WO2025200094A1 - Dispositif de réaction d'électroréduction de dioxyde de carbone ayant une fonction de génération directe d'un écoulement polyphasique - Google Patents

Dispositif de réaction d'électroréduction de dioxyde de carbone ayant une fonction de génération directe d'un écoulement polyphasique

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Publication number
WO2025200094A1
WO2025200094A1 PCT/CN2024/093335 CN2024093335W WO2025200094A1 WO 2025200094 A1 WO2025200094 A1 WO 2025200094A1 CN 2024093335 W CN2024093335 W CN 2024093335W WO 2025200094 A1 WO2025200094 A1 WO 2025200094A1
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WIPO (PCT)
Prior art keywords
cathode
carbon dioxide
flow channel
plate
anode
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Application number
PCT/CN2024/093335
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English (en)
Chinese (zh)
Inventor
陆奇
李明翰
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Tsinghua University
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Tsinghua University
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Publication of WO2025200094A1 publication Critical patent/WO2025200094A1/fr
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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
    • 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
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/23—Carbon monoxide or syngas
    • 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
    • C25B3/01—Products
    • C25B3/07—Oxygen containing compounds
    • 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
    • C25B3/26—Reduction of carbon dioxide
    • 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
    • C25B9/60—Constructional parts of cells

Definitions

  • the present application relates to the field of electrochemical reduction of carbon dioxide, and in particular to a carbon dioxide electrochemical reduction reaction device with a multiphase flow direct generation function.
  • CO2 carbon dioxide
  • the most important greenhouse gas generated by fossil fuel consumption continues to accumulate in the atmosphere, leading to a series of serious environmental pollution and climate change issues.
  • CO2 electroreduction strategies have attracted widespread attention due to their mild reaction conditions and excellent sustainability.
  • the gas diffusion electrode catalyst layer needs to be hydrophilic in order to form a path in direct contact with the electrolyte.
  • solution infiltration and salt precipitation make the electrolyte penetrate and Blocking the gas diffusion channels ultimately reduces the chances of carbon dioxide gas entering the catalyst surface, leading to a significant decrease in reaction activity. Therefore, under actual working conditions, gas diffusion electrodes often require complex and costly structural regulation to enhance overall stability. Even so, the actual activity of the optimized electrode (1-2kA/ m2 ) is still far lower than the theoretical activity of 10kA/ m2 , which has significant limitations. Based on this, the field of carbon dioxide electroreduction urgently needs to open up a technical route other than gas diffusion electrodes to further improve operational stability while maintaining a high reaction rate within the system.
  • multiphase flow technology can enhance the mass transfer process between the gas and liquid phases, thereby increasing the rate of carbon dioxide electroreduction reaction.
  • electrolysis devices based on multiphase flow technology generally adopt a scheme of pre-mixing and then electrolysis outside the device, that is, a multiphase flow is first generated in an external pipeline, and then introduced into the electrolysis device for reaction.
  • a multiphase flow is first generated in an external pipeline, and then introduced into the electrolysis device for reaction.
  • its flow pattern often changes, which may cause the gas-liquid phase contact area to decrease, and ultimately lead to a decrease in mass transfer efficiency; at the same time, the multiphase flow generation module and supporting pipelines outside the electrolysis device occupy a large amount of space, making the reaction system complicated.
  • the carbon dioxide electrolysis device disclosed in the patent application with publication number CN116288441A uses the above-mentioned multiphase flow technology to provide reaction raw materials for the cathode of the electrolytic cell, and it also has the above-mentioned problems worthy of attention.
  • the present application provides a carbon dioxide electroreduction reaction device with a multiphase flow direct generation function.
  • the present application provides a carbon dioxide electroreduction reaction device with a multiphase flow direct generation function, comprising:
  • a cathode plate wherein a first cathode feed channel and a second cathode feed channel are provided on the cathode plate, wherein the first cathode feed channel is used to introduce a first cathode material, and the second cathode feed channel is used to introduce a second cathode material;
  • cathode electrode wherein the cathode electrode is provided with a first hole connected to the first cathode feed channel and a second hole connected to the second cathode feed channel;
  • a cathode flow channel plate the cathode flow channel plate includes a first area with non-hollowed grooves and a hollowed second area, the first area is arranged on the side of the cathode flow channel plate close to the cathode electrode in the thickness direction, the first hole and the second hole are both connected to the first area, and the first area is connected to the second area, so that the cathode first material and the cathode second material can enter the first area through the cathode first feed channel and the cathode second feed channel respectively, intersect and mix in the first area, and then enter the second area.
  • the flow channel where the first cathode material and the second cathode material meet is perpendicular to the flow channel where the second cathode material meets.
  • the first region includes a first flow channel
  • the first hole and the second hole are respectively connected to the upstream and downstream of the first flow channel
  • the axis direction of the second hole is perpendicular to the cathode flow channel plate.
  • the axial direction of the first hole and the axial direction of the second hole are both perpendicular to the cathode flow channel plate.
  • the first region includes a first flow channel and a second flow channel that are perpendicular to each other, the first hole is connected to the first flow channel, and the second hole is connected to the second flow channel.
  • the first zone includes a third flow channel, and the third flow channel is located downstream of the intersection of the cathode first material and the cathode second material.
  • the carbon dioxide electroreduction reaction device further includes an ion exchange membrane, an anode electrode, and an anode plate arranged in sequence, and the ion exchange membrane is attached to the cathode flow channel plate.
  • the carbon dioxide electric reduction reaction device further includes an anode membrane electrode, an anode current collector, and an anode plate arranged in sequence, and the anode membrane electrode is attached to the cathode flow channel plate.
  • the cathode plate further has a cathode discharge channel.
  • the anode plate has an anode feed channel and an anode discharge channel.
  • FIG1 shows a dioxygen system with a multiphase flow direct generation function according to one embodiment of the present application. Schematic diagram of the disassembled carbon electroreduction reaction device.
  • FIG4 shows a schematic structural diagram of a cathode plate and a cathode flow channel plate of a carbon dioxide electroreduction reaction device with a multiphase flow direct generation function according to another embodiment of the present application.
  • FIG5 shows a relationship diagram between the total current density and product selectivity of the carbon dioxide electroreduction reaction device with a multiphase flow direct generation function according to Example 1 of the present application.
  • FIG6 shows a relationship diagram among the device operation time, voltage and product selectivity of the carbon dioxide electroreduction reaction device with multiphase flow direct generation function according to Example 2 of the present application.
  • the carbon dioxide electroreduction reaction device with a multiphase flow direct generation function provided herein may include a cathode plate 100, a cathode electrode 200, a cathode flow channel plate 300, an ion exchange membrane 410, an anode electrode 510, and an anode plate 600, which are sequentially arranged. Furthermore, the above components may be tightly fitted together.
  • the cathode plate 100 may be provided with a first cathode feed channel 110 and a second cathode feed channel 120.
  • the first cathode feed channel 110 is used to introduce a first cathode material, such as a cathode electrolyte
  • the second cathode feed channel 120 is used to introduce a second cathode material, such as carbon dioxide gas.
  • the cathode electrode 200 may be provided with a first hole 210 connected to the first cathode feed channel 110 and a second hole 220 connected to the second cathode feed channel 120 .
  • the cathode channel plate 300 may include a first region 310 provided with a non-hollowed groove and a hollowed second region 320.
  • the first region 310 is provided on the cathode channel plate 300 in the thickness direction.
  • the first hole 210 and the second hole 220 are both connected to the first zone 310, and the first zone 310 is connected to the second zone 320, so that the cathode first material and the cathode second material can enter the first zone 310 through the cathode first feed channel 110 and the cathode second feed channel 120 respectively, and intersect and mix in the first zone 310 to form a multiphase flow, and then enter the second zone 320.
  • the multiphase flow provided in the present application is a two-phase mixed flow consisting of carbon dioxide gas and electrolyte.
  • the carbon dioxide gas path and the electrolyte liquid path are separated from each other, and after passing through the first cathode feed channel 110 and the second cathode feed channel 120, they intersect in the first zone 310, and are in situ mixed on the surface of the cathode electrode 200 to form an electrolyte containing a large number of carbon dioxide microbubbles (the overall flow of the multiphase flow presents a bubble flow).
  • the multiphase flow flows to the second zone 320, it contacts the ion exchange membrane 410, and the multiphase flow undergoes a carbon dioxide electro-reduction reaction in the second zone 320.
  • the present application directly embeds the multiphase flow generation site between the cathode electrode 200 and the cathode flow channel plate 300, and directly generates a continuous multiphase flow in situ on the surface of the cathode electrode 200, so that the gas-liquid two-phase contact area is always maintained at a large level in the electro-reduction device.
  • the carbon dioxide gas in the bubbles will be continuously added to the electrolyte, so that the electrolyte maintains a high carbon dioxide concentration during the reaction process, further strengthening the interphase mass transfer while accelerating the dissolution of carbon dioxide gas, improving the carbon dioxide electro-reduction activity, overcoming the mass transfer limitation, and solving the problem mentioned in the background technology that the multiphase flow is generated in the external pipeline and then introduced into the electrolysis device for reaction, which will result in a reduction in the gas-liquid contact area and ultimately a decrease in mass transfer efficiency.
  • the present application does not require the installation of an additional multiphase flow generation module and supporting pipelines outside the electro-reduction reaction device, thereby simplifying the system flow path, making operation more convenient, and further reducing operation and maintenance costs.
  • the carbon dioxide electric reduction reaction device provided in the present application is superior to the carbon dioxide electric reduction reaction device based on gas diffusion type electrodes and the carbon dioxide electric reduction reaction device with external multiphase flow.
  • the first zone 310 includes a first flow channel 311.
  • the first hole 210 and the second hole 220 are respectively connected to the upstream and downstream of the first flow channel 311.
  • the second hole 220 connected to the downstream of the first flow channel 311 is perpendicular to the cathode flow channel plate 300, so that the first flow channel 311 is perpendicular to the axial direction of the second hole 220, thereby realizing the vertical intersection of the two fluids.
  • the cathode second feed channel 120 can also be perpendicular to the cathode flow channel plate 300, and the axial direction of the first hole 210 and the cathode first feed channel 110 can also be perpendicular to the cathode flow channel plate 300.
  • This application refers to the T-shaped structure of the flow channel at the intersection in this embodiment as a vertical T-shape.
  • the first zone 310 may include a first flow channel 311 and a second flow channel 312 that are perpendicular to each other, the first hole 210 is connected to the first flow channel 311, and the second hole 220 is connected to the second flow channel 312. That is, by making the first flow channel 311 and the second flow channel 312 where the two materials are located before they intersect perpendicular, the two fluids intersect vertically.
  • the axial direction of the first hole 210, the axial direction of the cathode first feed channel 110, the axial direction of the second hole 220 and the cathode second feed channel 120 can also be perpendicular to the cathode flow channel plate 300.
  • This application refers to the T-shaped structure of the flow channel at the intersection in this embodiment as a horizontal T-shape.
  • the cathode plate 100 can act as a current collector, and a cathode current collecting joint 140 can be provided on the cathode plate 100 for connecting to an external circuit.
  • the cathode current collecting joint 140 can be a threaded joint.
  • the cathode plate 100 can also act as a fixed plate, and the carbon dioxide electric reduction reaction device can include a sealing ring 700, and a sealing groove 150 for accommodating the sealing ring 700 can be provided on the cathode plate 100.
  • the first area 310 and the second area 320 can be arranged on the inner side of the sealing groove 150.
  • the sealing ring 700 can enhance the sealing performance and prevent the multiphase flow from flowing out from the side of the carbon dioxide electric reduction reaction device.
  • the material of the cathode plate 100 can be a metal or alloy material serving as a current collector, such as copper, titanium, silver, iron, nickel, aluminum and their alloys.
  • cathode electrode 200 may be a metal foil electrode or a supported conductive foil electrode.
  • the metal foil electrode may be made of metals and alloys including, but not limited to, tin, silver, copper, gold, bismuth, zinc, lead, and others, which exhibit carbon dioxide electroreduction activity.
  • the supported conductive foil electrode may be made by loading a catalyst onto a conductive substrate, which may be a metal-based or carbon-based material.
  • the material of the cathode flow channel plate 300 can be an insulating inert polymer material, such as polytetrafluoroethylene (PTFE), polyvinyl chloride (PVC), chlorinated polyvinyl chloride (CPVC), polyetheretherketone (PEEK), and polymethyl methacrylate (PMMA).
  • the flow channel in the cathode flow channel plate 300 can be a serpentine flow channel to maximize the time the multiphase flow flows in the second zone 320.
  • the thickness of the cathode flow channel plate 300 (the thickness of the area not hollowed out and not provided with grooves) can be set to less than 3 mm.
  • the ion exchange membrane 410 can be an anion exchange membrane or a cation exchange membrane.
  • the cation exchange membrane 410 can use Nafion 115 membrane, Nafion 117 membrane, Nafion XL membrane and Nafion N324 membrane produced by DuPont.
  • an anode feed channel 610 and an anode discharge channel 620 may be provided on the anode plate 600.
  • An anode plate groove 630 may be provided in the anode plate 600, and an anode plate flow channel 640 may be provided in the anode plate groove 630.
  • the anode electrode 510 may be embedded in the anode plate groove 630 and cover the anode plate groove 630.
  • the anode plate flow channel 640 may be formed as a serpentine flow channel.
  • the anode material (for example, the anode electrolyte) can enter the anode plate 600 from the anode feed channel 610 and flow along the anode plate flow channel 640. When energized, the anode electrolyte undergoes an oxidation reaction and is then discharged from the anode discharge channel 620.
  • the anode plate 600 can serve as a current collector, and a current collecting joint is provided thereon to connect to an external circuit, and the joint can be a threaded joint. Referring to Figure 1, the anode plate 600 can serve as a fixed plate, and a sealing groove 650 for accommodating a sealing ring 700 can also be provided thereon.
  • the material of the anode plate 600 can be a metal or alloy material that can serve as a current collector, such as copper, titanium, silver, iron, nickel, aluminum and alloys thereof.
  • Anode electrode 510 can be a fiber felt or porous metal foam loaded with a catalyst. Its base material can be a metal or metal oxide, such as titanium, nickel, copper, silver, aluminum, and their oxides. Anode electrode 510 catalyzes the oxidation reaction at the anode side while also providing support for ion exchange membrane 410. The anode catalyst loaded on anode electrode 510 must be active in the water oxidation reaction.
  • the anode catalyst can be a metal or metal oxide, such as iridium, platinum, palladium, ruthenium, rhodium, iron, cobalt, nickel, titanium, and their oxides. The loading amount can be 0.5 to 2 mg/ cm2 .
  • the ion exchange membrane 410 and the anode electrode 510 can be replaced with an anode membrane electrode and an anode current collector.
  • the anode membrane electrode can be an ion exchange membrane loaded with an anode catalyst.
  • the anode catalyst can be evenly loaded on one side of the ion exchange membrane using an ultrasonic spraying process, with the side with the anode catalyst in close contact with the anode current collector and the other side in close contact with the cathode flow channel plate 300.
  • the ion exchange membrane 410 in the anode membrane electrode can be an anion exchange membrane or a cation exchange membrane.
  • the cation exchange membrane can use Nafion 115 membrane, Nafion 117 membrane, Nafion XL membrane, and Nafion N324 membrane produced by DuPont.
  • the loaded anode catalyst needs to be active in the water oxidation reaction.
  • the anode catalyst can be a metal or metal oxide, such as iridium, platinum, palladium, ruthenium, rhodium, iron, cobalt, nickel, titanium, and their oxides, and the loading amount can be 0.5 to 2 mg/ cm2 .
  • the anode current collector can be an unloaded fiber felt or porous metal foam. It can be made of metals or metal oxides, such as titanium, nickel, copper, silver, aluminum, and their oxides.
  • the anode current collector can be embedded in the anode plate groove 630, with one side covering the anode plate flow channel 640 and the other side in close contact with the catalyst side of the anode membrane electrode.
  • the cathode electrolyte may be pressurized to further increase the carbon dioxide concentration in the electrolyte, thereby enabling the device to support a higher reaction current density.
  • the sealing ring 700 may be made of fluororubber, which can achieve effective sealing of the device under normal pressure and pressurized conditions.
  • the carbon dioxide electroreduction reaction device may further include a gas flow control device and a pump assembly to enable the addition of carbon dioxide and electrolyte to the cathode side.
  • the carbon dioxide electroreduction reaction device may further include a pressure control device such as a back pressure valve, and the cathode discharge channel 130 and the anode discharge channel 620 may be connected to the back pressure valve to control the pressure of the fluid within the device.
  • the flow rates of the cathode electrolyte and the anolyte can be controlled to 20 to 200 mL/min (milliliters per minute) by a pump assembly.
  • the flow rate of the carbon dioxide gas is controlled to 20 to 1000 sccm (standard milliliters per minute) by a gas flow control device. If the device is operated under pressurized conditions, the pressure of the multiphase flow can be controlled by a back pressure valve, and the adjustable pressure range is 1 to 40 bar (bar).
  • the pressure in the anode chamber and the cathode chamber can be kept consistent to balance the pressure difference on both sides of the ion exchange membrane 410 or the anode membrane electrode.
  • the reaction occurring on the cathode side of the carbon dioxide electroreduction device is carbon dioxide electroreduction, and the products may be formic acid, formate, carbon monoxide, etc.; the reaction occurring on the anode side is water oxidation to release oxygen.
  • the anolyte and catholyte may be the same or different.
  • the catholyte may be an aqueous solution of a first electrolyte, and the anolyte may be an aqueous solution of water, an acid, or a second electrolyte.
  • the first and second electrolytes may be the same or different and each independently be a soluble salt or a base.
  • the soluble salt may be selected from at least one of bicarbonate, carbonate, format, phosphate, hydrogenphosphate, hydrochloride, acetate, perchlorate, and sulfate.
  • the cation in the soluble salt may be a metal ion, such as potassium, sodium, lithium, or cesium.
  • the base may be selected from alkali metal hydroxides and/or ammonia water, such as sodium hydroxide, potassium hydroxide, or lithium hydroxide.
  • the acid may be at least one of aqueous sulfuric acid, aqueous perchloric acid, and hydrochloric acid. In the catholyte and the anolyte, the concentration of the solute may be 0.1 to 10 mol/L (mole/liter).
  • the cathode plate 100 is made of copper and measures 90 mm x 90 mm x 20 mm.
  • the cathode electrode 200 is a thin tin sheet measuring 60 mm x 60 mm x 0.1 mm.
  • the anode membrane electrode uses a Nafion 115 cation exchange membrane, loaded on one side with iridium oxide (2 mg/ cm2 ), with an overall area equal to that of the cathode electrode 200.
  • the anode current collector is a titanium fiber felt measuring 50 mm x 50 mm x 0.4 mm.
  • the anode plate 600 is made of titanium and measures 90 mm x 90 mm x 20 mm.
  • the anode plate flow channel 640 on the anode plate 600 is a single serpentine flow channel with a width of 2 mm, a depth of 1.5 mm, and a length of 0.85 m.
  • the structure of the cathode flow channel plate 300 is shown in Figure 3.
  • the cathode flow channel plate 300 is made of CPVC with a thickness (flow channel depth) of 1 mm.
  • the cathode electrolyte is a KHCO3 aqueous solution with a concentration of 0.5 mol/L, and the anolyte is deionized water.
  • the cathode electrolyte flow rate is 20 mL/min, the carbon dioxide gas flow rate is 200 sccm, and the anolyte flow rate is 40 mL/min.
  • the pressure within the device was controlled at 9 bar, and a constant current reaction was used.
  • the total current density was set to 1 kA/ m2 (total current 1.6 A), 2 kA/ m2 (total current 3.2 A), 3 kA/ m2 (total current 4.8 A), 4 kA/ m2 (total current 6.4 A), and 5 kA/ m2 (total current 8 A).
  • the changes in formate, carbon monoxide, and hydrogen selectivity (Faraday efficiency) as a function of current density during the reaction are shown in Figure 5.
  • the carbon dioxide electroreduction reaction was carried out according to the method of Example 1, except that the constant current method was used to set the current density at 3 kA/m 2 (total current 4.8 A).
  • the changes in voltage and formate, carbon monoxide, and hydrogen selectivity (Faraday efficiency) with device operation time are shown in FIG6 .
  • the device maintains a formic acid selectivity exceeding 85% during the 120 h (hour) electroreduction reaction time, and the device voltage is stabilized at approximately 4 V, indicating that the electroreduction device can operate stably for a long time at a high current density.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

L'invention concerne un dispositif de réaction d'électroréduction de dioxyde de carbone ayant la fonction de génération directe d'un écoulement polyphasique. Le dispositif de réaction d'électroréduction de dioxyde de carbone comprend une plaque de cathode, une électrode de cathode et une plaque de canal d'écoulement de cathode, qui sont agencées en séquence. La plaque de cathode est pourvue d'un premier canal d'alimentation de cathode et d'un second canal d'alimentation de cathode. L'électrode de cathode est pourvue d'un premier trou relié au premier canal d'alimentation de cathode et d'un second trou relié au second canal d'alimentation de cathode. La plaque de canal d'écoulement de cathode comprend une première zone pourvue de rainures non évidées et une seconde zone évidée, la première zone étant disposée sur le côté de la plaque de canal d'écoulement de cathode à proximité de l'électrode de cathode dans le sens de l'épaisseur ; et le premier trou et le second trou sont tous deux reliés à la première zone, et la première zone est reliée à la seconde zone, de telle sorte qu'un premier matériau de cathode et un second matériau de cathode peuvent entrer dans la première zone respectivement à travers le premier canal d'alimentation de cathode et le second canal d'alimentation de cathode, converger et se mélanger dans la première zone, puis entrer dans la seconde zone.
PCT/CN2024/093335 2024-03-27 2024-05-15 Dispositif de réaction d'électroréduction de dioxyde de carbone ayant une fonction de génération directe d'un écoulement polyphasique Pending WO2025200094A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202410359372.7 2024-03-27
CN202410359372.7A CN118223052B (zh) 2024-03-27 2024-03-27 具有多相流直接生成功能的二氧化碳电还原反应装置

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CN113089009A (zh) * 2021-03-29 2021-07-09 重庆大学 一种无膜流动式电化学还原二氧化碳反应器
CN116288441A (zh) * 2022-12-01 2023-06-23 清华大学 二氧化碳电解装置和二氧化碳的电解方法

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