Industrial gas carbon capture system and industrial gas carbon capture method

Abstract

The invention provides an industrial gas carbon capture system and an industrial gas carbon capture method, and belongs to the technical field of carbon neutralization, specifically, the industrial gas carbon capture system provided by the invention comprises: a membrane separation system for enriching carbon dioxide; the biological conversion system is connected with the membrane separation system through a pipeline, is used for reducing carbon dioxide gas into a multi-carbon compound and comprises an H-type three-electrode electrolytic tank, the H-type three-electrode electrolytic tank comprises a cathode chamber and an anode chamber, the cathode chamber and the anode chamber are separated through a proton exchange membrane, and the proton exchange membrane is connected with the membrane separation system through a pipeline. An electrolyte is arranged in the cathode chamber, and the electrolyte comprises a clostridium Young's cell breaking solution. By adopting the industrial gas carbon capture system and the industrial gas carbon capture method provided by the invention, the production quantity of multi-carbon compounds can be greatly increased on the basis of reducing the electrosynthesis cost.

Description

Technical Field

[0001] The present invention relates to the field of carbon neutrality technology, and in particular to an industrial gas carbon capture system and an industrial gas carbon capture method. Background Art

[0002] Excessive carbon dioxide emissions will lead to global climate change and energy crisis. In the context of "dual carbon", carbon capture, utilization and storage technology has become a key path to carbon neutrality. At present, traditional carbon dioxide capture technology has problems of high energy consumption and secondary pollution, and the independent microbial electrosynthesis (MES) system needs to rely on high-purity carbon dioxide. At the same time, the MES system also faces efficiency limitations due to gas compression and impurity interference.

[0003] Although membrane separation technologies (such as metal-organic frameworks / MOFs) offer environmentally friendly solutions for CO2 enrichment from industrial flue gases (10%–30% CO2 content), existing systems still lack direct coupling with downstream bioconversion. The separated CO2 typically requires energy-intensive compression and purification before entering the bioreactor, a process that not only increases operating costs by 20%–30% but also inhibits microbial activity. Furthermore, the low electron transfer efficiency of conventional whole-cell biocatalysts limits the yield of multi-carbon compounds. Summary of the Invention

[0004] The technical problem to be solved by the present invention is how to reduce the processing cost of a microbial electrosynthesis system while improving production efficiency.

[0005] To solve the above technical problems, a first aspect provides an industrial gas carbon capture system, comprising: Membrane separation systems for carbon dioxide enrichment; and A bioconversion system connected to a membrane separation system pipeline, the bioconversion system being used to reduce carbon dioxide gas to multi-carbon compounds, the bioconversion system comprising an H-type three-electrode electrolytic cell, the H-type three-electrode electrolytic cell comprising a cathode chamber and an anode chamber, the cathode chamber and the anode chamber being separated by a proton exchange membrane, the cathode chamber containing an electrolyte comprising Clostridium ljungdahlii lysis fluid.

[0006] In the industrial gas carbon capture system provided by the present invention, the membrane separation system and the biological conversion system are directly connected by a pipeline. The carbon dioxide enriched in the membrane separation system can directly enter the biological conversion system for reduction reaction to generate multi-carbon compounds. Unlike the existing technology, the carbon dioxide in the industrial gas carbon capture system provided by the present invention does not need to undergo carbon dioxide compression and storage steps. By using the industrial gas carbon capture system provided by the present invention, the energy consumption of the system can be effectively reduced.

[0007] At the same time, the industrial gas carbon capture system provided by the present invention uses Clostridium ljungdahlii lysate as a microbial electrosynthesis carrier. The Clostridium ljungdahlii lysate contains a complete polycarbonate synthase system, and the lysate has a better ability to tolerate the electrolytic environment than living cells, which can effectively increase the yield of polycarbon compounds.

[0008] Preferably, the membrane separation system comprises a metal organic framework glass membrane, and the metal organic framework glass membrane is selected from any one or more of a ZIF-4 glass membrane, a ZIF-62 glass membrane, a ZIF-76 glass membrane, and a TIF-4 glass membrane.

[0009] The present invention uses a metal organic framework glass membrane to separate industrial gas. The metal organic framework glass membrane has the characteristics of being amorphous. While improving the selectivity of carbon dioxide, it is not easy to collapse and fail during use.

[0010] Preferably, the protein concentration in the electrolyte is 1-10 mg / mL.

[0011] Preferably, the electrolyte further comprises 10-45 g / L of biochar, 0.2-1 g / L of cysteine ​​hydrochloride, 0.5-1.5 mg / L of resazurin, 10-15 mM of methyl viologen, 0.01-0.05 mM of NADH, and 0.01-0.05 mM of NADPH.

[0012] In the industrial gas carbon capture system provided by the present invention, biochar has a microporous-mesoporous structure, which can provide an electron transfer interface and increase the generation rate of multi-carbon compounds; resazurin serves as a redox indicator; and methyl viologen acts as an electron mediator to promote electron transfer between the enzyme and the electrode.

[0013] Preferably, the multi-carbon compound is selected from any one or more of acetic acid, ethanol, butanol, and isopropanol.

[0014] Preferably, the Clostridium ljungdahlii lysis solution is obtained by ultrasonic cell disruption or homogenization cell disruption.

[0015] Preferably, the working electrode of the H-type three-electrode electrolytic cell is a glassy carbon electrode, the auxiliary electrode is a graphite electrode, and the reference electrode is a silver-silver chloride electrode.

[0016] In the industrial gas carbon capture system provided by the present invention, the working electrode is connected to the cathode chamber for reducing carbon dioxide to multi-carbon compounds. The reason for using a glassy carbon electrode as the working electrode is that the glassy carbon electrode has high conductivity and high biocompatibility, which can effectively maintain the stability of the enzyme.

[0017] A second aspect of the present invention provides an industrial gas carbon capture method, which uses the industrial gas carbon capture system described in the first aspect to capture carbon dioxide.

[0018] Preferably, the industrial gas carbon capture method comprises the following steps: S1: passing industrial flue gas into a membrane separation system to obtain carbon dioxide enriched gas; S2: The carbon dioxide-enriched gas is directly introduced into the cathode chamber and a voltage of 0.5~1V is applied to react and generate multi-carbon compounds.

[0019] Compared with the prior art, the present invention has the following beneficial effects: The present invention combines metal-organic framework glass membrane separation and microbial electrosynthesis for the first time. By using the industrial gas carbon capture system provided by the present invention, the production of multi-carbon compounds can be increased while omitting the carbon dioxide compression and storage steps, which has broad application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 a in Example 1 of the present invention g XRD characterization results of TIF-4 and TIF-4; Figure 2 a in Example 1 of the present invention g SEM characterization results of TIF-4; Figure 3 a in Example 2 of the present invention g XRD characterization results of ZIF-62 and ZIF-62; Figure 4 a in Example 2 of the present invention g SEM characterization results of ZIF-62 cross section. DETAILED DESCRIPTION

[0021] To make the above-mentioned objects, features, and advantages of the present invention more clearly understood, specific embodiments of the present invention are described in detail below. It should be noted that the following embodiments are only intended to illustrate the implementation methods and typical parameters of the present invention, and are not intended to limit the parameter ranges described in the present invention. Reasonable variations derived therefrom are still within the scope of protection of the claims of the present invention.

[0022] It should be noted that the endpoints of the ranges and any values ​​disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be considered to be specifically disclosed herein.

[0023] The molar ratio of carbon dioxide in industrial gas and industrial flue gas is about 15%. Existing technologies cannot effectively separate carbon dioxide from industrial gas. To solve this problem, a specific embodiment of the present invention provides an industrial gas carbon capture system, which includes: Membrane separation systems for carbon dioxide enrichment; and A bioconversion system connected to a membrane separation system pipeline, the bioconversion system being used to reduce carbon dioxide gas to multi-carbon compounds, the bioconversion system comprising an H-type three-electrode electrolytic cell, the H-type three-electrode electrolytic cell comprising a cathode chamber and an anode chamber, the cathode chamber and the anode chamber being separated by a proton exchange membrane, the cathode chamber containing an electrolyte comprising Clostridium ljungdahlii lysis fluid.

[0024] In the above embodiment, the membrane separation system includes a metal organic framework glass membrane, and the metal organic framework glass membrane is selected from any one or more of ZIF-4 glass membrane, ZIF-62 glass membrane, ZIF-76 glass membrane, and TIF-4 glass membrane.

[0025] More specifically, in the above embodiment, the metal organic framework glass film is preferably prepared by the following steps: A1: Preparation of MOF crystal film by conventional method; A2: The MOF crystal film is heated using a Joule heater in an argon atmosphere to achieve the glass transition of the MOF crystal film and obtain a MOF glass film.

[0026] In the above embodiment, the heating temperature of the MOF crystal film using a Joule heater in an argon atmosphere is preferably 750-850° C., and the heating time is preferably 5-15 seconds.

[0027] In the above embodiment, the protein concentration in the electrolyte is 1-10 mg / mL.

[0028] In the above embodiment, the electrolyte further includes 10-45 g / L biochar, 0.2-1 g / L cysteine ​​hydrochloride, 0.5-1.5 mg / L resazurin, 10-15 mM methyl viologen, 0.01-0.05 mM NADH, and 0.01-0.05 mM NADPH.

[0029] In the above embodiment, the multi-carbon compound is selected from any one or more of acetic acid, ethanol, butanol, and isopropanol.

[0030] More specifically, in the above embodiment, if the cell lysis solution in the electrolyte is Clostridium ljungdahlii cell lysis solution, the industrial gas carbon capture system provided by the above embodiment can convert carbon dioxide into acetic acid and ethanol.

[0031] More specifically, in the above embodiment, if the electrolyte includes Clostridium acetobutylicum lysate in addition to Clostridium ljungdahlii lysate, the industrial gas carbon capture system provided by the above embodiment can convert carbon dioxide into acetic acid, ethanol, butanol, isopropanol, and butyric acid.

[0032] That is, by changing the composition of the cell lysate in the electrolyte, the industrial gas carbon capture system provided by the present invention can convert carbon dioxide into different multi-carbon compounds.

[0033] In the above embodiment, the cell lysis solution of Clostridium ljungdahlii or Clostridium acetobutylicum is obtained by ultrasonic cell lysis or homogenization cell lysis.

[0034] In the above embodiment, the working electrode of the H-type three-electrode electrolytic cell is a glassy carbon electrode, the auxiliary electrode is a graphite electrode, and the reference electrode is a silver-silver chloride electrode.

[0035] The technical solutions of the present invention are further described below by specific examples. Unless otherwise defined, all terms, symbols and other scientific terms used herein are intended to have the same meaning as those commonly understood by those skilled in the art to which the present invention belongs. In some cases, terms with conventional understandings are defined herein for the purpose of illustrating or facilitating reference. Such definitions herein should not be construed as indicating significant differences from conventional understandings in the art. The technical methods described or cited herein are generally well understood by those skilled in the art and are adopted by conventional methods. Unless otherwise stated, the use of commercially available kits, reagents and instruments is carried out in accordance with the protocols and parameters provided by the manufacturers.

[0036] Example 1 Preparation of TIF-4 glass membrane and its carbon dioxide separation performance test Preparation of TIF-4 glass membrane: Imidazole and 5-methylbenzimidazole were dissolved in DMF in appropriate proportions, mixed well, and then zinc nitrate hexahydrate was added and stirred for 30 minutes to obtain a precursor solution. The molar ratio of Zn, imidazole, 5-methylbenzimidazole, and DMF in the precursor solution was 1:23:2.5:69. A flaky alumina support was immersed in the precursor solution and dried in a forced air oven at 130 o The TIF-4 crystal film was heated from 25°C to 750°C at a heating rate of 600°C / s in a Joule heating apparatus under an argon atmosphere, then maintained at 750°C for 5 seconds and cooled to room temperature to obtain a TIF-4 glass film, which was labeled as a. g TIF-4,a g The membrane area of ​​TIF-4 is 0.88 cm 2 .

[0037] Characterization of TIF-4 glass membrane: a g The XRD characterization results of TIF-4 and TIF-4 are as follows Figure 1 As shown by Figure 1 It can be seen that the a prepared by Joule heating g The structure of TIF-4 is transformed from the crystalline structure of TIF-4 to an amorphous structure.

[0038] a g The SEM characterization results of TIF-4 are as follows Figure 2 As shown by Figure 2 It can be seen that a g The surface of TIF-4 membrane is a continuous glass membrane layer, which is dense and defect-free.

[0039] a g Carbon dioxide separation performance test of TIF-4: g TIF-4 was used to test the carbon dioxide separation performance. A mixture of CO2 and N2 with an equal molar ratio was introduced into the feed side. The pressure on the feed side was set to 3.5 bar. The permeation test was performed at atmospheric pressure. The final test results were: a g The carbon dioxide permeability of TIF-4 is 48.7×10 -9 mol m -2 s -1 Pa -1 , CO2 / N2 selectivity is 13.2. The carbon dioxide content in the permeate side gas is 93 vol.%, and the carbon dioxide flow rate is 0.025 mL / s. g TIF-4 has excellent carbon dioxide enrichment ability.

[0040] Example 2 Preparation of ZIF-62 glass membrane and its carbon dioxide separation performance test Preparation of ZIF-62 glass film: zinc nitrate hexahydrate, imidazole, benzimidazole, and DMF are mixed to obtain a precursor solution, wherein the molar ratio of Zn element, imidazole, benzimidazole, and DMF in the precursor solution is 1: 12.5: 3: 200. The sheet-like alumina carrier is immersed in the precursor solution and crystallized and grown at room temperature for 12 hours to obtain a ZIF-62 crystal film, which is labeled as ZIF-62. The ZIF-62 crystal film is heated from 25°C to 750°C at a heating rate of 600°C / s in a Joule heating apparatus under an argon atmosphere, and then maintained at 750°C for 5 seconds. The ZIF-62 glass film is naturally cooled to room temperature to obtain a ZIF-62 glass film, which is labeled as a. g ZIF-62,a g The membrane area of ​​ZIF-62 is 0.88 cm 2 .

[0041] Characterization of ZIF-62 glass membrane: a g The XRD characterization results of ZIF-62 and ZIF-62 are shown in Figure 2. Figure 3 As shown by Figure 3 It can be seen that the a prepared by Joule heating g The structure of ZIF-62 is transformed from the crystalline structure of ZIF-62 to an amorphous structure.

[0042] a g The SEM characterization results of ZIF-62 cross section are as follows Figure 4 As shown by Figure 4 It can be seen that the a prepared in this embodiment g ZIF-62 is thin and has an amorphous structure inside.

[0043] a g Carbon dioxide separation performance test of ZIF-62: g The carbon dioxide separation performance of ZIF-62 was tested. A CO2 / N2 mixture with a molar ratio of CO2:N2 = 3:1 was introduced into the feed side. The pressure on the feed side was set to 4 bar. The permeation test was performed at normal pressure. The final test results were: a g The carbon dioxide permeability of TIF-4 is 57.0×10 -9 mol m -2 s -1 Pa -1 , CO2 / N2 selectivity is 45.9. The carbon dioxide content in the permeate side gas is 99.3 vol.%, and the carbon dioxide flow rate is 0.0278 mL / s. g ZIF-62 has excellent carbon dioxide enrichment capacity.

[0044] Example 3 a g TIF-4-biotransformation system coupling system performance test The CO2 / N2 mixed gas with a volume ratio of CO2:N2 = 15:85 is introduced into the membrane separation system (a gThe permeate pressure of the TIF-4 was set at 3.5 bar. CO2-enriched gas (93.6% vol.%, flow rate 0.0246 mL / min) obtained from the permeate side was fed into the bioconversion system for electrosynthesis. Specifically, the bioconversion system employed an H-type three-electrode electrolytic cell as the electrocatalytic platform. The CO2-enriched gas was passed into the cathode chamber, with a glassy carbon electrode as the working electrode, a graphite electrode as the auxiliary electrode, and a silver-silver chloride electrode as the reference electrode. Both the cathode and anode chambers were connected to a potentiostat, set at a potential of -0.7 V. The electrolyte matrix of the cathode chamber and the anode chamber is PBS buffer with a pH of 6.0. The electrolyte in the cathode chamber contains 30g / L biochar, 0.5g / L cysteine ​​hydrochloride, 1mg / L resazurin, and Clostridium ljungdahlii cell extract. The protein concentration in the cathode chamber electrolyte is 5mg / mL, 12.5mM methyl viologen solution, 0.03mM NADH and 0.03mM NADPH solution; the electrolyte in the anode chamber contains 0.5g / L cysteine ​​hydrochloride and 1mg / L resazurin. The outer circulating water temperature of the H-type three-electrode electrolytic cell is 37℃. The results show that the coupling system works well and can enrich carbon dioxide in the carbon dioxide mixture and efficiently convert it into ethanol and acetic acid, a g The operating time, produced acetic acid concentration, and ethanol concentration of the TIF-4-bioconversion system coupling system are recorded in Table 1 .

[0045] Table 1 As can be seen from Table 1, the coupled system provided in this embodiment can produce 8.455 mM acetic acid and 4.4 mM ethanol after running for 56 hours, which confirms the feasibility of the industrial gas carbon capture system provided by the present invention in carbon capture.

[0046] Example 4 Performance test of coupled system of tandem membrane separation-bioconversion system A prepared in series with Example 1 g TIF-4 and a prepared in Example 2 gZIF-62 was used to prepare a two-stage membrane separation system. A CO2 / N2 mixture with a CO2:N2 volume ratio of 15:85 was used as the feed gas to simulate industrial flue gas. The feed gas was passed through the two-stage membrane separation system at 3.5 bar. It was determined that the volume proportion of carbon dioxide in the carbon dioxide-enriched gas obtained on the permeate side was 99.8%, and the flow rate was 0.0312 ml / min. The carbon dioxide-enriched gas obtained on the permeate side was passed into the bioconversion system at a flow rate of 0.0312 ml / min for electrosynthesis. Specifically, the bioconversion system used an H-type three-electrode electrolytic cell as the electrocatalytic platform. The carbon dioxide-enriched gas was passed into the cathode chamber. The working electrode was a glassy carbon electrode, the auxiliary electrode was a graphite electrode, and the reference electrode was a silver-silver chloride electrode. The cathode chamber and the anode chamber were connected to a constant potential meter, and the potential was set to -0.7 V. The electrolyte matrix for both the cathode and anode compartments was PBS buffer (pH 6.0). The cathode electrolyte contained 30 g / L biochar, 0.5 g / L cysteine ​​hydrochloride, 1 mg / L resazurin, and a Clostridium ljungdahlii cell extract. The cathode electrolyte contained 5 mg / mL protein, 12.5 mM methyl viologen solution, 0.03 mM NADH, and 0.03 mM NADPH solutions. The anode electrolyte contained 0.5 g / L cysteine ​​hydrochloride and 1 mg / L resazurin. The outer circulating water temperature of the H-type three-electrode electrolytic cell was 37°C. Results demonstrated that the coupled system performed well, capable of enriching CO2 from a CO2 mixture and efficiently converting it into ethanol and acetic acid. Table 2 shows the operating time, acetic acid concentration, and ethanol concentration of the coupled tandem membrane separation-bioconversion system.

[0047] Table 2 As can be seen from Table 2, compared with Example 1, the carbon dioxide-enriched gas produced by the series membrane separation-bioconversion system coupling system has a higher carbon dioxide concentration and also higher concentrations of acetic acid and ethanol.

[0048] Example 5 Production of acetic acid and butanol by coupling a tandem membrane separation-bioconversion system The agTIF-4 prepared in Example 1 and the agZIF-62 prepared in Example 2 were connected in series to prepare a two-stage membrane separation system. A CO2 / N2 mixture with a volume ratio of CO2:N2 = 15:85 was used to simulate industrial flue gas and the mixture was used as the raw gas. The raw gas was passed through the two-stage membrane separation system at 3.5 bar. It was determined that the volume proportion of carbon dioxide in the carbon dioxide-enriched gas obtained on the permeate side was 99.8%, and the flow rate was 0.0312 ml / min. The carbon dioxide-enriched gas obtained on the permeate side was passed into the bioconversion system at a flow rate of 0.0312 ml / min for electrosynthesis. The electrolyte in the bioconversion system included Clostridium ljungdahlii lysate and Clostridium acetobutylicum lysate. Specifically, the bioconversion system used an H-type three-electrode system electrolytic cell as the electrocatalytic platform, with a glassy carbon electrode as the working electrode, a graphite electrode as the auxiliary electrode, and a silver-silver chloride electrode as the reference electrode. The cathode chamber and the anode chamber were connected to a constant potential meter, and the potential was set to 0.7 V. The electrolyte matrix in both the cathode and anode compartments was PBS buffer at pH 6.0. The cathode compartment electrolyte contained 30 g / L biochar, 0.5 g / L cysteine ​​hydrochloride, 1 mg / L resazurin, lysed cells of Clostridium ljungdahlii and Clostridium acetobutylicum, 12.5 mM methyl viologen solution, 0.03 mM NADH, and 0.03 mM NADPH solution. The anode compartment electrolyte contained 0.5 g / L cysteine ​​hydrochloride and 1 mg / L resazurin. The outer circulating water temperature of the H-type three-electrode electrolytic cell was 37°C. The final conversion products and product concentrations are shown in Table 3. The results demonstrate that the coupled system works well. The industrial gas carbon capture system provided in this example can convert CO2 into multi-carbon products such as acetic acid, ethanol, butanol, and isopropanol. The industrial gas carbon capture system provided by the present invention is multifunctional and can produce a variety of value-added chemicals through the synergistic use of multiple microorganisms.

[0049] Table 3 Comparative Example 1 Single bioconversion system performance test A CO2 / N2 mixture with a volume ratio of CO2:N2 = 15:85 was used as the raw gas to simulate industrial flue gas. The raw gas was introduced into the bioconversion system at a flow rate of 0.0312 ml / min for electrosynthesis. Specifically, the bioconversion system used an H-type three-electrode electrolytic cell as the electrocatalytic platform. The carbon dioxide-enriched gas was introduced into the cathode chamber. The working electrode was a glassy carbon electrode, the auxiliary electrode was a graphite electrode, and the reference electrode was a silver-silver chloride electrode. The cathode chamber and the anode chamber were connected to a constant potential meter, and the potential was set to -0.7 V. The electrolyte matrix for both the cathode and anode compartments was PBS buffer (pH 6.0). The cathode electrolyte contained 30 g / L biochar, 0.5 g / L cysteine ​​hydrochloride, 1 mg / L resazurin, and a Clostridium ljungdahlii cell extract. The cathode electrolyte contained a protein concentration of 5 mg / mL, 12.5 mM methyl viologen solution, 0.03 mM NADH, and 0.03 mM NADPH solution. The anode electrolyte contained 0.5 g / L cysteine ​​hydrochloride and 1 mg / L resazurin. The external circulating water temperature of the H-type three-electrode electrolytic cell was 37°C. The operating time of the bioconversion system and the produced acetic acid and ethanol concentrations are recorded in Table 4.

[0050] Table 4 Although the present disclosure is disclosed as above, the protection scope of the present disclosure is not limited thereto. Those skilled in the art can make various changes and modifications without departing from the spirit and scope of the present disclosure, and these changes and modifications will fall within the protection scope of the present invention.

Claims

1. An industrial gas carbon capture system, characterized in that: include: Membrane separation systems for enriching carbon dioxide; and A bioconversion system connected to a membrane separation system pipeline, the bioconversion system being used to reduce carbon dioxide gas to multi-carbon compounds, the bioconversion system comprising an H-type three-electrode electrolytic cell, the H-type three-electrode electrolytic cell comprising a cathode chamber and an anode chamber, the cathode chamber and the anode chamber being separated by a proton exchange membrane, the cathode chamber containing an electrolyte comprising Clostridium ljungdahlii lysis fluid.

2. The industrial gas carbon capture system according to claim 1, wherein: The membrane separation system comprises a metal organic framework glass membrane, and the metal organic framework glass membrane is selected from any one or more of a ZIF-4 glass membrane, a ZIF-62 glass membrane, a ZIF-76 glass membrane, and a TIF-4 glass membrane.

3. The industrial gas carbon capture system according to claim 1, wherein: The protein concentration in the electrolyte is 1-10 mg / mL.

4. The industrial gas carbon capture system according to claim 1, wherein: The electrolyte further includes 10-45 g / L of biochar, 0.2-1 g / L of cysteine ​​hydrochloride, 0.5-1.5 mg / L of resazurin, 10-15 mM of methyl viologen, 0.01-0.05 mM of NADH, and 0.01-0.05 mM of NADPH.

5. The industrial gas carbon capture system according to claim 1, wherein: The multi-carbon compound is selected from any one or more of acetic acid, ethanol, butanol, and isopropanol.

6. The industrial gas carbon capture system according to claim 1, wherein: The Clostridium ljungdahlii cell lysis solution is obtained by ultrasonic cell lysis or homogenization cell lysis.

7. The industrial gas carbon capture system according to claim 1, wherein: The working electrode of the H-type three-electrode electrolytic cell is a glassy carbon electrode, the auxiliary electrode is a graphite electrode, and the reference electrode is a silver-silver chloride electrode.

8. A method for capturing carbon from industrial gas, characterized in that: Carbon dioxide is captured using the industrial gas carbon capture system described in any one of claims 1 to 7.

9. The industrial gas carbon capture method according to claim 8, characterized in that: The following steps are involved: S1: passing industrial flue gas into a membrane separation system to obtain carbon dioxide enriched gas; S2: The carbon dioxide-enriched gas is directly introduced into the cathode chamber and a voltage of 0.5~1V is applied to react and generate multi-carbon compounds.

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