CO2 desorption reactor based on electrochemical mediation amine regeneration and use method thereof

Abstract

The invention belongs to the technical field of carbon dioxide electrochemical trapping, and particularly relates to a CO2 desorption reactor based on electrochemical mediation amine regeneration and a use method thereof. The reactor includes an anode assembly, a cathode assembly, and a polymer electrolyte membrane separating both. According to the reactor, the CO2 trapping performance is improved, and compared with an H pool in a laboratory, the current intensity is improved by 10 times, and the desorption rate is improved by 40%. And the stability is excellent, and the current density almost has no fluctuation when the EMAR reactor is used for continuous operation for 24 hours. Cu generated by the cathode has good cyclicity, and copper on the cathode is deposited into high-purity copper elementary substance, so that repeated use of the copper electrode is ensured.

Description

Technical Field

[0001] The present invention belongs to the technical field of electrochemical capture of carbon dioxide, and specifically relates to a CO2 desorption reactor based on electrochemically mediated amine regeneration and a method of using the same, which are used to improve the CO2 desorption efficiency and reduce the overall energy consumption of carbon capture. Background Art

[0002] As one of the major greenhouse gases, the increasing emissions of carbon dioxide have had a profound impact on global climate change. With the acceleration of industrialization and urbanization, CO2 emissions are becoming increasingly serious, becoming a focal point for global environmental governance. Currently, the research and development of technologies to reduce emissions has become a key approach to effectively mitigate climate change in this century.

[0003] Traditional amine-based carbon capture technology relies on high-temperature thermal desorption, which presents challenges such as high energy consumption, solvent degradation, and equipment corrosion. While EMAR technology can regenerate organic amines at low temperatures, current research is primarily based on laboratory-scale studies, such as the use of H2 cells. However, these technologies suffer from limitations such as small electrode area, low mass transfer efficiency, and numerous side reactions, making them difficult to meet the requirements of industrial continuous operation. To further promote electrochemically mediated amine regeneration for CO2 capture, we needed to design an EMAR reactor for scale-up studies.

[0004] Large-scale electrochemically mediated amine regeneration systems include an absorption tower, a CO2 electrochemical desorption unit, a desorption tower, and a flash tank. The most critical component is the EMAR reactor. Changhong Wang (Wang C, Jiang K, Yu H, et al. Copper electrowinning-coupled CO2 capture in solvent-based post-combustion capture [J]. Applied Energy, 2022, 316:119086.) conducted ECC experiments using an electrochemically mediated reactor constructed with a 3D-printed cell (6 cm × 2.4 cm × 2.5 cm) and an anion exchange membrane. The reactor was optimized by adjusting experimental parameters. A validated ECC model calculated a theoretical energy consumption of 7.4-12.6 kJ / mol. Microkinetic modeling determined the actual operating conditions, with an energy consumption of 52 kJ / mol CO2 under optimal conditions. The CO2 desorption reactor reported in existing literature uses a plate-and-frame structure. Its core component consists of cathode and anode flow channels separated by an ion exchange membrane, with copper bipolar plates serving as the cathode and anode, respectively. The system integrates a temperature-controlled heating module and is enclosed in a stainless steel housing.

[0005] Wang et al. (Wang M, Hatton T A. Flue gas CO2 capture via electrochemically mediated amine regeneration: desorption unit design and analysis[J]. Industrial & Engineering Chemistry Research, 2020, 59(21): 10120-10129.) constructed a continuous flow experimental system based on the reactor structure and systematically studied the effects of key parameters such as electrolyte flow rate and current density on carbon dioxide precipitation rate and electron transfer efficiency. The research team used a dynamic test platform to perform 130 cycles in simulated flue gas for 20 hours, and the system energy consumption was approximately in the range of 80-120kJ / mol CO2.

[0006] Currently, research on electrochemically mediated amine regeneration reactors is limited. The design of the reactor's internal flow path directly impacts mass transfer and reaction kinetics. Traditional sandwich or fixed-bed reactors suffer from short-flow and dead spots, significantly reducing treatment efficiency upon scale-up. Amine regeneration energy consumption accounts for 80% of the total CO2 capture cost, and reducing energy consumption is a core goal. Research on electrochemically mediated amine regeneration reactors is also a key direction for the further development of EMAR systems. This research requires coordinated breakthroughs in materials, engineering, and system integration to achieve efficient, low-energy industrial application. Summary of the Invention

[0007] In order to further improve the CO2 carbon capture efficiency and reduce the reaction energy consumption, the present invention proposes an electrochemical mediated amine regeneration reactor (EMAR). Its characteristics and advantages are: (1) Optimizing the separation structure of the anode and cathode chambers, using SELEMION ion exchange membrane for isolation, effectively blocking the cross-interference of the anode and cathode solutions, significantly reducing side reactions, improving the CO2 desorption efficiency, and reducing the additional energy consumption caused by side reactions. (2) The electrode cost is low and the activity is high. Low-cost copper wire is used to replace precious metals. The large specific surface area design significantly increases the active site density, and the current intensity is increased by 10 times compared with the traditional H cell. The dense copper coating generated by the cathode can be reused, reducing the cost of industrial electrode replacement. (3) Dynamic circulation system, using a peristaltic pump to drive the electrolyte flow in the EMAR reactor, combined with the SELEMION membrane to optimize the ion migration path, reduce the mass transfer resistance, and increase the desorption rate. At the same time, the thermocouple and heating jacket accurately control the temperature to avoid excessive temperature causing the decomposition of organic amines.

[0008] In summary, the EMAR reactor has significant advantages in desorption efficiency, energy consumption, stability, etc. through structural innovation, process optimization and system circulation, and has clear prospects for industrial application.

[0009] The technical solutions of the present invention are as follows:

[0010] A CO2 desorption reactor based on electrochemically mediated amine regeneration includes an anode assembly, a cathode assembly, and a polymer electrolyte membrane separating the two.

[0011] The cathode assembly includes a cylindrical cathode chamber with openings at both ends and two annular cathode chamber covers, and a circle of baffles is provided at both ends of the cathode chamber; the anode assembly includes a cylindrical barrel with openings at both ends and two anode chamber covers, the diameter of the cylindrical barrel is smaller than the diameter of the cathode chamber, and the cylindrical barrel serves as the anode chamber; the cylindrical barrel is inserted into the cathode chamber, and the cathode chamber and the anode chamber are fixed as one from both ends through the cathode chamber cover, and the anode chamber cover is installed at both ends of the anode chamber; a strip hole is axially opened on the cylindrical barrel part located inside the cathode chamber, and the strip hole part is divided into two sections, a copper mesh is wrapped around one section of the strip hole as the anode, and then a polymer electrolyte membrane is wrapped around the entire strip hole part, and the strip hole part and the copper mesh are wrapped inside, and then a copper mesh is wrapped around the other section of the strip hole part that wraps the polymer electrolyte membrane as the cathode.

[0012] The top of the cathode chamber is provided with two through holes, which serve as the cathode liquid inlet and the N2 inlet respectively; the bottom is provided with two through holes, which serve as the product outlet and the cathode liquid outlet respectively.

[0013] The center of the anode cavity cover is provided with a through hole as a circulation port of the anode liquid, one of which is the anode liquid inlet and the other is the anode liquid outlet.

[0014] The anode cavity cover and cathode cavity cover are provided with internal threads, and both ends of the cathode cavity and anode cavity are provided with external threads. The anode cavity cover and both ends of the anode cavity are matched through threads, and the cathode cavity cover and both ends of the cathode cavity are matched through threads.

[0015] The cathode chamber is also provided with two through holes, which are used to install a reference electrode and a thermocouple temperature control detector respectively.

[0016] A sealing ring is provided at the baffle, and the cathode cavity cover is placed on the outer side of the baffle to prevent the cathode solution from overflowing.

[0017] The cathode chamber is externally wrapped with a heating device.

[0018] The polymer electrolyte membrane is a SELEMION ion exchange membrane.

[0019] The method of using the above-mentioned CO2 desorption reactor based on electrochemically mediated amine regeneration is as follows:

[0020] Connect the working electrode connector, counter electrode connector, and reference electrode connector of the electrochemical workstation to the cathode, anode, and reference electrode of the CO2 desorption reactor respectively;

[0021] The N2 inlet is connected to the N2 bottle to introduce N2; the product outlet is connected to the CO2 concentration detection device to detect the CO2 content, and the CO2 concentration detection device is connected to the air bag to collect the gas CO2;

[0022] Before the reaction starts, the cathode reaction solution is pumped into the cathode chamber from the cathode liquid inlet, and the anode reaction solution is pumped into the anode chamber from the anode liquid inlet; the cathode liquid outlet is connected to the reaction cathode liquid recovery bottle, and the anode liquid outlet is connected to the reaction anode liquid recovery bottle; the electrochemical workstation is started to perform the desorption process; during the reaction process, the anode waste liquid is pumped out to the anode liquid recovery bottle by a peristaltic pump, and the solution in the anode liquid recovery bottle is continuously pumped into the cathode chamber by the peristaltic pump as the cathode liquid for the subsequent reaction process; the cathode waste liquid is pumped out to the cathode liquid recovery bottle by a peristaltic pump, and the solution in the cathode liquid recovery bottle is continuously pumped into the anode chamber by the peristaltic pump as the anode solution for the subsequent reaction process, forming a closed loop.

[0023] The present invention has the following beneficial effects:

[0024] 1. Structure: a leap from laboratory level to industrial level.

[0025] (1) Two-chamber separation + ion exchange membrane design. The existing technology has no membrane or only uses ordinary membranes, which leads to cross-contamination of the anode and cathode solutions. The present invention uses ion exchange membranes to accurately block molecular-level interference and reduce side reactions by more than 50%;

[0026] (2) Dynamic circulation channel + temperature control integration. Traditional H-cells use static electrolytes, and mass transfer relies on diffusion, which is inefficient. The present invention designs a peristaltic pump-driven forced circulation channel, combined with the open-pore structure of the cathode chamber, to reduce mass transfer resistance. The precise temperature control module controls temperature fluctuations within ±1°C, avoiding the decomposition of the amine solution caused by traditional high-temperature desorption.

[0027] 2. Materials: High specific surface area copper electrodes replace precious metals to achieve a balance between low cost and high performance.

[0028] (1) Existing literature mostly uses platinum / electrodes, which are expensive and prone to corrosion. The present invention uses a wound copper mesh electrode to increase the active site density by 10 times, the current intensity reaches 32.26A, and the cost is reduced by 90% (the price of copper is about 1 / 500 of that of platinum).

[0029] (2) Recyclable coating technology: The dense pure copper coating generated by the cathode can be peeled off and reused, avoiding the disadvantage of one-time consumption of traditional electrodes. The cost of electrode replacement in industrial applications can be ignored.

[0030] Overall, the reactor of the present invention improves CO2 capture performance, achieving a 10-fold increase in current intensity and a 40% increase in desorption rate compared to a laboratory H2 cell. It also exhibits excellent stability, with virtually no fluctuation in current density during 24-hour continuous operation using the EMAR reactor. The copper generated at the cathode exhibits excellent recyclability, and the copper deposited on the cathode is high-purity copper, ensuring the reusability of the copper electrode. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] Figure 1(a) and Figure 1(b) are respectively a complete assembly diagram and a cross-sectional diagram of the EMAR reaction of the present invention; in the figure: 1 anode chamber cover a; 2 anode chamber cover b; 3 cathode chamber cover; 4 anode chamber; 5 cathode chamber; 6 reference electrode and temperature detection device mounting hole; 7 cathode liquid inlet; 8 N2 inlet; 9 product outlet; 10 baffle.

[0032] Figure 2 It is a complete electrochemically mediated amine regeneration CO2 capture circulation system of EMAR reactor; in the figure, 11EMAR reactor; 12 electrochemical workstation; 13 peristaltic pump; 14 reaction cathode liquid recovery flask; 15 reaction liquid anolyte recovery flask; 16N2 bottle; 17CO2 concentration detection device; 18 gas bag.

[0033] Figure 3 This is a comparison of the CO2 desorption performance between the EMAR reactor and the traditional H cell, with the potential values being -1.5V, -1.1V, -0.8V, and -0.5V respectively.

[0034] Figure 4 This is a SEM image of Cu deposited on the cathode during electrochemically mediated amine regeneration and CO2 capture in the EMAR reactor in Example 1.

[0035] Figure 5 This is the XRD pattern of Cu deposited on the cathode when the EMAR reactor in Example 1 performs electrochemically mediated amine regeneration to capture CO2.

[0036] Figure 6 This is a CV comparison diagram of the EMAR reactor and the H cell in Example 2.

[0037] Figure 7 This is a comparison diagram of the LSV of the EMAR reactor and the H pool in Example 2.

[0038] Figure 8 This is the 24h stability diagram of the EMAR reactor in Example 3. DETAILED DESCRIPTION

[0039] The specific real-time method of the present invention is further described below in conjunction with the accompanying drawings and technical solutions.

[0040] 1. Reactor Assembly

[0041] (1) Reactor structure:

[0042] The CO2 desorption reactor based on electrochemically mediated amine regeneration of the present invention comprises an anode assembly, a cathode assembly and a polymer electrolyte membrane separating the two.

[0043] The cathode assembly includes a cylindrical cathode chamber 5 with openings at both ends and two annular cathode chamber covers 3 . A circle of baffles 10 is provided at both ends of the cathode chamber 5 .

[0044] The anode assembly includes a cylindrical body with openings at both ends and two anode cavity covers (anode cavity cover a1 and anode cavity cover b2). The diameter of the cylindrical body is smaller than the diameter of the cathode cavity, and the cylindrical body serves as the anode cavity 4; the cylindrical body is inserted into the cathode cavity 5, and the cathode cavity 5 and the anode cavity 4 are fixed as one from both ends through the cathode cavity cover 3. The anode cavity cover a1 and the anode cavity cover b2 are installed at both ends of the anode cavity 4.

[0045] A strip hole is formed in the axial direction on the cylindrical portion inside the cathode cavity 5. The strip hole portion is divided into two sections. A copper mesh is wrapped around one section of the strip hole to serve as the anode. A polymer electrolyte membrane is then wrapped around the entire strip hole section, wrapping both the strip hole section and the copper mesh inside. Finally, a copper mesh is wrapped around the other section of the strip hole section that wraps the polymer electrolyte membrane to serve as the cathode.

[0046] The cathode chamber has two through holes on the top, serving as a cathode liquid inlet 7 and a nitrogen inlet 8, respectively; and two through holes on the bottom, serving as a product outlet 9 and a cathode liquid outlet, respectively.

[0047] The center of the anode chamber cover is provided with a through hole as a circulation port for the anolyte, one for the anolyte inlet and the other for the anolyte outlet;

[0048] The cathode chamber is further provided with two through holes, which serve as reference electrode and temperature detection device mounting holes 6, for mounting a reference electrode and a thermocouple temperature control detector respectively.

[0049] The completed assembly diagram is shown in Figure 1(a) and Figure 1(b).

[0050] (2) Assembling electrodes:

[0051] Use a wire wrapper to fix the anode copper mesh to the inner side of the electrolysis chamber, and control the area of the copper mesh to 400 cm 2 , wrap the copper wire around the copper mesh to fix it, and use it as the anode of the reactor. The cathode and cathode chambers are separated by the SELEMION ion exchange membrane. When installing the ion exchange membrane, use double-sided tape, heat shrink tubing and AB glue to seal and fix it at the opening, and check the sealing at the same time. After sealing, prevent it from standing for 24 hours. After standing, fix the cathode copper mesh to the outside of the electrolysis, and the copper mesh area is 400cm-2 , wrap the copper wire around the copper mesh to secure it, which will serve as the cathode. Set the wire wrapper to a path of 100 turns and a stroke of 5 cycles. Once the reactor electrode is prepared, place it in the reactor.

[0052] (3) Assemble the circulation system:

[0053] Connect the electrochemical workstation 12, the peristaltic pump 13, and the EMAR reactor 11 to form a circulation system. Figure 2 As shown. First, pour the cathode reaction liquid into the cathode chamber 5 of the EMAR reactor 1, and then pour the anode reaction liquid into the anode chamber 4. Connect the working electrode connector of the electrochemical workstation 12 to the cathode electrode in the cathode chamber 5, connect the counter electrode connector of the electrochemical workstation 12 to the anode electrode in the anode chamber 4, and connect the reference electrode connector of the electrochemical workstation 12 to the reference electrode in the EMAR reactor 11. The cathode reaction liquid outlet is connected to the reaction cathode liquid recovery flask 14, and the anode reaction liquid outlet is connected to the reaction liquid anode liquid recovery flask 15. During the electrochemical reaction, a peristaltic pump 13 is used to pump the anode waste liquid to the anode liquid recovery flask 15. The solution in the anode liquid recovery flask 15 is used as the cathode solution for subsequent experiments. The peristaltic pump 13 is continued to be used to pump the solution in the anode liquid recovery flask 15 into the cathode chamber 5. The peristaltic pump 13 is used to pump the cathode waste liquid to the cathode liquid recovery flask 14. The solution in the cathode liquid recovery flask 14 is used as the anode solution for subsequent experiments. The peristaltic pump 13 is continued to be used to pump the solution in the cathode liquid recovery flask 14 into the anode chamber 4, forming a closed loop. Because CO2 gas is generated at the anode during the reaction, the anode outlet is connected to a CO2 concentration detection device 17 to detect the CO2 content. The CO2 concentration detection device 17 is connected to an air bag 18 to collect gas in preparation for subsequent characterization. Before the reaction begins, the reactor is ventilated to check for leaks and an N2 bottle 16 is connected to sweep the entire reaction system to ensure that there are no other impurities that affect the cycle. During the reaction, a thermocouple was used to monitor the real-time temperature. A heating jacket was added to the reactor 11 to control the reaction temperature and an insulation jacket was added to reduce heat loss during the reaction. When the system was stable, an electrochemical carbon capture cycle test was performed.

[0054] Among them, the cathode chamber 5 is filled with Cu 2+ A total of 2000 ml of 30 wt% AEEA solution and Na2SO4 were added to the anode chamber 4, and a total of 1000 ml of CO2-saturated AEEA solution was added to the anode chamber 4.

[0055] 2. Run the process

[0056] (1) Before the reaction, start the nitrogen purge system and use the gas flow meter to measure the space-time flow rate for 5 minutes to eliminate the interference of impurity gases.

[0057] (2) Set the potential to -1.4 V, the temperature to 298.15 K, start the electrolyte circulation pump, and conduct a 24-h circulation stability experiment.

[0058] (3) Use a CO2 concentration detector to detect the concentration of CO2 desorbed from the reactor.

[0059] 2. Parameter Optimization

[0060] (1) Cu in the reaction solution 2+ The concentration is controlled at 0.5 mol / kg to reduce the charge transfer resistance.

[0061] (2) Add a small amount of surfactant to improve the interfacial mass transfer efficiency, thereby improving the desorption efficiency and reducing the desorption energy consumption.

[0062] Example 1: Reactor desorption performance verification

[0063] The cathode reaction solution is 30wt% AEEA + 0.5mol / kg CuSO4 + 1.0mol / kg Na2SO4. The anode solution is a 30wt% AEEA solution saturated with CO2. The potential is set to -1.4V, the temperature is 298.15K, and the circulation pump and nitrogen purge are started. Specific experimental results: Figure 3 The initial rate shown in b shows an increasing trend and remains stable after 60 minutes. The energy consumption is 52.756 kJ / g CO2 (Table 1). The electrode morphology is as follows Figure 4 The SEM image shows that the cathode copper coating is a dense coral-like structure. Figure 5 The XRD results confirmed that the copper was pure, ensuring the reuse of the Cu electrode. The electrochemical desorption rate and energy consumption of the EMAR reactor are shown in Table 1.

[0064] Table 1 Electrochemical desorption rate and energy consumption of EMAR reactor at -1.4V

[0065]

[0066] Example 2: Performance comparison of EMAR reactor and H cell

[0067] The specific steps are as follows:

[0068] The EMAR reactor and H cell were operated under the same parameters. The specific desorption results are as follows Figure 3 The maximum value of the vertical axis shown in b (electrochemically mediated amine regeneration reactor) is 70 mL / min, which is better than Figure 350mL / min of a (H cell). At the same potential (such as -1.5V), the initial desorption rate of the reactor is higher, indicating that its electrochemically mediated amine regeneration efficiency is better, which may be due to better mass transfer conditions or electrode design. In both figures, more negative potentials correspond to higher initial desorption rates, while the rate decreases significantly when the potential decreases (such as -0.5V). This shows that increasing the potential can effectively enhance the CO2 desorption kinetics, but a trade-off between energy consumption and efficiency is required. Under all voltage conditions, the desorption rate decreases with the extension of the experimental time, which may be due to the decrease in the CO2 concentration in the amine solution or the gradual saturation of the electrode activity. However, the rate decay of the reactor is relatively slow (such as Figure 3 (b) The -1.5V curve maintains a high value at 150 minutes, indicating its superior suitability for long-term, stable desorption. The structural differences between the H-cell and the reactor lead to significant differences in desorption rates. The optimized reactor design may have improved overall performance by improving electrochemical interfacial contact or reducing mass transfer resistance. The reactor performs better in electrochemically mediated amine regeneration, with higher desorption rates and more sustained desorption capacity. Figure 6 This is a CV performance comparison chart. The peak current of the reactor is increased by about 10 times compared with the H cell. Figure 7 The LSV comparison chart shows that the polarization curve of the EMAR reactor exhibits a significant current response at a more positive potential than that of the H-cell, indicating a lower initial overpotential and a more favorable reaction. At the same potential, the absolute value of the current density in the EMAR reactor is significantly higher than that in the H-cell, indicating a faster reaction rate and better energy consumption in the EMAR reactor.

[0069] Example 3: Low-energy CO2 desorption

[0070] The potential was adjusted to -0.8 V, and other parameters were the same as in Example 1. A small amount of ionic surfactant was added to optimize interfacial mass transfer. The results are as follows: the desorption energy consumption was reduced to 25.437 kJ / g CO2 (Table 2), which is 50% energy saving compared to the -1.4 V mode. Figure 8 The stability of the EMAR reactor is shown in Figure 1. The current density fluctuation is only ±0.2 A / cm during 24 hours of operation. 2 The small current fluctuation indicates that the reactor has good stability during CO2 electrodesorption.

[0071] Table 2 Comparison of electrochemical desorption rate and energy consumption of EMAR reactor at -1.4V and -0.8V.

[0072]

Claims

1. A CO2 desorption reactor based on electrochemically mediated amine regeneration, characterized in that: The CO2 desorption reactor based on electrochemically mediated amine regeneration includes an anode assembly, a cathode assembly, and a polymer electrolyte membrane separating the two; The cathode assembly comprises a cylindrical cathode chamber with openings at both ends and two annular cathode chamber covers, with a circle of baffles provided at both ends of the cathode chamber; the anode assembly comprises a cylindrical barrel with openings at both ends and two anode chamber covers, the diameter of the cylindrical barrel being smaller than the diameter of the cathode chamber, and the cylindrical barrel serving as the anode chamber; the cylindrical barrel is inserted into the cathode chamber, and the cathode chamber and the anode chamber are fixed as one from both ends by the cathode chamber covers, and the anode chamber covers are installed at both ends of the anode chamber; a strip hole is axially provided on the cylindrical barrel portion located inside the cathode chamber, and the strip hole portion is divided into two sections, a copper mesh is wound around one section of the strip hole as the anode, and then a polymer electrolyte membrane is wound around the entire strip hole portion, the strip hole portion and the copper mesh are both wrapped inside, and then a copper mesh is wound around the other section of the strip hole portion wrapped with the polymer electrolyte membrane as the cathode; The cathode chamber has two through holes on the top, serving as the cathode liquid inlet and the N2 inlet respectively; and two through holes on the bottom, serving as the product outlet and the cathode liquid outlet respectively; The center of the anode chamber cover is provided with a through hole as a circulation port for the anolyte, one for the anolyte inlet and the other for the anolyte outlet; The cathode chamber is also provided with two through holes, which are used to install a reference electrode and a thermocouple temperature control detector respectively.

2. A CO2 desorption reactor based on electrochemically mediated amine regeneration according to claim 1, characterized in that: The anode cavity cover and cathode cavity cover are provided with internal threads, and both ends of the cathode cavity and anode cavity are provided with external threads. The anode cavity cover and both ends of the anode cavity are matched through threads, and the cathode cavity cover and both ends of the cathode cavity are matched through threads.

3. A CO2 desorption reactor based on electrochemically mediated amine regeneration according to claim 1, characterized in that: A sealing ring is provided at the baffle, and the cathode cavity cover is placed on the outer side of the baffle.

4. A CO2 desorption reactor based on electrochemically mediated amine regeneration according to claim 1, characterized in that: The cathode chamber is externally wrapped with a heating device.

5. A CO2 desorption reactor based on electrochemically mediated amine regeneration according to claim 1, characterized in that: The polymer electrolyte membrane is a SELEMION ion exchange membrane.

6. The method for using the CO2 desorption reactor based on electrochemically mediated amine regeneration according to any one of claims 1 to 5, characterized in that: The details are as follows: Connect the working electrode connector, counter electrode connector, and reference electrode connector of the electrochemical workstation to the cathode, anode, and reference electrode of the CO2 desorption reactor respectively; The N2 inlet is connected to the N2 bottle to introduce N2; the product outlet is connected to the CO2 concentration detection device to detect the CO2 content, and the CO2 concentration detection device is connected to the air bag to collect the gas CO2; Before the reaction starts, the cathode reaction solution is pumped into the cathode chamber from the cathode liquid inlet, and the anode reaction solution is pumped into the anode chamber from the anode liquid inlet; the cathode liquid outlet is connected to the reaction cathode liquid recovery bottle, and the anode liquid outlet is connected to the reaction anode liquid recovery bottle; the electrochemical workstation is started to perform the desorption process; during the reaction process, the anode waste liquid is pumped out to the anode liquid recovery bottle by a peristaltic pump, and the solution in the anode liquid recovery bottle is continuously pumped into the cathode chamber by the peristaltic pump as the cathode liquid for the subsequent reaction process; the cathode waste liquid is pumped out to the cathode liquid recovery bottle by a peristaltic pump, and the solution in the cathode liquid recovery bottle is continuously pumped into the anode chamber by the peristaltic pump as the anode solution for the subsequent reaction process, forming a closed loop.

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