invention, the electrolysis-electrodialysis cell consisting of 5 single cells which are sequentially stacked and arranged is manufactured, the proton selective permeable membrane is a Nafion117 CS (DuPont company) proton exchange membrane, and the effective membrane area of each single cell is 80cm2The proton selective permeation membrane is provided with a cathode side support body, an upper polar plate, an anode side support body and a lower polar plate which are sequentially and symmetrically distributed on two sides. Cathode side supportAnd the support body on the anode side are 7cm of graphite felt (the porosity is 92 percent, and the carbon content is 99.8 percent). Before assembling, a Pt/C catalyst dispersed in Nafion solution is sprayed on one surface of the membrane facing to the proton selective permeable membrane, and then drying is carried out at 120 ℃ for 5 hours to obtain the graphite felt supporting body loaded with the Pt catalyst.
Both the upper and lower plates were 3mm flexible graphite plates (available from siegri, germany).
The cathode side supporting body and the anode side supporting body are wrapped by a cathode sealing ring and an anode sealing ring, and the materials of the cathode side supporting body and the anode side supporting body are Viton A fluororubber.
After the 5 battery units are stacked and arranged, aluminum alloy end plates are arranged on the two outermost sides, pull rods penetrating through the end plates are arranged, and after the pressure is applied to the battery units and the end plates through a press machine, the whole electrolysis-electrodialysis cell is fastened by screwing pull rod nuts.
H, HI in the above apparatus at 90 deg.C2O:I2Iodine-containing hydriodic acid solution (1: 6.3: 0.5) was subjected to electrolysis-electrodialysis treatment to measure the hydriodic acid concentration (i.e., [ HI]) At 5.48mol/l, iodine concentration (i.e. [ I ]2]) 2.74 mol/l.1500m L the solution circulated on the cathode side, 4500m L the solution circulated on the anode side, and external direct current was applied to maintain the current constant at 7.1A, and after 1 hour of treatment, the catholyte [ HI]Increase to 6.67mol/l, and [ I2]The reduction was 2.10 mol/l. I.e. HI is concentrated on the cathode side, I2And is correspondingly reduced.
Example 5:
using the electrolysis-electrodialysis apparatus described in example 1, the cathode feed was iodine-containing hydroiodic acid, [ HI ]]＝5.08mol/l，[I2]The total volume was 150ml, 1.20mol/l, and the flow was circulated. The anolyte was 1.75mol/l phosphoric acid, total 350ml, and circulated. At 70 deg.C, external direct current is kept constant at 15A, and after 1.5 hr treatment, the catholyte is converted into iodine-free colorless hydroiodic acid, [ HI ]]The increase was 6.87 mol/l. I.e. cathode side consumes I2HI was prepared.
Claims (6)
1. An electrolysis-electrodialysis cell for hydrogen iodide concentration, comprising one or more unit cells arranged in sequence, each unit cell comprising a proton permselective membrane (4), a cathode-side support (2), an anode-side support (5), and an upper plate (1) and a lower plate (7), characterized in that: the cathode side support body (2) and the anode side support body (5) adopt graphite felts; the upper polar plate (1) and the lower polar plate (7) adopt a flat plate-shaped structure.
2. An electrolysis-electrodialysis cell for hydrogen iodide concentration according to claim 1, wherein: and a single-layer or multi-layer carbon fiber grid or metal grid is attached to the surface or the interior of the graphite felt.
3. An electrolysis-electrodialysis cell for hydrogen iodide concentration according to claim 1 or 2, characterized in that: the porosity of the graphite felt is more than or equal to 70%, the carbon content is more than or equal to 98%, and the thickness of the graphite felt is 0.5 mm-10 cm.
4. An electrolysis-electrodialysis cell for hydrogen iodide concentration according to claim 3, wherein: the cathode-side support (2) and the anode-side support (5) carry a catalyst.
5. An electrolysis-electrodialysis cell for hydrogen iodide concentration according to claim 1, wherein: the periphery of the cathode side supporting body (2) is wrapped with a cathode sealing ring (3), and the periphery of the anode side supporting body (5) is wrapped with an anode sealing ring (6).
6. An electrolysis-electrodialysis cell for hydrogen iodide concentration according to claim 1, wherein: the upper polar plate (1) and the lower polar plate (7) adopt corrosion-resistant metal plates, rigid graphite plates or flexible graphite plates.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4443316A (en) * | 1980-11-06 | 1984-04-17 | Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung | Electrolysis cell with intermediate chamber for electrolyte flow |
| CN101545114A (en) * | 2009-05-08 | 2009-09-30 | 清华大学 | Electrolysis-electrodialysis device |
| CN101800322A (en) * | 2009-02-06 | 2010-08-11 | 北京金能燃料电池有限公司 | Electrode of liquid flow cell |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4443316A (en) * | 1980-11-06 | 1984-04-17 | Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung | Electrolysis cell with intermediate chamber for electrolyte flow |
| CN101800322A (en) * | 2009-02-06 | 2010-08-11 | 北京金能燃料电池有限公司 | Electrode of liquid flow cell |
| CN101545114A (en) * | 2009-05-08 | 2009-09-30 | 清华大学 | Electrolysis-electrodialysis device |
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