CN116815214A - Electrolytic tank device and method - Google Patents
Electrolytic tank device and method Download PDFInfo
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- CN116815214A CN116815214A CN202310773645.8A CN202310773645A CN116815214A CN 116815214 A CN116815214 A CN 116815214A CN 202310773645 A CN202310773645 A CN 202310773645A CN 116815214 A CN116815214 A CN 116815214A
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- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000003513 alkali Substances 0.000 claims abstract description 132
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 115
- 238000000926 separation method Methods 0.000 claims abstract description 80
- 239000001257 hydrogen Substances 0.000 claims abstract description 75
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 75
- 239000001301 oxygen Substances 0.000 claims abstract description 69
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 69
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 238000006243 chemical reaction Methods 0.000 claims abstract description 63
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000007788 liquid Substances 0.000 claims abstract description 58
- 230000036647 reaction Effects 0.000 claims abstract description 32
- 239000000498 cooling water Substances 0.000 claims description 66
- 210000004027 cell Anatomy 0.000 claims description 52
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 39
- 150000002431 hydrogen Chemical class 0.000 claims description 33
- 238000009826 distribution Methods 0.000 claims description 10
- 238000007789 sealing Methods 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 3
- 210000003339 pole cell Anatomy 0.000 claims 2
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 148
- 238000013461 design Methods 0.000 description 40
- 239000007769 metal material Substances 0.000 description 25
- 239000012670 alkaline solution Substances 0.000 description 22
- 239000000463 material Substances 0.000 description 22
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 20
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 19
- 230000008569 process Effects 0.000 description 18
- 239000007791 liquid phase Substances 0.000 description 12
- 238000010276 construction Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 11
- 230000010287 polarization Effects 0.000 description 11
- 230000007774 longterm Effects 0.000 description 10
- 238000012423 maintenance Methods 0.000 description 10
- 229910052751 metal Inorganic materials 0.000 description 10
- 239000002184 metal Substances 0.000 description 10
- 229910052759 nickel Inorganic materials 0.000 description 10
- 239000002918 waste heat Substances 0.000 description 10
- 238000003487 electrochemical reaction Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 230000001105 regulatory effect Effects 0.000 description 8
- 230000007797 corrosion Effects 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 6
- 239000003792 electrolyte Substances 0.000 description 6
- 230000004927 fusion Effects 0.000 description 6
- 230000009467 reduction Effects 0.000 description 6
- 229910000975 Carbon steel Inorganic materials 0.000 description 5
- 239000010962 carbon steel Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 239000011810 insulating material Substances 0.000 description 5
- 238000007747 plating Methods 0.000 description 5
- 229910001220 stainless steel Inorganic materials 0.000 description 5
- 239000010935 stainless steel Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910000963 austenitic stainless steel Inorganic materials 0.000 description 1
- 210000005056 cell body Anatomy 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000008151 electrolyte solution Substances 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
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- 230000000630 rising effect Effects 0.000 description 1
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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention relates to an electrolytic tank device and a method, wherein the device comprises a cathode plate, a cathode net, a diaphragm, an anode net, an anode plate, a cathode cell reaction channel, an anode cell reaction channel, an alkali liquor inlet chamber, a hydrogen separation chamber, an oxygen separation chamber, a cathode liquid dropping channel and an anode liquid dropping channel which are sequentially arranged. Compared with the prior art, the invention can reduce the complexity of the water electrolysis system, reduce the liquid holdup of the alkali liquor in the water electrolysis system, improve the operation efficiency and the utilization efficiency of the water electrolysis tank, and the like.
Description
Technical Field
The invention belongs to the technical field of electrolytic tank equipment, relates to an electrolytic tank device and an electrolytic tank method, and particularly relates to a built-in self-circulation heat exchange multi-system integrated efficient electrolytic tank device and an electrolytic tank method.
Background
With the increasing low-carbon emission reduction demands, green hydrogen preparation technology is widely paid attention to, and water electrolysis hydrogen production by using renewable energy sources is the process with the lowest carbon emission in numerous hydrogen source schemes at present. The popularization and application of hydrogen in the fields of energy storage, chemical industry, metallurgy, distributed generation and the like become one of effective ways for controlling greenhouse gas emission and slowing down global temperature rise. The original purpose of green utilization of hydrogen energy is maintained, the green hydrogen preparation technology represented by the hydrogen production by the electrolysis of water through a proton exchange membrane is actively developed, and the fusion development with renewable energy sources is realized.
Currently, in the market progress, alkaline Water Electrolysis (AWE) is dominant as the most mature electrolysis technology, especially for some large-scale projects. AWE uses aqueous potassium hydroxide (KOH) as an electrolyte to separate water to produce hydrogen and oxygen.
In general, the alkaline water electrolysis system comprises an electrolysis tank 1', an oxyhydrogen separation system, an alkali liquor circulation system and a heat exchange system. Wherein the oxyhydrogen separation system comprises: a hydrogen separator 2 ', an oxygen separator 3', a hydrogen product cooler and an oxygen product cooler, and auxiliary pipelines and valves thereof; the alkali liquor circulation system comprises: an alkali liquor circulating pump, an alkali liquor filter, an alkali liquor control valve and an accessory pipeline thereof; the heat exchange system comprises: the lye heat exchanger is shown in figure 1.
The system design has the following defects:
(1) In the traditional lye water electrolysis system, a design of removing heat outside an electrolysis tank is adopted. Except that the electrolytic tank is the main process equipment, other oxyhydrogen gas separation systems, alkali liquor circulation systems and alkali liquor heat exchange units are all accessory devices. Typically the attachment will account for 20-30% of the total construction cost of a conventional water electrolysis system.
(2) The auxiliary devices such as an oxyhydrogen gas separation system, an alkali liquor circulation system, an alkali liquor heat exchange unit and the like of the traditional alkali liquor water electrolysis system need to provide extra occupied space. The subsystem generally needs to occupy 25-40% of the total traditional alkaline water electrolysis system;
(3) The alkaline liquor circulation system of the traditional alkaline liquor electrolysis system generally needs to adopt an external forced circulation design for removing heat. Increasing the risk point of leakage. Greatly reduces the safety of the device.
(4) In order to reduce the manufacturing cost, the alkali liquor circulation pipeline of the traditional alkali liquor electrolysis system is mostly made of stainless steel. However, in order to reduce the corrosion rate of the alkaline liquor to the pipe, the operating temperature should not be more than 90 ℃. Therefore, the low-temperature waste heat generated by the alkali liquor in the water electrolysis process is difficult to be utilized. And energy is wasted.
(5) Since the operating temperature of the lye is not too high, however, the resistance of the electrolyte is inversely proportional to the temperature. The higher the temperature the higher the efficiency liquid of the electrolysis. Conventional water electrolysis systems are therefore limited by the operating temperature, resulting in higher consumption of electrolyte solution resistance.
(6) The traditional alkali liquid electrolysis device is subjected to adiabatic reaction in a cathode and anode small chamber, and the flow velocity in the small chamber is low. If the local heat generation is excessive, the diaphragm is difficult to remove quickly, and finally the diaphragm is damaged.
(7) The gas-liquid separator and the circulating pipeline system of the traditional alkali liquid electrolysis device have larger liquid holdup. The lye needs to be filled before the operation, so a large amount of KOH configuration lye needs to be purchased. However, the alkali liquor needs to be replaced after running for a period of time, so that the treatment capacity of the waste alkali liquor is increased. In particular, in order to ensure the electrolysis efficiency, V2O5 needs to be increased, so that the larger the system liquid holdup is, the larger the V2O5 consumption is;
(8) The gas-liquid separator and the circulating pipeline system of the traditional alkali liquid electrolysis device have larger liquid holdup, so that the alkali liquid temperature rising process is longer in the driving process.
Therefore, if the oxyhydrogen gas separation system, the alkali liquor circulation system and the alkali liquor heat exchange system can be designed in a highly integrated manner, the defects of the process can be effectively solved.
Disclosure of Invention
The invention aims to provide an electrolytic tank device and an electrolytic tank method, which are used for reducing the complexity of a water electrolysis system, reducing the liquid holdup of alkali liquor in the water electrolysis system, improving the operation efficiency and the utilization efficiency of the water electrolysis tank and the like.
The aim of the invention can be achieved by the following technical scheme:
one of the technical schemes of the invention provides an electrolytic tank device, which comprises an electrolytic tank body and a plurality of alkali liquid water electrolysis units which are arranged in sequence and are arranged in the electrolytic tank body, wherein each alkali liquid water electrolysis unit comprises a cathode plate, a cathode net, a diaphragm, an anode net and an anode plate which are arranged in sequence, and a cathode cell reaction channel, an anode cell reaction channel, an alkali liquid inlet chamber, a hydrogen separation chamber, an oxygen separation chamber, a cathode liquid dropping channel and an anode liquid dropping channel which are processed or formed according to alkali liquid flowing characteristics.
Further, the lye inlet chamber, the cathode small chamber reaction channel, the hydrogen separation chamber and the cathode liquid-reducing channel are sequentially communicated and form a cathode lye natural circulation loop, the lye inlet chamber, the anode small chamber reaction channel, the oxygen separation chamber and the anode liquid-reducing channel are sequentially communicated and form an anode lye natural circulation loop, and a circulating cooling water channel is formed between a cathode plate and an anode plate which are oppositely arranged in two adjacent lye electrolysis units.
Further, the cathode microchamber reaction channel is formed by one side of the cathode plate, the cathode net and one side of the diaphragm.
Further, the anode cell reaction channel is formed by one side of the anode plate, the anode net and the other side of the diaphragm.
Further, the cathode liquid-reducing channel, the anode liquid-reducing channel and the circulating cooling water channel are mutually independent and are positioned on the same side of the cathode plate or the anode plate.
Further, the circulating cooling water channel is arranged in the middle area of the cathode plate and the anode plate.
Furthermore, the middle positions of the top and the bottom of the cathode plate and the anode plate are respectively provided with a circulating cooling water outlet chamber and a circulating cooling water inlet chamber, and the circulating cooling water outlet chamber and the circulating cooling water inlet chamber are respectively connected with the upper end and the lower end of the circulating cooling water channel.
Furthermore, the front and back surfaces of the cathode plate and the anode plate are provided with patterns, and the shapes of the patterns meet the requirements of fluid distribution and heat exchange.
Further, the alkali liquor inlet chambers at the bottoms of the cathode plate and the anode plate are integrated into a whole chamber;
or the lye inlet chamber is divided into a cathode lye inlet chamber and an anode lye inlet chamber which correspond to the cathode plate and the anode plate respectively, at the moment, the cathode lye inlet chamber is communicated with the anode liquid-reducing channel, and the anode lye inlet chamber is communicated with the cathode liquid-reducing channel.
Further, the alkaline water electrolysis unit also comprises a pole frame for fixing the cathode plate and the anode plate, and a gasket arranged between the two pole frames for sealing.
Further, the connection positions of the cathode cell reaction channel and the hydrogen separation chamber, and the anode cell reaction channel and the oxygen separation chamber satisfy the following conditions: the alkali solution containing hydrogen and oxygen generated from the cathode cell reaction channel and the anode cell reaction channel enter the hydrogen separation chamber and the oxygen separation chamber from the upper part respectively.
The second technical scheme of the invention provides an alkaline water electrolysis method, which is based on the built-in self-circulation heat exchange multi-system integrated efficient electrolytic tank device, and comprises the following steps:
(1) When the cathode plate and the anode plate are electrified, alkali liquor enters the cathode small chamber reaction channel and the anode small chamber reaction channel from the alkali liquor inlet chamber respectively, and electrolysis is carried out on the surfaces of the cathode net and the anode net respectively to generate hydrogen and oxygen, so that alkali liquor containing hydrogen bubbles and alkali liquor containing oxygen bubbles are obtained;
(2) The alkali liquor containing hydrogen bubbles and the alkali liquor containing oxygen bubbles respectively ascend along the cathode cell reaction channel and the anode cell reaction channel to enter the hydrogen separation chamber and the oxygen separation chamber for gas-liquid separation, and the separated alkali liquor phase respectively returns the night channel to the alkali liquor inlet chamber through the cathode liquid dropping channel and the anode, so that a cathode alkali liquor natural circulation loop and an anode alkali liquor natural circulation loop are formed by means of the density difference of the gas-liquid two phases;
(3) The circulating cooling water in the circulating cooling water channel continuously runs to take away heat generated by electrolytic reaction on the cathode plate and the anode plate.
Compared with the traditional alkaline water electrolysis device, the self-circulation multi-system integrated design can reduce the complexity of the water electrolysis system; the construction cost of the water electrolysis system can be reduced by 20-30%; the occupied area of the water electrolysis system can be reduced; the liquid holdup of alkali liquor in the water electrolysis system can be reduced, so that the initial KOH input amount is saved, the discharge amount of waste alkali liquor in the later stage is reduced, and the heating time of the starting alkali liquor is saved; the operation efficiency of the water electrolysis tank can be improved through the heat management design; according to the requirement, the water heater can also generate hot water at 90-110 ℃, so that the utilization efficiency of the waste heat of the water electrolysis is greatly improved.
Drawings
FIG. 1 is a flow chart of conventional lye electrolysis water;
FIG. 2 is a schematic view of an electrolytic process according to the present invention;
FIG. 3 is a schematic view of the structure of the alkaline water electrolysis unit of the invention;
FIG. 4 is a schematic diagram showing the structure of the alkaline aqueous electrolysis unit in example 1;
FIG. 5 is a schematic diagram showing the structure of the alkaline aqueous electrolysis unit in example 2;
FIG. 6 is a schematic diagram showing the structure of an alkaline aqueous electrolysis unit in example 3;
the figure indicates:
1 ' -electrolytic tank, 2 ' -oxygen separator and 3 ' -hydrogen separator;
the electrolytic cell comprises a 1-electrolytic cell body, a 2-negative plate, a 3-positive plate, a 4-diaphragm, a 5-negative electrode net, a 6-positive electrode net, a 7-negative electrode cell reaction channel, an 8-positive electrode cell reaction channel, a 901-positive electrode lye inlet chamber, a 902-negative electrode lye inlet chamber, a 10-hydrogen separation chamber, a 11-oxygen separation chamber, a 12-negative electrode liquid dropping channel, a 13-positive electrode liquid dropping channel, a 14-circulating cooling water channel, a 15-circulating cooling water outlet chamber, a 16-circulating cooling water inlet chamber and a 17-polar frame.
Detailed Description
The invention will now be described in detail with reference to the drawings and specific examples. The present embodiment is implemented on the premise of the technical scheme of the present invention, and a detailed implementation manner and a specific operation process are given, but the protection scope of the present invention is not limited to the following examples.
In the following embodiments or examples, unless otherwise specified, functional components or structures are indicated as conventional components or structures employed in the art to achieve the corresponding functions.
In order to reduce the complexity of a water electrolysis system, reduce the liquid holdup of alkali liquor in the water electrolysis system, improve the operation efficiency and the utilization efficiency of a water electrolysis tank and the like, the invention provides an electrolysis tank device, the structure of which can be seen in fig. 2 to 6 and the like, and comprises an electrolysis tank body 1 and a plurality of alkali liquor electrolysis units which are arranged in sequence and are arranged in the electrolysis tank body 1, each alkali liquor electrolysis unit comprises a cathode plate 2, a cathode net 5, a diaphragm 4, an anode net 6 and an anode plate 3 which are arranged in sequence, and a cathode cell reaction channel 7, an anode cell reaction channel 8, an alkali liquor inlet chamber, a hydrogen separation chamber 10, an oxygen separation chamber 11, a cathode liquid reduction channel 12 and an anode liquid reduction channel 13 which are processed or formed according to the alkali liquor flow characteristics, wherein the alkali liquor inlet chamber, the cathode cell reaction channel 7, the hydrogen separation chamber 10 and the cathode liquid reduction channel 12 are sequentially communicated and form a cathode alkali liquor natural circulation loop, and the alkali liquor inlet chamber 8, the oxygen separation chamber 11 and the anode liquid reduction channel 13 are sequentially communicated and form an anode liquor natural circulation loop, and a cooling water channel 14 is formed between the two anode plate units 2 and the anode plate 3 which are arranged oppositely.
In some specific embodiments, the cathode cell reaction channel 7 is formed by one side of the cathode plate 2, the cathode net 5 and one side of the diaphragm 4, which mainly provides necessary areas for cathode water electrolysis reaction, and the alkaline solution entrains the hydrogen generated on the surface of the cathode net 5 to enter the hydrogen separation chamber 10 at the upper part of the polar plate along the cathode cell electrolysis reaction channel. In some embodiments, the anode cell reaction channel 8 is formed by one side of the anode plate 3, the anode mesh 6 and the other side of the membrane 4, which mainly provides a necessary area for the anode water electrolysis reaction, and the alkaline solution entrains the oxygen generated on the surface of the anode mesh 6 to enter the oxygen separation chamber 11 at the upper part of the anode plate along the cathode cell electrolysis reaction channel. Here, the structure of the cathode and anode microchamber may refer to, but is not limited to, the structures illustrated in fig. 4 to 6.
In some specific embodiments, the cathode liquid-reducing channel 12, the anode liquid-reducing channel 13 and the circulating cooling water channel 14 are independent from each other and are located on the same side of the cathode plate 2 or the anode plate 3. In addition, the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 are channels formed by the opposite sides of the part of cathode plate 2 and the part of anode plate 3, alkali liquid after flash evaporation in the oxyhydrogen separation chamber enters the alkali liquid inlet chamber through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively, two alkali liquids can be fully mixed in the alkali liquid inlet chamber, the concentration of the alkali liquid after mixing becomes uniform, and the problem of polarization of the alkali liquid can be eliminated in the electrolytic tank by the design.
In some embodiments, the cathode plate 2 and the anode plate 3 are provided with patterns on both sides, and the patterns are shaped to meet the requirements of fluid distribution and heat exchange. In particular, the pattern is mainly to provide fluid channels for alkaline solution and hydrogen and oxygen generated by electrolysis. The pattern is similar to the principle of a plate-frame heat exchanger, so that more heat exchange area can be provided, and the pattern is an effective measure for forced heat transfer, so that the heat exchange efficiency of alkali liquor can be improved, and the temperature distribution of the alkali liquor in an electrolysis reaction channel of a cathode/anode cell is similar to isothermal distribution.
In some specific embodiments, the circulating cooling water channel 14 is disposed in a middle region of the cathode plate 2 and the anode plate 3. In addition, the middle positions of the top and bottom of the cathode plate 2 and the anode plate 3 may be respectively provided with a circulating cooling water outlet chamber 15 and a circulating cooling water inlet chamber 16, and the circulating cooling water outlet chamber 15 and the circulating cooling water inlet chamber 16 are respectively connected with the upper and lower ends of the circulating cooling water channel 14. The circulating cooling water enters from the circulating cooling water inlet chamber 16 at the bottom of the bipolar plate, and the heat generated by the cathode/anode small-chamber electrolytic reaction channels at the two sides is removed through the circulating water cooling channels, so that the design requirements that the operation temperature of alkali liquor in the cathode/anode small-chamber electrolytic reaction channels is maintained at 60-130 ℃ and the like can be ensured. Specifically, the temperature of the circulating cooling backwater is controlled to be 40-110 ℃ by controlling the flow of the circulating cooling water in cascade with the temperature of the alkali liquor.
In some embodiments, the lye inlet chambers at the bottom of the cathode plate 2 and the anode plate 3 are integrated into one integral chamber; the lye inlet chamber mainly provides a mixing buffer space for lye from the negative/positive liquid reduction channel and is also a lye inlet of the electrolytic reaction channel of the negative/positive small chamber. Thus, the mutual return of yin and yang can be realized, and concentration polarization in the operation process is avoided.
In some specific embodiments, the lye inlet chamber is divided into a cathode lye inlet chamber 902 and an anode lye inlet chamber 901 corresponding to the cathode plate 2 and the anode plate 3 respectively, at this time, the cathode lye inlet chamber 902 is communicated with the anode liquid-reducing channel 13, and the anode lye inlet chamber 901 is communicated with the cathode liquid-reducing channel 12, which can also achieve the effect of eliminating the polarization phenomenon of lye in the electrolysis process.
In some embodiments, the lye water electrolysis unit further comprises a polar frame 17 for fixing the cathode plate 2 and the anode plate 3, and a gasket for sealing arranged between the polar frames 17.
In more specific embodiments, the material of the pole frame 17 may be an insulating nonmetallic material or a metallic material according to the actual construction cost. When the electrode frame 17 is made of insulating materials, higher Faraday efficiency can be obtained, and the unit hydrogen production energy consumption and the total amount of equipment are reduced, so that the civil engineering cost is reduced. However, due to the strength of the non-metallic material, the operating pressure of the electrolyzer is limited, and due to the non-metallic material, a gasket is required to seal the electrode frame 17 from the back cushion sheet. The long-term use may result in fusion of two materials, which makes it difficult to reuse the pole frame 17, and increases maintenance cost; when a metal material is used for the pole frame 17, although the operating pressure of the electrolyzer can be increased, this will increase stray currents and reduce faraday efficiency. An insulating part is required to be arranged on the alkaline liquor channel of the polar plate to reduce stray current, so that Faraday efficiency is improved. The design difficulty and complexity of the polar plate are also increased. The electrode frame 17 is made of a metal material, and the sealing gasket does not penetrate into the metal electrode frame 17 even after long-term use. Therefore, the metal pole frame 17 can be repeatedly used, and the later maintenance cost is reduced.
In some specific embodiments, the connection positions of the cathode cell reaction channel 7 and the hydrogen separation chamber 10, and the anode cell reaction channel 8 and the oxygen separation chamber 11 satisfy: the alkaline solution containing hydrogen and oxygen generated from the cathode cell reaction channel 7 and the anode cell reaction channel 8 enter the hydrogen separation chamber 10 and the oxygen separation chamber 11 from the upper part, respectively. Specifically, the hydrogen separation chamber 10 and the oxygen separation chamber 11 can be divided into an upper gas space and a lower alkali solution space, and alkali solution containing corresponding hydrogen or oxygen enters the upper gas space to be flashed, so that gas-liquid separation is realized.
In some specific embodiments, the cathode plate 2 and the anode plate 3 are made of materials only required to meet the requirement of alkali liquid corrosion resistance. For example, an austenitic stainless steel material such as 304L/316L/310 may be used, and nickel plating may be performed on carbon steel, pure nickel, or the like. Meanwhile, the shape of the material can be square or round, can also be other shapes, is not influenced by the shape, and can take various forms. The flow channels on the plates are simply fluid distribution and increase heat transfer area, so any form of improvement in flow channels on the plates is going toward these directions.
The second technical scheme of the invention provides a built-in self-circulation heat exchange multi-system integrated efficient electrolysis method, which is based on the built-in self-circulation heat exchange multi-system integrated efficient electrolysis tank device, and comprises the following steps:
(1) When the cathode plate 2 and the anode plate 3 are electrified, alkali liquor enters the cathode small chamber reaction channel 7 and the anode small chamber reaction channel 8 from the alkali liquor inlet chamber respectively, and electrolysis occurs on the surfaces of the cathode net 5 and the anode net 6 respectively to generate hydrogen and oxygen, so that alkali liquor containing hydrogen bubbles and alkali liquor containing oxygen bubbles are obtained;
(2) The alkali liquor containing hydrogen bubbles and the alkali liquor containing oxygen bubbles respectively ascend along the cathode small chamber reaction channel 7 and the anode small chamber reaction channel 8 to enter the hydrogen separation chamber 10 and the oxygen separation chamber 11 for gas-liquid separation, and the separated alkali liquor phase respectively returns the night channel to the alkali liquor inlet chamber through the cathode liquid dropping channel 12 and the anode, so that a cathode alkali liquor natural circulation loop and an anode alkali liquor natural circulation loop are formed by means of the density difference of the gas-liquid two phases;
(3) The circulating cooling water in the circulating cooling water channel 14 continuously runs to take away heat generated by the electrolytic reaction on the cathode plate 2 and the anode plate 3.
The above embodiments may be implemented singly or in any combination of two or more.
The above embodiments are described in more detail below in connection with specific examples.
Example 1:
the structure shown in fig. 2 and 3 is adopted.
The self-circulation multi-system integrated electrolytic cell of the embodiment consists of a pole frame 17, a cathode plate 2, an anode plate 3, a cathode, an anode, a gasket and a diaphragm 4.
The operating pressure of the electrolytic cell is 1bar to 1.5bar, and the shape of the polar plate is square. In order to avoid the problem of polarization of alkaline solution at the anode and cathode, the embodiment adopts that cathode alkaline solution returns to the anode alkaline solution inlet chamber 901 through the anode liquid dropping channel 13, and anode alkaline solution returns to the cathode alkaline solution inlet chamber 902 through the cathode liquid dropping channel 12.
The main purpose of the electrode frame 17 of the present embodiment is to fix the cathode plate 2 and the anode plate 3, thereby forming a cathode and anode cell. Meanwhile, the design of the pole frame 17 needs to bear certain internal pressure so as to meet the operation pressure of the electrolytic cell. The material of the pole frame 17 can be insulated nonmetallic material or metallic material according to the condition of the actual construction cost. When the electrode frame 17 is made of insulating materials, higher Faraday efficiency can be obtained, and the unit hydrogen production energy consumption and the total amount of equipment are reduced, so that the civil engineering cost is reduced. However, due to the strength of the non-metallic material, the operating pressure of the electrolyzer is limited, and due to the non-metallic material, a gasket is required to seal the electrode frame 17 from the back cushion sheet. The long-term use may result in fusion of two materials, which makes it difficult to reuse the pole frame 17, and increases maintenance cost; when a metal material is used for the pole frame 17, although the operating pressure of the electrolyzer can be increased, this will increase stray currents and reduce faraday efficiency. An insulating member is required to be provided on the alkaline channel of the plate to reduce stray current and thereby improve faraday efficiency. The design difficulty and complexity of the polar plate are also increased. The electrode frame 17 is made of a metal material, and the gasket for sealing does not penetrate into the metal electrode frame 17 even after long-term use. Therefore, the metal pole frame 17 can be repeatedly used, and the maintenance cost in the later period is reduced.
The present embodiment provides a cathode plate 2 and an anode plate 3. Different flow channels are arranged on the front surface and the back surface of the cathode plate 2 and the anode plate 3, as shown in figure 3. The cathode plate 2 and the diaphragm 4 form a cathode cell, and a cathode net 5 is arranged between the cathode plate 2 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the cathode net 5 through the channel of the cathode subchamber (namely the cathode subchamber reaction channel 7) to generate hydrogen, and the generated hydrogen is desorbed from the surface of the cathode net 5 in the form of bubbles and enters the alkali liquor. Similarly, the anode plate 3 and the diaphragm 4 form an anode cell, and an anode net 6 is arranged between the anode plate 3 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the anode net 6 through the passage of the anode microchamber (namely the anode microchamber reaction passage 8) to generate oxygen, and the generated oxygen is desorbed from the surface of the anode net 6 in the form of bubbles and enters the alkali liquor.
The passage formed between the cathode plate 2 and the anode plate 3 is a circulating cooling water passage 14. The heat generated by the electrolysis reaction is removed by circulating cooling water so as to ensure that the distribution of the operating temperature of the alkali liquor in the cathode/anode cell is in a quasi-isothermal reaction state. The operation temperature of the alkali liquor chamber can be freely controlled at 60-130 ℃, so that the diaphragm 4 is prevented from being damaged by local high temperature. The temperature of the circulating cooling water can be regulated according to different use conditions, and if a low-pressure steam user exists at the downstream, the backwater temperature of the circulating cooling water can be regulated to 90-110 ℃. The circulating cooling water at this temperature can be used downstream by a low temperature waste heat recovery process to produce 1 to 10barg steam.
The bipolar plate formed by the anode plate 3 and the cathode plate 2 is provided with an alkali liquor inlet chamber and a circulating cooling water chamber (namely a circulating water inlet chamber) at the bottom. The bottom of the lye inlet chamber is provided with a channel which is respectively communicated with the liquid phase outlets of the hydrogen separation chamber 10 and the oxygen separation chamber 11 which are arranged at the top of the bipolar plate. The channel connected to the hydrogen separation chamber 10 is called a cathode fall channel 12, and the channel connected to the oxygen separation chamber 11 is called an anode fall channel 13. The cathode fall passage 12, the anode fall passage 13 are arranged on the same side as the circulation cooling water passage 14, but they are not connected to the circulation cooling water passage 14.
In the electrolysis process, alkaline solution containing hydrogen and oxygen generated in the cathode and anode chambers enters the upper parts of the hydrogen separation chamber 10 and the oxygen separation chamber 11 at the top of the bipolar plate for gas-liquid separation. The separated lye liquid phase returns to the lye inlet chamber at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively. By means of the density difference between the gas phase and the liquid phase, alkali liquor circulation is naturally formed, so that the forced circulation design of the traditional electrolytic tank can be canceled. The purpose of self-circulation integrated design is achieved.
The patent of the embodiment adopts an integrated design. In order to avoid the polarization phenomenon of electrolyte in the electrolysis process, the lye separated by the hydrogen separation chamber 10 and the oxygen separation chamber 11 is returned to the lye inlet chamber at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively to be mixed, and then flows into the cathode and anode small chambers from the outlet of the lye inlet chamber to carry out the water electrolysis reaction.
The cathode plate 2 and the anode plate 3 can be made of corrosion-resistant stainless steel. For example 304L/316L/310. The nickel plating can also be performed by carbon steel, or pure nickel or other materials resistant to high temperature and high concentration alkali lye (usually 0-45% potassium hydroxide or sodium hydroxide).
In order to achieve the aim of the invention, the embodiment directly designs the hydrogen-oxygen separator unit, the circulating pipeline unit and the alkali liquor heat exchange unit in the traditional alkali liquor electrolysis system into a device in the electrolytic bath equipment in a highly concentrated and integrated way. Compared with the traditional alkali liquor electrolysis device, the self-circulation multi-system integrated design of the embodiment can reduce the complexity of a water electrolysis system; the construction cost of the water electrolysis system can be reduced by 20-30%; the occupied area of the water electrolysis system can be reduced; the operation efficiency of the water electrolysis tank can be improved through the heat management design; the hot water with the temperature of 90-110 ℃ can be generated, and the utilization efficiency of the waste heat of the water electrolysis is greatly improved.
Example 2:
the structure shown in fig. 2 and 4 is adopted.
The self-circulation multi-system integrated electrolytic tank of the embodiment consists of a pole frame 17, a cathode plate 2, an anode plate 3, a cathode, an anode, a gasket and a diaphragm 4.
The operating pressure of the electrolytic cell is 1bar to 1.5bar, and the shape of the polar plate is square. In order to avoid the problem of polarization of the alkaline solution at the cathode and the anode, the alkaline solution is mixed by the anode liquid-dropping channel 13 and the cathode liquid-dropping channel 12 and then returned to the cathode alkaline solution inlet chamber 901 respectively.
The main purpose of the electrode frame 17 of the present embodiment is to fix the cathode plate 2 and the anode plate 3, thereby forming a cathode and anode cell. Meanwhile, the design of the pole frame 17 needs to bear certain internal pressure so as to meet the operation pressure of the electrolytic cell. The material of the pole frame 17 can be insulated nonmetallic material or metallic material according to the condition of the actual construction cost. When the electrode frame 17 is made of insulating materials, higher Faraday efficiency can be obtained, and the unit hydrogen production energy consumption and the total amount of equipment are reduced, so that the civil engineering cost is reduced. However, due to the strength of the non-metallic material, the operating pressure of the electrolyzer is limited, and due to the non-metallic material, a gasket is required to seal the electrode frame 17 from the back cushion sheet. The long-term use may result in fusion of two materials, which makes it difficult to reuse the pole frame 17, and increases maintenance cost; when a metal material is used for the pole frame 17, although the operating pressure of the electrolyzer can be increased, this will increase stray currents and reduce faraday efficiency. An insulating part is required to be arranged on the alkaline liquor channel of the polar plate to reduce stray current, so that Faraday efficiency is improved. The design difficulty and complexity of the polar plate are also increased. The electrode frame 17 is made of a metal material, and the sealing gasket does not penetrate into the metal electrode frame 17 even after long-term use. Therefore, the metal pole frame 17 can be repeatedly used, and the later maintenance cost is reduced.
The present embodiment provides a cathode plate 2 and an anode plate 3. Different flow channels are arranged on the front and back surfaces of the cathode plate 2 and the anode plate 3, as shown in fig. 4. The cathode plate 2 and the diaphragm 4 form a cathode cell, and a cathode net 5 is arranged between the cathode plate 2 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the cathode net 5 through the channel of the cathode subchamber (namely the cathode subchamber reaction channel 7) to generate hydrogen, and the generated hydrogen is desorbed from the surface of the cathode net 5 in the form of bubbles and enters the alkali liquor. Similarly, the anode plate 3 and the diaphragm 4 form an anode cell, and an anode net 6 is arranged between the anode plate 3 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the anode net 6 through the passage of the anode microchamber (namely the anode microchamber reaction passage 8) to generate oxygen, and the generated oxygen is desorbed from the surface of the anode net 6 in the form of bubbles and enters the alkali liquor.
The passage formed between the cathode plate 2 and the anode plate 3 is a circulating cooling water passage 14. The heat generated by the electrolysis reaction is removed by circulating cooling water, so that the distribution of the operation temperature of the alkali liquor in the yin-yang small chamber is in a similar isothermal reaction state. The operation temperature of the alkali liquor chamber can be freely controlled at 60-130 ℃, so that the diaphragm 4 is prevented from being damaged by local high temperature. The temperature of the circulating cooling water can be regulated according to different use conditions, and if a low-pressure steam user exists at the downstream, the backwater temperature of the circulating cooling water can be regulated to 90-110 ℃. The circulating cooling water at this temperature can be used downstream by a low temperature waste heat recovery process to produce 1 to 10barg steam.
The bipolar plate consisting of the anode plate 3 and the cathode plate 2 is respectively provided with a cathode lye inlet chamber 902, an anode lye inlet chamber 901 and a circulating cooling water chamber at the bottom. The bottoms of the cathode lye inlet chamber 902 and the anode lye inlet chamber 901 are provided with channels which are respectively communicated with a hydrogen separation chamber 10 arranged at the top of the bipolar plate and a liquid phase outlet of an oxygen separation chamber 11. The channel connected with the hydrogen separation chamber 10 is called a cathode liquid-dropping channel 12, and the cathode liquid-dropping channel 12 is connected with the anode lye inlet chamber 901; the channel connected to the oxygen separation chamber 11 is called the anode drop channel 13, and the anode drop channel 13 is connected to the cathode lye inlet chamber 902. The cathode fall passage 12, the anode fall passage 13 are arranged on the same side as the circulation cooling water passage 14, but they are not connected to the circulation cooling water passage 14.
In the electrolysis process, alkaline solution containing hydrogen and oxygen is generated in the cathode and anode small chambers and enters the hydrogen-oxygen separation chamber 11 at the top of the bipolar plate and the upper part of the oxygen separation chamber 11 respectively for gas-liquid separation. The separated lye liquid phase returns to the lye inlet chamber at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively. By means of the density difference between the gas phase and the liquid phase, alkali liquor circulation is naturally formed, so that the forced circulation design of the traditional electrolytic tank can be canceled. The purpose of self-circulation integrated design is achieved.
The patent of the embodiment adopts an integrated design. In order to avoid electrolyte polarization during the electrolysis process, the lye separated by the hydrogen separation chamber 10 and the oxygen separation chamber 11 returns to the anode/cathode lye inlet chamber 902 at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively, and then flows into the cathode/anode chamber from the outlet of the cathode/anode lye inlet chamber 901 for water electrolysis reaction.
The cathode plate 2 and the anode plate 3 can be made of corrosion-resistant stainless steel. For example 304L/316L/310. The nickel plating can also be performed by carbon steel, or pure nickel or other materials resistant to high temperature and high concentration alkali lye (usually 0-45% potassium hydroxide or sodium hydroxide).
In order to achieve the aim of the invention, the embodiment directly designs the hydrogen-oxygen separator unit, the circulating pipeline unit and the alkali liquor heat exchange unit in the traditional alkali liquor electrolysis system into a device in the electrolytic bath equipment in a highly concentrated and integrated way. Compared with the traditional alkali liquor electrolysis device, the self-circulation multi-system integrated design of the embodiment can reduce the complexity of a water electrolysis system; the construction cost of the water electrolysis system can be reduced by 20-30%; the occupied area of the water electrolysis system can be reduced; the operation efficiency of the water electrolysis tank can be improved through the heat management design; the hot water with the temperature of 90-110 ℃ can be generated, and the utilization efficiency of the waste heat of the water electrolysis is greatly improved.
Example 3:
the structure shown in fig. 2 and fig. 5 is adopted.
The self-circulation multi-system integrated electrolytic tank of the embodiment consists of a pole frame 17, a cathode plate 2, an anode plate 3, a cathode, an anode, a gasket and a diaphragm 4.
The operating pressure of the electrolytic cell is 1-30 bar, and the shape of the polar plate is circular. In order to avoid the problem of polarization of the alkaline solution at the cathode and the anode, the cathode alkaline solution is mixed by the anode liquid dropping channel 13 and the cathode liquid dropping channel 12 and then returned to the cathode alkaline solution inlet chamber 901 respectively.
The main purpose of the electrode frame 17 of the present embodiment is to fix the cathode and anode plates 3, thereby forming a cathode and anode chamber. Meanwhile, the design of the pole frame 17 needs to bear certain internal pressure so as to meet the operation pressure of the electrolytic cell. The material of the pole frame 17 can be insulated nonmetallic material or metallic material according to the condition of the actual construction cost. When the electrode frame 17 is made of insulating materials, higher Faraday efficiency can be obtained, and the unit hydrogen production energy consumption and the total amount of equipment are reduced, so that the civil engineering cost is reduced. However, due to the strength of the non-metallic material, the operating pressure of the electrolyzer is limited, and due to the non-metallic material, a gasket is required to seal the electrode frame 17 from the back cushion sheet. The long-term use may result in fusion of two materials, which makes it difficult to reuse the pole frame 17, and increases maintenance cost; when a metal material is used for the pole frame 17, although the operating pressure of the electrolyzer can be increased, this will increase stray currents and reduce faraday efficiency. An insulating part is required to be arranged on the alkaline liquor channel of the polar plate to reduce stray current, so that Faraday efficiency is improved. The design difficulty and complexity of the polar plate are also increased. The electrode frame 17 is made of a metal material, and the sealing gasket does not penetrate into the metal electrode frame 17 even after long-term use. Therefore, the metal pole frame 17 can be repeatedly used, and the later maintenance cost is reduced.
The present embodiment provides a cathode plate 2 and an anode plate 3. Different flow channels are arranged on the front and back surfaces of the cathode plate 2 and the anode plate 3, as shown in fig. 5. The cathode plate 2 and the diaphragm 4 form a cathode cell, and a cathode net 5 is arranged between the cathode plate 2 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the cathode net 5 through the channel of the cathode subchamber (namely the cathode subchamber reaction channel 7) to generate hydrogen, and the generated hydrogen is desorbed from the surface of the cathode net 5 in the form of bubbles and enters the alkali liquor. Similarly, the anode plate 3 and the diaphragm 4 form an anode cell, and an anode net 6 is arranged between the anode plate 3 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the anode net 6 through the passage of the anode microchamber (namely the anode microchamber reaction passage 8) to generate oxygen, and the generated oxygen is desorbed from the surface of the anode net 6 in the form of bubbles and enters the alkali liquor.
The passage formed between the cathode plate 2 and the anode plate 3 is a circulating cooling water passage 14. The heat generated by the electrolysis reaction is removed by circulating cooling water, so that the distribution of the operation temperature of the alkali liquor in the yin-yang small chamber is in a similar isothermal reaction state. The operation temperature of the alkali liquor chamber can be freely controlled at 60-130 ℃, so that the diaphragm 4 is prevented from being damaged by local high temperature. The temperature of the circulating cooling water can be regulated according to different use conditions, and if a low-pressure steam user exists at the downstream, the backwater temperature of the circulating cooling water can be regulated to 90-110 ℃. The circulating cooling water at this temperature can be used downstream by a low temperature waste heat recovery process to produce 1 to 10barg steam.
The bipolar plate bottom formed by the anode plate 3 and the cathode plate 2 is respectively provided with a cathode-anode lye inlet chamber 901 and a circulating cooling water chamber. The bottom of the cathode and anode lye inlet chamber 901 is provided with a channel which is respectively communicated with the liquid phase outlet of the oxyhydrogen gas separation chamber 11 arranged at the top of the bipolar plate. The channel connected with the hydrogen separation chamber 10 is called a cathode liquid-dropping channel 12, and the cathode liquid-dropping channel 12 is connected with the anode lye inlet chamber 901; the channel connected to the oxygen separation chamber 11 is called the anode drop channel 13, and the anode drop channel 13 is connected to the cathode lye inlet chamber 902. The cathode fall passage 12, the anode fall passage 13 are arranged on the same side as the circulation cooling water passage 14, but they are not connected to the circulation cooling water passage 14.
In the electrolysis process, alkali liquor containing hydrogen and oxygen generated in the cathode and anode chambers enters the upper part of the hydrogen and oxygen separation chamber 11 at the top of the bipolar plate for gas-liquid separation. The separated lye liquid phase returns to the lye inlet chamber at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively. By means of the density difference between the gas phase and the liquid phase, alkali liquor circulation is naturally formed, so that the forced circulation design of the traditional electrolytic tank can be canceled. The purpose of self-circulation integrated design is achieved.
The patent of the embodiment adopts an integrated design. In order to avoid electrolyte polarization during the electrolysis process, the lye separated by the hydrogen separation chamber 10 and the oxygen separation chamber 11 returns to the anode/cathode lye inlet chamber 902 at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively, and then flows into the cathode/anode chamber from the outlet of the cathode/anode lye inlet chamber 901 for water electrolysis reaction.
The cathode plate 2 and the anode plate 3 can be made of corrosion-resistant stainless steel. For example 304L/316L/310. The nickel plating can also be performed by carbon steel, or pure nickel or other materials resistant to high temperature and high concentration alkali lye (usually 0-45% potassium hydroxide or sodium hydroxide).
In order to achieve the aim of the invention, the embodiment directly designs the hydrogen-oxygen separator unit, the circulating pipeline unit and the alkali liquor heat exchange unit in the traditional alkali liquor electrolysis system into a device in the electrolytic bath equipment in a highly concentrated and integrated way. Compared with the traditional alkali liquor electrolysis device, the self-circulation multi-system integrated design of the embodiment can reduce the complexity of a water electrolysis system; the construction cost of the water electrolysis system can be reduced by 20-30%; the occupied area of the water electrolysis system can be reduced; the operation efficiency of the water electrolysis tank can be improved through the heat management design; the hot water with the temperature of 90-110 ℃ can be generated, and the utilization efficiency of the waste heat of the water electrolysis is greatly improved.
Example 4:
the structure shown in fig. 2 and fig. 6 is adopted.
This example is identical to example 3 in its composition except that the plate form is replaced with the structure of fig. 6.
The self-circulation multi-system integrated electrolytic tank of the embodiment consists of a pole frame 17, a cathode plate 2, an anode plate 3, a cathode, an anode, a gasket and a diaphragm 4.
The operating pressure of the electrolytic cell is 1bar to 30bar, and the shape of the polar plate is round. In order to avoid the problem of polarization of alkaline solution at the anode and cathode, the embodiment adopts that cathode alkaline solution returns to the anode alkaline solution inlet chamber 901 through the anode liquid dropping channel 13, and anode alkaline solution returns to the cathode alkaline solution inlet chamber 902 through the cathode liquid dropping channel 12.
The main purpose of the electrode frame 17 of the present embodiment is to fix the cathode and anode plates 3, thereby forming a cathode and anode chamber. Meanwhile, the design of the pole frame 17 needs to bear certain internal pressure so as to meet the operation pressure of the electrolytic cell. The material of the pole frame 17 can be insulated nonmetallic material or metallic material according to the condition of the actual construction cost. When the electrode frame 17 is made of insulating materials, higher Faraday efficiency can be obtained, and the unit hydrogen production energy consumption and the total amount of equipment are reduced, so that the civil engineering cost is reduced. However, due to the strength of the non-metallic material, the operating pressure of the electrolyzer is limited, and due to the non-metallic material, a gasket is required to seal the electrode frame 17 from the back cushion sheet. The long-term use may result in fusion of two materials, which makes it difficult to reuse the pole frame 17, and increases maintenance cost; when a metal material is used for the pole frame 17, although the operating pressure of the electrolyzer can be increased, this will increase stray currents and reduce faraday efficiency. An insulating part is required to be arranged on the alkaline liquor channel of the polar plate to reduce stray current, so that Faraday efficiency is improved. The design difficulty and complexity of the polar plate are also increased. The electrode frame 17 is made of a metal material, and the sealing gasket does not penetrate into the metal electrode frame 17 even after long-term use. Therefore, the metal pole frame 17 can be repeatedly used, and the later maintenance cost is reduced.
The present embodiment provides a cathode plate 2 and an anode plate 3. Different flow channels are arranged on the front and back surfaces of the cathode plate 2 and the anode plate 3, as shown in fig. 6. The cathode plate 2 and the diaphragm 4 form a cathode cell, and a cathode net 5 is arranged between the cathode plate 2 and the diaphragm 4. When the polar plate is electrified, the alkali liquor is subjected to electrochemical reaction on the surface of the cathode net 5 through the channel of the cathode subchamber to generate hydrogen, and the generated hydrogen is desorbed from the surface of the cathode net 5 in the form of bubbles and enters the alkali liquor. Similarly, the anode plate 3 and the diaphragm 4 form an anode cell, and an anode net 6 is arranged between the anode plate 3 and the diaphragm 4. When the polar plate is electrified, alkali liquor is subjected to electrochemical reaction on the surface of the anode net 6 through the passage of the anode microchamber (namely the anode microchamber reaction passage 8) to generate oxygen, and the generated oxygen is desorbed from the surface of the anode net 6 in the form of bubbles and enters the alkali liquor.
The passage formed between the cathode plate 2 and the anode plate 3 is a circulating cooling water passage 14. The heat generated by the electrolysis reaction is removed by circulating cooling water, so that the distribution of the operation temperature of the alkali liquor in the yin-yang small chamber is in a similar isothermal reaction state. The operation temperature of the alkali liquor chamber can be freely controlled at 60-130 ℃, so that the diaphragm 4 is prevented from being damaged by local high temperature. The temperature of the circulating cooling water can be regulated according to different use conditions, and if a low-pressure steam user exists at the downstream, the backwater temperature of the circulating cooling water can be regulated to 90-110 ℃. The circulating cooling water at this temperature can be used downstream by a low temperature waste heat recovery process to produce 1 to 10barg steam.
The bipolar plate bottom formed by the anode plate 3 and the cathode plate 2 is respectively provided with a cathode-anode lye inlet chamber 901 and a circulating cooling water chamber. The bottom of the cathode and anode lye inlet chamber 901 is provided with a channel which is respectively communicated with the liquid phase outlet of the oxyhydrogen gas separation chamber 11 arranged at the top of the bipolar plate. The channel connected with the hydrogen separation chamber 10 is called a cathode liquid-dropping channel 12, and the cathode liquid-dropping channel 12 is connected with the anode lye inlet chamber 901; the channel connected to the oxygen separation chamber 11 is called the anode drop channel 13, and the anode drop channel 13 is connected to the cathode lye inlet chamber 902. The cathode fall passage 12, the anode fall passage 13 are arranged on the same side as the circulation cooling water passage 14, but they are not connected to the circulation cooling water passage 14.
In the electrolysis process, alkali liquor containing hydrogen and oxygen generated in the cathode and anode chambers enters the upper part of the hydrogen and oxygen separation chamber 11 at the top of the bipolar plate for gas-liquid separation. The separated lye liquid phase returns to the lye inlet chamber at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively. By means of the density difference between the gas phase and the liquid phase, alkali liquor circulation is naturally formed, so that the forced circulation design of the traditional electrolytic tank can be canceled. The purpose of self-circulation integrated design is achieved.
The patent of the embodiment adopts an integrated design. In order to avoid electrolyte polarization during the electrolysis process, the lye separated by the hydrogen separation chamber 10 and the oxygen separation chamber 11 returns to the anode/cathode lye inlet chamber 902 at the bottom of the bipolar plate through the cathode liquid-reducing channel 12 and the anode liquid-reducing channel 13 respectively, and then flows into the cathode/anode chamber from the outlet of the cathode/anode lye inlet chamber 901 for water electrolysis reaction.
The cathode plate 2 and the anode plate 3 can be made of corrosion-resistant stainless steel. For example 304L/316L/310. The nickel plating can also be performed by carbon steel, or pure nickel or other materials resistant to high temperature and high concentration alkali lye (usually 0-45% potassium hydroxide or sodium hydroxide).
In order to achieve the aim of the invention, the embodiment directly designs the hydrogen-oxygen separator unit, the circulating pipeline unit and the alkali liquor heat exchange unit in the traditional alkali liquor electrolysis system into a device in the electrolytic bath equipment in a highly concentrated and integrated way. Compared with the traditional alkali liquor electrolysis device, the self-circulation multi-system integrated design of the embodiment can reduce the complexity of a water electrolysis system; the construction cost of the water electrolysis system can be reduced by 20-30%; the occupied area of the water electrolysis system can be reduced; the operation efficiency of the water electrolysis tank can be improved through the heat management design; the hot water with the temperature of 90-110 ℃ can be generated, and the utilization efficiency of the waste heat of the water electrolysis is greatly improved.
The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. It will be apparent to those skilled in the art that various modifications can be readily made to these embodiments and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the present disclosure, should make improvements and modifications without departing from the scope of the present invention.
Claims (10)
1. The utility model provides an electrolytic bath device which characterized in that includes the electrolysis bath body and installs a plurality of lye electrolysis units that arrange in proper order in the electrolysis bath body, every lye electrolysis unit includes negative plate, negative pole net, diaphragm, positive pole net, the positive plate that arrange in proper order to and according to the processing of lye flow characteristic or the negative pole cell reaction channel of formation, positive pole cell reaction channel, lye entry cavity, hydrogen separation cavity, oxygen separation cavity, negative pole fall liquid channel and positive pole fall liquid channel.
2. The electrolyzer unit of claim 1 characterized in that the lye inlet chamber, the cathode small chamber reaction channel, the hydrogen separation chamber and the cathode liquid-reducing channel are sequentially communicated and form a cathode lye natural circulation loop, the lye inlet chamber, the anode small chamber reaction channel, the oxygen separation chamber and the anode liquid-reducing channel are sequentially communicated and form an anode lye natural circulation loop, and a circulating cooling water channel is formed between the cathode plate and the anode plate which are oppositely arranged in two adjacent lye electrolysis units.
3. An electrolyser apparatus as claimed in claim 2 wherein the circulating cooling water channels are arranged in the central region of the cathode and anode plates.
4. An electrolyzer unit in accordance with claim 2, wherein the cathode cell reaction channels are formed by one side of the cathode plate, the cathode mesh and one side of the membrane;
the anode cell reaction channel is formed by one side of the anode plate, an anode net and the other side of the diaphragm;
the cathode liquid-reducing channel, the anode liquid-reducing channel and the circulating cooling water channel are mutually independent and are positioned on the same side of the cathode plate or the anode plate.
5. An electrolyzer unit as claimed in claim 2 in which the intermediate positions of the top and bottom of the cathode and anode plates are each provided with a circulating cooling water outlet chamber and a circulating cooling water inlet chamber respectively connected to the upper and lower ends of the circulating cooling water channel.
6. An electrolyzer unit in accordance with claim 1, wherein the cathode plate and the anode plate are each provided with a pattern on both sides thereof, the pattern being shaped to meet the requirements of providing fluid distribution and heat exchange.
7. An electrolyzer unit in accordance with claim 1, characterized in that the alkaline liquor inlet chambers at the bottom of the cathode plate and anode plate are integrated into one integral chamber;
or the lye inlet chamber is divided into a cathode lye inlet chamber and an anode lye inlet chamber which correspond to the cathode plate and the anode plate respectively, at the moment, the cathode lye inlet chamber is communicated with the anode liquid-reducing channel, and the anode lye inlet chamber is communicated with the cathode liquid-reducing channel.
8. An electrolyzer unit in accordance with claim 1, characterized in that the alkaline aqueous electrolysis unit further comprises a polar frame for fixing the cathode plate and the anode plate, and a gasket for sealing disposed between the polar frames.
9. An electrolyzer unit in accordance with claim 1, characterized in that the connection locations of the cathode cell reaction channel and the hydrogen separation chamber, the anode cell reaction channel and the oxygen separation chamber are as follows: the alkali solution containing hydrogen and oxygen generated from the cathode cell reaction channel and the anode cell reaction channel enter the hydrogen separation chamber and the oxygen separation chamber from the upper part respectively.
10. A method for electrolysis of alkaline water based on an electrolyzer unit according to any one of claims 1-9, characterized in that the method comprises the steps of:
(1) When the cathode plate and the anode plate are electrified, alkali liquor enters the cathode small chamber reaction channel and the anode small chamber reaction channel from the alkali liquor inlet chamber respectively, and electrolysis is carried out on the surfaces of the cathode net and the anode net respectively to generate hydrogen and oxygen, so that alkali liquor containing hydrogen bubbles and alkali liquor containing oxygen bubbles are obtained;
(2) The alkali liquor containing hydrogen bubbles and the alkali liquor containing oxygen bubbles respectively ascend along the cathode cell reaction channel and the anode cell reaction channel to enter the hydrogen separation chamber and the oxygen separation chamber for gas-liquid separation, and the separated alkali liquor phase respectively returns the night channel to the alkali liquor inlet chamber through the cathode liquid dropping channel and the anode, so that a cathode alkali liquor natural circulation loop and an anode alkali liquor natural circulation loop are formed by means of the density difference of the gas-liquid two phases;
(3) The circulating cooling water in the circulating cooling water channel continuously runs to take away heat generated by electrolytic reaction on the cathode plate and the anode plate.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117735678A (en) * | 2024-02-18 | 2024-03-22 | 成都思达能环保设备有限公司 | Water treatment method and electrolysis device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117735678A (en) * | 2024-02-18 | 2024-03-22 | 成都思达能环保设备有限公司 | Water treatment method and electrolysis device |
| CN117735678B (en) * | 2024-02-18 | 2024-05-31 | 成都思达能环保设备有限公司 | Water treatment method and electrolysis device |
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