WO2020184824A1 - Procédé électrochimique pour la conversion du dioxyde de carbone en acide oxalique - Google Patents

Procédé électrochimique pour la conversion du dioxyde de carbone en acide oxalique Download PDF

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WO2020184824A1
WO2020184824A1 PCT/KR2019/018664 KR2019018664W WO2020184824A1 WO 2020184824 A1 WO2020184824 A1 WO 2020184824A1 KR 2019018664 W KR2019018664 W KR 2019018664W WO 2020184824 A1 WO2020184824 A1 WO 2020184824A1
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oxalate
electrode
electrode portion
electrolysis
carbon dioxide
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신운섭
박미정
서지혜
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Sogang University Research Foundation
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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
    • C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
    • C25C1/16—Electrolytic production, recovery or refining of metals by electrolysis of solutions of zinc, cadmium or mercury
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present application relates to an electrolysis system for converting carbon dioxide (CO 2 ) into oxalic acid (H 2 C 2 O 4 ) using an electrochemical method, and an electrolysis method using the same.
  • CCU technology Carbon Capture and Utilization
  • CCS Carbon Capture and Sequestration
  • the electrochemical method has the advantage of selectively converting carbon dioxide into various types of organic compounds according to the type of electrode material, and being able to operate under normal temperature and pressure conditions, and easy to increase capacity through stacking.
  • it is attracting attention as a method that can be applied in various industries in terms of cost or scale-up.
  • Active research is being conducted when formic acid, carbon monoxide, methanol, ethylene, oxalic acid, etc. are considered as target materials for electrochemically converting carbon dioxide.
  • Oxalic acid a substance intended to be produced electrochemically from carbon dioxide, is used in pharmaceutical production, agriculture, textile and leather manufacturing, and chemical products, and is produced around 700,000 tons per year worldwide.
  • the reaction of electrochemically converting carbon dioxide to oxalate ions is a two-electron reaction, which is the same as carbon monoxide and formic acid, compared to methanol (6 electrons) and methane (8 electrons) conversion reactions. , Has the advantage of consuming relatively little energy.
  • the advantages of the electrochemical method are that it is eco-friendly because the electrolyte can be reused and the reaction is possible even in a single cell form, and that it has a low cost of device construction, and that there is little cost of raw material consumption because carbon dioxide in the reaction is a raw material. Can be seen as. Due to these advantages, the process of converting carbon dioxide to oxalic acid through an electrochemical method is believed to be able to replace the existing process.
  • the reduction reaction of carbon dioxide goes through different routes depending on the conditions of the metal and the electrolyte.
  • TEAP Tetraethylammonium perchlorate
  • tin (Sn) and indium (In ) Has been reported to be reduced to carbon monoxide, lead (Pb) to oxalic acid, and zinc (Zn) to oxalic acid, carbon monoxide, and glyoxylic acid.
  • the electrochemical system that converts carbon dioxide to oxalate ions has a problem in that it is difficult to separate the generated oxalate ions from an organic solvent, so a sacrificial zinc anode is used as a counter electrode to generate zinc oxalate (ZnC 2 O 4 ).
  • Post-precipitation method has been developed, and since zinc oxalate is insoluble in a neutral organic solvent, oxalate can be efficiently separated (Weixin Lv, J. Solid State Electrochem. (2013) 17, 2789-2794) (Fig. 2) .
  • the present application sets the material consumed to convert carbon dioxide and oxalic acid, which has a low energy cost, as a conversion material, and effectively recovers and reuses metals such as zinc consumed as a sacrificial electrode for the production of oxalate, an intermediate product. It has improved efficiency and economy.
  • a first aspect of the present application is an electrolysis system for electrochemical conversion of carbon dioxide to oxalic acid, comprising: a first electrolysis tank for electrochemical conversion of carbon dioxide to oxalate; And a second electrolysis tank for separating and obtaining the oxalate obtained from the first electrolysis tank into oxalic acid and a metal.
  • a second aspect of the present application provides an electrolysis method for electrochemical conversion of carbon dioxide to oxalic acid using the electrolysis system according to the first aspect.
  • the second electrolysis tank is divided into a divided cell equipped with an anion exchange membrane, an anion. It is designed as a three compartment cell equipped with an exchange membrane and a cation exchange membrane and a single pot cell without a separation membrane, so that it is possible to scale up and has excellent oxalic acid generation and zinc recovery rate, so it can be used as an industrial scale. There is an advantage.
  • FIG. 1 is a schematic diagram showing a carbon dioxide reduction reaction in (A) a carbon dioxide reduction reaction in an aqueous solution, and (B) a carbon dioxide reduction reaction in a neutral organic solvent in an electrochemical reduction mechanism of carbon dioxide in an embodiment of the present application.
  • FIG. 2 is a schematic diagram showing a system for electrochemical reduction of oxalate oxalate of carbon dioxide using a lead electrode in an embodiment of the present application.
  • FIG. 3 shows an electrochemical process (A) for converting carbon dioxide into oxalic acid and a chemical reaction equation (B) of each process in an embodiment of the present application: 1 a first electrolysis tank, and 2 a second electrolysis tank.
  • FIG. 4 is a schematic diagram showing the configuration of an experimental apparatus for producing oxalate through electrochemical conversion of carbon dioxide of a single pot type, according to an embodiment of the present disclosure.
  • FIG. 5 is a graph showing a cyclic voltage-current plot (Cyclic Voltammogram, scanning speed: 50 mV/s) of argon (Ar) phase and carbon dioxide (CO 2 ) phase in a reaction solution in an embodiment of the present application .
  • FIG. 7 is a schematic diagram showing oxalate, which is a carbon dioxide electrolysis product, measured by XRD in an example of the present application.
  • FIG. 8 is a schematic diagram of a design of a first electrolysis tank of a stack type according to an embodiment of the present disclosure.
  • FIG. 9 is a graph showing a result of a scale-up test of conversion of carbon dioxide to oxalate in a first electrolysis tank according to an embodiment of the present application.
  • FIG. 10 is a graph showing a result of performing a scale-up test for conversion of carbon dioxide to oxalate in a first electrolysis tank according to an embodiment of the present application.
  • FIG. 11 is a schematic diagram showing the device configuration of a second electrolysis tank of a divided cell type provided with an anion exchange membrane according to an embodiment of the present application.
  • FIG. 12 is a schematic diagram showing an electrochemical oxidation and reduction system for converting oxalic acid from zinc oxalate and recovering zinc in an embodiment of the present application.
  • FIG. 13 is a schematic diagram showing the device configuration of a second electrolysis tank of a three compartment cell type provided with an anion exchange membrane and a cation exchange membrane according to an embodiment of the present disclosure.
  • FIG. 14 is a schematic diagram showing an electrochemical oxidation and reduction system for converting oxalic acid from zinc oxalate and recovering zinc in an embodiment of the present application.
  • FIG. 15 is a graph showing a circulating voltage-current plot of zinc oxalate in a 0.2 M NaC 2 O 4 solution (Cyclic Voltammogram, potential scan rate: 50 mV/s, Ar purging) in an example of the present disclosure.
  • 16 is a graph showing a circulating voltage-current plot of zinc oxalate in a 0.2 MK 2 C 2 O 4 solution (Cyclic Voltammogram, potential scan rate: 50 mV/s, Ar purging) in an example of the present application .
  • 17 is a graph showing a current of an electroplating experiment in which -1.5 V vs. Ag/AgCl was applied to a 0.2 M sodium oxalate solution of a zinc oxalate precipitate in an embodiment of the present application.
  • FIG. 18 is a graph showing a current of an electroplating experiment in which -1.5 V vs. Ag/AgCl was applied in a 0.2 M potassium oxalate solution of a zinc oxalate precipitate in an embodiment of the present application.
  • 19 is a photograph showing SEM data of zinc electroplating after (A) electroplating and (B) electroplating in an embodiment of the present application.
  • 20 is a graph showing XRD data of the recovered zinc electroplating in an embodiment of the present application.
  • 21 is a photograph showing the recovered zinc electroplating in an embodiment of the present application.
  • 22 is a graph showing XRD data of recovered oxalic acid in an example of the present application.
  • step (to) or “step of” does not mean “step for”.
  • the term “combination(s) thereof” included in the expression of the Makushi format refers to one or more mixtures or combinations selected from the group consisting of components described in the expression of the Makushi format, It means to include at least one selected from the group consisting of the above components.
  • a first aspect of the present application is an electrolysis system for electrochemical conversion of carbon dioxide to oxalic acid, comprising: a first electrolysis tank for electrochemical conversion of carbon dioxide to oxalate; And a second electrolysis tank for separating and obtaining the oxalate obtained from the first electrolysis tank into oxalic acid and a metal.
  • the present inventor has completed the effective precipitation of zinc oxalate of carbon dioxide through the prior registration patent (10-1750279), but the next process has not been suggested, so that zinc oxalate is actually carbon dioxide. Noting that it is not being used for conversion of, an electrochemical method of effectively converting zinc oxalate to oxalic acid was completed (FIG. 3).
  • the first electrolysis tank includes: a first reduction electrode portion including a first metal-containing electrode; A first oxide electrode portion including a sacrificial electrode; And an aprotic polar organic solvent and a first auxiliary electrolyte, and may include a first electrolyte portion in contact with the reduction electrode portion and the oxidizing electrode portion.
  • the second electrolysis tank is supplied with the oxalate obtained in the first electrolysis tank, a second reduction electrode portion including a second metal-containing electrode; A second oxide electrode portion; And a second electrolyte part positioned at each of the reduction electrode part and the oxidation electrode part and including a second auxiliary electrolyte, and metal ions contained in the oxalate supplied to the reduction electrode part are reduced to a metallic state. It may be recovered, and oxalic acid may be obtained from the oxidizing electrode part.
  • carbon dioxide in the first electrolysis tank, carbon dioxide can be converted to zinc oxalate precipitation in an organic solvent using a lead reduction electrode and a zinc oxide electrode in a single bath type.
  • the resulting zinc oxalate precipitate is separated and placed in the reduction part of the second electrolysis tank in the form of a separated cell with an anion exchange membrane, and then electrolysis proceeds.
  • zinc is plated in the reduction part and recovered by plating. Since the rate (oxalate, C 2 O 4 2- ) moves to the oxidation part through the separation membrane, and hydrogen ions (H + ) are generated in the oxidation part by the oxidation reaction of water, oxalic acid (H 2 ) is generated in the oxidation part.
  • a lead electrode as a working electrode
  • a sacrificial zinc electrode as a counter electrode
  • Ag/Ag + (1 mM AgClO 4 + 0.1 M tetrabutylammonium hexafluoroborate in DMSO) as a reference electrode
  • DMSO as a solvent
  • auxiliary electrolyte tetrabutylammonium hexafluoroborate (TBA ⁇ PF 6 ) can be used, and the conversion efficiency of carbon dioxide to zinc oxalate is 95% on average, and the average purity of zinc oxalate is about 90%. (zinc oxalate) form.
  • each of the first reduction electrode portion and the first oxidation electrode portion may be arranged as a plurality of alternately to form a stack, but is not limited thereto.
  • the reaction area of each of the first reduction electrode part and the first oxidation electrode part may be 5 cm 2 or more, but is not limited thereto.
  • the reaction area of each of the first reduction electrode part and the first oxidation electrode part is 5 cm 2 or more, 50 cm 2 or more, 100 cm 2 or more, 500 cm 2 or more, 1000 cm 2 or more, 5 cm 2 to It may be 500 cm 2 , 10 cm 2 to 500 cm 2 , 100 cm 2 to 500 cm 2 , 10 cm 2 to 450 cm 2 , 10 cm 2 to 400 cm 2, or 15 cm 2 to 350 cm 2 .
  • an exchange membrane separating the second reduction electrode part and the second oxidation electrode part may be further included.
  • the exchange membrane may include an anion exchange membrane, a cation exchange membrane, or both.
  • the recovered zinc oxalate precipitate is dried, and then an aqueous electrolyte containing sodium oxalate (Na 2 C 2 O 4 ) is added to the reduction unit as a precipitate to reduce zinc. It can be used as a secondary electrode.
  • an aqueous electrolyte containing sodium oxalate Na 2 C 2 O 4
  • the whole electrolysis system was formed using platinum as the oxidation part electrode. It can be recovered by making oxalic acid from the oxidized part through the transfer of the oxalate produced by electroplating to the oxidized part.
  • the reaction area of each of the second reduction electrode part and the second oxidation electrode part may be 5 cm 2 or more, but is not limited thereto.
  • the reaction area of each of the second reduction electrode unit and the second oxidation electrode unit is 5 cm 2 or more, 10 cm 2 or more, 50 cm 2 or more, 100 cm 2 or more, 500 cm 2 or more, 1000 cm 2 or more , 5 cm 2 to 100 cm 2 , 10 cm 2 to 100 cm 2 , 20 cm 2 to 100 cm 2 , 10 cm 2 to 90 cm 2 , 10 cm 2 to 80 cm 2 or 10 cm 2 to 70 cm 2 I can.
  • the oxalate may be represented by the following formula (1).
  • M is Zn, Mg, Li, Na, or Al, and x is 1 or 2.
  • the first metal-containing electrode Hg, Ag, Sn, Cu, Zn, Sb, Pb, Bi, alloys thereof, amalgam including those selected from the group consisting of combinations thereof It may be, but is not limited thereto.
  • the sacrificial electrode may include one selected from the group consisting of Zn, Mg, Li, Na, Al, Ca, and combinations thereof, but is not limited thereto.
  • the second metal-containing electrode may include a material selected from the group consisting of Zn, Mg, Li, Na, Al, Ca, and combinations thereof, but is not limited thereto. .
  • the second oxide electrode part may include a Pt electrode or a dimension stable anode (DSA), but is not limited thereto.
  • DSA dimension stable anode
  • the aprotic polar organic solvent may include one selected from the group consisting of dimethyl sulfoxide, dimethyl formamide, and combinations thereof, but is not limited thereto.
  • the first auxiliary electrolyte is tetrabutylammonium hexafluorophosphate (TBA ⁇ PF 6 ), tetrabutylammonium perchlorate (TBAP), tetrabutylammonium tetrafluoroborate (TBA ⁇ BF 4 ), And it may be to include those selected from the group consisting of combinations thereof, but is not limited thereto.
  • the second auxiliary electrolyte may include sodium oxalate (Na 2 C 2 O 4 ), potassium oxalate (K 2 C 2 O 4 ), or potassium sulfate (K 2 SO 4 ). , But is not limited thereto.
  • the electrolysis system obtains zinc oxalate in the first electrolysis tank, and obtains oxalic acid and zinc in the second electrolysis tank, so that carbon dioxide can be recycled as an effective material as well as the process. It relates to a whole system that can be cycled, including the process of regenerating zinc used in it. Therefore, it is possible to provide an effective conversion system for carbon dioxide to oxalic acid, and the system can simultaneously achieve carbon dioxide reduction and production of oxalic acid, a useful material, and thus, the basis of a carbon dioxide recycling process that can be used industrially due to high efficiency and economy is high. Can be.
  • the second electrolysis tank is a divided cell equipped with an anion exchange membrane, an anion exchange membrane. And it is designed as a three compartment cell with a cation exchange membrane and a single pot cell without a separation membrane, so that it is possible to scale up, so that the generation of oxalic acid and zinc recovery are excellent, so it can be used as an industrial scale. There is this.
  • a second aspect of the present application provides an electrolysis method for electrochemical conversion of carbon dioxide to oxalic acid using the electrolysis system according to the first aspect.
  • content that may be in common with each other may be applied to both the first aspect and the second aspect even if the description thereof is omitted.
  • Example 1 Preparation of zinc oxalate through carbon dioxide reduction reaction (first electrolysis tank)
  • a lead electrode as a working electrode, a sacrificial zinc electrode as a counter electrode, and Ag/Ag + (1 mM AgClO 4 + 0.1 M tetrabutylammonium hexafluoroborate in DMSO) were used as a reference electrode, and dimethyl sulfoxide (DMSO) as a solvent was used.
  • DMSO dimethyl sulfoxide
  • As an electrolyte a solution containing tetrabutylammonium hexafluorophosphate (TBA ⁇ PF 6 ) at a concentration of 0.1 M was used as a reaction solution, and a single pot type was used as the first electrolysis tank. Carbon dioxide electrochemical reduction reaction was performed.
  • the sacrificial electrode zinc was surrounded by lead, the reactive electrode, and the distance between the electrodes was minimized, and the solution was constantly circulated using a magnetic stirrer.
  • gas was injected into the reaction solution of the experimental apparatus (Fig. 4).
  • the voltage at which the difference between the reduction reaction of the electrolyte and the reduction reaction of carbon dioxide was the greatest was -3.0 V ⁇ -3.2 V vs Ag/Ag + when confirmed by the cyclic current method, so -2.8 V ⁇ -3.2 V vs.
  • the constant voltage method (Chronoamperometry) Ag/Ag + was applied and electrolyzed for 24 to 28 hours to conduct an experiment for conversion of zinc oxalate, an oxalate of carbon dioxide (FIG. 6). It was observed that the precipitate was continuously generated while the electrolysis proceeded, and it was confirmed that it can be easily separated through filtering and drying after the reaction.
  • the resulting oxalate was identified by two methods: titration and quantification using permanganic acid and analysis using High-Performance Liquid Chromatography (HPLC), and the purity and Faraday efficiency of the product were standardized potassium permanganate.
  • HPLC High-Performance Liquid Chromatography
  • the solution was calculated by the following equation 1, which is the reaction equation of the oxalate and permanganate ions in the product:
  • Amount of oxalate in the product (purity can be calculated):
  • n oxalate cx V x 5/2
  • Equation 2 n oxalate : number of moles of oxalate , c: concentration of KMnO 4 solution, V: volume of KMnO 4 solution added dropwise.
  • ⁇ oxalate n oxalate xnx F/Q
  • Equation 3 n: number of electrons required for reaction, F: Faraday constant, Q: total charge.
  • the conversion efficiency of carbon dioxide to zinc oxalate obtained using the above calculation formula was 95% on average, and the average purity of the produced zinc oxalate was about 90%.It was confirmed that carbon dioxide was effectively converted into zinc oxalate and precipitated. In addition, through XRD analysis, it was confirmed that the produced material was zinc oxalate (ZnC 2 O 4 ) (FIG. 7).
  • Example 2 Scale-up of production of zinc oxalate through carbon dioxide reduction reaction (first electrolysis tank)
  • a first electrolysis tank of a stack type was designed and manufactured to perform a scale-up test (FIG. 8).
  • Table 1 shows the degree of formation of oxalate according to the reaction area.
  • Example 3 Production of oxalic acid from zinc oxalate using an electroplating method (second electrolysis tank)
  • An electroplating method was applied to separate and recover the zinc oxalate produced in Examples 1 and 2 into zinc and oxalic acid.
  • the experiment was conducted for the purpose of recycling the zinc recovered through electroplating in the oxalate conversion reaction (the 1st electrolysis tank), and producing the remaining oxalic acid as a useful product.
  • the amount of zinc oxalate added to the solution was 0.11 per 11 mL. It proceeded by setting the ratio of 100:1 as g.
  • the reaction solution was prepared by adding an auxiliary electrolyte because electroplating was not performed when only zinc oxalate was added.
  • Sodium oxalate (Na 2 ) a material that does not affect the purity of the recovered material even when ionized while having a neutral pH.
  • C 2 O 4 was used as an auxiliary electrolyte, and potassium oxalate (K 2 C 2 O 4 ) or potassium sulfate (K 2 SO 4 ) may also be used.
  • the concentration of sodium oxalate was prepared to 0.2 M.
  • the second electrolysis tank for recovering zinc by electroplating unlike the first electrolysis tank for reducing carbon dioxide to oxalate, a divided cell equipped with an anion exchange membrane (FIGS. 11 and 12 ), an anion exchange membrane and a cation A three-compartment cell equipped with an exchange membrane (Figs. 13 and 14) and a single pot cell without a separation membrane were fabricated and studied.
  • a zinc plate was used as the reaction electrode and a platinum foil (Pt coil) was used as the counter electrode, but the present invention is not limited thereto, and a commercial DSA electrode (dimension stable anode, insoluble electrode) may be used.
  • Example 4 Scale-up of production of oxalic acid from zinc oxalate using an electroplating method (second electrolysis tank)
  • the oxalic acid recovery was performed from zinc oxalate using the electroplating method in the same manner as in Example 3, but the amount of oxalic acid generation and zinc recovery generated while increasing the scale of the second electrolysis tank was confirmed.
  • Table 2 shows the amount of oxalic acid generation and zinc recovery according to the reaction area.

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Abstract

La présente invention concerne un système d'électrolyse pour convertir le dioxyde de carbone (CO2) en acide oxalique (H2C2O4) à l'aide d'un procédé électrochimique, et un procédé d'électrolyse le mettant en œuvre.
PCT/KR2019/018664 2019-03-08 2019-12-27 Procédé électrochimique pour la conversion du dioxyde de carbone en acide oxalique Ceased WO2020184824A1 (fr)

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Cited By (1)

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CN119049574A (zh) * 2024-08-22 2024-11-29 浙江大学 基于技术经济性分析的二氧化碳电化学还原系统设计评估方法及系统

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