WO2025200094A1 - 具有多相流直接生成功能的二氧化碳电还原反应装置 - Google Patents

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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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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cathode
carbon dioxide
flow channel
plate
anode
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English (en)
French (fr)
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陆奇
李明翰
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Tsinghua University
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Tsinghua University
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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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  • Organic Chemistry (AREA)
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Abstract

具有多相流直接生成功能的二氧化碳电还原反应装置。该二氧化碳电还原反应装置包括顺序设置的阴极板、阴极电极和阴极流道板。阴极板上设置有阴极第一进料通道和阴极第二进料通道。阴极电极上设置有连接于阴极第一进料通道的第一孔和连接于阴极第二进料通道的第二孔。阴极流道板包括设置有未镂空的沟槽的第一区和镂空的第二区，第一区设置于阴极流道板的在厚度方向上靠近阴极电极的一侧，第一孔和第二孔都连接于第一区，第一区连接于第二区，使得阴极第一物料和阴极第二物料能够分别通过阴极第一进料通道和阴极第二进料通道进入第一区，在第一区交汇混合，而后进入第二区。

Description

具有多相流直接生成功能的二氧化碳电还原反应装置
相关申请的引用
本申请要求申请日为2024年3月27日、申请号为202410359372.7，发明名称为“具有多相流直接生成功能的二氧化碳电还原反应装置”的在中国递交的在先发明专利申请的优先权，该在先申请的全部内容通过引用合并于此。
技术领域
本申请涉及二氧化碳电化学还原领域，尤其涉及具有多相流直接生成功能的二氧化碳电还原反应装置。
背景技术
随着全球工业化发展的持续推进，化石燃料消耗产生的二氧化碳作为现存最主要的温室气体在大气中不断积累，这将导致一系列严重的环境污染和气候变化问题。在诸多二氧化碳转化与利用技术中，二氧化碳电还原策略因其具有反应条件温和、可持续性好等优势而受到广泛关注。
在对于二氧化碳电还原的早期研究中，间歇式电解槽较为常用，二氧化碳气体分子作为多相催化反应的原料需要首先溶解于电解液中，进而通过迁移扩散至电极表面参与反应。由于二氧化碳在水溶液中的溶解度低，这极大地减缓了电极表面气体反应物的供应，导致反应速率较慢。相较而言，具有多孔结构的气体扩散型电极能够直接将二氧化碳从气相输送至催化剂表面，有效削弱了的传质限制。因此，与间歇式电解槽相比，对于装配有气体扩散型电极的流动电解池，其二氧化碳电还原的理论反应活性可提高了几个数量级(例如达到10kA/m2)。
然而，气体扩散型电极催化剂层需要具备亲水性以便与电解液直接接触形成通路，在长时间的电解过程中，溶液浸润和盐类析出使得电解液渗透并 堵塞气体扩散孔道，最终减少了二氧化碳气体进入催化剂表面的机会，导致反应活性的大幅降低。因而在实际工况下，气体扩散型电极往往需要通过工艺复杂、高成本的结构调控来增强整体的稳定性，即便如此，优化后电极的实际活性(1～2kA/m2)依然远低于10kA/m2的理论活性，具有较大的局限性。基于此，二氧化碳电还原领域亟待开辟出一条气体扩散型电极之外的技术路线，在维持体系内高反应速率的同时进一步提升运行稳定性。
多相流技术作为一项应用广泛的微化工技术，可实现气液两相间的传质过程强化，进而提升二氧化碳电还原反应速率。目前，基于多相流技术的电解装置一般采用装置外预混合再电解的方案，即先于外部管路中生成多相流，而后通入电解装置中进行反应。然而，多相流在外部管路内输送的过程中，其流型往往会发生变化，进而可能造成气液相接触面积缩小，最终导致传质效率下降；同时，电解装置外部的多相流生成模块及配套管路占据大量空间，使得反应体系复杂化。公布号为CN116288441A的专利申请公开的二氧化碳电解装置即使用上述多相流技术为电解池的阴极提供反应原料，其也具有上述值得在意的问题。
因此，二氧化碳电还原反应装置还有改进空间。
发明内容
为了解决或缓解背景技术提到的至少一个问题，本申请提供了具有多相流直接生成功能的二氧化碳电还原反应装置。
本申请提供给的具有多相流直接生成功能的二氧化碳电还原反应装置包括顺序设置的：
阴极板，所述阴极板上设置有阴极第一进料通道和阴极第二进料通道，所述阴极第一进料通道用于通入阴极第一物料，所述阴极第二进料通道用于通入阴极第二物料；
阴极电极，所述阴极电极上设置有连接于所述阴极第一进料通道的第一孔和连接于所述阴极第二进料通道的第二孔；
阴极流道板，所述阴极流道板包括设置有未镂空的沟槽的第一区和镂空的第二区，所述第一区设置于所述阴极流道板的在厚度方向上靠近所述阴极电极的一侧，所述第一孔和所述第二孔都连接于所述第一区，所述第一区连接于所述第二区，使得所述阴极第一物料和所述阴极第二物料能够分别通过所述阴极第一进料通道和所述阴极第二进料通道进入所述第一区，在所述第一区交汇混合，而后进入所述第二区。
在至少一个实施方式中，所述阴极第一物料和所述阴极第二物料交汇处的所述阴极第一物料所在的流道垂直于所述阴极第二物料所在的流道。
在至少一个实施方式中，所述第一区包括第一流道，所述第一孔和所述第二孔分别连接于所述第一流道的上下游，所述第二孔的轴线方向垂直于所述阴极流道板。
在至少一个实施方式中，所述第一孔的轴线方向和所述第二孔的轴线方向都垂直于所述阴极流道板。
在至少一个实施方式中，所述第一区包括相互垂直的第一流道和第二流道，所述第一孔连接于所述第一流道，所述第二孔连接于所述第二流道。
在至少一个实施方式中，所述第一区包括第三流道，所述第三流道位于所述阴极第一物料和所述阴极第二物料交汇处的下游。
在至少一个实施方式中，所述二氧化碳电还原反应装置还包括顺序设置的离子交换膜、阳极电极和阳极板，所述离子交换膜贴合于所述阴极流道板。
在至少一个实施方式中，所述二氧化碳电还原反应装置还包括顺序设置的阳极膜电极、阳极集流体和阳极板，所述阳极膜电极贴合于所述阴极流道板。
在至少一个实施方式中，所述阴极板还具有阴极出料通道。
在至少一个实施方式中，所述阳极板具有阳极进料通道和阳极出料通道。
附图说明
图1示出了根据本申请一个实施方式的具有多相流直接生成功能的二氧 化碳电还原反应装置的拆解示意图。
图2示出了根据本申请一个实施方式的具有多相流直接生成功能的二氧化碳电还原反应装置的多相流生成位点的结构示意图。
图3示出了根据本申请一个实施方式的具有多相流直接生成功能的二氧化碳电还原反应装置的阴极板和阴极流道板的结构示意图。
图4示出了根据本申请另一个实施方式的具有多相流直接生成功能的二氧化碳电还原反应装置的阴极板和阴极流道板的结构示意图。
图5示出了根据本申请实施例1的具有多相流直接生成功能的二氧化碳电还原反应装置的装置运行总电流密度与产物选择性的关系图。
图6示出了根据本申请实施例2的具有多相流直接生成功能的二氧化碳电还原反应装置的装置运行时间与电压、产物选择性的关系图。
具体实施方式
下面参照附图描述本申请的示例性实施方式。应当理解，这些具体的说明仅用于示教本领域技术人员如何实施本申请，而不用于穷举本申请的所有可行的方式，也不用于限制本申请的范围。
参见图1，本申请提供的具有多相流直接生成功能的二氧化碳电还原反应装置(后面，有时简称“二氧化碳电还原反应装置”)可以包括顺序设置的阴极板100、阴极电极200、阴极流道板300、离子交换膜410、阳极电极510和阳极板600。并且，上述部件可以紧密贴合在一起。
其中，阴极板100上可以设置阴极第一进料通道110和阴极第二进料通道120。阴极第一进料通道110用于通入阴极第一物料，例如通入阴极电解液。阴极第二进料通道120用于通入阴极第二物料，例如通入二氧化碳气体。
阴极电极200上可以设置连接于阴极第一进料通道110的第一孔210和连接于阴极第二进料通道120的第二孔220。
参见图2至图4，阴极流道板300可以包括设置有未镂空的沟槽的第一区310和镂空的第二区320，第一区310设置于阴极流道板300的在厚度方向上靠 近阴极电极200的一侧(即第一区310的沟槽开口朝向阴极电极200)。第一孔210和第二孔220都连接于第一区310，第一区310连接于第二区320，使得阴极第一物料和阴极第二物料能够分别通过阴极第一进料通道110、阴极第二进料通道120进入第一区310，并在第一区310交汇混合成多相流，然后再进入第二区320。
示例性地，参见图2，第一区310和第二区320处都形成有流道，阴极电极200和阴极流道板300形成为第一区310处流道的两侧壁，阴极电极200和离子交换膜410形成为第二区320处流道的两侧壁。两阴极物料可以在第一区310处(例如图2所示的第二孔220所对应的第一区310位点)交汇形成多相流，并流入第二区320处的流道。在通电情况下，多相流将在阴极电极200表面发生还原反应。
可以理解，本申请提供的多相流为二氧化碳气体和电解液组成的两相混合流。在二氧化碳电还原反应装置外，二氧化碳气路和电解液液路彼此分离，分别通过阴极第一进料通道110和阴极第二进料通道120后于第一区310交汇，在阴极电极200表面原位混合形成含有大量二氧化碳微气泡的电解液(多相流整体流动呈现气泡流)。多相流流动至第二区320后与离子交换膜410接触，多相流在第二区320进行二氧化碳电还原反应。
可以理解，本申请基于气液多相流技术，没有采用气体扩散型电极，避免了背景技术所述的气体扩散型电极的相应缺点。
并且，本申请将多相流生成位点直接内置于阴极电极200和阴极流道板300之间，在阴极电极200表面直接原位生成连续多相流，使得气液两相接触面积在电还原装置内始终保持在较大的水平。在多相流的流动过程中，气泡中的二氧化碳气体会不断补充入电解液中，使得电解液在反应过程中保持较高的二氧化碳浓度，进一步强化相间传质的同时加快二氧化碳气体的溶解，提升二氧化碳电还原活性，克服传质限制，解决了背景技术所提到的外部管路中生成多相流，而后通入电解装置中进行反应时会产生的气液相接触面积缩小，最终导致传质效率下降的问题。
进一步地，本申请不必在电还原反应装置外额外设置多相流生成模块及配套管路，简化了体系流路，使得操作更加便捷，运行和维护成本进一步降低。
因此，本申请提供的二氧化碳电还原反应装置能够优于基于气体扩散型电极的二氧化碳电还原反应装置和外置多相流的二氧化碳电还原反应装置。
在本申请的一个实施方式中，参见图2，阴极第一物料和阴极第二物料通过各自的流道在第一区310交汇，且在交汇处阴极第一物料所在的流道垂直于阴极第二物料所在的流道。可以理解，两物料交汇处的流道相互垂直的形式利于两物料相互切割形成多相流。两物料交汇处的流道可以形成为T形。
例如，参见图3，第一区310包括第一流道311。第一孔210和第二孔220分别连接于第一流道311的上游和下游。并且，参见图2，连接于第一流道311的下游的第二孔220垂直于阴极流道板300，使得第一流道311垂直于第二孔220的轴线方向，实现两流体垂直交汇。当然，阴极第二进料通道120也可以垂直于阴极流道板300，第一孔210的轴线方向和阴极第一进料通道110也都可以垂直于阴极流道板300。本申请将该实施方式中的交汇处的流道的T形结构称为垂直T形。
或者，参见图4，第一区310可以包括相互垂直的第一流道311和第二流道312，第一孔210连接于第一流道311，第二孔220连接于第二流道312。即通过使两物料交汇前分别所在的第一流道311和第二流道312垂直，进而使得两流体垂直交汇。当然，该实施方式中，第一孔210的轴线方向、阴极第一进料通道110、第二孔220的轴线方向和阴极第二进料通道120也都可以垂直于阴极流道板300。本申请将该实施方式中的交汇处的流道的T形结构称为水平T形。
进一步地，第一区310还可以包括第三流道313，第三流道313位于阴极第一物料和阴极第二物料交汇处的下游。即在图3中位于第一流道311的下游。在图4中位于第一流道311和第二流道312的交汇处的下游。可以理解，多相流在交汇处(交汇点)生成后，将沿未镂空的第三流道313继续流动一段距 离，以保证多相流流型的稳定。
在本申请的一个实施方式中，参见图1，阴极板100还可以包括阴极出料通道130，阴极出料通道130用于供产物及相关物料排出。例如，液相产物溶于电解液中，气相产物形成为气泡的形式，最后从阴极出料通道130排出。
参见图3和图4，阴极板100可以充当集流体，阴极板100上可以设置阴极集流接头140，以用于连接外部电路。该阴极集流接头140可以为螺纹接头。阴极板100还可以充当固定板，二氧化碳电还原反应装置可以包括密封圈700，阴极板100上可以设置容纳密封圈700的密封沟槽150。第一区310、第二区320可以设置在密封沟槽150的内侧。密封圈700可以增强密封性能，避免多相流从二氧化碳电还原反应装置的侧面流出。阴极板100的材料可以为作为集流体的金属或合金材料，例如铜、钛、银、铁、镍、铝及其合金。
在本申请的一个实施方式中，阴极电极200可以为金属薄片电极或负载型导电薄片电极。金属薄片电极的材料可以包括但不限于锡、银、铜、金、铋、锌、铅等金属及合金，具有二氧化碳电还原活性。负载型导电薄片电极则可以采用催化剂负载于导电基底的方式制成，基底可为金属基或碳基材料。
在本申请的一个实施方式中，阴极流道板300的材料可以为绝缘性的惰性高分子材料，如聚四氟乙烯(PTFE)、聚氯乙烯(PVC)、氯化聚氯乙烯(CPVC)、聚醚醚酮(PEEK)和聚甲基丙烯酸甲酯(PMMA)等。阴极流道板300中的流道可以为蛇形流道，以尽量延长多相流在第二区320内流动的时间。为了避免因阴极流道板300厚度过大而导致电阻提高，阴极流道板300的厚度(未镂空、未设置凹槽的区域的厚度)可以设置成小于3mm。
在本申请的一个实施方式中，离子交换膜410可选阴离子交换膜或阳离子交换膜，阳离子交换膜410可使用杜邦公司生产的Nafion 115膜、Nafion 117膜、Nafion XL膜和Nafion N324膜等。
在本申请的一个实施方式中，参见图1，阳极板600上可以设置阳极进料通道610和阳极出料通道620。阳极板600内可以设置阳极板凹槽630，阳极板凹槽630内设置阳极板流道640，阳极电极510可以嵌入阳极板凹槽630并覆盖 阳极板流道640，阳极板流道640可以形成为蛇形流道。
阳极物料(例如为阳极电解液)可以从阳极进料通道610进入阳极板600，并沿阳极板流道640流动。在通电情况下阳极电解液发生氧化反应，而后从阳极出料通道620排出。阳极板600可以作为集流体，其上设置有集流接头，以连接外部电路，该接头可以为螺纹接头。参见图1，阳极板600可以充当固定板，其上也可以设置容纳密封圈700的密封沟槽650。阳极板600的材质可以为能够作为集流体的金属或合金材料，例如铜、钛、银、铁、镍、铝及其合金。
阳极电极510可以为负载有催化剂的纤维毡类或多孔泡沫类金属，其基底材料可以选择金属或金属氧化物，例如钛、镍、铜、银、铝及其氧化物。阳极电极510在催化阳极侧的发生氧化反应的同时可对离子交换膜410起到一定的支撑作用。阳极电极510负载的阳极催化剂需要对水氧化反应具有活性，阳极催化剂可以为金属或金属氧化物，例如铱、铂、钯、钌、铑、铁、钴、镍、钛及其氧化物，负载量可以为0.5～2mg/cm2。
在本申请的一个实施方式中，可以用阳极膜电极、阳极集流体替换离子交换膜410和阳极电极510。阳极膜电极可以为负载有阳极催化剂的离子交换膜，可以使用超声喷涂的工艺将阳极催化剂均匀负载在离子交换膜的一侧，并使具有阳极催化剂的一侧紧贴阳极集流体，另一侧紧贴阴极流道板300。阳极膜电极中的离子交换膜410可选阴离子交换膜或阳离子交换膜，其中阳离子交换膜可使用杜邦公司生产的Nafion 115膜、Nafion 117膜、Nafion XL膜和Nafion N324膜等。负载的阳极催化剂需要对水氧化反应具有活性，阳极催化剂可以为金属或金属氧化物，例如铱、铂、钯、钌、铑、铁、钴、镍、钛及其氧化物，负载量可以为0.5～2mg/cm2。
阳极集流体可以为无负载的纤维毡类或多孔泡沫类金属，其材料可以为金属或金属氧化物，如钛、镍、铜、银、铝及其氧化物。阳极集流体可以嵌入阳极板凹槽630，一侧覆盖于阳极板流道640，另一侧紧贴阳极膜电极的催化剂一侧。
在本申请的一个实施方式中，可以对阴极电解液进行加压处理，使电解液中二氧化碳浓度进一步增大，进而可使装置支持更高的反应电流密度。
在本申请的一个实施方式中，密封圈700可以为氟橡胶，可在常压和加压条件下实现装置的有效密封。
在本申请的一个实施方式中，二氧化碳电还原反应装置还可以包括气体流量控制装置和泵组件，以能够向阴极侧加入二氧化碳和电解液。二氧化碳电还原反应装置还可以包括背压阀等压力调控设备，可以使例如阴极出料通道130、阳极出料通道620连接背压阀，用以控制装置内流体的压力。
示例性地，可以通过泵组件将阴极电解液和阳极电解液的流量控制为20～200mL/min(毫升/分钟)。通过气体流量控制装置将二氧化碳气体的流量控制为20～1000sccm(标准毫升/分钟)。若装置在加压条件下运行，多相流的压强可以通过背压阀控制，可调压强范围为1～40bar(巴)。阳极腔室与阴极腔室内的压强可以保持一致，以此平衡离子交换膜410或阳极膜电极两侧的压差。
二氧化碳电还原反应装置的阴极侧发生的反应为二氧化碳电还原反应，产物可为甲酸、甲酸盐、一氧化碳等；阳极侧发生的反应为水氧化析出氧气。阳极电解液和阴极电解液可以相同或不同。阴极电解液可以为第一电解质的水溶液，阳极电解液为水、酸或第二电解质的水溶液。其中的第一电解质和第二电解质可以相同或不同，且各自独立地为可溶性盐或碱。可溶性盐可以选自碳酸氢盐、碳酸盐、甲酸盐、磷酸盐、磷酸氢盐、盐酸盐、乙酸盐、高氯酸盐、硫酸盐中的至少一种。可溶性盐中的阳离子可以为金属离子，例如钾离子、钠离子、锂离子、铯离子等。碱可选自碱金属的氢氧化物和/或氨水，碱金属的氢氧化物例如为氢氧化钠、氢氧化钾、氢氧化锂等。酸可以为硫酸水溶液、高氯酸水溶液和盐酸中的至少一种。在阴极电解液和阳极电解液中，溶质的浓度可以为0.1～10mol/L(摩尔/升)。
下面，本申请还提供了几个具体的实施例。
实施例1：
在二氧化碳电还原反应装置中，阴极板100的材料为铜，尺寸为90mm×90mm×20mm。阴极电极200为金属锡薄片，尺寸为60mm×60mm×0.1mm；阳极膜电极使用Nafion 115阳离子交换膜，单面负载氧化铱(氧化铱负载量为2mg/cm2)，整体面积与阴极电极200一致。阳极集流体为纤维钛毡，尺寸为50mm×50mm×0.4mm。阳极板600的材料为钛，尺寸为90mm×90mm×20mm。阳极板600上的阳极板流道640为单蛇形流道，流道宽度为2mm，深度为1.5mm，流道长为0.85m。阴极流道板300的结构如图3所示，其前端(第一区310)的流道与阴极板100、阴极电极200中的通道、孔共同构成垂直T型多相流直接生成位点，阴极流道板300的材料为CPVC，厚度(流道深度)为1mm，采用单蛇形流道，流道长1.6m，流道宽度为1mm，流道区域面积50mm×50mm。阴极电解液采用浓度为0.5mol/L的KHCO3水溶液，阳极电解液采用去离子水，阴极电解液流量为20mL/min，二氧化碳气体流量为200sccm，阳极电解液流量为40mL/min。装置内压力控制为9bar，采用恒电流反应，分别设定总电流密度为1kA/m2(总电流1.6A)、2kA/m2(总电流3.2A)、3kA/m2(总电流4.8A)、4kA/m2(总电流6.4A)、5kA/m2(总电流8A)。反应运行中，甲酸盐、一氧化碳、氢气选择性(法拉第效率)随电流密度的变化结果如图5所示。
由图5可知，在1～5kA/m2的总电流密度范围内，目标产物甲酸盐的选择性可始终维持在90％以上，展现出较高的电还原活性，具有较大的应用潜力。
实施例2：
按照实施例1的方法进行二氧化碳电还原反应，不同的是，使用恒电流法设定电流密度为3kA/m2(总电流4.8A)不变，电压与甲酸盐、一氧化碳、氢气选择性(法拉第效率)随着装置运行时间的变化结果如图6所示。
由图6可知，本实施例在设定电流密度3kA/m2下，装置在运行120h(小时)的电还原反应时间中维持超过85％的甲酸选择性，且装置电压稳定在4V左右，说明电还原装置在高电流密度下可长期稳定运行。
实施例3：
在二氧化碳电还原反应装置中，将阳极膜电极更换为离子交换膜410，例如无负载的Nafion 115阳离子交换膜，并将阳极集流体更换为阳极电极510，例如为负载氧化铱的纤维钛毡，氧化铱负载量为1mg/cm2，其它同实施例1。阴极电解液采用浓度为0.5mol/L的KHCO3水溶液，阳极电解液采用0.1mol/L的H2SO4水溶液。阴极电解液流量为20mL/min，二氧化碳气体流量为200sccm，阳极电解液流量为40mL/min，装置内不做加压处理，控制在常压，采用恒电流反应，设定电流密度为2kA/m2(总电流3.2A)。反应运行中，不同时间的甲酸盐选择性(法拉第效率)变化结果如表1所示。
表1
由表1可见，本实施例在设定电流密度为2kA/m2、装置电压为4.7V时，仅在常压条件(不对阴极电解液等进行加压处理)下即可使甲酸盐选择性超过72％。
实施例4：
在二氧化碳电还原反应装置中，除了将阴极电极200调整为金属薄片(材料为银)，并将阴极板100和阴极流道板300的结构调整为如图4所示外，其它同实施例1。阴极流道板300的前端流道与阴极板100、阴极电极200共同构成水平T型多相流直接生成位点，流道板材质为CPVC，厚度(即流道深度)为1mm，采用单蛇形流道，流道长为1.45m，流道宽度为1mm，流道区域所占区域的尺寸为50mm×50mm。阴极电解液采用浓度为0.5mol/L的KHCO3水溶液，阳极电解液采用去离子水。阴极电解液流量为20mL/min，二氧化碳气体流量为200sccm，阳极电解液流量为40mL/min，装置内压力控制为9bar，采用恒电流反应，设定电流密度为2kA/m2(总电流2.9A)。反应运行中， 不同时间的CO选择性(法拉第效率)结果如表2所示。
表2
由表2可见，本实施例在设定电流密度为2kA/m2时，CO选择性可达75％以上，装置电压约3.9V。
通过上述实施例可以看出，本申请提供的二氧化碳电还原反应装置能够在节约空间和成本的同时具有优异的产物选择性(甲酸盐、一氧化碳的法拉第效率高)和稳定性。由于结构简化，其在反应装置放大和工业化应用方面的潜力也更大。
以上所述是本申请的优选实施方式，应当指出，对于本领域技术人员来说，在不脱离本申请原理的前提下，还可以做出若干改进和润饰，这些改进和润饰也应视为本申请的保护范围。
附图标记列表
100 阴极板
110 阴极第一进料通道
120 阴极第二进料通道
130 阴极出料通道
140 阴极集流接头
150 密封沟槽
200 阴极电极
210 第一孔
220 第二孔
300 阴极流道板
310 第一区
311 第一流道
312 第二流道
313 第三流道
320 第二区
410 离子交换膜
510 阳极电极
600 阳极板
610 阳极进料通道
620 阳极出料通道
630 阳极板凹槽
640 阳极板流道
650 密封沟槽
700 密封圈

Claims (10)

  1. 一种具有多相流直接生成功能的二氧化碳电还原反应装置，其中，包括顺序设置的：
    阴极板(100)，所述阴极板(100)上设置有阴极第一进料通道(110)和阴极第二进料通道(120)，所述阴极第一进料通道(110)用于通入阴极第一物料，所述阴极第二进料通道(120)用于通入阴极第二物料；
    阴极电极(200)，所述阴极电极(200)上设置有连接于所述阴极第一进料通道(110)的第一孔(210)和连接于所述阴极第二进料通道(120)的第二孔(220)；
    阴极流道板(300)，所述阴极流道板(300)包括设置有未镂空的沟槽的第一区(310)和镂空的第二区(320)，所述第一区(310)设置于所述阴极流道板(300)的在厚度方向上靠近所述阴极电极(200)的一侧，所述第一孔(210)和所述第二孔(220)都连接于所述第一区(310)，所述第一区(310)连接于所述第二区(320)，使得所述阴极第一物料和所述阴极第二物料能够分别通过所述阴极第一进料通道(110)和所述阴极第二进料通道(120)进入所述第一区(310)，在所述第一区(310)交汇混合，而后进入所述第二区(320)。
  2. 根据权利要求1所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述阴极第一物料和所述阴极第二物料交汇处的所述阴极第一物料所在的流道垂直于所述阴极第二物料所在的流道。
  3. 根据权利要求2所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述第一区(310)包括第一流道(311)，所述第一孔(210)和所述第二孔(220)分别连接于所述第一流道(311)的上下游，所述第二孔(220)的轴线方向垂直于所述阴极流道板(300)。
  4. 根据权利要求3所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述第一孔(210)的轴线方向和所述第二孔(220)的轴线方向都垂直于所述阴极流道板(300)。
  5. 根据权利要求2所述的具有多相流直接生成功能的二氧化碳电还原反 应装置，其特征在于，所述第一区(310)包括相互垂直的第一流道(311)和第二流道(312)，所述第一孔(210)连接于所述第一流道(311)，所述第二孔(220)连接于所述第二流道(312)。
  6. 根据权利要求2所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述第一区(310)包括第三流道(313)，所述第三流道(313)位于所述阴极第一物料和所述阴极第二物料交汇处的下游。
  7. 根据权利要求1所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述二氧化碳电还原反应装置还包括顺序设置的离子交换膜(410)、阳极电极(510)和阳极板(600)，所述离子交换膜(410)贴合于所述阴极流道板(300)。
  8. 根据权利要求1所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述二氧化碳电还原反应装置还包括顺序设置的阳极膜电极、阳极集流体和阳极板(600)，所述阳极膜电极贴合于所述阴极流道板(300)。
  9. 根据权利要求1所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述阴极板(100)还具有阴极出料通道(130)。
  10. 根据权利要求7或8所述的具有多相流直接生成功能的二氧化碳电还原反应装置，其特征在于，所述阳极板(600)具有阳极进料通道(610)和阳极出料通道(620)。
PCT/CN2024/093335 2024-03-27 2024-05-15 具有多相流直接生成功能的二氧化碳电还原反应装置 Pending WO2025200094A1 (zh)

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