WO2012137344A1 - Dispositif pour générer un gaz mixte - Google Patents

Dispositif pour générer un gaz mixte Download PDF

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Publication number
WO2012137344A1
WO2012137344A1 PCT/JP2011/058895 JP2011058895W WO2012137344A1 WO 2012137344 A1 WO2012137344 A1 WO 2012137344A1 JP 2011058895 W JP2011058895 W JP 2011058895W WO 2012137344 A1 WO2012137344 A1 WO 2012137344A1
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WO
WIPO (PCT)
Prior art keywords
mixed gas
cathode
reduction catalyst
electrolytic cell
cathode chamber
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PCT/JP2011/058895
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English (en)
Japanese (ja)
Inventor
正樹 設楽
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トヨタ自動車株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by トヨタ自動車株式会社 filed Critical トヨタ自動車株式会社
Priority to PCT/JP2011/058895 priority Critical patent/WO2012137344A1/fr
Publication of WO2012137344A1 publication Critical patent/WO2012137344A1/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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/40—Carbon monoxide
    • 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
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • 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
    • C25B15/02—Process control or regulation
    • 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
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the present invention relates to a mixed gas generator. More specifically, the present invention relates to a mixed gas generating device that generates a mixed gas composed of H 2 and CO using an electrolytic device.
  • Fossil fuels such as oil, coal, and natural gas are used as raw materials for heat and electricity generation and as transportation fuels, and support the modern energy consumption society.
  • fossil fuels are used up and their reserves are limited. Therefore, it goes without saying that it is necessary to prepare for the depletion of fossil fuels.
  • the release of CO 2 into the atmosphere due to the combustion of fossil fuels contributes to global warming. For this reason, reducing CO 2 emissions has become a challenge in recent years.
  • Patent Literature 1 discloses a system for producing hydrocarbon fuel (HC) using CO 2 as a raw material.
  • This system comprises an electrolyte cell having an oxygen ion conducting membrane composed of a solid oxide electrolyte, and a cathode and an anode respectively disposed on both sides thereof.
  • CO gas and H 2 gas can be generated from CO 2 gas and water vapor, respectively.
  • HC can be obtained by recovering the produced CO gas and H 2 gas from the electrolyte cell and subjecting them to a Fischer-Tropsch reaction (FT reaction) in a known production apparatus.
  • FT reaction Fischer-Tropsch reaction
  • Patent Document 2 discloses that the ratio of the amount of CO to H 2 in the raw material gas during the FT reaction is 1/4 ⁇ CO / H 2 ⁇ 2. If the substance amount ratio in the raw material gas is within the above range, HC can be produced with good energy efficiency (referred to the calorific value of the product with respect to the input energy; the same applies hereinafter).
  • H 2 and CO that are HC source gases can be generated simultaneously from the electrolyte cell. Therefore, in order to produce energy efficiently HC, when co-produce CO and H 2 from the electrolytic cell, so that the ratio of the amounts of substances CO to H 2 is 1/4 ⁇ CO / H 2 ⁇ 2 Electrolysis is necessary.
  • the amount of CO and H 2 produced in the electrolyte cell depends on the electrolysis conditions such as the amount of CO 2 gas and water vapor supplied to the electrolyte cell per unit time. Therefore, in order to simultaneously generate CO and H 2 at a desired substance amount ratio, it is necessary to make further improvements at the configuration level of the generator.
  • an object of the present invention is to provide a mixed gas generating device capable of simultaneously generating CO and H 2 at a desired substance amount ratio.
  • a first invention is a mixed gas generating device that electrolyzes carbon dioxide and water to generate a mixed gas containing carbon monoxide and hydrogen,
  • An electrolytic aqueous solution containing a predetermined concentration of carbon dioxide, and an insoluble reduction catalyst that is insoluble in the electrolytic aqueous solution and functions as a catalyst at the time of the reduction reaction of carbon dioxide to carbon monoxide;
  • An anode and a cathode provided in the electrolytic cell;
  • Voltage applying means for applying a voltage between the anode and the cathode;
  • a stirring means provided in the electrolytic cell for stirring the aqueous electrolyte solution in the electrolytic cell; It is characterized by providing.
  • the second invention is the first invention, wherein
  • the stirring unit includes a control unit that controls the stirring unit such that the insoluble reduction catalyst contacts the cathode.
  • the third invention is the second invention, wherein A substance amount ratio acquisition means for acquiring a substance amount ratio of carbon monoxide to hydrogen in the mixed gas generated in the electrolytic cell;
  • the control means changes the contact frequency of the insoluble reduction catalyst to the cathode according to the substance amount ratio.
  • 4th invention is set in 3rd invention,
  • the control means controls the agitation means so that the contact frequency increases when the substance amount ratio is smaller than a set ratio, and the agitation means when the substance amount ratio is larger than the set ratio. The control is stopped.
  • a fifth invention is any one of the first to fourth inventions,
  • the electrolytic cell includes a cathode chamber filled with the electrolyte aqueous solution, an anode chamber filled with water, and a proton-conductive diaphragm that separates the anode chamber and the cathode chamber.
  • the sixth invention is the fifth invention, wherein The insoluble reduction catalyst and the stirring means are provided in the cathode chamber.
  • the stirring means can be controlled by the control means so that the insoluble reduction catalyst contacts the cathode.
  • CO 2 is reduced if an insoluble reduction catalyst comes into contact with the cathode during voltage application. Therefore, if the stirring means is further controlled when this voltage is applied, the contact frequency of the insoluble reduction catalyst to the cathode (hereinafter simply referred to as “contact frequency”) can be controlled.
  • the insoluble reduction catalyst can be precipitated on the bottom surface of the electrolytic cell when the stirring means is not controlled to reduce the contact frequency, and can be dispersed in the electrolyte aqueous solution when the stirring means is controlled to increase the contact frequency. Therefore, according to the present invention, the progress of the reduction reaction of water and CO 2 can be controlled, so that CO and H 2 can be simultaneously generated at a desired substance amount ratio.
  • the contact frequency can be changed according to the substance amount ratio acquired by the substance amount ratio acquisition means.
  • the progress of the reduction reaction of water or CO 2 can be controlled by controlling the contact frequency. Therefore, if the contact frequency is changed according to the substance amount ratio acquired by the substance amount ratio acquisition means, the substance amount ratio of CO to H 2 in the mixed gas to be generated can be changed. Therefore, according to the present invention, the substance amount ratio of CO to H 2 can be adjusted to a desired substance amount ratio.
  • the stirring unit when the substance amount ratio acquired by the substance amount ratio acquisition unit is smaller than the set ratio, the stirring unit can be controlled so that the contact frequency increases.
  • the case where the ratio of the amount of CO to H 2 is smaller than the set ratio means that the amount of H 2 is large and the amount of CO is small. Therefore, if the stirring means is controlled so that the contact frequency increases, the progress of the CO 2 reduction reaction can be promoted and the amount of CO produced can be increased.
  • the control of the stirring unit when the substance amount ratio acquired by the substance amount ratio acquisition unit is larger than the set ratio, the control of the stirring unit can be stopped.
  • the case where the substance amount ratio of CO to H 2 is larger than the set ratio means that the substance amount of H 2 is small and the substance amount of CO is large. Therefore, if the control of the stirring means is stopped, only the reduction reaction of water proceeds and the amount of H 2 produced can be increased. From the above, according to the present invention, the substance amount ratio between CO and H 2 can be adjusted to be the set ratio.
  • mixing of the electrolyte aqueous solution in the cathode chamber and the water in the anode chamber can be prevented by the proton conductive diaphragm. If mixing can be prevented by the proton-conducting diaphragm, control of the CO 2 concentration and proton concentration in the cathode chamber and control of the amount of water in the anode chamber are facilitated. Therefore, according to the present invention, the substance amount ratio of CO to H 2 in the mixed gas generated in the cathode chamber can be easily adjusted.
  • the insoluble reduction catalyst and the stirring means are provided in the cathode chamber, the insoluble reduction catalyst can be reliably brought into contact with the cathode. Therefore, the accuracy of control of the contact frequency can be increased.
  • FIG. 1 is an overall configuration diagram of a mixed gas generation device according to an embodiment of the present invention. It is the schematic of the electrolyzer 10 of FIG. It is a figure for demonstrating operation
  • 4 is a flowchart illustrating catalyst agitation control executed by a control device 70 in the embodiment.
  • FIG. 1 is an overall configuration diagram of a mixed gas generation apparatus according to an embodiment of the present invention.
  • the mixed gas generation apparatus of this embodiment includes an electrolysis apparatus 10 that simultaneously generates CO gas and H 2 gas by electrolysis.
  • the electrolyzer 10 is an electrolyzer with a temperature controller 12 that controls the temperature in the apparatus within a predetermined range.
  • the detailed configuration of the electrolyzer 10 will be described in the description of FIG.
  • a KHCO 3 tank 14 in which an aqueous potassium hydrogen carbonate (KHCO 3 ) solution is stored is provided on the upstream side of the electrolyzer 10.
  • the KHCO 3 tank 14 is connected to the electrolysis device 10 via the flow path 16.
  • a liquid feed pump 18 configured to supply the KHCO 3 aqueous solution stored in the KHCO 3 tank 14 to the flow path 16 at a predetermined pressure is provided.
  • the KHCO 3 tank 14 is connected to a CO 2 tank 20 filled with CO 2 gas via a CO 2 valve 22.
  • the CO 2 valve 22 is configured to supply the CO 2 gas in the CO 2 tank 20 into the KHCO 3 tank 14.
  • the CO 2 valve 22 is constituted by an electromagnetic valve or the like, and its opening degree is controlled according to a control signal. By opening the CO 2 valve 22, and the CO 2 tank 20 and KHCO 3 tank 14 communicate with each other, the constant constantly CO 2 concentration of the aqueous KHCO 3 of KHCO 3 tank 14 (e.g., CO 2 saturation) Kept.
  • a water tank 24 in which water is stored is provided on the upstream side of the electrolysis apparatus 10.
  • the water tank 24 is connected to the electrolysis device 10 via the flow path 26.
  • a liquid feed pump 28 configured to supply water stored in the water tank 24 to the flow path 26 at a predetermined pressure is provided.
  • a gas-liquid separator 30 is provided on the downstream side of the electrolysis apparatus 10. As will be described later, CO, H 2 and H 2 O are generated in the cathode chamber of the electrolysis apparatus 10. These products are discharged from the electrolysis apparatus 10 in a state of being mixed with the KHCO 3 aqueous solution, and sent to the gas-liquid separator 30 for gas-liquid separation.
  • a mixed gas tank 32 is provided on the downstream side of the gas-liquid separator 30.
  • the mixed gas tank 32 is a pressure-resistant container (volume is known) having a sealed structure, and is connected to the gas-liquid separator 30 via a flow path 34.
  • the flow path 34 is provided with a mixed gas valve 36 configured to control the opening degree.
  • the mixed gas valve 36 is configured by an electromagnetic valve or the like, and its opening degree is controlled according to a control signal.
  • the gas-liquid separator 30 is connected to the KHCO 3 tank 14 via the flow path 38.
  • a concentration device 40 and a liquid feed pump 42 are provided on the flow path 38.
  • Concentrator 40 which has a heating device and a cooling device therein, was removed by heating the product water considerable amount of water from the aqueous KHCO 3, then substantially equal to the temperature of aqueous KHCO 3 in the mixing tank 32 It is configured to cool to temperature.
  • the liquid feed pump 42 is configured to supply the cooled KHCO 3 aqueous solution to the flow path 38 at a predetermined pressure.
  • the liquid feed pumps 18 and 42 function as circulation pumps that circulate the KHCO 3 aqueous solution in the KHCO 3 tank 14, the electrolyzer 10, the gas-liquid separator 30, and the concentrator 40.
  • the mixed gas generation apparatus of this embodiment further includes a control device 70.
  • a concentration sensor 44 that detects the concentrations of CO and H 2 in the mixed gas tank 32 is connected to the input side of the control device 70.
  • the electrolysis device 10, the temperature control device 12, the CO 2 valve 22, the liquid feed pumps 18, 28 and 42, the mixed gas valve 36 and the concentrating device 40 are connected to the output side of the control device 70.
  • FIG. 2 is a schematic view of the electrolyzer 10 of FIG.
  • the electrolysis apparatus 10 includes a three-electrode electrolytic tank 50.
  • the electrolytic cell 50 includes a cathode chamber 52 filled with a KHCO 3 aqueous solution, an anode chamber 54 filled with water, and a diaphragm 56 that partitions the cathode chamber 52 and the anode chamber 54.
  • the cathode chamber 52 is connected to the KHCO 3 tank 14 and the gas-liquid separator 30 shown in FIG.
  • a working electrode (WE) 58 corresponds to the cathode of the electrolytic cell 50, and is made of a metal (for example, Pt) that is difficult to reduce CO 2 during electrolysis.
  • the mixer 66 is a blade type stirring device that stirs the aqueous KHCO 3 solution in the cathode chamber 52.
  • CO 2 reduction catalyst 68 which functions as a reduction catalyst for selectively reducing the CO to CO 2 is disposed in a state of precipitation.
  • the CO 2 reduction catalyst 68 is a hydrophobic compound (that is, a compound insoluble in a KHCO 3 aqueous solution), and examples thereof include an organometallic complex disclosed in Japanese Unexamined Patent Publication No. 4-13883. Note that the CO 2 reduction catalyst 68 in the drawing is visualized for convenience of explanation, and does not necessarily precipitate as illustrated.
  • the water tank 24 of FIG. 1 is connected to the anode chamber 54.
  • a counter electrode (CE) 62 is disposed in the anode chamber 54.
  • the CE 62 corresponds to the anode of the electrolytic cell 50, and is made of a metal (eg, Au, Pt) that does not dissolve during electrolysis.
  • the diaphragm 56 has a function of transporting protons from the anode chamber 54 side to the cathode chamber 52 side, and is made of a polymer electrolyte such as NAFION (registered trademark).
  • the electrolysis apparatus 10 includes a power source 64.
  • the power source 64 is connected to the WE 58, RE 60, CE 62, and the control device 70 of FIG.
  • the power supply 64 controls the value of the current that flows between the WE 58 and the CE 62 so that the voltage between the RE 60 and the WE 58 becomes a predetermined value.
  • reaction of the above formula (1) proceeds at a location where the CO 2 reduction catalyst 68 electrically connected to the WE 58 by the drive of the mixer 66 is in contact with the KHCO 3 aqueous solution. Further, the reaction of the above formula (2) proceeds at a place where the main body portion of WE58 is in contact with the KHCO 3 aqueous solution. In addition, the reaction of the above formula (3) proceeds at a location where CE 62 is in contact with water.
  • Protons can be continuously generated on the CE 62 by driving the liquid feed pump 28 and supplying water to the anode chamber 54 while passing an electric current between the WE 58 and the CE 62 (the above formula (3)). .
  • the liquid feed pump 18 is driven to supply the aqueous KHCO 3 solution to the cathode chamber 52, CO 2 and protons can be continuously supplied to the cathode chamber 52. Therefore, if the liquid feed pumps 18 and 28 and the mixer 66 are driven while a current is passed between the WE 58 and the CE 62, CO and H 2 can be continuously generated on the WE 58 (the above formula (1)). (2)). Since CO and H 2 have low solubility in the aqueous KHCO 3 solution, almost all of the produced CO and H 2 will be present as gases.
  • the FT reaction is known as a reaction for synthesizing HC from CO and H 2 .
  • the driving of the mixer 66 is controlled based on the detection value of the concentration sensor 44 (catalyst stirring control).
  • FIG. 3 is a diagram for explaining the operation of the mixer 66 during the catalyst agitation control.
  • 3A shows before the mixer 66 is driven
  • FIG. 3B shows after the mixer 66 is driven.
  • the CO 2 reduction catalyst 68 is a hydrophobic compound, and before the mixer 66 is stirred, they are collected and settled near the bottom surface of the cathode chamber 52 (FIG. 3A). Therefore, as shown in the figure, before the mixer 66 is stirred, only the proton reduction reaction proceeds on the WE 58 (the above formula (2)).
  • FIG. 4 is a flowchart showing the catalyst agitation control executed by the control device 70 in the present embodiment. Note that the routine shown in FIG. 4 is repeatedly executed during operation of the mixed gas generation apparatus.
  • the control device 70 starts stirring the mixer 66 (step 100). Thereby, the inside of the cathode chamber 52 is in the state shown in FIG. Subsequently, the control device 70 causes a current to flow between WE58 and CE62 so that the voltage between RE60 and WE58 becomes a predetermined value (step 110). Thus, the CO 2 reduction reaction (the above formula (1)) proceeds on the CO 2 reduction catalyst 68 in contact with the WE 58, and the proton reduction reaction (the above formula (2)) proceeds on the other WE 58. (Step 120). When executing the processing of steps 110 and 120, the control device 70 activates the temperature control device 12, the CO 2 valve 22, the liquid feed pumps 18, 28 and 42, and the mixed gas valve 36. As a result, the reactions of the above formulas (1) and (2) proceed continuously, so that CO gas and H 2 gas are generated and flow into the mixed gas tank 32.
  • control device 70 detects the CO and H 2 concentrations in the mixed gas tank 32 from the concentration sensor 44 (step 130). Subsequently, the control device 70 obtains CO / H 2 from the CO and H 2 concentrations detected in step 130, and determines whether or not CO / H 2 > 1/2 is satisfied (step 140). As described above, since the volume of the mixed gas tank 32 is known, CO / H 2 can be obtained using the detection value from the concentration sensor 44.
  • step 140 If it is determined in step 140 that CO / H 2 > 1/2, it can be determined that the amount of CO generated should be reduced and the amount of H 2 generated should be increased. Therefore, the control device 70 stops the stirring of the mixer 66 (step 150) and returns to step 110 again. If the procedure returns to step 110 with stirring of the mixer 66 stopped, the cathode chamber 52 is in the state shown in FIG. 3A, and therefore only H 2 can be generated on the WE 58. On the other hand, when it is determined in step 140 that CO / H 2 > 1/2 is not satisfied, the control device 70 determines whether CO / H 2 ⁇ 1/2 is satisfied (step 160). .
  • CO / H 2 is obtained from the CO and H 2 concentrations obtained from the concentration sensor 44, and a KHCO 3 aqueous solution by the mixer 66 is obtained by comparing the obtained CO / H 2 with 1/2. Can be controlled. Therefore, CO / H 2 in the mixed gas tank 32 can always be maintained at 1 ⁇ 2.
  • stirred for aqueous KHCO 3 may be other stirring device.
  • a stirring bar such as a magnetic stirrer may be used instead of the mixer 66.
  • a three-electrode electrolytic cell 50 is used, and a voltage is applied between RE 60 and WE 58 by a power source 64.
  • CE 62 replaces RE 60.
  • a two-electrode electrolytic cell that also serves as an electrode may be used. That is, any configuration that can apply a voltage between WE58 and CE62 can be applied as a modification of the electrolyzer 10 of the present embodiment.
  • the diaphragm 56 is used between the cathode chamber 52 and the anode chamber 54, but the diaphragm 56 may be omitted.
  • the KHCO 3 aqueous solution is circulated in the cathode chamber 52 and the like, but the circulated solution is not necessarily limited to this. That is, any liquid having CO 2 absorption characteristics to which a general electrolyte (supporting electrolyte) is added can be used instead of the KHCO 3 aqueous solution.
  • water is provided in the anode chamber 54 and the like. However, any liquid that can generate protons by electrolysis can be used instead of water.
  • the power source 64 corresponds to the “voltage applying means” in the first invention
  • the mixer 66 corresponds to the “stirring means” in the first invention
  • the control device 70 corresponds to the “control means” in the second invention.
  • the concentration sensor 44 corresponds to the “substance amount acquisition unit” of the third aspect of the invention.
  • Electrolyzer 12 Temperature controller 14 KHCO 3 tank 16, 26, 34, 38 Flow path 18, 28, 42 Liquid feed pump 20 CO 2 tank 22 CO 2 valve 24 Water tank 30 Gas-liquid separator 32 Mixed gas tank 36 Mixed gas valve 40 Concentrator 44 Concentration Sensor 50 Electrolyzer 52 Cathode Chamber 54 Anode Chamber 56 Diaphragm 58 Working Electrode 60 Reference Electrode 62 Counter Electrode 64 Power Source 66 Mixer 68 CO 2 Reduction Catalyst 70 Controller

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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)
  • Automation & Control Theory (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

La présente invention concerne un dispositif pour générer un gaz mixte, qui est capable de générer simultanément du CO et du H2 dans un rapport molaire souhaité. Ledit dispositif comporte une cellule électrolytique (50) qui comprend une chambre cathodique (52) remplie d'une solution aqueuse de KHCO3 et une chambre anodique (54) remplie d'eau. Une électrode de travail WE (58), une électrode de référence RE (60) et un mélangeur (66) sont disposés dans la chambre cathodique (52). La WE (58), qui correspond à la cathode de la cellule électrolytique (50), est constituée d'un métal qui est moins apte à réduire le CO2 pendant l'électrolyse. Le mélangeur (66) est un agitateur à palettes qui agite la solution aqueuse de KHCO3 dans la chambre cathodique (52). Un catalyseur de réduction de CO2 (68) qui permet de réduire sélectivement le CO2 en CO est disposé dans un état sédimenté au fond de la chambre cathodique (52). Le catalyseur de réduction de CO2 (68) est un composé hydrophobe qui se disperse à l'intérieur de la chambre cathodique (52) lors du fonctionnement du mélangeur (66) pour venir en contact avec la surface de la WE (58).
PCT/JP2011/058895 2011-04-08 2011-04-08 Dispositif pour générer un gaz mixte WO2012137344A1 (fr)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017160476A (ja) * 2016-03-08 2017-09-14 富士通株式会社 二酸化炭素還元装置
US20180094355A1 (en) * 2016-10-04 2018-04-05 Johna Leddy Carbon dioxide reduction and carbon compound electrochemistry in the presence of lanthanides
WO2019049476A1 (fr) * 2017-09-05 2019-03-14 千代田化工建設株式会社 Système de production de gaz de synthèse
JP2020500258A (ja) * 2016-08-29 2020-01-09 ダイオキサイド マテリアルズ，インコーポレイティド 再生可能燃料および化学品を製造するための装置および方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6415388A (en) * 1987-07-07 1989-01-19 Terumo Corp Electrode for reducing gaseous carbon dioxide
JPH0959791A (ja) * 1995-08-24 1997-03-04 Mitsui Mining & Smelting Co Ltd 亜鉛電解液中の塩素濃度の低減法
JP2004176129A (ja) * 2002-11-27 2004-06-24 Kotaro Ogura 二酸化炭素からのエチレンの選択的製造方法

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6415388A (en) * 1987-07-07 1989-01-19 Terumo Corp Electrode for reducing gaseous carbon dioxide
JPH0959791A (ja) * 1995-08-24 1997-03-04 Mitsui Mining & Smelting Co Ltd 亜鉛電解液中の塩素濃度の低減法
JP2004176129A (ja) * 2002-11-27 2004-06-24 Kotaro Ogura 二酸化炭素からのエチレンの選択的製造方法

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017160476A (ja) * 2016-03-08 2017-09-14 富士通株式会社 二酸化炭素還元装置
JP2020500258A (ja) * 2016-08-29 2020-01-09 ダイオキサイド マテリアルズ，インコーポレイティド 再生可能燃料および化学品を製造するための装置および方法
US20180094355A1 (en) * 2016-10-04 2018-04-05 Johna Leddy Carbon dioxide reduction and carbon compound electrochemistry in the presence of lanthanides
US10774430B2 (en) * 2016-10-04 2020-09-15 Johna Leddy Carbon dioxide reduction and carbon compound electrochemistry in the presence of lanthanides
WO2019049476A1 (fr) * 2017-09-05 2019-03-14 千代田化工建設株式会社 Système de production de gaz de synthèse
JP2019044238A (ja) * 2017-09-05 2019-03-22 千代田化工建設株式会社 合成ガス生成システム
US11268198B2 (en) 2017-09-05 2022-03-08 Chiyoda Corporation Synthesis gas production system

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