WO2019212071A1 - Réacteur de déshydratation électrochimique et procédé de production d'hydrogène à l'aide de celui-ci - Google Patents

Réacteur de déshydratation électrochimique et procédé de production d'hydrogène à l'aide de celui-ci Download PDF

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WO2019212071A1
WO2019212071A1 PCT/KR2018/005040 KR2018005040W WO2019212071A1 WO 2019212071 A1 WO2019212071 A1 WO 2019212071A1 KR 2018005040 W KR2018005040 W KR 2018005040W WO 2019212071 A1 WO2019212071 A1 WO 2019212071A1
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electrochemical
catalyst
hydrogen
dehydrogenation reactor
reaction
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PCT/KR2018/005040
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English (en)
Korean (ko)
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문상봉
최윤기
윤대진
문창환
정혜영
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(주)엘켐텍
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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
    • 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
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • 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
    • C25B13/00—Diaphragms; Spacing elements
    • C25B13/04—Diaphragms; Spacing elements characterised by the material
    • C25B13/08—Diaphragms; Spacing elements characterised by the material based on organic materials
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C25B9/77—Assemblies comprising two or more cells of the filter-press type having diaphragms

Definitions

  • the present invention relates to an electrochemical dehydrogenation reactor, and more particularly, to an electrochemical dehydrogenation reactor in which hydrogenated hydrogenated organics are oxidized in an anode chamber and hydrogen is generated by a reduction reaction in a cathode chamber.
  • the present invention also relates to a method for producing hydrogen using the electrochemical dehydrogenation reactor as described above.
  • renewable energy is actively introduced at home and abroad for the purpose of reducing CO 2 .
  • renewable energy such as wind power generation and solar power generation has a problem in that the power generation is irregular and the inconsistency between the power demand and the power generation is very large.
  • a device such as a battery can be used for instantaneous energy storage and output control, but it is difficult to apply due to the high cost due to seasonal factors (summer and winter) and long distance energy transmission.
  • Energy carriers capable of storing power obtained from these renewable energies for a long time or transporting them to remote locations are being considered.
  • Energy carriers include liquid hydrogen (or compressed hydrogen), ammonia, organic hydride (Liquid Organic Hydrogen Carrier, hereinafter referred to as "LOHC"), and the like.
  • LOHC Liquid Organic Hydrogen Carrier
  • LOHC is a hydrogen carrier that is liquid at room temperature and atmospheric pressure, has similar properties to petroleum, and is easy to transport using existing infrastructure.
  • Representative LOHCs include benzene, naphthalene, toluene, N-ethylcarbazole, pyridine, and the like, which are hydrogenated organic compounds by hydrogenation.
  • an electrochemical dehydrogenation reactor for supplying a hydrogenated hydrogenated organic material to the anode chamber to oxidize it at the anode, and to produce hydrogen at the cathode and this Its purpose is to provide a method for producing used hydrogen.
  • the electrochemical dehydrogenation reactor of the present invention for achieving the above object is provided with a cathode chamber and a cathode chamber on each side of the solid polymer electrolyte membrane, the hydrogenated organic material supplied to the anode chamber is an organic compound, protons and electrons After decomposition to move to the cathode chamber is characterized in that for producing hydrogen.
  • the hydrogenated organic material is methylcyclohexane
  • the organic compound is characterized in that toluene (toluene).
  • a reaction layer and a diffusion layer in which electrochemical oxidation and reduction occur on both sides of the solid polymer electrolyte membrane are further sequentially formed to form a membrane electrode assembly.
  • the solid polymer electrolyte membrane is a fluorine-based polymer membrane-based or hydrocarbon-based polymer membrane-based material, characterized in that having a thickness of 5 ⁇ 300 ⁇ m.
  • the reaction layer includes a catalyst and a carrier supporting the catalyst to enlarge the reaction surface area of the catalyst, the particle size of the catalyst is 0.001 ⁇ 0.1 ⁇ m, the particle size of the carrier is 10 It is characterized by a ⁇ 1000nm.
  • the diffusion layer is made of carbon or metal, and has a thickness of 0.1 to 2 mm and an opening ratio of 30 to 70%.
  • Hydrogen production method of the present invention for achieving the above object is characterized in that for producing hydrogen using the electrochemical dehydrogenation reactor configured as described above.
  • the supplied current is 0.01A / cm 2 ⁇ 2.0A / cm 2 per unit area, characterized in that the operating temperature is 10 °C ⁇ 100 °C.
  • the pressure of the hydrogen supplied is characterized in that 0.1bar ⁇ 350bar.
  • the present invention is to supply the hydrogenated hydrogenated organic material to the anode chamber to oxidize it at the anode, and to produce hydrogen at the cathode, because it uses an electrochemical method that can be operated at room temperature and atmospheric pressure, not the reaction of high temperature and high pressure during the dehydrogenation reaction. In addition, there is an advantage in that the operation at the start and stop operation is excellent.
  • the present invention is a method of using an electrolysis cell in which the anode and the cathode are integrated into the membrane, and thus it is possible to operate at low power, thereby reducing the operating cost significantly.
  • FIG. 2 is a structural diagram of a membrane electrode assembly applied to the electrochemical dehydrogenation reactor of the present invention
  • FIG. 3 is a structural diagram of an electrochemical cell used as an electrochemical dehydrogenation reactor of the present invention
  • FIG. 4 is a structural diagram of an electrochemical stack used as an electrochemical dehydrogenation reactor of the present invention
  • 5 and 6 are graphs of the voltage-current density and the hydrogenation amount for the embodiments tested by applying the electrochemical dehydrogenation reactor according to the present invention.
  • the electrochemical dehydrogenation reactor of the present invention is composed of a positive electrode 110, a solid polymer electrolyte membrane 120, and a negative electrode 130.
  • the MCH when the MCH is supplied to the anode 110, the MCH is decomposed into toluene (TL), protons, and electrons at the anode, and the proton passes through the solid polymer electrolyte membrane 120 to the cathode 130. It is configured to move and cause a hydrogen reaction.
  • the theoretical electrode reaction is 1.20V
  • the actual operation is about 2.0V in consideration of the overvoltage, etc., it is possible to significantly reduce the operating energy compared to the operation method of the conventional catalytic decomposition process.
  • FIG. 2 is a structural diagram of a membrane electrode assembly 200 applied to the electrochemical dehydrogenation reactor of the present invention.
  • MEA membrane electrode assembly
  • the MEA 200 integrates the reaction layers 204 and 208 where the electrochemical oxidation reaction and the reduction reaction take place and the solid polymer electrolyte membrane (hereinafter referred to as Proton exchange membrane, hereinafter referred to as "PEM”), or This means that the diffusion layers 202 and 210 are integrated in addition to the reaction layers 204 and 208 and the PEM 206 of the same oxidation and reduction reaction.
  • PEM Solid polymer electrolyte membrane
  • the place where the oxidation reaction occurs is described as the first electrochemical reaction layer 204 and the place where the reduction reaction occurs as the second electrochemical reaction layer 208, where the current is applied to the oxidation reaction and Reduction reactions occur simultaneously.
  • MCH is supplied to the first electrochemical reaction layer 204 via the first diffusion layer 202
  • MCH is toluene (TL)
  • electrons (e) in the first electrochemical catalyst 212 oxidation catalyst, positive electrode active material electrode) -
  • it is decomposed into hydrogen ions (H +) (proton) (see scheme 1).
  • the hydrogen ion (H + ) is passed through the PEM 206 by the electric field to the second electrochemical catalyst 216 (reduction catalyst, negative electrode active material, or hydrogen gas generating electrode)
  • electron (e ⁇ ) is
  • the first electrochemical catalyst 212 moves to the second electrochemical catalyst 216 through the first diffusion layer 202, an external circuit (not shown), and the second diffusion layer 210.
  • the electrochemical reactions occurring in the first electrochemical catalyst 112 and the second electrochemical catalyst 116, respectively, are represented by the following Reaction Schemes 1, 2, and 3.
  • the PEM 206 has a sulfonic acid ion exchange group that is excellent in oxidation reaction or long-term stability against organic compounds (TL and MCH), and has excellent hydrogen ion (proton or H + ) conductivity, and an anode chamber material (TL, MCH). It should be possible to prevent the mixing and diffusion of the cathode chamber material (hydrogen).
  • afion Nafion (Nafion, registered trademark) of DuPont
  • Flemion Flemion (Flemion, registered trademark) of Asahi Glass Co., Ltd.
  • Aciplex Asahi Glass Co., Ltd.
  • hydrocarbon-based polymer membranes include sulfonated polyether ketones, sulfonated polyether sulfones, sulfonated polyether ether sulfones, sulfonated polysulfides and sulfonated polyphenylenes. Etc. can be used.
  • the thickness of a PEM is preferable and, as for the thickness of a PEM, 20-170 micrometers is especially preferable. If the thickness of the PEM is less than 5 ⁇ m, cross leakage (product leakage from the cathode chamber to the anode chamber) is likely to occur, and if the thickness of the PEM becomes thicker than 300 ⁇ m, the proton resistance becomes large, which consumes a lot of electrical energy, which is undesirable. not.
  • the first and second electrochemical catalysts 212 and 216 are platinum, palladium, ruthenium, iridium, rhodium, osmium, platinum group elements, iron, lead, copper, chromium, cobalt, nickel, manganese, vanadium, molybdenum, gallium, Metals such as aluminum, alloys thereof, oxides, and complex oxides may be used. Platinum, palladium, rhodium, ruthenium, and iridium may be used for excellent electrode reactivity and to efficiently and stably use the electrode reaction for a long time. Preference is given to using one or two or more metals or oxides selected from.
  • the particle size of the first and second electrochemical catalysts 212 and 216 is too low, so that the activity of the catalyst is lowered. If the particle size is too small, the stability of the catalyst is lowered. Preferably it is 1-50 nm.
  • carriers (or carriers) 214 and 218 supporting the catalyst are preferably in the form of electron conductive particles, and include metal oxides including titanium, carbon black, graphite, graphite, activated carbon, and carbon. Preference is given to using fibers, carbon nanotubes, fullerenes.
  • the carriers 214 and 218 are difficult to form an electron conductive pathway generated when the particle size is too small.
  • the particle diameter is preferably 10 to 1,000 nm, more preferably 10 to 100 nm.
  • the first and second diffusion layers 202 and 210 may be made of carbon or metal. In addition, the first and second diffusion layers 202 and 210 may use cloth, paper, sintered fiber, or the like.
  • the first diffusion layer 202 is coated with a hydrophobic material such as polytetrafluoroethylene (PTFE) on the surface to facilitate gas fluid flow, and a carbon-based material having excellent corrosion resistance against hydrogen is particularly preferable.
  • PTFE polytetrafluoroethylene
  • the second diffusion layer 210 is not limited to the material.
  • the first and second diffusion layers 202 and 210 preferably have a thickness of 0.1 to 2 mm and an opening ratio of about 30 to 70% to promote diffusion of gas.
  • the manufacturing process of the MEA 200 is composed of a catalyst synthesis process, a catalyst ink production process, a catalyst ink transfer process, and a thermocompression process (a process of forming the transferred catalyst ink in a PEM or diffusion layer).
  • catalysts and carriers may use commercially available particles, but may be synthesized according to a known method and used.
  • combination may employ
  • the catalyst ink manufacturing process includes the catalysts 212 and 216 obtained in the catalyst synthesis process and the carriers 214 and 218 having the same, hydrophobic resins, solvents, and the like so that catalysts are easily formed in the PEM 206 or the diffusion layers 202 and 210. It is a process of mixing Nafion (trademark) dispersion liquid which is an ionomer.
  • the catalyst ink for the first electrochemical reaction layer 204 includes a first electrochemical catalyst 212, a carrier 214, a polymer electrolyte ionomer, a solvent and a hydrophobic resin, and the second electrochemical reaction layer 208.
  • Catalyst inks include a second electrochemical catalyst 216, a carrier 218, a polymer electrolyte ionomer, a solvent and a hydrophobic resin.
  • Hydrophobic resin fluorine-type high molecular component is a gas permeable material, It is preferable that the particle diameter of the powder is 0.005-10 micrometers.
  • the amount of catalyst in each layer is 0.01 mg / cm 2 is preferably such that more than, 10mg / cm 2 or less. This is because the reaction efficiency is lowered at less than 0.01 mg / cm 2 , and the installation cost of the electrochemical reaction cell is increased at more than 10 mg / cm 2 .
  • the catalyst ink transfer process is a process of transferring the catalyst ink prepared under the above conditions to a transfer paper (eg, Teflon sheet, polyimide sheet), leaving the main catalyst component and removing the solvent component. This transfer step may be omitted in the case where the catalyst ink is directly sprayed onto the PEM or the diffusion layer.
  • a transfer paper eg, Teflon sheet, polyimide sheet
  • the thermocompression process is a process of transferring the catalyst layer formed on the transfer paper to the film or the diffusion layer through thermal and compression.
  • a processing apparatus well-known apparatuses, such as a hot press and a hot roller, can be used.
  • press conditions room temperature-360 degreeC, and the pressure of 0.1-5 Mpa are preferable.
  • Figure 3 is an electrochemical cell used as the electrochemical dehydrogenation reactor of the present invention, a structural diagram of an electrochemical cell 300 having a membrane electrode assembly shown in Figure 2
  • Figure 4 is an electrochemical dehydrogenation reactor of the present invention
  • an electrochemical stack used as a structure it is a structural diagram of an electrochemical stack 400 formed by stacking a plurality of unit electrochemical cells shown in FIG. 3.
  • the electrochemical cell 300 includes a first end plate 302, a first insulating plate 304, a first current supply plate 306, and a first electrochemical reaction chamber frame 308), the first electrochemical reaction chamber 310, the MEA (200 in FIG. 2), the second electrochemical reaction chamber 312, the second electrochemical reaction chamber frame 314, and the second current supply plate 316.
  • a power converter 324 for supplying a current to the electrochemical cell is provided with a DC power supply.
  • first electrochemical reaction chamber 310 anode chamber
  • second electrochemical reaction chamber 312 cathode chamber
  • flow paths for supplying and discharging respective reactants or products are formed. It is configured to perform a function of mechanically supporting the MEA 200 and an electrical connection function with an adjacent unit cell.
  • the first end plate 302 and the second end plate 320 provide a bolt / nut fastening hole (not shown) for the unit electrochemical cell assembly, and a passage (not shown) for reactants and products, and a first insulating plate.
  • 304 and the second insulating plate 318 are electrically connected between the first end plate 302 and the first current supply plate 306 and between the second end plate 320 and the second current supply plate 316, respectively. Insulating function, the first current supply plate 306 and the second current supply plate 316 is connected to the power converter 324 serves to supply the current required for the electrochemical cell 300.
  • the first electrochemical catalyst 212 when the first electrochemical catalyst 212 is located in the first electrochemical reaction chamber 310 and the oxidation reaction occurs, it becomes a space for the movement of the reactant MCH, the product TL (toluene), PEM (206) In the second electrochemical reaction chamber 312 which is located opposite to the first electrochemical reaction chamber 310 with respect to), space for external discharge of hydrogen by a reduction reaction is provided.
  • the first electrochemical reaction chamber 310 is isolated from the outside by the first electrochemical reaction chamber frame 308, and the second electrochemical reaction chamber 312 is external by the second electrochemical reaction chamber frame 314. Is blocked.
  • a gasket (or packing) 322 is installed between the MEA 200, the first electrochemical reaction chamber frame 308, and the second electrochemical reaction chamber frame 314 to prevent external leakage of reactants and products. .
  • the first electrochemical reaction chamber frame 308, the second electrochemical reaction chamber frame 314, and the gasket 322 are introduced into a reactant or a product through the electrochemical cell. And an appropriate hole to facilitate outflow, and a flow path (indicated by a dotted line in FIG. 3A) is formed in the first electrochemical reaction chamber frame 308 and the second electrochemical reaction chamber frame 314.
  • a plurality of unit electrochemical cells are required, and at this time, a collection of two or more stacked electrochemical cells may be formed as an electrochemical stack 400 and operated (see FIG. 4).
  • reactant 1 MCH, methylcyclohexane
  • MCH methylcyclohexane
  • the current supplied to the first electrochemical reaction layer 204 and the second electrochemical reaction layer 208 is preferably 0.01 A / cm 2 to 2.0 A / cm 2 per unit area. This is because, in the case of 0.01A / cm 2 or less, the electrolytic reaction area is increased, which increases the investment cost, and in 2.0A / cm 2 or more, there is a problem in that durability of the components of the electrolysis cell due to overvoltage is deteriorated. .
  • the operating temperature of an electrolysis cell is 10 degreeC-100 degreeC, 50 degreeC-80 degreeC is more preferable. This is because the proton transfer resistance increases at 10 ° C. or lower, and deterioration in durability of the electrolysis cell component is a problem at 100 ° C. or higher.
  • the hydrogen pressure supplied to the electrolysis cell is appropriately 0.1 bar to 350 bar. This is because, at 0.1 bar or less, electrolysis efficiency is reduced due to despreading of the cathode chamber, and at least 350 bar, the durability deterioration of components of the electrolysis cell becomes a problem.
  • MEF 200 Nafion 117 perfluorocarbonsulfonic acid film (thickness 170), first electrochemical reaction layer 204 (anode catalyst, Pt / C carrier (Tanaka Precious Metal Industry)) 0.5 mg / cm 2 and agent 2 electrochemical reaction layer 208 (cathode catalyst, Pt-Ru / C carrier (Tanaka Precious Metal Industry)) 0.5 mg / cm 2 , first diffusion layer 202 (carbon paper) and second diffusion layer 210, titanium sintered fiber aperture ratio 80%, thickness 0.2mm, Descartes, Germany).
  • the area (electrochemical reaction area) of the MEA 200 was 25 cm 2 .
  • MCH was supplied to the lower part of the first electrochemical reaction chamber 310 (anode chamber) of the electrochemical cell 300 to obtain hydrogen in the second electrochemical reaction chamber 312 (cathode chamber).
  • the current supplied to the electrochemical cell 300 was 1A / cm 2
  • the temperature was 80 ° C.
  • the hydrogen supply pressure was 5 bar.
  • the performance was evaluated for the voltage-current performance of the electrochemical cell (Example 1 of FIG. 5), and the degree of dehydrogenation (amount of hydrogenation) was measured by measuring the weight change rate (Example 1 of FIG. 6) of the product TL.
  • the MEA was configured in the same manner as the MEA 200 of the first embodiment.
  • Performance is dehydrogenated by evaluating the voltage-current performance of the electrochemical cell (Example 2 of FIG. 5) and measuring the weight change rate (Example 2 of FIG. 6) of the product N-ethylcarbazole. Degree (hydrogenation amount) was measured.

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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

Le réacteur de déshydratation électrochimique de la présente invention comporte une chambre d'électrode positive et une chambre d'électrode négative sur les deux côtés d'une membrane d'électrolyte polymère solide, respectivement. Une matière organique hydrogénée introduite dans la chambre d'électrode positive est dégradée en un composé organique, des protons et des électrons, qui sont ensuite déplacés dans la chambre d'électrode négative pour produire de l'hydrogène.
PCT/KR2018/005040 2018-04-30 2018-04-30 Réacteur de déshydratation électrochimique et procédé de production d'hydrogène à l'aide de celui-ci WO2019212071A1 (fr)

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KR10-2018-0050262 2018-04-30
KR1020180050262A KR20190125885A (ko) 2018-04-30 2018-04-30 전기화학적 탈수소화 반응기 및 이것을 이용한 수소의 제조방법

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AU2022223845A1 (en) * 2021-02-19 2023-08-17 Eneos Corporation Apparatus for producing organic hydride and method for producing organic hydride

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20130037649A (ko) * 2011-10-06 2013-04-16 가부시키가이샤 히타치세이사쿠쇼 막 전극 접합체 및 유기 하이드라이드 제조 장치
KR20140133301A (ko) * 2013-05-10 2014-11-19 (주)엘켐텍 전기화학셀용 막전극 접합체
JP2015165043A (ja) * 2014-02-07 2015-09-17 パナソニックＩｐマネジメント株式会社 有機ハイドライド変換装置
KR20170083593A (ko) * 2014-11-10 2017-07-18 고쿠리츠다이가쿠호진 요코하마 고쿠리츠다이가쿠 산소 발생용 애노드
US20170362084A1 (en) * 2016-06-16 2017-12-21 Panasonic Intellectual Property Management Co., Ltd. Hydrogen desorption method and dehydrogenation apparatus

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20130037649A (ko) * 2011-10-06 2013-04-16 가부시키가이샤 히타치세이사쿠쇼 막 전극 접합체 및 유기 하이드라이드 제조 장치
KR20140133301A (ko) * 2013-05-10 2014-11-19 (주)엘켐텍 전기화학셀용 막전극 접합체
JP2015165043A (ja) * 2014-02-07 2015-09-17 パナソニックＩｐマネジメント株式会社 有機ハイドライド変換装置
KR20170083593A (ko) * 2014-11-10 2017-07-18 고쿠리츠다이가쿠호진 요코하마 고쿠리츠다이가쿠 산소 발생용 애노드
US20170362084A1 (en) * 2016-06-16 2017-12-21 Panasonic Intellectual Property Management Co., Ltd. Hydrogen desorption method and dehydrogenation apparatus

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