JP5705214B2 - Organic hydride production equipment - Google Patents

Description

  The present invention relates to an organic hydride manufacturing apparatus for electrochemically manufacturing an organic hydride.

  As global warming due to carbon dioxide and the like becomes serious, hydrogen is attracting attention as an energy source for the next generation instead of fossil fuels. Hydrogen fuel has a low environmental impact because it is the only substance that is discharged when fuel is consumed and does not emit carbon dioxide. On the other hand, since hydrogen is a gas at normal temperature and pressure, transportation, storage, and supply systems are major issues.

  In recent years, organic hydride systems using hydrocarbons such as cyclohexane, methylcyclohexane, and decalin have attracted attention as hydrogen storage methods that are excellent in safety, transportability, and storage capacity. Since these hydrocarbons are liquid at room temperature, they are excellent in transportability. For example, toluene and methylcyclohexane are cyclic hydrocarbons having the same carbon number, but toluene is an unsaturated hydrocarbon in which the bonds between hydrocarbons are double bonds, whereas methylcyclohexane has double bonds. It is a saturated hydrocarbon that does not have. Methylcyclohexane is obtained by hydrogenation reaction of toluene, and toluene is obtained by dehydrogenation reaction of methylcyclohexane. That is, hydrogen can be stored and supplied by utilizing the hydrogenation reaction and dehydrogenation reaction of these hydrocarbons.

  In order to produce an organic hydride such as methylcyclohexane, it is necessary to first produce hydrogen and react the hydrogen and toluene on a catalyst. That is, the current process is a two-stage process in which hydrogen is generated in a water electrolysis apparatus or the like, and hydrogen and toluene are reacted in a hydrogen addition reaction apparatus to generate organic hydride.

  Therefore, a plurality of devices are required until the manufacture of the organic hydride, which causes a problem that the device is complicated. Moreover, since it is gaseous hydrogen from hydrogen production to hydrogen addition reaction, a problem arises regarding storage and transportation. If the hydrogen production apparatus and the hydrogen addition apparatus are constructed adjacent to each other, the above problem is solved, but there is a problem of construction and operation costs, and the overall energy efficiency is also lowered. Moreover, since the apparatus is enlarged, the installation place is limited.

  In recent years, a technique for producing an organic hydride in a single stage using a single apparatus has been disclosed (for example, Patent Document 1). The technique disclosed in Patent Document 1 is to produce an organic hydride electrochemically. For example, in Patent Document 1, metal catalysts are arranged on both sides of a hydrogen ion permeable electrolyte membrane that selectively transmits hydrogen ions, water or steam is supplied to one side, and a hydride is supplied to the other side. Organic hydrides are produced by causing hydrogen addition reaction between hydrogen ions generated by electrolysis of water or water vapor on the anode side and hydrides on the cathode side.

JP 2003-45449 A

  However, these organic hydride manufacturing methods have difficulty in obtaining high energy efficiency, and the organic hydride manufacturing efficiency is poor. The reason is considered to be a problem with the electrode structure. The electrode reaction is considered to occur at a three-phase interface where three of metal catalyst / proton conductive solid polymer electrolyte / reactive substance (hydrogenated substance) are in contact. In addition, in order for the electrode reaction to proceed on the catalyst, electrons and protons must be supplied to or moved from the metal catalyst, and therefore a network connecting the metal catalyst and the solid polymer electrolyte is required. is there. However, when the metal catalyst is directly deposited and placed on the solid polymer electrolyte membrane, high energy as described above due to the formation of the three-phase interface and the formation of the network of the solid polymer electrolyte and the metal catalyst is small. It seems that it was difficult to obtain efficiency.

  An object of the present invention is to provide a small and efficient organic hydride manufacturing apparatus in an apparatus for electrochemically manufacturing an organic hydride.

  In view of this situation, the present inventors have conducted intensive research, and as a result, a high-performance electrode can be obtained by forming a three-phase interface and a layer in which a solid polymer electrolyte and a metal catalyst network are formed in advance on the electrolyte membrane. I found out. In the present invention, the catalyst layer has a structure in which a carrier carrying a metal catalyst or a metal catalyst is in a matrix appropriately mixed with a proton-conductive solid polymer electrolyte, and these layers have a high proton-conductive solid content. It is formed on the front and back surfaces of the molecular electrolyte membrane, respectively.

The organic hydride production apparatus of the present invention includes a membrane electrode assembly in which a cathode catalyst layer for reducing a hydride and an anode catalyst layer for oxidizing water are disposed so as to sandwich a proton conductive solid polymer electrolyte membrane. A first metal for supplying a hydride to the cathode catalyst layer and a member for supplying water or water vapor to the anode catalyst layer, wherein the cathode catalyst layer reduces the hydride to generate a hydride. and a catalyst comprising a proton conductive solid polymer electrolyte, wherein the anode catalyst layer, a second metal catalyst to produce protons by oxidation of water, seen including a proton conductive solid polymer electrolyte, the the cathode catalyst layer comprises a carbon support carrying the first metal catalyst, wherein the anode catalyst layer, characterized in that it comprises a non-carbon carrier supporting the second metal catalyst

  ADVANTAGE OF THE INVENTION According to this invention, in the apparatus which manufactures an organic hydride electrochemically, a small and efficient organic hydride manufacturing apparatus can be provided.

It is a figure which shows one Example of the organic hydride manufacturing apparatus of this invention. It is a figure which shows the membrane electrode assembly (MEA) of the organic hydride manufacturing apparatus of this invention, Comprising: (a) is the top view which looked at MEA from the cathode side, (b) is the DE section in (a) Sectional drawing, (c) is an F section enlarged view in (b), and (d) is an G section enlarged view in (b). It is a figure which shows the membrane electrode assembly of the conventional organic hydride manufacturing apparatus, Comprising: (a) is the top view which looked at MEA from the cathode side, (b) is DE sectional drawing in (a), (c) is the F section enlarged view in (b). It is a graph which shows load voltage (V) and current density (mA / cm < ² >) regarding one Example of the organic hydride manufacturing apparatus of this invention. It is a graph which shows the conversion rate (%) from the load voltage (V) and toluene to methylcyclohexane regarding one Example of the organic hydride manufacturing apparatus of this invention. It is a graph which shows load voltage (V) and current density (mA / cm < ² >) regarding one Example of the organic hydride manufacturing apparatus of a prior art. It is a graph which shows the conversion rate (%) from the load voltage (V) and toluene to methylcyclohexane regarding one Example of the organic hydride manufacturing apparatus of a prior art.

  The present invention relates to an apparatus for electrochemically producing organic hydride, wherein a catalyst layer having a structure in which a proton-conducting solid polymer electrolyte and a carrier supporting a metal catalyst or a metal catalyst are mixed in a moderately mixed manner, It has the electrode structure formed in the front and back of a proton conductive solid polymer electrolyte membrane, It is characterized by the above-mentioned. In this electrode, at least one of water and water vapor is supplied to the anode side and a hydride is supplied to the cathode side, and a voltage is applied between the anode and the cathode, so that the electrolysis reaction of water at the anode. In the cathode, a hydrogenation reaction to the hydride is caused to generate an organic hydride.

  Embodiments according to the present invention will be described in detail with reference to the drawings.

  FIG. 1 shows an example of the organic hydride manufacturing apparatus of the present invention. In the organic hydride manufacturing apparatus of this embodiment, an anode catalyst layer 13 is joined to one surface of a solid polymer electrolyte membrane 12, and a cathode catalyst layer 14 is joined to the other surface, and an integrated membrane electrode assembly (MEA: Membrane). Electrode Assembly) is sandwiched between a gas diffusion layer 15 and a separator 11 in which a gas flow path is formed. A gasket 16 for gas sealing is inserted between the pair of separators 11.

The separator 11 has conductivity, and the material is preferably a dense graphite plate, a carbon plate formed by molding a carbon material such as graphite or carbon black with a resin, or a material having excellent corrosion resistance such as stainless steel or titanium. Further, it is also desirable to plate the surface of the separator 11 with a noble metal or to apply a surface treatment with a conductive paint having excellent corrosion resistance and heat resistance. On the surface of the separator 11 facing the anode catalyst layer 13 and the cathode catalyst layer 14, a groove serving as a reaction gas or liquid channel is formed. Water or water vapor is supplied to the flow channel of the anode-side separator 11. Water or water vapor flowing through the flow channel is supplied to the anode catalyst layer 13 through the gas diffusion layer 15. Further, a hydride is supplied to the cathode-side separator 11. The hydride flowing through the flow channel is supplied to the cathode catalyst layer 14 through the gas diffusion layer 15. As a method for supplying the hydride, a liquid hydride may be supplied as it is, or a vapor hydride using He gas or N ₂ gas as a carrier may be supplied.

  The gas diffusion layer 15 is provided to uniformly supply the reactant (gas or liquid) supplied to the flow path of the separator 11 into the surface of the catalyst layer, and has a breathable base such as carbon paper or carbon cloth. Is used. In particular, those obtained by subjecting these substrates to a water repellent treatment are preferable.

  The gasket 16 is insulative, and any material can be used as long as it is resistant to hydrogen, hydride, and organic hydride, and the permeation thereof is small and the confidentiality is maintained. For example, butyl rubber, viton rubber, EPDM rubber, Can be mentioned.

When a voltage is applied between the anode and the cathode while water or water vapor is supplied to the anode side and toluene is supplied as a hydride to the cathode side, an electrolysis reaction of water of formula (1) occurs at the anode. Protons generated by the electrolysis reaction of the formula (1) move to the cathode 14 through the solid polymer electrolyte membrane 12, and the hydrogen addition reaction of the formula (2) occurs at the cathode to generate methylcyclohexane as an organic hydride.
H ₂ O → 2H ⁺ + 1 / 2O ₂ + 2e ⁻ (1)
C ₇ H ₈ + 6H ⁺ + 6e ⁻ → C ₇ H ₁₄ (2)

  The organic hydride apparatus of the present embodiment is an apparatus for producing organic hydride electrochemically by the above reaction.

  FIG. 2 shows an electrode portion of the organic hydride manufacturing apparatus of the present embodiment. 2A is a plan view of the MEA 20 as viewed from the cathode side, in which the cathode catalyst layer 22 is formed on the surface of the solid polymer electrolyte membrane 21 and the anode catalyst layer 23 (see FIG. 2B) is formed on the back surface. 4B is a cross-sectional view taken along the line D-E in FIG. 4A, FIG. 4C is an enlarged view of the F part in FIG. 2B, and FIG.

In the MEA 20, as shown in the sectional view taken along the line D-E in FIG. 2B, the cathode and the anode are formed as dense catalyst layers above and below the solid polymer electrolyte membrane 21, respectively.
In the cathode catalyst layer 22, a reduction reaction of the hydride occurs. In the cathode catalyst layer 22, a metal catalyst (corresponding to the first metal catalyst in the claims) 24 in which the hydride is reduced to generate a hydride, as shown in the enlarged view of F part of FIG. And a proton-conducting solid polymer electrolyte 26. Here, the cathode catalyst layer 22 may include a carrier 25 carrying a metal catalyst 24. The carriers 25 are bonded to each other by a solid polymer electrolyte 26.
That is, the metal catalyst 24 in the cathode catalyst layer 22 has a network structure connected to each other through the carrier 25, and forms an electron path necessary for the reaction of the formula (2). Similarly, the solid polymer electrolyte 26 in the catalyst layer also has a connected network structure, and forms a passage for protons necessary for the reaction of the formula (2).

  The electrode reaction is performed at a three-phase interface where the metal catalyst 24 on the support 25 is in contact with the electrolyte and the reactant. In the electrode of this embodiment, since the passage of protons is formed by the solid polymer electrolyte 26, a three-phase interface is also formed in the metal catalyst 24 that is not in direct contact with the solid polymer electrolyte membrane 21. Therefore, it has a structure in which many metal catalysts 24 can contribute to the electrode reaction.

In the anode catalyst layer 23, an oxidation reaction of water occurs. In the anode catalyst layer 23, as shown in the enlarged view of part G of FIG. 2D, a metal catalyst 24 (corresponding to the second metal catalyst in the claims) 24 that oxidizes water to generate protons, and a proton And a conductive solid polymer electrolyte 26. The metal catalyst 24 in the anode catalyst layer 23 has a network structure connected to each other, and forms a path for electrons necessary for the reaction of the formula (1). Similarly, the solid polymer electrolyte 26 in the catalyst layer also has a connected network structure, and forms a passage for protons necessary for the reaction of the formula (1). Also in the anode, the electrode reaction is performed at the three-phase interface where the metal catalyst 24 contacts the electrolyte and the reactant.
In the electrode of this embodiment, since the passage of protons is formed by the solid polymer electrolyte 26, a three-phase interface is also formed in the metal catalyst 24 that is not in direct contact with the solid polymer electrolyte membrane 21. Therefore, it has a structure in which many metal catalysts 24 can contribute to the electrode reaction.

  Unlike the cathode catalyst layer 22, the anode catalyst layer 23 of the organic hydride production apparatus of the present embodiment is characterized by comprising only the metal catalyst 24. The reactions of the formulas (1) and (2) occur when a voltage of 1.2 V or more is applied between the anode and the cathode. When carbon is used as the carrier in the anode catalyst layer 23, the carbon may burn or the like due to an oxidation reaction when a voltage of 1.2 V or higher is applied. Therefore, the anode catalyst layer 23 of the organic hydride manufacturing apparatus of this embodiment is characterized in that no carbon is contained. Since the anode catalyst layer 23 does not need to contain carbon, the anode catalyst layer 23 may include a metal catalyst 24 and a non-carbon support (not shown in FIG. 2D) carrying the metal catalyst 24. Needless to say.

For comparison, FIG. 3 shows a membrane electrode assembly (MEA) of a conventional organic hydride manufacturing apparatus. 3A is a plan view of the MEA 30 as viewed from the cathode side, in which the cathode catalyst layer 32 is formed on the surface of the solid polymer electrolyte membrane 31 and the anode catalyst layer 33 (see FIG. 3B) is formed on the back surface. FIG. 4B is a cross-sectional view taken along the line D-E in FIG. 4A, and FIG. 4C is an enlarged view of the F part in FIG.
As shown in FIGS. 3A to 3C, the MEA 30 directly forms a catalyst carrier 35 such as carbon carrying a metal catalyst 34 on the surface of the solid polymer electrolyte membrane 31, and FIG. The solid polymer electrolyte 26 is not included like the MEA 20 used in the present invention illustrated in FIG. Therefore, the metal catalyst 34 not in direct contact with the solid polymer electrolyte membrane 31 has a structure that cannot contribute to the electrode reaction. That is, as shown in FIG. 3C, in the MEA 30 of the conventional organic hydride manufacturing apparatus, the catalyst that contributes to the electrode reaction is only the metal catalyst 34 that is in direct contact with the solid polymer electrolyte membrane 31. Therefore, the number of three-phase interfaces is small, the number of catalysts contributing to the reaction is limited, and the formation of a catalyst network structure is also small. As a result, it is difficult to obtain high energy efficiency, and the production efficiency of organic hydride is deteriorated.

  The MEA 20 (see FIG. 2) used in the present invention can be manufactured by the following method. First, a carrier 25 supporting a metal catalyst 24 such as platinum, a solid polymer electrolyte 26, and a cathode catalyst paste in which a solvent for dissolving the solid polymer electrolyte 26 is added and mixed sufficiently; a metal catalyst 24; a solid polymer electrolyte; Then, a solvent for dissolving the solid polymer electrolyte 26 is added to prepare a fully mixed anode catalyst paste. Each of these pastes is sprayed onto a release film such as a polyfluoroethylene (PTFE) film by a spray drying method, etc., dried at 80 ° C. to evaporate the solvent, and the cathode catalyst layer 22 and the anode catalyst layer 23 are formed. To do. Next, by using the cathode catalyst layer 22 and the anode catalyst layer 23, the solid polymer electrolyte membrane 21 is sandwiched from both sides so as to be centered and bonded by a hot press method, and the release film (PTFE) is peeled off, The MEA 20 used in the present invention can be manufactured. As a solvent used for preparing the cathode catalyst paste and the anode catalyst paste, a solution (221 solution) in which 1-propanol, 2-propanol and water are mixed at a mass ratio of 2: 2: 1 is preferably cited. Can do. Here, it goes without saying that the anode catalyst paste may include a non-carbon support carrying the metal catalyst 24 instead of the metal catalyst 24.

  Further, as another example for producing the MEA 20 used in the present invention, the carrier 25 supporting the metal catalyst 24 such as platinum, the solid polymer electrolyte 26, and a solvent for dissolving the solid polymer electrolyte 26 are sufficiently added. The mixed cathode catalyst paste, the metal catalyst 24, the solid polymer electrolyte 26, and the anode catalyst paste sufficiently mixed by adding a solvent for dissolving the solid polymer electrolyte 26 are directly solid polymer electrolyte membranes by a spray drying method or the like. It can also be produced by spraying on 21. In addition, it cannot be overemphasized that the anode catalyst paste may contain the non-carbon support | carrier which carry | supported the metal catalyst 24 instead of the metal catalyst 24. FIG.

  Examples of the organic polymer constituting the solid polymer electrolyte membrane 21 include perfluorocarbon sulfonic acid, polystyrene, polyether ketone, polyether ether ketone, polysulfone, polyether sulfone, other engineering plastic materials, sulfonic acid groups, A proton donor such as a phosphonic acid group or a carboxyl group that is immobilized by doping or chemically bonding can be used. In addition, it is also desirable to improve the material stability by forming a crosslinked structure or partially fluorinating the material.

  For the solid polymer electrolyte 26 contained in the catalyst layer, a polymer material exhibiting proton conductivity is used. For example, sulfonated or alkylenesulfonated typified by perfluorocarbon-based sulfonic acid resin or polyperfluorostyrene-based sulfonic acid resin. Fluorinated polymers and polystyrenes. Other examples include polysulfones, polyether sulfones, polyether ether sulfones, polyether ether ketones, and materials obtained by introducing a proton donor such as a sulfonic acid group into a hydrocarbon polymer. Moreover, the above-mentioned composite electrolyte of organic polymer and metal oxide hydrate can also be used. The solid polymer electrolyte 26 can also be obtained by dissolving a part of the solid polymer electrolyte membrane 21 using a solvent that can dissolve the solid polymer electrolyte membrane 21.

As the metal catalyst 24 used in the present invention, a catalyst material having a hydrogen addition action can be used. For example, metals such as Ni, Pd, Pt, Rh, Ir, Re, Ru, Mo, W, V, Os, Cr, Co, and Fe, and alloy catalysts thereof can be used. The hydrogenation catalyst is preferably finely divided in order to reduce the cost by reducing the metal catalyst 24 and increase the reaction surface area. Further, in order to prevent a decrease in specific surface area due to aggregation of fine particles, it may be supported on a carrier described later. The method for producing the catalyst is not particularly limited, such as a coprecipitation method, a thermal decomposition method, and an electroless plating method.
As the carrier 25 contained in the cathode catalyst layer 22 and supporting the metal catalyst 24, carbon materials such as activated carbon, carbon nanotubes, and graphite, and alumina silicate such as silica, alumina, and zeolite can be used.
As described above, a non-carbon support (not shown) is used as the support that is contained in the anode catalyst layer 23 and can support the metal catalyst 24. As the non-carbon support, alumina silicate such as silica, alumina and zeolite can be used. The anode catalyst layer 23 may use only the metal catalyst 24 without using a non-carbon carrier.

  As the hydride, benzene, toluene, xylene, mesitylene, naphthalene, methylnaphthalene, anthracene, biphenyl, phenanthroline, and alkyl substitution products thereof or a mixture thereof can be used. Hydrogen can be stored by adding hydrogen to the double bond between these carbon atoms.

  Hereinafter, the present invention will be described in detail with reference to examples. In addition, this invention is not limited to the following Example.

  Nafion (registered trademark) manufactured by DuPont was used as the electrolyte membrane.

  The cathode catalyst layer was formed by directly applying a catalyst paste to Nafion using a spray coater. The cathode catalyst layer was applied to Nafion in the following order.

  Nafion was placed on the hot plate of the substrate and fixed by suction. Here, the temperature of the hot plate was 50 ° C.

Next, a mask was applied from above, and the cathode catalyst paste was applied with a spray coater (manufactured by Nordson). As cathode catalyst paste, platinum-supported carbon catalyst TEC10E70TPM (manufactured by Tanaka Kikinzoku) and water, 5% by mass Nafion solution, 221 solution (1-propanol: 2-propanol: water = 2: 2: 1 solution) is 2: 1. What was mixed by the mass ratio of 2: 5.4: 10.6 was used. The application conditions were a liquid pressure of 0.01 MPa, a swirl pressure of 0.15 MPa, an atomization pressure of 0.15 MPa, a gun / substrate distance of 60 mm, and a substrate temperature of 50 ° C. The amount of the metal catalyst in the cathode catalyst layer was 0.4 mg · cm ^{−2 in} terms of the amount of Pt per unit area.

After the cathode catalyst layer was formed on the Nafion surface, an anode catalyst layer was formed on the back surface. The anode catalyst layer was formed by a transfer method. First, an anode catalyst paste was prepared. As an anode catalyst paste, a mixture of platinum black HiSPEC1000 (manufactured by Johnson Matthey), 5% by mass Nafion solution and 221 solution at a mass ratio of 1: 1.11: 2.22 was used. It was apply | coated on the Teflon (trademark) sheet | seat with the applicator. An anode catalyst layer coated on a Teflon (registered trademark) sheet was formed on the surface of Nafion by thermal transfer using a hot press (SA-401-M manufactured by Tester Sangyo Co., Ltd.). The hot press pressure was 3.65 MPa (37.2 kgf · cm ⁻² ), the hot press temperature was 120 ° C., and the hot press time was 2 minutes. The amount of the metal catalyst in the anode catalyst layer was 4.8 mg · cm ^{−2 in} terms of the amount of Pt per unit area.

  The produced MEA was incorporated into the organic hydride manufacturing apparatus of FIG. The cell resistance was 200 mΩ.

  A voltage was applied between the anode and the cathode in a state where toluene to be hydride was supplied to the cathode at 10 ml / min and pure water was supplied to the anode at 5 ml / min. The cell temperature was 40 ° C. FIG. 4 shows the current value with respect to the load voltage. When a load of 1.6 V or higher was applied, current flowed and the reaction proceeded. As the voltage was increased to 2.2 V, the current increased and the reaction proceeded. When the cathode exhaust gas was analyzed by gas chromatography, toluene and methylcyclohexane were detected. Therefore, it was suggested that methylcyclohexane was produced by the hydrogenation reaction of toluene. FIG. 5 shows the conversion rate (%) from toluene to methylcyclohexane calculated from the peak intensity of gas chromatography. The higher the voltage, the higher the conversion rate, and the maximum value under this condition was 60% when a load of 2.2 V was applied.

[Comparative Example 1]
Nafion was used for the electrolyte membrane, and the metal catalyst was deposited directly on the membrane surface by a deposition method.

  The produced MEA was incorporated into the organic hydride production apparatus of FIG. 1, and a hydrogen addition reaction test on toluene was performed under the same conditions as in Example 1. The cell resistance was 950 mΩ. The reason why the cell resistance is larger than in Example 1 is that a network between the catalysts is not formed. FIG. 6 shows the current value with respect to the load voltage. The current value was smaller than that in Example 1. This may be because the resistance is large or the formation of the three-phase interface is small. FIG. 7 shows the conversion (%) from toluene to methylcyclohexane. The maximum value under this condition was 12% when a load of 2.2 V was applied.

[Comparative Example 2]
A cathode catalyst layer was formed under the same conditions and in the same manner as in Example 1. In Comparative Example 2, a platinum-supported carbon catalyst was used for the anode catalyst layer as well as the cathode catalyst layer. The production conditions for the anode catalyst paste were the same as the production conditions for the cathode catalyst paste of Example 1.

  The produced MEA was incorporated into the organic hydride production apparatus of FIG. 1, and a hydrogen addition reaction test on toluene was performed under the same conditions as in Example 1. The cell resistance was 180 mΩ. When a voltage was applied between the anode and the cathode, the drainage from the anode became black and cloudy at 1.8 V or higher. This is presumably because the carbon used as the support for the anode catalyst layer was oxidized. It was found that the reaction of the formula (1) does not occur in the anode of Comparative Example 2.

11 Separator 12, 21, 31 Solid polymer electrolyte membrane 13, 23, 33 Anode catalyst layer 14, 22, 32 Cathode catalyst layer 15 Gas diffusion layer 16 Gasket 20, 30 MEA (membrane electrode assembly)
24 metal catalyst 25 carrier 26 solid polymer electrolyte 35 catalyst carrier

Claims (7)

An organic hydride production apparatus for producing organic hydride,
A membrane electrode assembly in which a cathode catalyst layer for reducing hydride and an anode catalyst layer for oxidizing water sandwich a proton-conducting solid polymer electrolyte membrane, and a hydride on the cathode catalyst layer A member to supply, and a member to supply water or water vapor to the anode catalyst layer,
The cathode catalyst layer includes a first metal catalyst that reduces a hydride to generate a hydride, and a proton-conducting solid polymer electrolyte;
The anode catalyst layer, viewed contains a second metal catalyst to produce protons by oxidation of water, and a proton conductive solid polymer electrolyte, a,
The cathode catalyst layer includes a carbon support carrying the first metal catalyst;
The organic hydride manufacturing apparatus , wherein the anode catalyst layer includes a non-carbon carrier supporting the second metal catalyst . Oite to claim 1,
The hydride is one of benzene, toluene, xylene, mesitylene, naphthalene, methylnaphthalene, anthracene, biphenyl, phenanthroline, and alkyl-substituted products thereof, or a mixture thereof. apparatus. Oite to claim 1,
The first metal catalyst is any metal selected from nickel, palladium, platinum, rhodium, iridium, rhenium, ruthenium, molybdenum, tungsten, vanadium, osmium, chromium, cobalt and iron, or at least a part thereof. Made of an alloy containing
The second metal catalyst is any metal selected from nickel, palladium, platinum, rhodium, iridium, rhenium, ruthenium, molybdenum, tungsten, vanadium, osmium, chromium, cobalt and iron, or at least a part thereof. An organic hydride manufacturing apparatus comprising an alloy containing A membrane electrode assembly in which a cathode catalyst layer for reducing a hydride and an anode catalyst layer for oxidizing water are disposed so as to sandwich a proton conductive solid polymer electrolyte membrane, and the cathode catalyst layer and the anode catalyst layer And a gas diffusion layer disposed on the surface of the gas diffusion layer and a separator disposed on the surface of the gas diffusion layer and having a channel groove formed on a surface in contact with the gas diffusion layer. A hydride manufacturing device,
The cathode catalyst layer includes a first metal catalyst that reduces a hydride to generate a hydride, and a proton-conducting solid polymer electrolyte;
The anode catalyst layer, viewed contains a second metal catalyst to produce protons by oxidation of water, and a proton conductive solid polymer electrolyte, a,
The cathode catalyst layer includes a carbon support carrying the first metal catalyst;
The organic hydride manufacturing apparatus , wherein the anode catalyst layer includes a non-carbon carrier supporting the second metal catalyst . Oite to claim 4,
The hydride is supplied to the channel groove of the separator on the cathode catalyst layer side,
An organic hydride manufacturing apparatus, wherein at least one of water and water vapor is supplied to a flow path groove of the separator on the anode catalyst layer side. Oite to claim 4,
The hydride is one of benzene, toluene, xylene, mesitylene, naphthalene, methylnaphthalene, anthracene, biphenyl, phenanthroline, and alkyl-substituted products thereof, or a mixture thereof. apparatus. Oite to claim 4,
The first metal catalyst is any metal selected from nickel, palladium, platinum, rhodium, iridium, rhenium, ruthenium, molybdenum, tungsten, vanadium, osmium, chromium, cobalt and iron, or at least a part thereof. Made of an alloy containing
The second metal catalyst is any metal selected from nickel, palladium, platinum, rhodium, iridium, rhenium, ruthenium, molybdenum, tungsten, vanadium, osmium, chromium, cobalt and iron, or at least a part thereof. An organic hydride manufacturing apparatus comprising an alloy containing

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