Electrochemical regeneration and conversion method and system for carbon dioxide supported absorbent

Abstract

The invention provides a carbon dioxide supported absorbent electrochemical regeneration and conversion method and system, and belongs to the technical field of carbon dioxide capture and conversion. According to the method, CO2 is in contact with a vitreous body mixed solvent VMS, the VMS absorbing the CO2 is used as an electrolyte for electrochemical conversion and desorption, and a generated VMS regeneration solution is used as a CO2 capture solution for absorbing the CO2 again. The CO2 absorbent with the characteristics of high absorption load, low viscosity and high conductivity is utilized, so that efficient absorption and low-energy-consumption regeneration are realized. The electrochemical regeneration and conversion method for the CO2 supported absorbent provided by the invention is simple in process flow and convenient to operate, and has multiple advantages of renewable energy source compatibility and system integration; the efficient desorption of CO2 at room temperature is realized, the capture cost and regeneration energy consumption are reduced, the cooperative operation of CO2 capture, desorption and conversion is realized, and the deep carbon reduction in the carbon capture process is promoted.

Description

Technical Field

[0001] This invention belongs to the field of carbon dioxide capture and conversion technology, and relates to a method and system for electrochemical regeneration and conversion of carbon dioxide supported absorbent. Background Technology

[0002] Reducing greenhouse gas emissions is a core pathway to mitigating global warming. Carbon dioxide is one of the most significant greenhouse gases contributing to climate change, accounting for up to 76% of the total greenhouse gas enhancement effect. With the large-scale use of fossil fuels, the concentration of carbon dioxide in the atmosphere has surged from 280 ppm before the Industrial Revolution to 426.57 ppm. Achieving deep reductions in greenhouse gas emissions and stabilizing the concentration of carbon dioxide in the atmosphere within the threshold of 450 ppm is crucial for limiting global warming to no more than 1.5°C.

[0003] Carbon capture, utilization, and storage (CCUS) technology not only separates carbon dioxide generated by industry and related sectors, transforming it into high-value-added products, but also promotes closed-loop management of carbon emission reduction, becoming a key technology supporting low-carbon transformation. Among these technologies, capture technology based on the principle of chemical absorption, with its mature process and high adaptability, has become the most commercialized and widely used carbon emission reduction pathway at present. This technology utilizes specific absorbents such as amine solutions (patent CN114950072A), alkaline solutions (patent CN117654262A), ionic liquids (patent CN113813747A), and eutectic solvents (patent CN113617304A, CN108993125A) to achieve capture through a reversible chemical reaction with carbon dioxide in flue gas. Subsequently, by applying specific energy (mainly thermal or pressure energy) to the carbon dioxide-loaded absorbent, the absorbent is regenerated and high-purity carbon dioxide is released.

[0004] The regeneration process of the absorbent is the core of evaluating the system's energy consumption, and its efficiency directly affects the economics and carbon reduction effectiveness of the entire CCUS technology. Patent CN119909644A discloses a method for photothermal-driven regeneration of carbon dioxide capture materials, which involves doping the prepared carbon dioxide capture particles with manganese trioxide at a speed of 4.5 kW / m³. 2Under illumination, regeneration is essentially completed by heating to 74℃, but the preparation of the capture material is complex and the absorption capacity is low. Patent CN120249998A discloses a method for the co-capture and conversion of flue gas carbon dioxide to produce formate, which eliminates the need for pretreatment of small amounts of oxygen and trace amounts of nitrogen oxides and sulfur oxides in the flue gas, reducing the energy consumption for carbon dioxide regeneration. However, the capture and utilization rate of flue gas carbon dioxide is low, and the low-value oxygen generated by the anode reaction is directly emitted into the atmosphere, resulting in low energy utilization of the entire reaction. Patents CN119258730A and CN119607801A respectively disclose a carbon dioxide absorbent composed of functionalized ionic liquid triethylenetetramine-3-bromophenol salt and polyethylene glycol 200, and a mixed alkaline carbon dioxide absorbent with sodium carbonate as the main absorbent, as well as their capture methods. However, the absorbent requires a temperature above 100℃ to achieve carbon dioxide desorption, resulting in high regeneration energy consumption for the system.

[0005] Therefore, controlling the regeneration energy consumption of CO2 absorbents and achieving low-temperature desorption while ensuring high-efficiency capture performance is a key step in promoting deep carbon emission reduction. Summary of the Invention

[0006] To address the aforementioned technical problems, the present invention aims to provide a CO2 capture method driven by electrochemical desorption and conversion. This method utilizes a CO2 absorbent with high absorption load, low viscosity, and high conductivity to achieve efficient absorption and low-energy regeneration. Compared with traditional thermal regeneration methods, this method achieves CO2 desorption under mild conditions, significantly reducing the operating costs of carbon capture. The electricity consumed in the desorption process can be generated from renewable energy sources, thus transforming the energy-intensive CO2 desorption process into a flexible carrier for absorbing unstable green electricity, constructing an integrated low-energy green electricity-carbon capture system, and significantly improving the economics of the CCUS process.

[0007] To achieve the above objectives, the present invention adopts the following technical solution:

[0008] The first aspect of this invention provides a method for the electrochemical regeneration and conversion of a carbon dioxide supported absorbent, comprising the following steps:

[0009] (1) Absorption: The gas containing carbon dioxide is contacted with a glassy mixed solvent VMS to capture CO2, resulting in a CO2-loaded VMS absorbent; wherein the glassy mixed solvent VMS is composed of a superbase, an alcohol, and additives, and its maximum CO2 saturation absorption load is 0.30 g CO2 / g VMS, the viscosity after CO2 absorption is less than 30 mPa·s, and the maximum conductivity is 13.38 mS·cm. -1 ;

[0010] (2) Electrochemical desorption and conversion: The CO2-loaded VMS absorbent obtained in step (1) is used as the electrolyte and placed in an electrolytic cell to carry out electrochemical desorption and conversion reactions. The cathode chamber or cathode region generates regenerated VMS collecting liquid, CO2 and H2, and the anode chamber or anode region generates carboxylate.

[0011] (3) Return of regenerated absorbent: The regenerated VMS capture solution generated at the cathode in step (2) is returned to step (1) for CO2 capture again;

[0012] The electrolytic cell is a single-chamber electrolytic cell or a diaphragm electrolytic cell.

[0013] When the electrolytic cell is a diaphragm electrolytic cell, during the electrochemical desorption and conversion process, the CO2-loaded VMS absorbent is used as the cathode electrolyte, and the alkaline methanol solution is used as the anode electrolyte; wherein, the alkaline methanol solution is obtained by mixing 0.5mol / L~4mol / L soluble alkali and methanol at a molar ratio of (2~6):1.

[0014] The method further includes:

[0015] (4) CO2 and H2 are extracted and synthesized into methanol, low-carbon olefins or liquid hydrocarbon fuels in a CO2 catalytic reactor under the action of a catalyst;

[0016] (5) When the electrolytic cell is a diaphragm electrolytic cell, the electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0017] In step 2, during the absorption process, the CO2 loading in the VMS is 30%-85% of the saturated CO2 absorption capacity of the VMS; during the desorption process, the CO2 loading in the VMS regenerated solution is 5%-30% of the saturated CO2 absorption capacity of the VMS; wherein, the CO2 loading in the VMS is characterized by measuring the conductivity of the VMS trapping agent.

[0018] In the electrochemical desorption and conversion process, the cathode material used is selected from one of graphite, zinc, titanium, nickel, and platinum, or one of the corresponding alloys, oxides, sulfides, nitrides, and phosphides of zinc, titanium, nickel, and platinum.

[0019] In the electrochemical regeneration and conversion process, the anode material is selected from one of the platinum group noble metals, nickel, cobalt, iron, and manganese, or one of the corresponding alloys, metal oxides and hydroxides of the platinum group noble metals, nickel, cobalt, iron, and manganese, or a carbon-supported catalyst, or a coating with catalytic activity for conversion reaction is coated on an alkali metal conductive substrate.

[0020] The molar ratio of the superbase to the alcohol is 1:(1~3), and the additive content does not exceed 20% of the molar amount of the superbase.

[0021] The superbase comprises one or more of the following: 1,1,3,3-tetramethylguanidine, 1,5,7-triazabicyclo[4.4.0]dec-5-ene, 7-methyl-1,5,7-triazabicyclo[4.4.0]dec-5-ene, 2-tert-butylimino-2-diethylamino-1,3-dimethylperhydro-1,3,2-diazaphosphine, and phosphazene ligand P2-tert-butyl solution;

[0022] The additive is selected from one or more of amines, imines, and imidazoles.

[0023] The conditions for the electrochemical regeneration and conversion method are as follows: electrochemical regeneration temperature is 10℃~40℃, electrolysis potential is -0.5V vs. Pt~-5.0V vs. Pt, and the CO2 absorption load in the initial electrolyte is preferably 60%-80% of the VMS saturation absorption capacity;

[0024] After undergoing the aforementioned “absorption-electrochemical desorption” cycle, the CO2 absorption capacity recovery rate of VMS is no less than 95% of the initial capacity.

[0025] The preferred electrochemical regeneration temperature is 20℃~30℃, and the preferred electrolysis potential is -1.0V vs. Pt to -2.0V vs. Pt. Under these conditions, the current efficiency of CO2 desorption is higher than 70%, and the energy consumption for regenerating a unit mass of CO2 is lower than 1.3 GJ / tCO2.

[0026] The method for preparing the glassy mixed solvent is as follows: a superalkali and an alcohol are mixed in a certain proportion and stirred to form a homogeneous and transparent solution. Then, an additive is added to the solution, and the mixture is stirred continuously at 30°C to 50°C until a homogeneous and transparent solution is obtained again. Finally, the mixture is cooled to room temperature to obtain the target solvent.

[0027] An electrochemical regeneration and conversion system for a carbon dioxide-supported absorbent, used to implement the method, includes a CO2 trapping liquid storage tank, a pump, and an electrolytic cell; the CO2 trapping liquid storage tank is used to store CO2-loaded VMS absorbent and VMS regenerated liquid; the pump is used to transport or output various liquids from the storage tank to the electrolytic cell; the electrolytic cell is used to carry out electrochemical desorption and conversion reactions; the regenerated VMS trapping liquid is returned to the CO2 trapping liquid storage tank for the CO2 absorption process;

[0028] The electrolytic cell is a single-cell electrolytic cell or a diaphragm electrolytic cell.

[0029] An ion exchange membrane is provided between the cathode chamber and the anode chamber of the diaphragm electrolytic cell. The ion exchange membrane is either a cation exchange membrane or a bipolar membrane.

[0030] Compared with existing technologies, the present invention has the following significant advantages:

[0031] (1) Simplicity of operation: The electrochemical regeneration and conversion method of CO2 supported absorbent proposed in this invention has a simple process flow and is easy to operate, which greatly reduces the complexity of the system;

[0032] (2) Low-temperature desorption and energy consumption optimization: Achieve efficient CO2 desorption at room temperature, which is significantly lower than the high temperature (>100℃) required for traditional thermal regeneration, avoids the core problem of sensible heat loss, and greatly reduces the energy consumption and operating cost of carbon dioxide capture;

[0033] (3) Improved absorbent stability: The low-temperature electrochemical regeneration mechanism effectively inhibits the thermal degradation and volatility loss of the absorbent, extends its service life, reduces the frequency of replenishment and the generation of harmful substances, and reduces the cost of waste treatment;

[0034] (4) Advantages of renewable energy compatibility and system integration: With electricity as the core driving energy, it supports coordinated operation with intermittent renewable energy sources such as wind power and photovoltaics; through intelligent scheduling, it can regenerate during the green electricity surplus period to achieve grid load balance. At the same time, it completely eliminates the dependence on steam boilers and pipelines, simplifies the layout of factory infrastructure, and is especially suitable for scenarios without cheap steam sources, promoting deep carbon reduction in the carbon capture process. Attached Figure Description

[0035] Figure 1 This is the linear voltammetry (LSV) curve of CO2 absorbed by the carbon dioxide supported absorbent (TMG-MeOH) in Example 1 of this invention;

[0036] Figure 2 This is a schematic diagram of the system of the present invention for carbon capture, electrochemical regeneration and conversion of carbon dioxide supported absorbent using a single-chamber electrolyzer;

[0037] In the diagram: 1-Industrial carbon-containing flue gas I; 2-CO2 collection liquid storage tank I; 3-Liquid pump; 4-Single-chamber electrolytic cell; 5-Cathode conductive plate; 6-Cathode I; 7-Anode I; 8-Anode conductive plate; 9-Gas outlet.

[0038] Figure 3 This is a schematic diagram of the system of the present invention for carbon capture, electrochemical regeneration and conversion of carbon dioxide supported absorbent using a diaphragm electrolyzer;

[0039] In the diagram: 10-Industrial carbon-containing flue gas II; 11-CO2 collection liquid storage tank II; 12-Liquid pump I; 13-Cathode chamber; 14-Anode chamber; 15-Cathode II; 16-Ion exchange membrane; 17-Anode II; 18-CO2 catalytic hydrogenation tower; 19-Liquid pump II; 20-Alkaline methanol solution storage tank.

[0040] Figure 4These are chromatograms of the gaseous products from the cathode chamber of the electrolytic cell in Examples 2 and 5 of this invention;

[0041] Figure 5 This refers to the electrolyte in the cathode chamber and the electrolyte in the anode chamber of the electrolytic cell in Embodiment 2 of the present invention. 13 C NMR spectrum;

[0042] Figure 6 This is the curve showing the change of current density over time during the electrolysis process in Embodiment 3 of the present invention. Detailed Implementation

[0043] This invention provides an electrochemical regeneration and conversion method for a carbon dioxide-supported absorbent. A vitreous mixture solvent (VMS) after CO2 capture is added to an electrolytic cell. Electrolysis is performed by applying a potential to obtain a capture solution and a carboxylate. The capture solution is used for CO2 capture. The electrolytic cell used in this invention is a single-chamber electrolytic cell or a diaphragm electrolytic cell. When the electrolytic cell is a diaphragm electrolytic cell, the initial cathode electrolyte is the vitreous mixture solvent after CO2 capture. The anode electrolyte is an alkaline methanol solution composed of 0.5 mol / L to 4 mol / L soluble alkali and methanol in a molar ratio of soluble alkali:methanol = (2~6):1. An ion exchange membrane separates the cathode and anode chambers. Electrolysis is performed by applying a potential. The cathode chamber undergoes a regeneration reaction to obtain the capture solution, which is used for CO2 capture. The anode chamber undergoes an electrochemical conversion to generate a carboxylate.

[0044] In the electrochemical regeneration and conversion method of carbon dioxide supported absorbent provided by the present invention, the electrochemical regeneration temperature is 10℃~40℃, the CO2 absorption load in the vitreous mixture solvent (VMS) after CO2 capture is in the range of 0.05g CO2 / g VMS~0.30g CO2 / g VMS, and the electrolysis potential is -1.0V vs. Pt~-5.0V vs. Pt.

[0045] The vitreous mixed solvent in this invention is the collecting solution, which is composed of an additive in a molar ratio of superbase to alcohol of 1:(1~3) and an addition amount not exceeding 20% ​​of the molar amount of the superbase, and is prepared according to the following method:

[0046] The superbase and alcohol are mixed in a certain proportion and stirred to form a homogeneous and transparent solution. Then, an additive is added and the mixture is stirred continuously at 30℃~50℃ until a homogeneous and transparent solution is obtained again. Finally, the mixture is cooled to room temperature to obtain the target solvent.

[0047] The vitreous mixed solvent of the present invention is used at a pressure of 0.1 bar to 30 bar within the range of 10°C to 50°C, at a rate of 50 mL / min. -1 ~300mL·min -1 The gas flow rate is used to capture CO2. The CO2 absorption load of the glassy mixed solvent reaches a maximum of 0.30 g CO2 / g VMS, and the viscosity after CO2 absorption is less than 30 mPa·s, with a maximum conductivity of 13.38 mS·cm. -1 .

[0048] In preparing the glass-like mixed solvent, the superbase used in this invention includes one or more of the following: 1,1,3,3-tetramethylguanidine, 1,5-diazabicyclo[4.3.0]non-5-ene, 1,8-diazabicyclo[5.4.0]undec-7-ene, 1,5,7-triazabicyclo[4.4.0]dec-5-ene, 7-methyl-1,5,7-triazabicyclo[4.4.0]dec-5-ene, 2-tert-butylimino-2-diethylamino-1,3-dimethylperhydro-1,3,2-diazaphosphine, and the phosphazene ligand P2-tert-butyl solution; the alcohol includes methyl... One or more of the following: alcohol, ethanol, ethylene glycol, n-propanol, isopropanol, propylene glycol, glycerol, n-butanol, isobutanol, tert-butanol, cyclobutanol, butanediol, glycerol, menthol, and dodecanol; additives include one or more of the following: monoethanolamine, diethanolamine, triethanolamine, N-methyldiethanolamine, diisopropanolamine, succinimide, maleimide, hexamethyleneimide, N-hydroxysuccinimide, triethylenediamine, tetramethylethylenediamine, imidazole, 2-methylimidazole, 2-imidazolidineone, imidazole-2-methanol, pyridine, acetamide, propionamide, succinamide, salicylamide, and thioamide.

[0049] Soluble alkaline solutions include sodium hydroxide (NaOH), potassium hydroxide (KOH), sodium carbonate (Na2CO3), sodium bicarbonate (NaHCO3), potassium carbonate (K2CO3), and potassium bicarbonate (KHCO3).

[0050] The ion exchange membrane in this invention is selected from cation exchange membranes and bipolar membranes, and is used to separate the anode chamber and the cathode chamber and to perform ion transport. The cation exchange membrane is preferably a proton exchange membrane.

[0051] The cathode material includes one of the following: graphite, a metallic element or its alloy, oxide, sulfide, nitride, or phosphide; wherein the metallic element includes one of zinc, titanium, lead, tin, platinum, or molybdenum.

[0052] The anode material includes platinum group noble metals or their alloys (such as platinum-ruthenium, platinum-lead, platinum-bismuth), or one of nickel, cobalt, iron, manganese-based transition metals and their alloys, oxides and hydroxides, or a carbon-supported catalyst, or a material coated with a catalytically active coating on an alkali metal conductive substrate.

[0053] The present invention also provides two systems for the synergistic execution of carbon capture, electrochemical regeneration and conversion using carbon dioxide supported absorbents, employing a single-chamber electrolyzer and a membrane electrolyzer, respectively.

[0054] The single-chamber electrolytic cell system includes a CO2 capture liquid storage tank, a pump, and an electrolytic cell. The cathode and anode electrodes are fixed to the cathode conductive plate and anode conductive metal plate respectively via plug-in structures. The number and spacing of the electrodes can be adjusted according to different electrolytes and electrolysis requirements, effectively improving the electrolytic cell's adaptability to various operating conditions. Both the cathode and anode electrodes are located inside the electrolytic cell and connected to the power supply via the cathode and anode conductive plates, avoiding the traditional design where the electrodes are exposed for power connection, thus improving the effective utilization rate of electrode materials. During system operation, industrial carbon-containing flue gas is introduced into the CO2 capture liquid storage tank and pumped to the electrolytic cell for desorption and conversion reactions. The regenerated VMS capture liquid is then output to the CO2 capture liquid storage tank for CO2 reabsorption.

[0055] The diaphragm electrolyzer system includes a CO2 capture solution storage tank, an alkaline methanol solution storage tank, a CO2 catalytic hydrogenation tower, an electrolytic cell, and two pumps. The cathode CO2 capture solution storage tank also serves as a CO2 absorption tower, absorbing industrial carbon-containing flue gas. In the electrolytic cell, the anode and cathode chambers are separated by an ion-exchange membrane. The cathode electrode is inserted into the electrolyte in the cathode chamber, and the anode electrode is inserted into the electrolyte in the anode chamber. The cathode CO2 capture solution storage tank, pump I, and the cathode chamber are connected in series via pipelines. Similarly, the anode alkaline methanol solution storage tank, pump II, and the anode chamber are connected in series via pipelines. The two ends of the CO2 catalytic hydrogenation tower are connected to the cathode chamber and the alkaline methanol solution storage tank, respectively, via pipelines. During system operation, industrial carbon-containing flue gas is introduced into the cathode CO2 capture liquid storage tank. The solvents in different tanks are respectively transported to the electrolytic cell for desorption and conversion reactions by two pumps, and then output to the corresponding storage tanks for subsequent unit operations such as CO2 reabsorption and separation and purification of valuable substances.

[0056] This invention discloses an electrochemical regeneration and conversion method for carbon dioxide-supported absorbents. Using superalkalis, alcohols and amines, imidazoles, and pyridines as precursor components, a glassy mixed solvent is synthesized to efficiently capture CO2. In a single-chamber electrolyzer, the carbon-rich absorbent can be electrochemically regenerated, releasing CO2 and generating carboxylate, along with H2 and O2. When a diaphragm electrolyzer is used, the glassy mixed solvent after CO2 capture is directly used as the cathode electrolyte. Under applied potential, an electrochemically driven CO2 desorption reaction occurs. The CO2 and H2 generated in the cathode chamber are converted into methanol under the action of a catalyst. The generated methanol is added to the anode chamber for further conversion into the high-value chemical carboxylate. This integrated process significantly simplifies traditional production and regeneration processes, effectively reducing absorbent regeneration energy consumption and operating costs while greatly improving the system's environmental performance.

[0057] The mechanism of this invention lies in the following: the glassy mixed solvent mainly achieves CO2 capture by reacting with deprotonated alcohols and CO2 to generate alkyl carbonates. During the electrochemical regeneration process, a proton-coupled electron transfer reaction occurs in the cathode region, the protonated superbase undergoes a deprotonation reaction, is regenerated into a superbase, and is reduced to release hydrogen (H2). The alkyl carbonate reacts with hydrogen protons (H2) to form hydrogen gas. + The reaction occurs, resulting in CO2 desorption and conversion into alcohol. In the anode region of a single-chamber electrolyzer, alkyl carbonates are oxidized to produce oxygen (O2) and carboxylates; in the anode chamber of a diaphragm electrolyzer, alcohol molecules undergo deprotonation and oxidation to produce carboxylates. The protons (H+) removed during this process... + Hydrogen ions generated by water ionization in the system can migrate through the ion exchange membrane to the cathode chamber to participate in the reaction.

[0058] This invention provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, which solves the technical challenge of the source of "green hydrogen" in the CO2 catalytic hydrogenation process to methanol. It converts CO2 in industrial flue gas into valuable chemicals methanol and carboxylate, achieving synergistic operation of CO2 capture, desorption, and conversion.

[0059] The present invention provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbent, in which CO2 and H2 are extracted and synthesized into methanol, low-carbon olefins or liquid hydrocarbon fuels in a CO2 catalytic reactor under the action of a catalyst.

[0060] The present invention provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbent. When the electrolytic cell is a diaphragm electrolytic cell, the electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by electrodialysis to obtain a soluble alkaline solution and a carboxylic acid solution.

[0061] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative and not intended to limit the invention.

[0062] Example 1:

[0063] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a single-chamber electrolytic cell for electrochemical conversion and regeneration, including the following steps:

[0064] (1) Absorption: TMG and MeOH were mixed in a 1:1 ratio and stirred to form a homogeneous and transparent solution. Additive IM was added at a concentration of 10% of the molar amount of the superbase TMG. The mixture was stirred continuously at a constant temperature of 40°C to obtain a VMS solution. The VMS was cooled to 30°C, and CO2 was brought into contact with the VMS at a constant flow rate of 100 mL / min. CO2 was captured at 30°C and 0.1 bar. The mass of CO2 in the capture tank was recorded in real time until the CO2 absorption load of the VMS was 0.18 g CO2 / g VMS. The linear voltammetry (LSV) curve after CO2 absorption is shown below. Figure 1 As shown, a VMS absorbent loaded with CO2 was obtained; at this point, the CO2 absorption load of the VMS was 60% of the saturation absorption capacity.

[0065] (2) Electrochemical desorption and conversion: The CO2-loaded VMS absorbent was used as the electrolyte and placed in a single-chamber electrolytic cell. The working electrode was a platinum electrode, the counter electrode was a nickel foam electrode, and the reference electrode was a platinum electrode. The electrolysis was carried out at a constant potential of -5.0V vs. Pt at 25℃ and 1 bar. The cathode region generated regenerated VMS trapping solution, CO2 and H2. The anode region generated carboxylates was measured by ion chromatography. The CO2 absorption load of the absorbent was 30% of the saturated absorption capacity by measuring the conductivity of the system, thus realizing the electrochemical desorption and conversion of CO2.

[0066] (3) Regeneration absorbent return: The regenerated VMS capture liquid is returned to the CO2 capture liquid storage tank for CO2 capture again.

[0067] This embodiment also provides an electrochemical regeneration and conversion system for carbon dioxide supported absorbents, such as... Figure 2As shown, the method described in this embodiment includes a CO2 trapping liquid storage tank I2, a pump 3, a single-chamber electrolytic cell 4, a cathode I6, an anode I7, a gas outlet I9, and a carboxylate outlet. The CO2 trapping liquid storage tank I2, the pump 3, and the single-chamber electrolytic cell 4 are connected in series via pipes. The cathode I6 and anode I7 are fixed to the cathode conductive plate 5 and the anode conductive plate 8 respectively via plug-in structures. Each cathode I6 and anode I7 is arranged crosswise on the same plane. The cathodes I6 and anodes I7 are connected to the power supply via wires connected to the cathode conductive plate 5 and the anode conductive plate 8, respectively. This avoids the traditional design where the electrodes are exposed to connect to the power supply, thereby improving the effective utilization rate of the electrode materials. The gas outlet 9 is located at the top of the single-chamber electrolytic cell 4, and the carboxylate outlet is located at the bottom of the single-chamber electrolytic cell 4. Three cathodes I6 and three anodes I7 are provided. The distance between each electrode is adaptively adjusted according to the requirements of the electrolyte and electrolyte solution, thereby effectively improving the adaptability of the electrolytic cell to different operating conditions. During system operation, industrial carbon-containing flue gas 1 is introduced into CO2 capture liquid storage tank I 2, and then transported to the electrolytic cell for desorption and conversion reaction by the pump 3. The regenerated capture liquid is output to CO2 capture liquid storage tank I 2 for CO2 reabsorption.

[0068] Example 2:

[0069] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a membrane electrolyzer for electrochemical conversion and regeneration, including the following steps:

[0070] (1) Absorption: DBN and MeOH were mixed in a ratio of 1:1.5 and stirred to form a homogeneous and transparent solution, thus obtaining a VMS solution. The VMS was cooled to 25°C, and CO2 was brought into contact with the VMS at a constant flow rate of 150 mL / min. CO2 was captured at 25°C and 1 bar, and the mass in the CO2 capture tank was recorded in real time until the CO2 absorption load of the VMS reached 0.21 g CO2 / g VMS, resulting in a CO2-loaded VMS absorbent. At this point, the CO2 absorption load of the VMS was 80% of its saturation absorption capacity. The viscosity of the VMS absorbent after CO2 absorption was 28.15 mPa·s, and the conductivity was 4.39 mS·cm. -1 ;

[0071] (2) Electrochemical desorption and conversion: A CO2-loaded VMS absorbent was used as the cathode electrolyte, and a mixture of NaOH solution and methanol at a molar ratio of 2:1 (with a KOH concentration of 3 mol / L) was used as the anode electrolyte. Lead was used as the cathode material, nickel-manganese alloy as the anode material, and a cation exchange membrane as the ion exchange membrane. Electrolysis was performed at 25°C and 1 bar using a constant potential of -1.8 V vs. Pt. The cathode chamber produced regenerated VMS trapping solution, CO2, and H2, while the anode chamber produced carboxylates. The products from the cathode and anode chambers of the electrolytic cell were analyzed by gas chromatography and nuclear magnetic resonance spectroscopy, respectively, as follows:

[0072] The carbon dioxide capture process in the method is mainly achieved through the following reaction (1):

[0073] DBN + CH3OH + CO2→ DBNH + + CH3OCO2 - (1)

[0074] In the method, the electrochemical regeneration of the cathode chamber and the conversion of the anode chamber of the carbon dioxide supported absorbent are achieved through the following reactions (2) and (3):

[0075] DBNH + + CH3OCO2 - + 2H + + 2e - → DBN + CH3OH + H2 + CO2(2)

[0076] CH3OH + 5OH - - 4e - → HCOO - + 4H2O (3)

[0077] Analyzing gas chromatograms ( Figure 4 It can be seen that the gaseous products of the cathode chamber of the electrolytic cell mainly include carbon dioxide and hydrogen. The characteristic peak with an elution time of 0.1 min is the characteristic peak of hydrogen, and the characteristic peak with an elution time of 4 min is the characteristic peak of carbon dioxide. The proportions of carbon dioxide and hydrogen are 84.65% and 15.35%, respectively.

[0078] Analysis of cathode products 13 C NMR spectrum ( Figure 5 It can be seen that the chemical shift of C shifts to higher fields to varying degrees and decreases, indicating that DBNH +A deprotonation reaction occurred; furthermore, a new set of signal peaks appeared at δ = 174 ppm, which can be attributed to carboxylate ions formed by the reduction of a small amount of CO2. The CO2 absorption load of the absorbent was characterized by 5% of the saturation absorption capacity, the current efficiency of the desorption process was 80%, and the regeneration energy consumption per unit mass of CO2 was 1.1 GJ / t CO2. At the anode products... 13 In the C NMR spectrum, the signal peak at δ = 178 ppm indicates that methanol was oxidized to carboxylate ions with a yield of 91%. The liquid phase product in the anode chamber was extracted by a pump to obtain carboxylate, thus realizing the electrochemical regeneration and conversion of the absorbent.

[0079] (3) Return of regenerated absorbent: The regenerated VMS trapping solution is returned to the CO2 trapping solution storage tank for CO2 trapping again. After five “absorption-electrochemical desorption” cycles, its CO2 absorption capacity is restored to 95% of the initial capacity.

[0080] (4) CO2 and H2 are extracted and methanol and ethylene are synthesized in a CO2 catalytic reactor under the action of a catalyst.

[0081] (5) The electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by bipolar membrane electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0082] This embodiment also provides a system for the synergistic implementation of carbon capture, electrochemical regeneration, and conversion using a carbon dioxide supported absorbent, to achieve the above-mentioned method, such as... Figure 3 As shown, the system includes a CO2 trapping liquid storage tank II 11, an alkaline methanol solution storage tank 20, a diaphragm electrolyzer, a CO2 catalytic hydrogenation tower 18, and two pumps. The CO2 trapping liquid storage tank II 11 also serves as a CO2 absorption tower, absorbing industrial carbon-containing flue gas II 10. In the electrolyzer, the anode chamber 14 and the cathode chamber 13 are separated by an ion exchange membrane 16. The cathode II 15 is inserted into the electrolyte in the cathode chamber 13, and the anode II 17 is inserted into the electrolyte in the anode chamber 14. The CO2 trapping liquid storage tank II 11, pump I 12, and cathode chamber 13 are connected in series via pipelines. The alkaline methanol solution storage tank 20, pump II 19, and anode chamber 14 are also connected in series via pipelines. The two ends of the CO2 catalytic hydrogenation tower 18 are connected to the top of the cathode chamber 13 and the top of the alkaline methanol solution storage tank 20 via pipelines, respectively. During system operation, industrial carbon-containing flue gas II 10 is introduced into CO2 capture liquid storage tank II 11. The solvents in different tanks are respectively transported to the electrolytic cell for desorption and conversion reaction through two pumps, and then output to the corresponding storage tanks for subsequent unit operations such as CO2 reabsorption and separation and purification of valuable substances.

[0083] Example 3:

[0084] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a membrane electrolyzer for electrochemical conversion and regeneration, including the following steps:

[0085] (1) Absorption: DBN and EtOH were mixed in a 1:1 ratio and stirred to form a homogeneous and transparent solution. Additive Suc, with a content of 10% of the molar amount of the superbase DBN, was added. The mixture was stirred continuously at a constant temperature of 40℃ until a homogeneous and transparent solution was obtained again, thus obtaining the VMS solution. The VMS solution was then cooled to 20℃, and CO2 was brought into contact with VMS at a constant flow rate of 100 mL / min. CO2 was captured at 20℃ and 1 bar, and the mass in the CO2 capture tank was recorded in real time until the CO2 absorption load of VMS was 0.14 g CO2 / g VMS, thus obtaining the CO2-loaded VMS absorbent; at this time, the CO2 absorption load of VMS was 55% of the saturated absorption capacity. After the introduction of the additive, the viscosity of the system increased slightly from 9.30 mPa·s to 10.10 mPa·s, while the conductivity increased from 89.22 μS·cm. -1 Significantly increased to 1235 μS·cm -1 This results in minimal fluctuations in the system's conductivity throughout the absorption process. The introduced additive Suc and the deprotonated alcohol are both active sites for the CO2 reaction, achieving carbon capture by generating Suc-2CO2 complexes and alkyl carbonates, respectively, thereby regulating the binding form of CO2.

[0086] (2) Electrochemical desorption and conversion: VMS absorbent with a CO2 absorption load of 0.14 g CO2 / g VMS was used as the cathode electrolyte, and a mixture of KOH solution and methanol at a molar ratio of 2:1 (with NaOH concentration of 2 mol / L in the mixture) was used as the anode electrolyte. Graphite was used as the cathode material, nickel foam as the anode material, and a proton exchange membrane as the ion exchange membrane. Electrolysis was performed at 25℃ and 1 bar using a constant potential of -1.8 V vs. Pt for 60 min. The current density change curve over time is shown in the figure. Figure 6 As shown, the current density of the electrolytic cell system is maintained at 30 mA·cm⁻¹. -2 Gas chromatography analysis revealed that the main gaseous products in the cathode chamber of the electrolytic cell were CO2 and H2. The cathode chamber produced regenerated VMS trapping solution, CO2, and H2, while the anode chamber produced carboxylates. Measurements of the system's conductivity showed that the CO2 absorption load of the regenerated VMS trapping solution was 25% of its saturation absorption capacity.

[0087] (3) Return of regenerated absorbent: The regenerated VMS trap is returned to the CO2 trap storage tank for CO2 trapping again. After two “absorption-electrochemical desorption” cycles, its CO2 absorption capacity recovers to 96% of the initial capacity.

[0088] (4) CO2 and H2 are extracted and methanol and ethylene are synthesized in a CO2 catalytic reactor under the action of a catalyst.

[0089] (5) The electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by bipolar membrane electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0090] Example 4:

[0091] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a membrane electrolyzer for electrochemical conversion and regeneration, including the following steps:

[0092] (1) Absorption: MTBD and PrOH were mixed in a 1:3 ratio and stirred to form a homogeneous and transparent solution. Additive MEA, at a concentration of 10% of the molar amount of the superbase MTBD, was added. The mixture was stirred continuously at a constant temperature of 50°C until a homogeneous and transparent solution was obtained again, thus obtaining the VMS solution. CO2 was contacted with VMS at a constant flow rate of 50 mL / min, and CO2 was captured at 50°C and 10 bar. The mass in the CO2 capture tank was recorded in real time until the CO2 absorption load of VMS reached 0.11 g CO2 / g VMS, resulting in a CO2-loaded VMS absorbent solution. At this point, the CO2 absorption load of VMS was 55% of the saturated absorption capacity. The viscosity of the VMS absorbent solution after CO2 absorption was 16.5 mPa·s, and the conductivity was 8.62 mS·cm. -1 .

[0093] (2) Electrochemical desorption and conversion: A CO2-loaded VMS absorbent was used as the cathode electrolyte, and a mixture of K2CO3 solution and methanol at a molar ratio of 5:1 (with a K2CO3 concentration of 2 mol / L) was used as the anode electrolyte. Titanium-titanium oxide was used as the cathode material, platinum-ruthenium alloy as the anode material, and a bipolar membrane was used as the ion exchange membrane. Electrolysis was performed at 40℃ and 1 bar using a constant potential of -1.8 V vs. Pt. The cathode chamber generated regenerated VMS trapping solution, CO2, and H2, while the anode chamber generated carboxylates. The CO2 absorption load of the absorbent was 25% of the saturated absorption capacity, the current efficiency of the desorption process was 83%, and the regeneration energy consumption per unit mass of CO2 was 1.3 GJ / t CO2.

[0094] (3) Regeneration absorbent return: The regenerated VMS capture liquid is returned to the CO2 capture liquid storage tank for CO2 capture again.

[0095] (4) CO2 and H2 are extracted and methanol and propylene are synthesized in a CO2 catalytic reactor under the action of a catalyst.

[0096] (5) The electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by bipolar membrane electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0097] Example 5:

[0098] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a membrane electrolyzer for electrochemical conversion and regeneration, including the following steps:

[0099] (1) Absorption: DBU and MeOH were mixed in a 1:3 ratio and stirred to form a homogeneous and transparent solution. Suc, an additive, was added at 10% of the molar amount of the superbase DBU. The mixture was stirred continuously at a constant temperature of 40℃ until a homogeneous and transparent solution was obtained again, thus obtaining the VMS solution. CO2 was contacted with VMS at a constant flow rate of 250 mL / min, and CO2 was captured at 50℃ and 1 bar. The mass in the CO2 capture tank was recorded in real time until the CO2 absorption load of VMS reached 0.05 g CO2 / g VMS, resulting in a CO2-loaded VMS absorbent. At this point, the CO2 absorption load of VMS was 30% of the saturated absorption capacity. The viscosity of the VMS absorbent after CO2 absorption was 9.35 mPa·s, and the conductivity was 13.38 mS·cm. -1 .

[0100] (2) Electrochemical desorption and conversion: A CO2-loaded VMS absorbent was used as the cathode electrolyte, and a mixture of KHCO3 solution and methanol at a molar ratio of 4:1 (with a KHCO3 concentration of 3 mol / L) was used as the anode electrolyte. Zinc was used as the cathode material, platinum-bismuth alloy as the anode material, and a cation exchange membrane as the ion exchange membrane. Electrolysis was performed at 20℃ and 1 bar using a constant potential of -1.6 V vs. Pt. The cathode chamber produced regenerated VMS trapping solution, CO2, and H2, while the anode chamber produced carboxylates. The CO2 absorption load of the absorbent was characterized as 10% of the saturated absorption capacity by measuring the conductivity of the system.

[0101] (3) Return of regenerated absorbent: The regenerated VMS trapping solution is returned to the CO2 trapping solution storage tank for CO2 trapping again. After three “absorption-electrochemical desorption” cycles, its CO2 absorption capacity is restored to 96% of the initial capacity.

[0102] (4) CO2 and H2 are extracted and methanol and aromatics are synthesized in a CO2 catalytic reactor under the action of a catalyst.

[0103] (5) The electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by bipolar membrane electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0104] Example 6:

[0105] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a membrane electrolyzer for electrochemical conversion and regeneration, including the following steps:

[0106] (1) Absorption: TMG, MeOH and EG were mixed in a ratio of 6:4:1 and stirred to form a homogeneous and transparent solution. Additive MEA was added at a concentration of 15% of the molar amount of the superbase TMG. The mixture was stirred continuously at a constant temperature of 30°C until a homogeneous and transparent solution was obtained again, thus obtaining the VMS solution. The VMS solution was cooled to 25°C, and CO2 was brought into contact with VMS at a constant flow rate of 300 mL / min. CO2 was captured at 25°C and 30 bar, and the mass in the CO2 capture tank was recorded in real time until the CO2 absorption load of VMS was 0.25 g CO2 / g VMS, thus obtaining the CO2-loaded VMS absorbent. At this point, the CO2 absorption load of VMS was 85% of the saturation absorption capacity.

[0107] (2) Electrochemical desorption and conversion: A CO2-loaded VMS absorbent was used as the cathode electrolyte, and a mixture of KOH solution and methanol at a molar ratio of 6:1 (KOH concentration of 4 mol / L) was used as the anode electrolyte. Platinum was used as the cathode material, nickel-cobalt alloy as the anode material, and a proton exchange membrane as the ion exchange membrane. Electrolysis was performed at 20℃ and 1 bar using a constant potential of -1.0 V vs. Pt. The cathode chamber produced regenerated VMS trapping solution, CO2, and H2, while the anode chamber produced carboxylates. The CO2 absorption load of the absorbent was characterized as 20% of the saturated absorption capacity by measuring the conductivity of the system.

[0108] (3) Regeneration absorbent return: The regenerated VMS capture liquid is returned to the CO2 capture liquid storage tank for CO2 capture again.

[0109] (4) CO2 and H2 are extracted and methanol and aromatics are synthesized in a CO2 catalytic reactor under the action of a catalyst.

[0110] (5) The electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by bipolar membrane electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0111] Example 7:

[0112] This embodiment provides an electrochemical regeneration and conversion method for carbon dioxide supported absorbents, employing a membrane electrolyzer for electrochemical conversion and regeneration, including the following steps:

[0113] (1) Absorption: DBN, MTBD, EtOH and PrOH were mixed in the same molar ratio and stirred to form a homogeneous and transparent quaternary glassy mixed solvent, thus obtaining a VMS solution. CO2 was brought into contact with VMS at a constant flow rate of 150 mL / min, and CO2 was captured at 10 °C and 5 bar. The mass in the CO2 capture tank was recorded in real time until the CO2 absorption load of VMS was 0.08 g CO2 / g VMS, thus obtaining a CO2-loaded VMS absorbent; at this point, the CO2 absorption load of VMS was 80% of the saturation absorption capacity.

[0114] (2) Electrochemical desorption and conversion: A CO2-loaded VMS absorbent was used as the cathode electrolyte, and a mixture of K2CO3 and KHCO3 in a 3:1 molar ratio with methanol (K2CO3 and KHCO3 concentrations were both 0.5 mol / L) was used as the anode electrolyte. Graphite was used as the cathode material, platinum-ruthenium alloy as the anode material, and a bipolar membrane as the ion exchange membrane. Electrolysis was performed at 10℃ and 1 bar using a constant potential of -1.5 V vs. Pt. The cathode chamber produced regenerated VMS trapping solution, CO2, and H2, while the anode chamber produced carboxylates. The CO2 absorption load of the absorbent was characterized as 25% of the saturated absorption capacity by measuring the conductivity of the system.

[0115] (3) Regeneration absorbent return: The regenerated VMS capture liquid is returned to the CO2 capture liquid storage tank for CO2 capture again.

[0116] (4) CO2 and H2 are extracted and methanol and ethylene are synthesized in a CO2 catalytic reactor under the action of a catalyst.

[0117] (5) The electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by bipolar membrane electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

[0118] The above embodiments should be understood as being used only to illustrate the present invention more clearly, and not to limit the scope of the present invention. After reading the present invention, any modifications of the present invention in various equivalent forms by those skilled in the art fall within the scope of protection of the present invention.

Claims

1. A method for electrochemical regeneration and conversion of a carbon dioxide supported absorbent, characterized in that, Includes the following steps: (1) Absorption: The gas containing carbon dioxide is contacted with a glassy mixed solvent VMS to capture CO2, resulting in a CO2-loaded VMS absorbent; wherein the glassy mixed solvent VMS is composed of a superbase, an alcohol, and additives, and its maximum CO2 saturation absorption load is 0.30 g CO2 / g VMS, the viscosity after CO2 absorption is less than 30 mPa·s, and the maximum conductivity is 13.38 mS·cm. -1 ; (2) Electrochemical desorption and conversion: The CO2-loaded VMS absorbent obtained in step (1) is used as the electrolyte and placed in an electrolytic cell to carry out electrochemical desorption and conversion reactions. The cathode chamber or cathode region generates regenerated VMS collecting liquid, CO2 and H2, and the anode chamber or anode region generates carboxylate. (3) Return of regenerated absorbent: The regenerated VMS capture solution generated at the cathode in step (2) is returned to step (1) for CO2 capture again; The electrolytic cell is a single-chamber electrolytic cell or a diaphragm electrolytic cell.

2. The electrochemical regeneration and conversion method for a carbon dioxide supported absorbent according to claim 1, characterized in that, When the electrolytic cell is a diaphragm electrolytic cell, during the electrochemical desorption and conversion process, the CO2-loaded VMS absorbent is used as the cathode electrolyte, and the alkaline methanol solution is used as the anode electrolyte; wherein, the alkaline methanol solution is obtained by mixing 0.5mol / L~4mol / L soluble alkali and methanol at a molar ratio of (2~6):

1.

3. The electrochemical regeneration and conversion method for a carbon dioxide supported absorbent according to claim 1 or 2, characterized in that, Also includes: (4) CO2 and H2 are extracted and synthesized into methanol, low-carbon olefins or liquid hydrocarbon fuels in a CO2 catalytic reactor under the action of a catalyst; (5) When the electrolytic cell is a diaphragm electrolytic cell, the electrolyte in the anode chamber containing carboxylate after the electrochemical reaction is recovered and regenerated by electrodialysis to obtain soluble alkaline solution and carboxylic acid solution.

4. The electrochemical regeneration and conversion method for a carbon dioxide supported absorbent according to claim 1 or 2, characterized in that, During absorption, the CO2 loading in VMS is 30%-85% of the saturated CO2 absorption capacity of VMS; during desorption, the CO2 loading in VMS regenerated solution is 5%-30% of the saturated CO2 absorption capacity of VMS; the CO2 loading in VMS is characterized by measuring the conductivity of the VMS trapping agent.

5. A method for electrochemical regeneration and conversion of a carbon dioxide supported absorbent according to claim 1 or 2, characterized in that, In the electrochemical desorption and conversion process, the cathode material used is selected from one of graphite, zinc, titanium, nickel, and platinum, or one of the corresponding alloys, oxides, sulfides, nitrides, and phosphides of zinc, titanium, nickel, and platinum. In the electrochemical regeneration and conversion process, the anode material is selected from one of the platinum group noble metals, nickel, cobalt, iron, and manganese, or one of the corresponding alloys, metal oxides and hydroxides of the platinum group noble metals, nickel, cobalt, iron, and manganese, or a carbon-supported catalyst, or a coating with catalytic activity for conversion reaction is coated on an alkali metal conductive substrate. The molar ratio of the superbase to the alcohol is 1:(1~3), and the additive content does not exceed 20% of the molar amount of the superbase. The superbase comprises one or more of the following: 1,1,3,3-tetramethylguanidine, 1,5,7-triazabicyclo[4.4.0]dec-5-ene, 7-methyl-1,5,7-triazabicyclo[4.4.0]dec-5-ene, 2-tert-butylimino-2-diethylamino-1,3-dimethylperhydro-1,3,2-diazaphosphine, and phosphazene ligand P2-tert-butyl solution; The additive is selected from one or more of amines, imines, and imidazoles.

6. A method for electrochemical regeneration and conversion of a carbon dioxide supported absorbent according to claim 1 or 2, characterized in that, The conditions for the electrochemical regeneration and conversion method are as follows: electrochemical regeneration temperature is 10℃~40℃, electrolysis potential is -0.5V vs. Pt~-5.0V vs. Pt, and the CO2 absorption load in the initial electrolyte is preferably 60%-80% of the VMS saturation absorption capacity; After undergoing the "absorption-electrochemical desorption" cycle as described in claim 1, the CO2 absorption capacity recovery rate of VMS is not less than 95% of the initial capacity.

7. The electrochemical regeneration and conversion method for a carbon dioxide supported absorbent according to claim 6, characterized in that, The preferred electrochemical regeneration temperature is 20℃~30℃, and the electrolysis potential is -1.0V vs. Pt~-2.0V vs. Pt. Under these conditions, the current efficiency of CO2 desorption is higher than 70%, and the energy consumption for regenerating a unit mass of CO2 does not exceed 1.3 GJ / t CO2.

8. A method for electrochemical regeneration and conversion of a carbon dioxide supported absorbent according to claim 1 or 2, characterized in that, The method for preparing the glassy mixed solvent is as follows: a superalkali and an alcohol are mixed in a certain proportion and stirred to form a homogeneous and transparent solution. Then, an additive is added to the solution, and the mixture is stirred continuously at 30°C to 50°C until a homogeneous and transparent solution is obtained again. Finally, the mixture is cooled to room temperature to obtain the target solvent.

9. A carbon dioxide supported absorbent electrochemical regeneration and conversion system for implementing the method of claim 1, characterized in that, It includes a CO2 capture liquid storage tank, a pump, and an electrolytic cell; the CO2 capture liquid storage tank is used to store CO2-loaded VMS absorbent and VMS regenerated liquid; the pump is used to transport or output various liquids from the storage tank to the electrolytic cell; the electrolytic cell is used to carry out electrochemical desorption and conversion reactions; the regenerated VMS capture liquid is sent back to the CO2 capture liquid storage tank for CO2 absorption; The electrolytic cell is a single-chamber electrolytic cell or a diaphragm electrolytic cell.

10. The carbon dioxide supported absorbent electrochemical regeneration and conversion system according to claim 9, characterized in that, An ion exchange membrane is provided between the cathode chamber and the anode chamber of the diaphragm electrolytic cell. The ion exchange membrane is either a cation exchange membrane or a bipolar membrane.

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