Electrochemical acid-base generator

Abstract

The application discloses an electrochemical acid-base generator, and relates to the technical field of electrochemistry, comprising an anode chamber, a first material chamber, an alkali chamber, a catalytic chamber, an acid chamber, a second material chamber and a cathode chamber; the anode chamber and the first material chamber are separated by a proton exchange membrane; the first material chamber and the alkali chamber are separated by a cation exchange membrane; the alkali chamber and the catalytic chamber are separated by an anion exchange membrane; the catalytic chamber and the acid chamber are separated by a cation exchange membrane; the acid chamber and the second material chamber are separated by an anion exchange membrane; and the second material chamber and the cathode chamber are separated by a proton exchange membrane. The multi-chamber structure optimizes the ion transmission path, significantly reduces the mass transfer resistance, and the special catalytic layer design further improves the hydrolysis reaction efficiency, so that the current density is improved compared with a traditional three-separation-chamber structure, and the production efficiency is improved.

Description

Technical Field

[0001] This invention relates to the field of electrochemical technology, and more specifically to an electrochemical acid-base generator. Background Technology

[0002] Electrochemical acid-base preparation technology utilizes ion-exchange membranes to decompose salt solutions or water into acids and bases under the influence of an electric field. Given the urgent need for efficient carbon management technologies due to global warming, traditional thermally driven or amine absorption methods suffer from high energy consumption and material stability issues. Electrochemical methods can directly utilize renewable electricity to achieve distributed decarbonization, aligning with the goal of carbon neutrality. Simultaneously, it can promote resource recycling, such as reducing lithium production costs through lithium extraction from salt lakes or recovering heavy metals and regenerating acids and bases in wastewater treatment, thus reducing chemical consumption.

[0003] Currently, the electrochemical preparation of acids and bases mainly employs bipolar membrane electrodialysis, with inorganic salt conversion primarily utilizing a three-compartment configuration. A three-compartment bipolar membrane electrodialysis reactor comprises a feed chamber, an acid chamber, and an alkali chamber, and consists of a bipolar membrane, a cation exchange membrane, and an anion exchange membrane. Under the influence of an electric field, water is dissociated through the bipolar membrane to generate hydrogen ions and hydroxide ions, while the cations and anions of the raw inorganic salt are separated and converted into corresponding acid and alkali solutions through the ion exchange membrane. This technology still faces many challenges in practical applications that urgently need to be addressed. One key challenge is increasing the reaction rate, as the current density in traditional three-compartment reactors is relatively low (typically suppressed to 30-60 mA / cm²). 2 This limitation restricts the reaction rate and production efficiency. Secondly, improving the stability of the bipolar membrane is crucial. During long-term operation, under alternating strong acid and alkali shocks, the anode and cathode layers are prone to interfacial delamination due to the difference in their thermal expansion coefficients, leading to a significant increase in membrane resistance. Simultaneously, issues such as catalyst loss from the intermediate layer of the bipolar membrane exist, causing a gradual decline in equipment performance. These key challenges urgently need to be overcome to promote the widespread application and industrialization of this technology.

[0004] To overcome the aforementioned bottlenecks, related research focuses on membrane material innovation and process optimization. This includes using raw material pre-concentration (patent CN102267747 B) and overflow-saturated feeding methods (patent CN 114288857 B) to match high current densities and improve reaction rates and product concentrations. However, this requires the addition of an electrodialysis unit or feeding device, increasing system complexity and energy consumption simultaneously. By developing a novel catalytic layer for bipolar membranes (patent CN 118976382 B) and optimizing the bipolar membrane preparation process (patent CN117106216 B), the stability of the bipolar membrane can be improved. Although upgrading membrane materials can slow down the failure rate, the current density remains limited. Based on the above analysis, this invention develops a new reactor configuration to increase operating current density while reducing operating energy consumption. Summary of the Invention

[0005] In view of this, the present invention provides a novel electrochemical acid-base generator to improve the reaction rate and long-term operational stability of electrochemical acid-base preparation.

[0006] To achieve the above objectives, the present invention adopts the following technical solution:

[0007] The electrochemical acid-base generator of the present invention adopts a multi-chamber separation structure design, and includes an anode chamber, a first feed chamber, an alkali chamber, a catalyst chamber, an acid chamber, a second feed chamber, and a cathode chamber; The anode chamber and the first feed chamber are separated by a proton exchange membrane; The first feed chamber and the alkali chamber are separated by a cation exchange membrane; The alkali chamber and the catalytic chamber are separated by an anion exchange membrane. The catalytic chamber and the acid chamber are separated by a cation exchange membrane; The acid chamber and the second feed chamber are separated by an anion exchange membrane; The second feed chamber and the cathode chamber are separated by a proton exchange membrane.

[0008] This invention incorporates a catalytic chamber, allowing the catalytic layer to exist as an independent functional compartment. A separate ion exchange membrane separates the alkali and acid compartments, eliminating the interfacial stress problem associated with direct ion exchange membrane bonding. The catalytic chamber requires only a small amount of deionized water to maintain the hydration and ion conductivity of the catalytic layer, rather than a large flow rate, thus reducing water consumption and pumping energy consumption.

[0009] Preferably, a catalytic layer is disposed within the catalytic chamber, and the catalytic layer is a composite material of water dissociation catalyst / porous solid electrolyte. This composite catalytic layer has high conductivity and excellent water dissociation catalytic activity, and its integrated structure effectively avoids the catalyst loss and interface delamination problems of traditional bipolar membranes. Thanks to this stable integrated structure, the system can operate stably within the range of 20-80℃. High-temperature conditions significantly improve ion conductivity and reaction kinetics, reduce membrane resistance, and enable the system to operate at higher current densities (200 mA / cm²). 2 High-efficiency operation. Traditional bipolar film systems are typically limited to operating temperatures below 40°C, which restricts further improvements in system performance.

[0010] Preferably, the catalyst layer is a composite material of nano-tin oxide / perfluorosulfonic acid polymer (SnO2 / Nafion), titanium oxide / sulfonated polyether ether ketone (TiO2 / SPEEK), iron oxide / graphene oxide (Fe2O3 / GO), ruthenium oxide / conductive metal-organic framework Ni3(HITP)2 (RuO2 / Ni3(HITP)2), iridium oxide / metal-organic framework UiO66-SO3H (IrOx / UiO66-SO3H), iron oxide@iron carbide core-shell structure nanoparticles / perfluorosulfonic acid polymer (Fe3O4@Fe5C2 / Nafion), nickel-iron layered bimetallic hydroxide / hydrophilic modified carbon felt / iridium oxide (NiFe-LDH / Hydrophilic Carbon Felt / IrOx), etc.

[0011] The preferred loading of the water dissociation catalyst is 0.5-3.0 mg / cm³. 2 The thickness of the catalyst layer is preferably 50-300 μm, and the catalyst layer is preferably prepared by one or more of the following methods: spraying, hot pressing, electrochemical deposition, impregnation-pyrolysis, and in-situ hydrothermal growth.

[0012] Preferably, the cation exchange membrane includes one of sulfonated polystyrene-divinylbenzene membrane, sulfonated polyvinyl fluoride membrane, and sulfonated polyarylene ether membrane.

[0013] Anion exchange membranes include one of the following: poly(aryl-piperidine) membranes, fluorinated polyaromatic quaternary ammonium membranes, quaternized polyvinyl fluoride membranes, and polyaryl ether-grafted quaternary ammonium membranes.

[0014] Preferably, the anolyte undergoes a hydrogenation reaction (HOR), H 2 →2H + +2e - The anode is one of platinum-based, iridium-based, ruthenium-based, transition metal sulfide, or transition metal phosphide electrodes; the electrolyte is one of low-concentration sulfuric acid solution, water vapor, or low-concentration perchloric acid solution; the raw material H2 is provided by the cathode product; the hydrogen evolution reaction (HER) takes place at the cathode end. + +2e - →H2, the cathode material is one of platinum-based, nickel-based, or cobalt-based electrodes, and the electrolyte is one of low-concentration sulfuric acid solution or pure water. The hydrogen produced at the cathode is piped to the anode chamber for recycling; the hydrogen circulation is closed-loop with no additional consumption. The hydrogen at the cathode outlet contains a small amount of water vapor, which is removed by a condenser (5℃) to prevent supersaturation of the anode side. The cathode side pressure is slightly higher than atmospheric pressure and is monitored in real time by a hydrogen concentration sensor.

[0015] Preferably, the reactor operates on the following principle: Metal cations (M...) are added to the feed chamber... + ) and anions (X)- Using a salt solution MX as a raw material, deionized water is added to the alkali chamber, acid chamber, and catalytic chamber. Under the influence of an electric field, M in the feed chamber... + and X - They migrate through cation exchange membranes and anion exchange membranes to the alkaline and acidic chambers, respectively, while simultaneously dissociating water in the catalytic chamber layer to produce H₂. + and OH - H + and OH - The ions migrate through the cation exchange membrane and anion exchange membrane in the catalytic chamber to the acid chamber and base chamber, respectively, thus preparing HX and MOH solutions in the acid and base chambers. The entire process utilizes ion-selective membranes to achieve directional ion migration, ensuring high product purity and high-efficiency preparation.

[0016] To address the passivation problem that may occur in the catalyst layer during long-term operation, the catalyst layer is regenerated by pulsed current, with pulsed regeneration performed every 500 hours.

[0017] The regeneration steps include: (1) reducing the operating current and maintaining it for 3-15 minutes, preferably with a current density of 5-20 mA / cm². 2 ; (2) Reverse pulse operation for 5-60s, with a preferred current density of 30-70mA / cm. 2 The regeneration step is repeated once or multiple times.

[0018] As can be seen from the above technical solution, compared with the prior art, the present invention has the following technical effects: The multi-chamber structure of this invention optimizes the ion transport path, significantly reduces mass transfer resistance, and the dedicated catalyst layer design further improves the efficiency of water dissociation reaction, resulting in a higher current density compared to the traditional three-chamber structure. It can operate stably in a wide temperature range of 20-80℃, thereby improving production efficiency.

[0019] Regarding equipment lifespan, this invention avoids the delamination problem of bipolar membranes. The high degree of immobilization of the water dissociation catalyst@porous solid electrolyte composite material effectively prevents catalyst loss, thus extending the continuous operating life of the equipment.

[0020] In terms of energy consumption control, the optimized electrode configuration and ion transport path effectively reduce system resistance, and the highly efficient catalyst layer significantly reduces overpotential loss, resulting in lower overall energy consumption and reduced operating costs. This invention can be applied to electrochemical carbon capture, lithium extraction from salt lakes, and the recovery of heavy metals and regeneration of acids and alkalis in wastewater treatment. Attached Figure Description

[0021] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0022] Figure 1 This is a schematic diagram of the electrochemical acid-base generator of the present invention. In the diagram, PEM is a proton exchange membrane, CEM is a cation exchange membrane, and AEM is an anion exchange membrane. Detailed Implementation

[0023] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0024] Example 1 The catalyst layer is made of SnO2 / Nafion composite material and prepared by spraying. The operation steps are as follows: (1) Preparation of catalyst slurry: Mix nano SnO2 powder (particle size 10-50nm) with Nafion solution (5wt%) at a mass ratio of 3:7, add isopropanol as a dispersant, and ultrasonically disperse for 30 minutes; (2) Substrate treatment: Hydrophilic modified carbon felt was used as the substrate and pre-dried in vacuum at 120°C for 2 hours; (3) Spraying process: Use automatic spraying equipment, spray gun distance 15cm, pressure 0.3MPa, spray in 5-8 times, with each spray drying for 5 minutes (80℃). (4) Curing treatment: Vacuum drying at 130℃ for 4 hours to fully cure Nafion.

[0025] Catalyst loading 2.0 mg / cm³ 2 Thickness 230 μm. For example... Figure 1As shown, the reactor is assembled in the order from anode to cathode: anode chamber - proton exchange membrane - first feed chamber - cation exchange membrane - alkali chamber - anion exchange membrane - catalytic chamber - cation exchange membrane - acid chamber - anion exchange membrane - second feed chamber - proton exchange membrane - cathode chamber. This symmetrical structure improves the utilization efficiency of the salt solution and reduces concentration polarization. Each chamber is separated by a corresponding ion exchange membrane, each with an effective membrane area of ​​100 cm². The cation exchange membrane is a sulfonated polystyrene-divinylbenzene membrane, and the anion exchange membrane is a poly(aryl-piperidine) membrane. The anode uses an iridium-based electrode, and the anode chamber is purged with moistened hydrogen gas. The cathode uses a platinum-based electrode, and the cathode chamber is purged with deionized water. The feed chamber is fed with 1.0 M sodium chloride solution at a flow rate of 50 mL / min. The alkali, acid, and catalytic chambers are all fed with deionized water at a flow rate of 8 mL / min. The operating temperature is 60 °C, and a current density of 100 mA / cm² is applied. After 8 hours of continuous operation, the acid chamber produced a 0.73 M hydrochloric acid solution with a purity >99.3%, and the alkali chamber produced a 0.75 M sodium hydroxide solution with a purity >99.5%. The system voltage was 2.4V, the energy consumption was 1.71 kWh / kg NaOH, and the current efficiency was 94%.

[0026] The system underwent long-term stability testing, running continuously for 500 hours. The system voltage rose to 2.6V, with an increase of less than 9%. No delamination of the catalyst layer was observed, and the product purity and concentration remained stable. The current efficiency was maintained above 92%.

[0027] Example 2 The catalyst layer and reactor structure were the same as in Example 1. After a 500-hour long-term stability test, a reverse pulse was applied. The operating current density was reduced from 100 mA / cm² to 10 mA / cm². 2 Maintain for 10 minutes, then reverse pulse for 50 seconds, applying a current density of 60 mA / cm². 2 This cycle is repeated once. A current density of 100 mA / cm² is applied again, and the system voltage drops by 80 mV. The catalytic activity recovers to 95% of its pre-regeneration value. After 1000 hours of cumulative operation, the performance of the pulse group is still better than the initial value of 85% of the constant current group. No obvious stratification of the catalyst layer occurs, product purity and concentration remain stable, and current efficiency remains above 85%.

[0028] Example 3 The catalyst layer and reactor structure are the same as in Example 1, with each compartment separated by a corresponding ion exchange membrane, each with an effective membrane area of ​​100 cm². The cation exchange membrane is a sulfonated polystyrene-divinylbenzene membrane, and the anion exchange membrane is a poly(aryl-piperidine) membrane. A platinum-based electrode is used as the anode, and humidified hydrogen gas is introduced into the anode chamber. A nickel-based electrode is used as the cathode, and deionized water is introduced into the cathode chamber. A 0.8 M lithium sulfate solution is fed into the feed chamber at a flow rate of 40 mL / min. Deionized water is fed into the alkali, acid, and catalyst chambers at a flow rate of 6 mL / min. The operating temperature is 50°C, and a current density of 80 mA / cm² is applied. After 6 hours of continuous operation, the acid chamber produces a 0.37 M sulfuric acid solution with a purity >99.0%. The alkali chamber produces a 0.67 M sodium hydroxide solution with a purity >98.8%. The system voltage is 2.0 V, the energy consumption is 2.48 kWh / kg LiOH, and the current efficiency is 90%.

[0029] The system underwent long-term stability testing, running continuously for 400 hours. The system voltage rose to 2.1V, an increase of 5%, and no delamination of the catalyst layer was observed. The purity and concentration of the product remained stable, and the current efficiency remained above 88%.

[0030] Example 4 The catalyst layer is made of Fe3O4@Fe5C2 / Nafion composite material, with a catalyst loading of 2.8 mg / cm³. 2 The thickness is 180 μm. It is prepared by hot pressing. First, core-shell Fe3O4@Fe5C2 nanoparticles are premixed with Nafion to form a self-supporting film. Then, it is hot-pressed at 140℃ and 5MPa for 5 minutes to composite with a carbon felt substrate.

[0031] The reactor structure is the same as in Example 1, with each compartment separated by a corresponding ion exchange membrane, each with an effective membrane area of ​​100 cm². The cation exchange membrane is a sulfonated polystyrene-divinylbenzene membrane, and the anion exchange membrane is a poly(aryl-piperidine) membrane. An iridium-based electrode is used as the anode, and humidified hydrogen gas is introduced into the anode chamber. A platinum-nickel alloy electrode is used as the cathode, and deionized water is introduced into the cathode chamber. A 2.0 M sodium chloride solution is fed into the feed chamber at a flow rate of 70 mL / min. Deionized water is fed into the alkali, acid, and catalytic chambers at a flow rate of 6 mL / min. The operating temperature is 80°C, and an application rate of 150 mA / cm² is applied. 2 The current density was [not specified]. After 6 hours of continuous operation, the acid chamber produced 1.43 M hydrochloric acid solution with a purity >99.1%. The alkali chamber produced 1.47 M sodium hydroxide solution with a purity >99.3%. The system voltage was 2.8V, the energy consumption was 2.04 kWh / kg NaOH, and the current efficiency was 92%.

[0032] This embodiment demonstrates the reactor's performance under high current density and high temperature conditions. Operation at 80°C significantly improves ion conductivity and reaction kinetics, reduces membrane resistance, and enables stable operation at higher current densities. Compared to traditional three-compartment structures (30-60 mA / cm²), this significantly enhances performance. 2 The current density is increased by 2.5-5 times, which significantly improves production efficiency.

[0033] The system underwent long-term stability testing. After 500 hours of continuous operation, the system voltage rose to 3.0 V, an increase of 7%. The catalyst layer structure remained intact, with no obvious delamination or peeling. The product concentration and purity remained stable, demonstrating the system's long-term stable operation capability under high current density.

[0034] Example 5 The catalyst layer is made of TiO2 / SPEEK composite material with a catalyst loading of 1.5 mg / cm³. 2 The thickness is 150 μm. The reactor structure is the same as in Example 1, with each compartment separated by a corresponding ion exchange membrane, the effective area of ​​which is 100 cm². 2 The cation exchange membrane was a sulfonated polystyrene-divinylbenzene membrane, and the anion exchange membrane was a poly(aryl-piperidine) membrane. An iridium-based electrode was used as the anode, and humidified hydrogen gas was introduced into the anode chamber. A nickel-based electrode was used as the cathode, and deionized water was introduced into the cathode chamber. A 1.0 M sodium chloride solution was fed into the feed chamber at a flow rate of 50 mL / min. Deionized water was fed into the alkali, acid, and catalytic chambers at a flow rate of 10 mL / min. The operating temperature was 40 °C, and a current density of 50 mA / cm² was applied. After 8 hours of continuous operation, the acid chamber produced a 0.27 M hydrochloric acid solution with a purity >98.5%, and the alkali chamber produced a 0.28 M sodium hydroxide solution with a purity >98.8%. The system voltage was 2.1 V, the energy consumption was 1.60 kWh / kg NaOH, and the current efficiency was 88%.

[0035] This embodiment demonstrates the reactor's stable operation at lower current densities. Compared to the performance of a conventional three-compartment structure at the same current density (Comparative Example 1 at 50 mA / cm², energy consumption 2.2 kWh / kg NaOH, current efficiency 82%), the catalytic chamber design of this invention still significantly reduces energy consumption by 27% and improves current efficiency by 6 percentage points. This proves that even under lower current density conditions, the novel catalytic chamber structure still has significant advantages in catalytic efficiency and ion transport optimization.

[0036] The system underwent long-term stability testing, running continuously for 500 hours. The system voltage rose to 2.18 V, with an increase of less than 4%. No delamination of the catalyst layer was observed, and the product purity and concentration remained stable. The current efficiency was maintained above 86%.

[0037] Comparative Example 1 The conventional three-compartment bipolar membrane electrodialysis system is employed: anode-proton exchange membrane-cation exchange membrane-alkali compartment-bipolar membrane-acid compartment-anion exchange membrane-feed compartment-proton exchange membrane-cathode. The bipolar membrane is composed of anion exchange layers and cation exchange layers, with a water dissociation catalyst in the middle layer. The effective membrane area is 100 cm². The cation exchange membrane is a sulfonated polystyrene-divinylbenzene membrane, and the anion exchange membrane is a poly(aryl-piperidine) membrane. The anode uses an iridium-based electrode with a 0.5 M sodium sulfate solution as the electrolyte for the oxygen evolution reaction (OER). The cathode uses a nickel-based electrode with a 0.5 M sodium sulfate solution as the electrolyte for the HER reaction. The feed compartment is fed with a 1.0 M sodium chloride solution at a flow rate of 50 mL / min. The alkaline, acid, and catalyst compartments are all fed with deionized water at a flow rate of 50 mL / min. The operating temperature is 40 °C, and a current density of 100 mA / cm² is applied. After running for 2 hours, the system voltage rose to 3.8 V, the alkali chamber produced 0.33 M sodium hydroxide solution with a purity of 83%, energy consumption was 3.5 kWh / kg NaOH, and current efficiency was 68%. After running for another 3 hours, the system voltage rose further to 4.2 V, and the product purity continued to drop below 75%, at which point the system was shut down.

[0038] This comparative example illustrates that the traditional three-compartment bipolar membrane system cannot operate stably under high current density (100 mA / cm²). Compared with the excellent performance of Example 1 under the same conditions (system voltage 2.4 V, product purity >99%, current efficiency 94%, stable operation for 500 hours), it proves the superiority of the independent catalytic chamber and its catalyst design and the selection of the anode reaction (hydrogenation reaction) of the present invention.

[0039] Comparative Example 2 A traditional three-compartment bipolar membrane electrodialysis configuration was adopted, with the reactor structure identical to Comparative Example 1. The feed chamber was fed with 1.0 M sodium chloride solution at a flow rate of 50 mL / min. The alkali and acid chambers were both fed with deionized water at a flow rate of 50 mL / min. The operating temperature was 40°C, and a current density of 50 mA / cm² was applied. After 8 hours of continuous operation, the acid chamber produced 0.28 M hydrochloric acid solution with a purity of 88%, and the alkali chamber produced 0.29 M sodium hydroxide solution with a purity of 86%. The system voltage was 2.9 V, energy consumption was 2.6 kWh / kg NaOH, and current efficiency was 76%.

[0040] The system underwent long-term stability testing. After 200 hours of continuous operation, significant delamination appeared at the bipolar membrane interface (the detection thickness increased by 25%), and the system voltage rose to 3.5 V, an increase of 20.7%. Product purity decreased to 82% and 80%, respectively, and current efficiency dropped to 68%. Disassembly inspection revealed partial detachment of the bipolar membrane's anode and cathode layers at the interface.

[0041] This comparative example illustrates that in traditional three-compartment bipolar membrane systems, under medium current density, long-term operation can easily lead to bipolar membrane delamination failure. Compared to the examples in terms of energy consumption, current efficiency, and electrochemical stability, this invention eliminates interfacial stress through an independent catalytic chamber design, and the integrated catalytic layer structure effectively prevents catalyst loss, enabling the system to operate stably for a wide temperature range of 20-80°C for extended periods. The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on its differences from other embodiments. Similar or identical parts between embodiments can be referred to interchangeably. For the apparatus disclosed in the embodiments, since they correspond to the methods disclosed in the embodiments, the description is relatively simple; relevant details can be found in the method section.

[0042] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. An electrochemical acid-base generator, characterized in that, It includes an anode chamber, a first feed chamber, an alkali chamber, a catalyst chamber, an acid chamber, a second feed chamber, and a cathode chamber; The anode chamber and the first feed chamber are separated by a proton exchange membrane; The first feed chamber and the alkali chamber are separated by a cation exchange membrane; The alkali chamber and the catalytic chamber are separated by an anion exchange membrane. The catalytic chamber and the acid chamber are separated by a cation exchange membrane; The acid chamber and the second feed chamber are separated by an anion exchange membrane; The second feed chamber and the cathode chamber are separated by a proton exchange membrane.

2. The electrochemical acid-base generator according to claim 1, characterized in that, The catalytic chamber is provided with a catalytic layer, which is a composite material of water dissociation catalyst / porous solid electrolyte.

3. An electrochemical acid-base generator according to claim 2, characterized in that, The composite material of the water dissociation catalyst / porous solid electrolyte specifically includes one or more of the following: nano-tin oxide / perfluorosulfonic acid polymer composite material, titanium oxide / sulfonated polyether ether ketone composite material, iron oxide / graphene oxide composite material, ruthenium oxide / conductive metal-organic framework composite material, iridium oxide / metal-organic framework composite material, iron oxide@iron carbide core-shell structure nanoparticle / perfluorosulfonic acid polymer composite material, and nickel-iron layered bimetallic hydroxide / hydrophilically modified carbon felt / iridium oxide composite material.

4. An electrochemical acid-base generator according to claim 2, characterized in that, The catalyst layer has a thickness of 50-300 μm, and the water dissociation catalyst loading is 0.5-3.0 mg / cm³. 2 The catalyst layer is prepared by one or more of the following methods: spraying, hot pressing, electrochemical deposition, impregnation-pyrolysis, and in-situ hydrothermal growth.

5. An electrochemical acid-base generator according to claim 1, characterized in that, The cation exchange membrane includes one of sulfonated polystyrene-divinylbenzene membrane, sulfonated polyvinyl fluoride membrane, and sulfonated polyarylene ether membrane. The anion exchange membrane includes one of the following: poly(aryl-piperidine) type membrane, fluorinated polyaromatic quaternary ammonium membrane, quaternized polyvinyl fluoride membrane, and polyaryl ether grafted quaternary ammonium membrane.

6. An electrochemical acid-base generator according to claim 1, characterized in that, The anode in the anode chamber is one of platinum-based, iridium-based, ruthenium-based, transition metal sulfide, and transition metal phosphide electrodes, and the electrolyte in the anode chamber is one of low-concentration sulfuric acid solution, water vapor, and low-concentration perchloric acid solution.

7. An electrochemical acid-base generator according to claim 1, characterized in that, The cathode material in the cathode chamber is one of platinum-based, nickel-based, or cobalt-based electrodes, and the electrolyte is one of low-concentration sulfuric acid solution or pure water.

8. An electrochemical acid-base generator according to any one of claims 1-7, characterized in that, The method of use is as follows: Salt solutions containing metal cations and anions are added as raw materials to the first and second material chambers, respectively; deionized water is added to the alkali chamber, acid chamber, and catalytic chamber. Under the action of an electric field, the cations and anions in the material chambers migrate to the alkali chamber and acid chamber, respectively, through the cation exchange membrane and anion exchange membrane. At the same time, H+ is generated by the dissociation of water in the inner layer of the catalytic chamber. + and OH - H + and OH - The ions migrate through the cation exchange membrane and anion exchange membrane in the catalytic chamber to the acid chamber and the base chamber, respectively, thereby preparing acid and base solutions in the acid chamber and the base chamber, respectively. The entire process achieves directional migration of ions through ion-selective membranes, ensuring high purity and high efficiency of product preparation.

9. An electrochemical acid-base generator according to claim 8, characterized in that, When passivation occurs in the catalyst layer, the catalyst layer is regenerated by pulsed current, and pulsed regeneration is performed once every 500 hours.

10. An electrochemical acid-base generator according to claim 9, characterized in that, The regeneration includes: (1) Reduce the operating current and maintain it for 3-15 minutes, with a current density of 5-20 mA / cm². 2 ; (2) Reverse pulse operation for 5-60 seconds, current density of 30-70 mA / cm² 2 ; (3) The regeneration step is performed once or multiple times.

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