Electrolysis equipment

Abstract

To suppress decrease in electrolytic efficiency.SOLUTION: An electrolytic apparatus comprises: a humidifier that humidifies cathode gas; a cathode discharge flow passage through which cathode fluid containing the cathode gas and a reduction product flows as it exits the cathode flow passage; an anode collector that separates anode fluid supplied from the anode discharge flow passage into an anode effluent containing an anode solution and an anode exhaust containing an oxidation product; a first chiller that cools the anode exhaust supplied from the anode collector and condenses the water vapor contained in the anode exhaust to produce anode condensed water; a first flow channel that connects the anode collector to the anode supply passage, and through which the anode solution flows from the anode collector to the anode supply passage; a second flow channel through which the anode condensed water flows from a condensed water collector to the humidifier; and a first heat exchange structure that conducts heat exchange between the anode solution flowing in the first flow channel and the anode condensed water flowing in the second flow channel.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] SUMMARY OF THE INVENTION An embodiment of the present invention relates to an electrolysis device. [Background technology]

[0002] In recent years, concerns have arisen about the depletion of fossil fuels such as oil and coal, and expectations are growing for sustainable renewable energy sources. Examples of renewable energy sources include solar cells and wind power generation. However, these have the challenge of making it difficult to provide a stable supply of electricity because the amount of power they generate depends on weather and natural conditions. For this reason, attempts have been made to stabilize the power supply by storing the electricity generated by renewable energy sources in storage batteries. However, storing electricity comes with problems such as the cost of storage batteries and the occurrence of losses during storage.

[0003] In response to these issues, electrolysis devices are attracting attention. These devices use electricity generated from renewable energy to electrolyze water (H2O) to produce hydrogen (H2) from water, or electrochemically reduce carbon dioxide (CO2) to convert it into chemical substances (chemical energy) such as carbon compounds like carbon monoxide (CO), formic acid (HCOOH), methanol (CH3OH), methane (CH4), acetic acid (CH3COOH), ethanol (C2H5OH), ethane (C2H6), and ethylene (C2H4). Storing these chemical substances in cylinders or tanks has the advantage of lowering energy storage costs and minimizing storage losses compared to storing electricity (electrical energy) in batteries.

[0004] An example of an electrolysis device is one that includes a cathode flow path facing the cathode, an anode flow path facing the anode, and a separator disposed between the cathode flow path and the anode flow path. When an electrolysis device having such a configuration is used to carry out an electrolysis reaction over a long period of time, for example, by passing a constant current between the cathode and the anode, there is a problem that degradation of cell performance over time occurs, such as a decrease in the amount of product or an increase in cell voltage. Therefore, there is a demand for an electrolysis device that can suppress degradation of cell performance over time. [Prior art documents] [Non-patent literature]

[0005] [Non-Patent Document 1] Zengcal Liu et al., Journal of CO2 Utilization, 15, p.50-56(2015) [Non-patent document 2] Sinchao Ma et al., Journal of The Electrochemical Society, 161(10), F1124-F1131(2014) Summary of the Invention [Problem to be solved by the invention]

[0006] The problem to be solved by the present invention is to suppress the decrease in electrolysis efficiency. [Means for solving the problem]

[0007] The electrolysis device includes an anode that oxidizes a first substance to generate an oxidation product, a cathode that reduces a second substance to generate a reduction product, an anode flow path facing the anode, a cathode flow path facing the cathode, an anode supply flow path connected to the inlet of the anode flow path and supplying an anode solution containing the first substance to the anode flow path, an anode discharge flow path through which an anode fluid that is discharged from the outlet of the anode flow path and contains the anode solution and the oxidation product flows, a cathode gas supply source that supplies a cathode gas that contains the second substance, a humidifier that humidifies the cathode gas, a cathode supply flow path connected to the inlet of the cathode flow path and supplying the humidified cathode gas to the cathode flow path, and a cathode gas that is discharged from the outlet of the cathode flow path and contains the cathode gas and the reduction product. anode discharge flow path through which anode fluid flows; an anode collector that separates the anode fluid supplied from the anode discharge flow path into an anode effluent containing an anode solution and an anode exhaust containing oxidation products; a first cooler that cools the anode exhaust supplied from the anode collector and condenses water vapor contained in the anode exhaust to produce anode condensed water; a condensed water collector that stores the anode condensed water; a first flow path that connects the anode collector to the anode supply flow path and through which the anode solution flows from the anode collector to the anode supply flow path; a second flow path that connects the condensed water collector to the humidifier and through which the anode condensed water flows from the condensed water collector to the humidifier; and a first heat exchange structure that exchanges heat between the anode solution flowing in the first flow path and the anode condensed water flowing in the second flow path. [Brief explanation of the drawings]

[0008] [Figure 1] FIG. 1 is a schematic diagram illustrating a configuration example of an electrolysis device according to a first embodiment. [Figure 2] 10 is a schematic diagram for explaining another structural example of the electrolysis unit 100. FIG. [Figure 3] 10 is a schematic diagram for explaining another structural example of the electrolysis unit 100. FIG. [Figure 4] 2 is a schematic diagram showing an example of the planar structure of a flow channel plate 114 having an anode flow channel 112. FIG. [Figure 5]1 is a schematic diagram showing an example of the planar structure of a flow path plate having a cooling flow path 141. FIG. [Figure 6] 10 is a schematic diagram showing another example of the planar structure of a flow path plate 153 having a cooling flow path 141. FIG. [Figure 7] 10 is a schematic diagram showing another example of the planar structure of a flow path plate 153 having a cooling flow path 141. FIG. [Figure 8] FIG. 4 is a schematic diagram for explaining a configuration example of an electrolysis device according to a second embodiment. [Figure 9] FIG. 10 is a schematic diagram for explaining a configuration example of an electrolysis device according to a third embodiment. [Figure 10] FIG. 10 is a schematic diagram for explaining a configuration example of an electrolysis device according to a fourth embodiment. [Figure 11] FIG. 10 is a schematic diagram for explaining a configuration example of an electrolysis device according to a fifth embodiment. [Figure 12] FIG. 10 is a schematic diagram for explaining a configuration example of an electrolysis device according to a sixth embodiment. [Figure 13] FIG. 12 is a schematic diagram for explaining a configuration example of an electrolysis device according to a seventh embodiment. [Figure 14] FIG. 13 is a schematic diagram for explaining a configuration example of an electrolysis device according to an eighth embodiment. DETAILED DESCRIPTION OF THE INVENTION

[0009] Hereinafter, electrolysis devices according to embodiments will be described with reference to the drawings. In each of the following embodiments, substantially identical components are denoted by the same reference numerals, and some of their descriptions may be omitted. The drawings are schematic, and the relationship between thickness and planar dimensions, the thickness ratio of each component, etc. may differ from the actual ones.

[0010] In this specification, unless otherwise specified, "connect" may include not only direct connection but also indirect connection.

[0011] (First embodiment) 1 is a schematic diagram illustrating an example of the configuration of the electrolysis device of the first embodiment. The electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700.

[0012] The electrolysis unit 100 includes an anode 111, an anode flow channel 112, an anode current collector 113, a cathode 121, a cathode flow channel 122, a cathode current collector 123, a separator 131, a cooling flow channel 141, a power supply 150, and a detector 151. The anode 111, the anode flow channel 112, the cathode 121, the cathode flow channel 122, and the separator 131 constitute an electrolysis cell. Examples of electrolysis cells include a carbon dioxide electrolysis cell and a nitrogen electrolysis cell.

[0013] The anode supply unit 200 includes an anode collector 201 , a flow rate controller 202 , a flow rate controller 205 , a heat exchanger 206 , and a flow rate controller 207 .

[0014] The cathode supply unit 300 includes a cathode gas supply source 301 , a humidifier 302 , a water supply source 303 , a flow rate controller 304 , and a pressure controller 305 .

[0015] The cathode exhaust section 400 includes a cathode collector 401 and a valve 402 .

[0016] The cooling unit 500 includes a cooler 501 and a condensed water collector 502 .

[0017] The circulation unit 600 includes a heat exchanger 601 and a flow rate controller 602 .

[0018] The control unit 700 includes a control device 701 .

[0019] Fig. 2 is a schematic diagram illustrating another structural example of the electrolysis unit 100. Fig. 3 is a schematic diagram illustrating another structural example of the electrolysis unit 100. As shown in Figs. 2 and 3, the electrolysis unit 100 may also include multiple electrolysis cells. The multiple electrolysis cells may be sandwiched between a pair of support plates (not shown) and further fastened with bolts or the like, for example.

[0020] The anode 111 is in contact with the separator 131. The anode 111 is an electrode for oxidizing a substance to be oxidized to generate an oxidation product. The anode 111 oxidizes, for example, water, which is a substance to be oxidized, to generate oxygen (O) and hydrogen ions (H + ) or hydroxide ions (OH - ) to produce oxygen and water.

[0021] The anode 111 preferably contains a catalytic material (anode catalytic material) capable of reducing the overvoltage of the oxidation reaction. Examples of such catalytic materials include metals such as platinum (Pt), palladium (Pd), and nickel (Ni), alloys and intermetallic compounds containing these metals, binary metal oxides such as manganese oxide (Mn-O), iridium oxide (Ir-O), nickel oxide (Ni-O), cobalt oxide (Co-O), iron oxide (Fe-O), tin oxide (Sn-O), indium oxide (In-O), ruthenium oxide (Ru-O), lithium oxide (Li-O), and lanthanum oxide (La-O), ternary metal oxides such as Ni-Co-O, Ni-Fe-O, La-Co-O, Ni-La-O, and Sr-Fe-O, quaternary metal oxides such as Pb-Ru-Ir-O and La-Sr-Co-O, and metal complexes such as Ru complexes and Fe complexes.

[0022] The anode 111 includes a substrate having a porous structure, such as a mesh material, punched material, porous material, or sintered metal fiber material, that allows for the transfer of liquid or ions between the separator 131 and the anode flow path 112. The substrate may be made of a metal material such as titanium (Ti), nickel (Ni), or iron (Fe), or an alloy containing at least one of these metals (e.g., SUS), or may be made of the above-mentioned anode catalyst material. When an oxide is used as the anode catalyst material, it is preferable to form a catalyst layer by adhering or laminating the anode catalyst material to the surface of a substrate made of the above-mentioned metal material. The anode catalyst material preferably contains nanoparticles, nanostructures, nanowires, or the like to enhance the oxidation reaction. A nanostructure is a structure in which nanoscale irregularities are formed on the surface of a catalyst material.

[0023] The cathode 121 is in contact with the separator 131. The cathode 121 is an electrode (reduction electrode) for causing a reduction reaction of a substance to be reduced and generating a reduction product. Examples of the substance to be reduced include carbon dioxide and nitrogen. Examples of the reduction product include carbon compounds and ammonia. Examples of carbon compounds include carbon monoxide, formic acid (HCOOH), ethane, ethylene, methanol, acetic acid (CHCOOH), ethanol, propanol (CHOH), and ethylene glycol (CHO). The reduction reaction at the cathode 121 may include a side reaction of causing a reduction reaction of water to generate hydrogen (H) in addition to the reduction reaction of the substance to be reduced.

[0024] The cathode 121 has a gas diffusion layer and a cathode catalyst layer provided on the gas diffusion layer. A porous layer denser than the gas diffusion layer may be disposed between the gas diffusion layer and the cathode catalyst layer. The gas diffusion layer is disposed on the cathode flow channel 122 side, and the cathode catalyst layer is disposed on the separator 131 side. The cathode catalyst layer may be embedded in the gas diffusion layer. The cathode catalyst layer preferably contains catalyst nanoparticles or catalyst nanostructures. The gas diffusion layer is made of, for example, carbon paper or carbon cloth, and may be treated to be water-repellent. The porous layer is made of a porous material with a smaller pore size than the carbon paper or carbon cloth.

[0025] By applying an appropriate water-repellent treatment to the gas diffusion layer, the gas of the substance to be reduced reaches the cathode catalyst layer mainly by gas diffusion. The reduction reaction of the substance to be reduced and the reduction reaction of the resulting carbon compound occur near the boundary between the gas diffusion layer and the cathode catalyst layer, or near the cathode catalyst layer that has penetrated into the gas diffusion layer.

[0026] The cathode catalyst layer is preferably made of a catalyst material (cathode catalyst material) capable of reducing the overvoltage of the reduction reaction when reducing carbon dioxide. Examples of such materials include metals such as gold (Au), silver (Ag), copper (Cu), platinum (Pt), palladium (Pd), nickel (Ni), cobalt (Co), iron (Fe), manganese (Mn), titanium (Ti), cadmium (Cd), zinc (Zn), indium (In), gallium (Ga), lead (Pb), and tin (Sn), metal materials such as alloys and intermetallic compounds containing at least one of these metals, carbon materials such as carbon (C), graphene, carbon nanotubes (CNTs), fullerenes, and ketjen black, and metal complexes such as Ru complexes and Re complexes. The cathode catalyst layer can be in various shapes, such as a plate, mesh, wire, particle, porous, thin film, or island shape.

[0027] The cathode catalyst layer may be made of a cathode catalyst material capable of reducing nitrogen to produce ammonia. Such a material may include molybdenum complexes. Examples of such materials include the molybdenum complexes (A) to (D) shown below.

[0028] A first example is a molybdenum complex having, as a PCP ligand (A), N,N-bis(dialkylphosphinomethyl)dihydrobenzimidazolidene (wherein the two alkyl groups may be the same or different, and at least one hydrogen atom on the benzene ring may be substituted with an alkyl group, an alkoxy group, or a halogen atom). A second example is a molybdenum complex having, as a PNP ligand (B), 2,6-bis(dialkylphosphinomethyl)pyridine (wherein the two alkyl groups may be the same or different, and at least one hydrogen atom on the pyridine ring may be substituted with an alkyl group, an alkoxy group, or a halogen atom). A third example is a molybdenum complex having, as the (C)PPP ligand, a bisbis(dialkylphosphinomethyl)arylphosphine (where the two alkyl groups may be the same or different). A fourth example is a molybdenum complex represented by (D) trans-Mo(N2)2(R1R2R3P)4 (where R1, R2, and R3 may be the same or different and are alkyl or aryl groups, and two R3s may be bonded to each other to form an alkylene chain).

[0029] In the molybdenum complexes described above, the alkyl group may be, for example, a linear or branched alkyl group such as a methyl group, an ethyl group, a propyl group, a butyl group, a pentyl group, a hexyl group, or a structural isomer thereof, or a cyclic alkyl group such as a cyclopropyl group, a cyclobutyl group, a cyclopentyl group, or a cyclohexyl group. The alkyl group preferably has 1 to 12 carbon atoms, more preferably 1 to 6 carbon atoms. The alkoxy group may be, for example, a linear or branched alkoxy group such as a methoxy group, an ethoxy group, a propoxy group, a butoxy group, a pentoxy group, a hexyloxy group, or a structural isomer thereof, or a cyclic alkoxy group such as a cyclopropoxy group, a cyclobutoxy group, a cyclopentoxy group, or a cyclohexyloxy group. The alkoxy group preferably has 1 to 12 carbon atoms, more preferably 1 to 6 carbon atoms. Examples of halogen atoms include a fluorine atom, a chlorine atom, a bromine atom, and an iodine atom.

[0030] The molybdenum complex (A) may be, for example, a molybdenum complex represented by the following formula (A1).

[0031] [ka] (wherein R1 and R2 are alkyl groups which may be the same or different, X is an iodine atom, a bromine atom, or a chlorine atom, and at least one hydrogen atom on the benzene ring may be substituted with an alkyl group, an alkoxy group, or a halogen atom)

[0032] Examples of the alkyl group, alkoxy group, and halogen atom include those already exemplified. R1 and R2 are preferably bulky alkyl groups (e.g., tert-butyl or isopropyl). It is preferred that the hydrogen atoms on the benzene ring are unsubstituted or that the hydrogen atoms at the 5th and 6th positions are substituted with linear, cyclic, or branched alkyl groups having 1 to 12 carbon atoms.

[0033] Examples of the molybdenum complex (B) include molybdenum complexes represented by the following formulae (B1), (B2) and (B3).

[0034] [ka] (wherein R1 and R2 are alkyl groups which may be the same or different, X is an iodine atom, a bromine atom, or a chlorine atom, and at least one hydrogen atom on the pyridine ring may be substituted with an alkyl group, an alkoxy group, or a halogen atom)

[0035] Examples of the alkyl group, alkoxy group, and halogen atom include those already exemplified. R1 and R2 are preferably bulky alkyl groups (e.g., tert-butyl or isopropyl). The hydrogen atom on the pyridine ring is preferably unsubstituted, or the hydrogen atom at position 4 is preferably substituted with a linear, cyclic, or branched alkyl group having 1 to 12 carbon atoms.

[0036] The molybdenum complex (C) may be, for example, a molybdenum complex represented by the following formula (C1).

[0037] [ka] (wherein R1 and R2 are alkyl groups which may be the same or different, R3 is an aryl group, and X is an iodine atom, a bromine atom, or a chlorine atom)

[0038] Examples of the alkyl group include the same groups as those already exemplified. Examples of the aryl group include a phenyl group, a tolyl group, a xylyl group, a naphthyl group, and groups in which at least one of the cyclic hydrogen atoms is substituted with an alkyl group or a halogen atom. Examples of the alkyl group and the halogen atom include the same groups as those already exemplified. R1 and R2 are preferably bulky alkyl groups (e.g., tert-butyl group or isopropyl group). R3 is preferably, for example, a phenyl group.

[0039] Examples of the molybdenum complex (D) include molybdenum complexes represented by the following formulae (D1) and (D2).

[0040] [ka] (wherein R1, R2, and R3 are alkyl or aryl groups which may be the same or different, and n is 2 or 3).

[0041] Examples of the alkyl group and aryl group include those already exemplified. In formula (D1), it is preferred that R1 and R2 are aryl groups (e.g., phenyl groups) and R3 is an alkyl group having 1 to 4 carbon atoms (e.g., methyl group), or that R1 and R2 are alkyl groups having 1 to 4 carbon atoms (e.g., methyl group) and R3 is an aryl group (e.g., phenyl group). In formula (D2), it is preferred that R1 and R2 are aryl groups (e.g., phenyl groups) and n is 2.

[0042] The cathode catalyst material constituting the cathode catalyst layer preferably comprises nanoparticles of the above-mentioned metal material, nanostructures of the metal material, nanowires of the metal material, or a composite in which nanoparticles of the above-mentioned metal material are supported on a carbon material such as carbon particles, carbon nanotubes, graphene, etc. By using catalyst nanoparticles, catalyst nanostructures, catalyst nanowires, catalyst nanosupport structures, etc. as the cathode catalyst material, the reaction efficiency of the reduction reaction of the target substance to be reduced in the cathode 121 can be increased.

[0043] The anode flow channel 112 faces the anode 111. The anode flow channel 112 has a function of supplying the anode 111 with the substance to be oxidized by allowing an anode solution containing the substance to be oxidized to flow therethrough.

[0044] The anode solution is preferably a solution containing at least water (HO) of the substance to be oxidized. The substance to be reduced is supplied from the cathode flow channel 122, so the anode solution may or may not contain the substance to be reduced.

[0045] The anode solution may be an electrolytic solution containing an electrolyte, such as hydroxide ions (OH - ), hydrogen ions (H + ), potassium ions (K + ), sodium ions (Na + ), lithium ion (Li + ), chloride ions (Cl - ), bromide ion (Br - ), iodide ion (I - ), nitrate ions (NO3 - ), sulfate ions (SO4 2- ), phosphate ions (PO4 2- ), borate ion (BO3 3- ), and bicarbonate ions (HCO3 -) is an aqueous solution containing at least one selected from the group consisting of: a) anode solution (anode solution containing at least one of the following electrolytes): ...

[0046] The anode flow path 112 is provided on the surface of a flow path plate 114. The material of the flow path plate 114 includes, for example, a material that has low chemical reactivity and no electrical conductivity. Examples of such materials include insulating resin materials such as acrylic resin, polyether ether ketone (PEEK), and fluororesin. The flow path plate 114 has screw holes for fastening (not shown).

[0047] The cathode flow channel 122 faces the cathode 121. The cathode flow channel 122 has a function of supplying the cathode 121 with the substance to be reduced by allowing a cathode gas containing the substance to be reduced to flow therethrough.

[0048] The cathode flow path 122 is provided on the surface of a flow path plate 124. The flow path plate 124 is preferably made of a material that has low chemical reactivity and high conductivity. Examples of such materials include metal materials such as Ti and SUS, and carbon. The flow path plate 124 has an inlet and outlet for the cathode flow path 122, not shown, as well as screw holes for fastening. Furthermore, packing not shown is inserted in front of and behind each flow path plate as needed.

[0049] The separator 131 includes an ion exchange membrane that allows ions to move between the anode 111 and the cathode 121 and that can separate the anode 111 and the cathode 121. Examples of ion exchange membranes include cation exchange membranes such as Nafion and Flemion, and anion exchange membranes such as Neosepta and Selemion. In addition to ion exchange membranes, any material that allows ions to move between the anode 111 and the cathode 121, such as a glass filter, a porous polymer membrane, or a porous insulating material, may be used for the separator 131.

[0050] The anode 111 and the cathode 121 can be connected to a power source 150. Examples of the power source 150 are not limited to a normal power grid or a battery, and may include a power source that supplies power generated by renewable energy such as solar cells or wind power. The power source 150 may further include a power controller that adjusts the output of the power source to control the voltage between the anode 111 and the cathode 121. The power source 150 may be provided outside the electrolysis device 1.

[0051] The detector 151 has at least one of a thermometer for measuring the temperature of the electrolysis cell, and an ammeter or voltmeter having a reference electrode for measuring the voltage difference between the anode 111 and the cathode 121 (cell voltage) or the current (cell current). The detector 151 is not necessarily provided.

[0052] The inlet of the anode flow channel 112 is connected to the anode supply flow channel P1. The outlet of the anode flow channel 112 is connected to the anode discharge flow channel P2. The anode supply flow channel P1 and the anode discharge flow channel P2 are formed of, for example, piping.

[0053] An inlet of the cathode flow channel 122 is connected to a cathode supply flow channel P3. An outlet of the cathode flow channel 122 is connected to a cathode discharge flow channel P4. The cathode supply flow channel P3 and the cathode discharge flow channel P4 are formed of, for example, piping.

[0054] 2, the anode flow channel 112 and the cathode flow channel 122 can be provided on both sides of a flow channel plate 132. A flow channel plate having flow channels on both sides is also called a bipolar flow channel plate.

[0055] FIG. 4 is a schematic diagram showing an example of the planar structure of a flow path plate 114 having an anode flow path 112. The anode flow path 112 has an inlet IN and an outlet OUT provided in the flow path plate 114. The anode flow path 112 has a serpentine shape on the surface of the flow path plate 114, and the regions between the turning portions are branched. This shape allows the liquid to be efficiently supplied to the anode flow path 112. Note that, like the anode flow path 112, the cathode flow path 122 may also have a serpentine shape as shown in FIG. 4.

[0056] Cooling water for cooling the electrolysis cell flows through the cooling flow path 141. The cooling flow path 141 is disposed, for example, opposite the anode flow path 112 or the cathode flow path 122. For example, the cooling flow path 141 may be provided on the opposite side of the anode 111 with respect to the anode flow path 112. Alternatively, the cooling flow path 141 may be provided on the opposite side of the cathode 121 with respect to the cathode flow path 122. The cooling flow path 141 may be connected in parallel to a cooling water supply source (not shown), for example, so that the cooling water may be circulated while being cooled by the cooling water supply source. The cooling flow path 141 is not necessarily provided.

[0057] 5 is a schematic diagram showing an example of the planar structure of a flow path plate having a cooling flow path 141. The cooling flow path 141 has an inlet (IN) and an outlet (OUT) provided in a flow path plate 153. The inlet (IN) of the cooling flow path 141 is closer to the outlet (OUT) of the anode flow path 112 than the inlet (IN) of the anode flow path 112, and the outlet (OUT) of the cooling flow path 141 is closer to the inlet (IN) of the anode flow path 112 than the outlet (OUT) of the anode flow path 112. This allows, for example, the flow of anode fluid in the anode flow path 112 and the flow of cooling fluid in the cooling flow path 141 to be reversed. During electrolysis, the anode solution is supplied from the inlet (IN) of the anode flow path 112 to the inside of the electrolysis cell, the temperature rises inside the electrolysis cell, and the temperature rises at the outlet (OUT) of the anode flow path 112, where the anode fluid is discharged from the electrolysis cell. Therefore, even inside the electrolysis cell, the temperature is low near the inlet and high near the outlet. In response to this, by providing the inlet IN of the cooling flow passage 141 on the outlet OUT side of the anode flow passage 112, the temperature uniformity of the electrolysis cell can be improved.

[0058] The cooling channels 141 have a serpentine shape on the surface of the channel plate 153. This shape allows a liquid containing water to be efficiently supplied to the cooling channels 141. Note that the channel width of the cooling channels 141 can be made wider than the channel width of the anode channel 112 to increase cooling efficiency.

[0059] 6 is a schematic diagram showing another example of the planar structure of a channel plate 153 having a cooling channel 141. The cooling channel 141 shown in FIG. 6 differs from the cooling channel 141 shown in FIG. 5 in that the cooling channel 141 has different channel widths between the central and peripheral portions of the cooling channel 141. The channel width of the central portion of the cooling channel 141 is preferably wider than the channel width of the peripheral portion of the cooling channel 141. This can improve cooling efficiency. The central portion of the electrolysis cell dissipates less heat and is therefore more likely to become hot, while the peripheral portion of the electrolysis cell is more likely to become colder.

[0060] 7 is a schematic diagram showing another example of the planar structure of a channel plate 153 having a cooling channel 141. The cooling channel 141 shown in FIG. 7 differs from the cooling channel 141 shown in FIG. 5 in that the cooling channel 141 is provided in the center of the surface of the channel plate 153, and the cooling channel 141 is not provided in the outer periphery surrounding the center. Furthermore, the channel width of the central portion of the cooling channel 141 is preferably wider than the channel width of the peripheral portion of the cooling channel 141. This can reduce the in-plane temperature distribution of the electrolysis cell.

[0061] The electrolysis unit 100 may include multiple cooling channels. The electrolysis unit 100 shown in Fig. 2 includes a cooling channel 141 and a cooling channel 142. The electrolysis unit 100 shown in Fig. 3 includes a cooling channel 141, a cooling channel 142, and a cooling channel 143. However, the electrolysis unit 100 may include at least one of the cooling channel 141, the cooling channel 142, and the cooling channel 143.

[0062] The cooling channels 141 are provided on the surface of the channel plate 153. The cooling channels 142 are farther from the electrolysis cell at the center of the electrolysis unit 100 than the cooling channels 141. The cooling channels 142 may be provided, for example, on the opposite side of the anode 111 with respect to the anode current collector 113, and may face the anode current collector 113. The cooling channels 142 may be provided, for example, on the opposite side of the cathode 121 with respect to the cathode current collector 123, and may face the cathode current collector 123.

[0063] The cooling channels 143 are provided on the surface of the channel plate 152. The cooling channels 143 are closer to the electrolytic cells in the center of the electrolysis unit 100 than the cooling channels 141. For example, the electrolytic cells at the ends of the stack tend to have lower cell temperatures due to a larger amount of heat dissipation from the clamping plates, whereas the electrolytic cells in the center of the stack tend to have higher temperatures. Therefore, by making the channel width of the cooling channels 143 facing the electrolytic cells in the center larger than the channel width of the cooling channels 141, it is possible to suppress temperature variations in the multiple electrolytic cells. Alternatively, the channel depth of the cooling channels 143 may be made larger than the channel depth of the cooling channels 141 to suppress temperature variations in the multiple electrolytic cells.

[0064] Examples of materials for the flow channel plates 153 and 152 include materials applicable to the flow channel plates 114 and materials applicable to the flow channel plates 124, for example.

[0065] The anode collector 201 is connected to the anode discharge flow path P2. The anode collector 201 includes an anode tank that can store the anode fluid discharged from the anode flow path 112 and flowing through the anode discharge flow path P2, and an anode gas-liquid separator that separates the anode fluid into an anode effluent and an anode exhaust. The anode effluent contains an anode solution. The anode effluent is returned to the anode supply flow path P1 via a circulation flow path P7 that connects the anode supply flow path P1 and the anode exhaust flow path P2, and is reused as the anode solution. The anode exhaust contains oxidation products and water vapor. The anode exhaust may also contain unreacted substances to be oxidized.

[0066] The anode collector 201 has a detector 211. The detector 211 includes at least one of a concentration meter that measures the concentration of at least one ion contained in the anode fluid contained in the anode collector 201, and a water level meter that measures the water level of the anode fluid contained in the anode collector 201 from the bottom surface of the anode collector 201. The detector 211 is not necessarily provided.

[0067] The anode tank is connected to an electrolyte supply source 212. The electrolyte supply source 212 can replenish the electrolyte in the anode wastewater contained in the anode tank. The electrolyte supply source 212 is not necessarily provided.

[0068] The flow rate controller 202 is provided midway along the anode supply flow path P1. The flow rate controller 202 has, for example, a pump, and controls the flow rate of the anode solution supplied to the anode flow path 112 via the anode supply flow path P1.

[0069] The pressure controller 204 is provided in the anode exhaust flow path P2. The pressure controller 204 controls the pressure in the anode flow path 112 by controlling the pressure in the anode exhaust flow path P2.

[0070] The cathode gas supply source 301 has, for example, a cylinder cabinet that can store a cathode gas containing a substance to be reduced. The cathode gas contains, for example, carbon dioxide or nitrogen.

[0071] The humidifier 302 is provided midway along the cathode supply flow path P3. The humidifier 302 can humidify the cathode gas. The humidifier 302 has a tank that can store, for example, hot water. The temperature of the hot water is not particularly limited, but is, for example, 50°C or higher and 60°C or lower. The humidifier 302 further has a detector 311 that measures the water level from the bottom of the tank of stored hot water. The detector 311 is not necessarily provided. The humidifier 302 may have a heater.

[0072] Water supply source 303 can supply water such as hot water to humidifier 302. The amount of water supplied from water supply source 303 can be controlled using, for example, a valve provided midway in a flow path connecting water supply source 303 and humidifier 302. Water supply source 303 is not necessarily provided.

[0073] The flow rate controller 304 is provided midway along the cathode supply flow path P3 and at the rear of the humidifier 302. The flow rate controller 304 has, for example, a pump, and can control the flow rate of the humidified cathode gas.

[0074] The pressure controller 305 is provided in the cathode exhaust flow path P4. The pressure controller 305 can control the pressure in the cathode flow path 122 by controlling the pressure in the cathode exhaust flow path P4.

[0075] The cathode collector 401 is connected to the cathode discharge flow path P4. The cathode collector 401 has a tank that can store the cathode fluid that is discharged from the cathode flow path 122 and flows through the cathode discharge flow path P4, and a gas-liquid separator that separates the cathode fluid into a cathode effluent and a cathode exhaust. The cathode effluent contains reduction products and hydrogen gas and water vapor resulting from side reactions. The cathode effluent may contain an anode solution. The cathode effluent may also contain unreacted substances to be reduced. The cathode exhaust may be collected from the cathode collector 401 to the outside.

[0076] The valve 402 is provided in the middle of the circulation flow path P5 that connects the cathode collector 401 and the anode collector 201. By opening the valve 402, the cathode effluent can be supplied from the cathode collector 401 to the anode collector 201. The circulation flow path P5 is formed of, for example, piping. A pump may be provided in the middle of the circulation flow path P5.

[0077] The cooler 501 condenses water vapor contained in the anode exhaust gas supplied from the anode collector 201 to generate water (anode condensed water). Oxygen products contained in the anode exhaust gas are collected in gaseous form. The cooler 501 is provided midway along a flow path P6 that connects the anode collector 201 and the condensed water collector 502. The flow path P6 is formed of, for example, piping. The cooler 501 may have a double pipe.

[0078] The condensed water collector 502 has a tank for storing anode condensed water. The condensed water collector 502 is connected to the cooler 501.

[0079] The detector 511 can measure the temperature of the anode exhaust gas supplied to the cooler 501. The detector 511 is provided, for example, in the middle of the flow path P6 and before the cooler 501.

[0080] Heat exchanger 601 forms a heat exchange structure that exchanges heat between the anode solution in the anode effluent flowing through a circulation flow path P7 that connects anode supply flow path P1 and anode discharge flow path P2, and anode condensed water flowing through a circulation flow path P8 that connects condensed water collector 502 and humidifier 302. This allows the anode solution in the anode effluent flowing through circulation flow path P7 to be cooled, and the anode condensed water flowing through circulation flow path P8 to be heated. The heat exchange structure can be formed, for example, by connecting circulation flow path P7 and circulation flow path P8 with a heat exchange member. Circulation flow path P7 and circulation flow path P8 are formed, for example, by piping.

[0081] The flow rate controller 602 is provided midway along the circulation flow path P8. The flow rate controller 602 has, for example, a pump that controls the flow rate of the anode condensed water supplied to the humidifier 302 via the circulation flow path P8.

[0082] The control device 701 receives detection signals from, for example, detectors 151, 211, 311, and 511, and transmits control signals to the flow rate controller 202, valve 402, and flow rate controller 602. The control device 701 is electrically connected to each component via bidirectional signal lines, some of which are not shown, and controls these components collectively. Note that each pipe is provided with a valve (not shown), and the opening and closing operation of the valve may be controlled by a signal from the control device 701.

[0083] The control device 701 may be configured using hardware that uses, for example, a processor, etc. Note that each operation may be stored as an operation program in a computer-readable recording medium such as a memory, and each operation may be executed by the hardware by appropriately reading out the operation program stored in the recording medium.

[0084] Next, a description will be given of an example of an electrolysis method using the electrolysis device 1. In the example of the electrolysis method, the flow rate controller 202 and the pressure controller 204 are controlled to supply the anode solution to the anode flow path 112 via the anode supply flow path P1, the flow rate controller 304 and the pressure controller 305 are controlled to supply the cathode gas humidified by the humidifier 302 from the cathode gas supply source 301 to the cathode flow path 122 via the cathode supply flow path P3, and a voltage is applied between the anode current collector 113 and the cathode current collector 123 from the power source 150 to supply a current to the anode 111 and the cathode 121.

[0085] When a current is passed through the anode 111 and the cathode 121, an oxidation reaction occurs near the anode 111 and a reduction reaction occurs near the cathode 121, as shown below. Here, we will explain the case where carbon dioxide, a substance to be reduced, is reduced to produce the reduction product carbon monoxide (CO), but the reduction product is not limited to carbon monoxide and may be other carbon compounds such as the organic compounds mentioned above or ammonia. In addition, the reaction process in the electrolytic cell mainly involves the production of hydrogen ions (H + ) or mainly hydroxide ions (OH - ), but the present invention is not limited to these reaction processes.

[0086] It mainly oxidizes water (H2O) to produce hydrogen ions (H + When a current is supplied between the anode 111 and the cathode 121, an oxidation reaction of water (H2O) occurs at the anode 111, which is in contact with the anode solution flowing through the anode flow path 112. Specifically, as shown in the following formula (1), the H2O contained in the anode solution is oxidized to produce oxygen (O2) and hydrogen ions (H + ) is generated. 2H2O → 4H + +O2+4e - …(1)

[0087] H generated at anode 111 +The electrons move through the cathode gas in the cathode flow channel 122 via the anode 111 and the separator 131 and reach the vicinity of the cathode 121. - ) and H that has moved to the vicinity of cathode 121 + This causes a reduction reaction of carbon dioxide (CO2). Specifically, as shown in the following formula (2), CO2 contained in the cathode gas supplied from the cathode flow channel 122 to the cathode 121 is reduced to produce CO. 2CO2+4H + +4e - → 2CO+2H2O …(2)

[0088] Next, carbon dioxide (CO2) is mainly reduced to hydroxide ions (OH - When a current is supplied between the anode 111 and the cathode 121, water (HO) and carbon dioxide (CO) are reduced near the cathode 121 to produce carbon monoxide (CO) and hydroxide ions (OH), as shown in the following formula (3): - ) and hydroxide ions (OH - ) diffuses to the vicinity of the anode 111 and converts into hydroxide ions (OH - ) is oxidized to produce oxygen (O2). 2CO2+2H2O+4e - → 2CO+4OH - …(3) 4OH - → 2H2O+O2+4e - …(4)

[0089] Furthermore, when nitrogen (N2), a substance to be reduced, is reduced to produce ammonia (NH3), a reduction product, water or hydroxide ions are electrochemically oxidized near the anode 111 according to the following formula (5) or formula (6), producing oxygen. Near the cathode 121, nitrogen is reduced according to the following formula (7) or formula (8), producing ammonia. 3H2O → 3 / 2O2+6H + +6e - …(5) 6OH - → 3 / 2O2+3H2O+6e - …(6) N2+6H2O+6e - → 2NH3+6OH - …(7) N2+6H + +6e - → 2NH3…(8)

[0090] Humidifying the cathode gas with the humidifier 302 can prevent the cations in the anode solution from reacting with the substance to be reduced, resulting in the precipitation of carbonates of the cations in the cathode flow channel 122. In some cases, water is supplied from the inlet of the cathode flow channel 122 to dissolve the precipitated salts.

[0091] When a porous membrane is used for separator 131, if the pressure loss in cathode flow channel 122 is large due to salt precipitation, the amount of water moving from cathode flow channel 122 to anode flow channel 112 also increases. Furthermore, if the pressure loss in the membrane decreases due to deterioration of the porous membrane, the amount of water moving from cathode flow channel 122 to anode flow channel 112 increases.

[0092] The anode fluid discharged from the anode flow channel 112 is supplied to the anode collector 201 via the anode exhaust flow channel P2. A portion of the anode solution supplied to the anode flow channel 112 may be supplied to the cathode flow channel 122 via the anode 111, the separator 131, and the cathode 121. On the other hand, the cathode fluid discharged from the cathode flow channel 122 is sent to the cathode collector 401 via the cathode exhaust flow channel P4, and the cathode exhaust containing reduction products is separated from the cathode fluid and collected by the cathode collector 401.

[0093] When cations in the anode solution migrate to the cathode flow channel 122 as the electrolysis reaction proceeds, the amount of cations in the entire reaction system, including the anode flow channel 112, decreases as the reaction proceeds, and the electrolyte concentration in the anode effluent decreases. A decrease in the electrolyte concentration increases the cell resistance, and the efficiency of the electrolysis reaction also decreases due to the reduced amount of ion migration.

[0094] As the electrolysis reaction proceeds, water may move from the cathode flow channel 122 to the anode flow channel 112. This is particularly noticeable when the cathode gas is humidified and supplied to the electrolysis unit 100 to prevent salt deposition in the cathode flow channel 122, or when water is supplied to the cathode flow channel 122. When water moves, the amount of water in the anode solution increases, further reducing the electrolyte concentration and the efficiency of the electrolysis reaction.

[0095] When the operation of the electrolysis device 1 is continued for a long period of time, the temperature of the anode solution rises, and the temperature of the electrolytic cell also rises. To address this, the anode solution may be directly cooled, or the cooled anode solution may be supplied to the cooling flow path 141 to cool the electrolytic cell.

[0096] When the electrolysis cell is cooled using cooled anode solution, if the anode solution is cooled along the way in the anode discharge flow path P2, the anode fluid, which is discharged from the anode flow path 112 and contains the anode solution heated by the electrolysis reaction, is cooled and moves to the anode collector 201. The anode collector 201 separates the anode fluid into an anode exhaust containing oxidation products produced by the electrolysis reaction, and an anode effluent containing the anode solution. Furthermore, if the anode exhaust is cooled by the anode collector 201 to condense the water vapor contained in the anode exhaust to generate anode condensed water, the amount of water discharged as water vapor decreases, further reducing the electrolyte concentration and causing a decrease in electrolysis efficiency.

[0097] On the other hand, if the heated anode fluid discharged from the anode flow path 112 is supplied to the anode collector 201 without being cooled, the temperature of the anode effluent stored in the tank of the anode collector 201 will rise, which will increase the temperature of the electrolysis cell.

[0098] The anode solution may be cooled, for example, between the electrolytic cell and the anode collector 201. In this case, the amount of water vapor discharged increases, but when the temperature of the electrolytic cell is about 70°C and the temperature of the anode solution is about 50 to 60°C, the amount of water vapor in the anode exhaust is such that even if the amount of anode solution decreases, the electrolyte concentration decreases and cell performance deteriorates. Therefore, if the temperature of the electrolytic cell is increased and operation of the electrolysis device 1 is continued, the electrolyte concentration can be maintained, but the amount of electrolyte gradually decreases, making it difficult to continue the reaction.

[0099] This is undesirable because it results in a large energy loss, since the cooled anode effluent must be reheated in the electrolysis section 100. If cooling is performed midway through the anode discharge flow path P2, a small amount of cooled anode fluid must be used to cool a large amount of anode solution in the tank of the anode collector 201, and since the ambient temperature is expected to be high due to the equipment inside the device, the cooling efficiency is very poor.

[0100] To prevent a decrease in the concentration of the electrolyte in the anode solution, the cathode effluent stored in the cathode collector 401 can be returned to the tank of the anode collector 201. However, because the amount of electrolyte changes, it is difficult to stabilize the cell output. For this reason, it is possible to provide a mechanism for supplying water and electrolyte components to the anode collector 201. However, in this case, water and electrolyte components are required separately, the number of devices increases, and both the device costs and operating costs increase, which is undesirable.

[0101] Furthermore, as mentioned above, water must be supplied to the humidifier 302 to humidify the cathode gas. Therefore, it is conceivable to supply water contained in the anode effluent from the anode collector 201 to the humidifier 302. However, at normal cooling temperatures (approximately 5°C to 25°C), the amount of electrolyte decreases, resulting in a shortage of water that can be supplied to the humidifier 302. Furthermore, directly supplying the anode effluent to the humidifier 302 or the cathode flow path 122 also creates other problems. Because only water evaporates within the humidifier 302, the electrolyte components within the humidifier 302 become concentrated, causing salt precipitation. Furthermore, the cooled anode effluent must be reheated to be returned to the humidifier 302, resulting in reduced energy efficiency.

[0102] Therefore, in the electrolysis device of this embodiment, after separating the anode exhaust from the anode fluid by the anode collector 201, the anode exhaust separated by the anode collector 201 is cooled using a cooler 501 provided separately from the anode collector 201, thereby condensing the water vapor contained in the anode exhaust to produce anode condensed water. The produced anode condensed water is distilled water, and therefore can be supplied to the humidifier 302. With this configuration, it is possible to suppress the loss of water from within the reaction system, and it is possible to operate for a long period of time without the need to replenish water or the electrolyte from outside.

[0103] Furthermore, the electrolysis device of this embodiment has a heat exchange structure that performs heat exchange between the anode effluent flowing through circulation flow path P7 and the anode condensed water flowing through circulation flow path P8. The anode condensed water supplied to the humidifier 302 is heated by the anode effluent, and the anode effluent is cooled by the anode condensed water before being supplied to the anode flow path 112 as the anode solution. This allows the anode solution and the electrolytic cell to be cooled, and the anode condensed water to be heated and supplied to the humidifier 302, thereby achieving a highly energy-efficient configuration.

[0104] The heat exchange structure preferably has a heat exchanger 601. Due to cost and device size considerations, it is not necessary to use a heat exchanger 601, and due to limitations on cost and device size, the two pipes may be connected by a heat exchange member. When heat exchange performance is taken into consideration, the heat exchange member is preferably a metal member such as gold, silver, or copper, but other metal members may be used in terms of cost and corrosion resistance.

[0105] As described above, to prevent salt precipitation in the cathode flow channel 122, the cathode gas containing the substance to be reduced is humidified from the cathode supply flow channel P3. However, to prevent water condensation inside the electrolysis unit 100, it is preferable to constantly supply water to the humidifier 302 to deliver saturated water vapor at a temperature approximately 0°C to 20°C lower than the cell temperature. In contrast, by performing heat exchange between the anode condensed water and the anode effluent and heating the anode condensed water, it is possible to reduce the thermal energy input from the heater to the humidifier 302 compared to supplying ordinary water to the humidifier 302, thereby improving the energy efficiency of the entire system. Furthermore, even when water moves from the cathode flow channel 122 to the anode flow channel 112, the water that moved to the anode flow channel 112 returns to the humidifier 302, thereby suppressing the loss of water throughout the entire system.

[0106] The anode condensed water may be cooled and used to cool the anode exhaust or the cathode exhaust, and the water vapor contained in these exhausts may be condensed to generate cathode condensed water, which may then be used to directly cool the electrolytic cell and returned to the condensed water collector 502. In this case, the cathode condensed water may be supplied to the humidifier 302 via the circulation flow path P8 to replenish humidification water. This is advantageous because it allows the necessary amount of condensed water to be supplied depending on the progress of the humidification water. This is also advantageous in terms of adjusting the cooling by the circulation rate of the condensed water. The circulation of the condensed water makes it easy to adjust the liquid volume, and it is advantageous because it allows the cooling capacity to be adjusted depending on the heat generation of the electrolytic cell and the amount and temperature of water vapor in the anode exhaust or cathode exhaust. Furthermore, the cooling of the anode exhaust, the cathode exhaust, and the electrolytic cell does not necessarily have to be performed in this order; some or all of the cooling operations may be performed in parallel.

[0107] The only water discharged from the reaction system due to the electrolysis reaction is water vapor contained in the cathode exhaust containing reduction products such as carbon monoxide and water vapor contained in the anode exhaust containing oxidation products such as oxygen. However, since extremely low cooling temperatures require excessive energy to prevent the loss of water from the reaction system, it is preferable to remove water vapor from the anode exhaust containing oxidation products at temperatures ranging from room temperature (25°C) to approximately 40°C. Similarly, for the cathode exhaust, if it is desirable to avoid water vapor in the reaction for further converting the reduction products to other compounds such as methanol, it is preferable to remove as much water vapor as possible. In either case, since water is lost from the reaction system, a mechanism for supplying water, such as water supply source 303, to one of the flow paths in the reaction system may be provided. Furthermore, for electrolyte components, a mechanism for supplying electrolyte components, such as electrolyte supply source 212, to one of the flow paths for circulating the electrolyte may be provided to adjust the electrolyte concentration due to factors such as the water level in the anode collector 201 tank and the cathode collector 401 tank, or the discharge of solid fine powder of carbonate electrolyte components from the reaction system.

[0108] Control device 701 may receive and analyze detection signals from sensors such as detector 211, which measures the amount and concentration of anode solution, detector 311, which measures the level of hot water contained in the tank of humidifier 302, and detector 151, which measures the cell output and cell temperature. Based on the analysis results, control device 701 transmits control signals to, for example, flow rate controller 202, valve 402, and flow rate controller 602, thereby enabling flow rate controller 202 to adjust the flow rate of anode solution, valve 402 to adjust the flow rate of cathode effluent returned to anode collector 201, and flow rate controller 602 to adjust the flow rates of anode condensed water and cathode condensed water supplied to humidifier 302. Control device 701 may also adjust the amount of water supplied from water supply source 303 by controlling a valve provided in the flow path connecting water supply source 303 and humidifier 302 using a control signal based on each detection signal. The control device 701 allows the electrolysis device 1 to be operated by freely setting objectives such as improving cell output, low-cost operation, and long-life operation. In addition, the degree of freedom in adjusting the concentration and amount of the electrolyte is improved, allowing for stable operation over long periods of time.

[0109] The control device 701 may perform a cooling operation when the cell output of the electrolytic cell during electrolysis does not satisfy a required standard. The required standard for the cell output is set, for example, based on the relationship between the cell output and the temperature of the electrolytic cell. When the temperature of the electrolytic cell rises, the cell output is likely to decrease.

[0110] The necessity of the cooling operation can be determined not only from changes in the cell voltage, cell current, and cell temperature of the electrolytic cell, but also from the performance of gas-liquid separation between the anode 111 and the cathode 121, i.e., the amount of liquid and gas transferred between the anode 111 and the cathode 121, the amount of product gas, the difference between the cell voltage and the potential of the reference electrode, and an estimated value of the Faraday efficiency based on these parameters. Furthermore, the determination can be made comprehensively from each parameter, and any combination of values ​​and calculation methods can be used.

[0111] When the current density of the electrolytic cell is low and the electrolysis efficiency is high, the amount of heat generated is small, and the in-plane temperature uniformity of the electrolytic cell can be maintained by supplying cathode condensed water to the cooling flow path 141. On the other hand, when the current density of the cell is high and the electrolysis efficiency is low, the amount of heat generated is large, and it is necessary to maintain the in-plane temperature uniformity of the electrolytic cell by circulating the cathode condensed water supplied to the cooling flow path 141. Therefore, it is simple and preferable to determine whether or not cooling operation is necessary according to the current density and electrolysis efficiency of the electrolytic cell.

[0112] The need for cooling may be determined taking into account the operating time of the electrolytic cell. The operating time can be calculated by estimating or predicting the rate of temperature rise based on the heat dissipation rate of the electrolytic cell and the heat dissipation rate associated with the temperature rise of the anode solution. Therefore, it is preferable to control the temperature of the anode solution according to a prediction of future operation of the electrolytic cell. Calculated values ​​such as the product of an integrated voltage value and time or a current value and time can also be used, and any combination and calculation method can be used. Furthermore, determination based on these calculated combinations is preferable because it takes into account differences due to the operating method of the electrolytic cell rather than determination based solely on the duration. Furthermore, fluctuations in current and voltage, the pH value of the anode solution, the change in value, the amount of oxygen generated, and the amount of fluctuation can also be used to determine the need for cooling.

[0113] The anode solution preferably has an electrical conductivity of at least 10 mS / m or more, and more preferably 100 mS / m or more. This can reduce the internal resistance of the electrolytic cell and increase thermal conductivity. Considering cooling performance, it is preferable to use an electrolyte solution with a thermal conductivity higher than that of water for the anode solution. High thermal conductivity allows the heat of the electrolytic cell to be efficiently transferred to the electrolyte, thereby cooling the electrolytic cell. Cooling is important because the reduction reaction of the target substance has low electrolysis efficiency and generates a large amount of heat. Here, electrolysis efficiency is defined as the theoretical voltage / reaction voltage.

[0114] The anode solution containing ions can lower its freezing point to below 0°C. This prevents the anode solution from freezing even in temperatures below 0°C, facilitating use in cold regions, for example. Furthermore, freezing inside the electrolysis cell can cause physical damage to cell components. For example, freezing and expansion of the inside of the anode flow channel 112 or the inside of the cooling flow channel 141 can damage screws and other components that hold down the clamping plates. Furthermore, because the clamping pressure significantly affects electrolysis cell performance, expansion can cause changes in the clamping pressure. This can lead to distortion of the clamping plates, distortion of the screws, distortion of the flow channel plates, and other problems. Furthermore, swelling, expansion, and other problems can cause damage to the separator 131, as well as a decrease in the ion exchange performance of the electrolyte. Freezing can also cause cracks in the gas diffusion layer and cathode catalyst layer, resulting in a decrease in performance.

[0115] All unused energy from the electrolysis operation is discharged to the outside as heat. In particular, in stacks containing multiple electrolysis cells, the reaction volume density is large, making cooling even more important. In addition, the electrolysis reaction of the substance to be reduced changes reaction characteristics significantly depending on the temperature. Therefore, the electrolysis efficiency decreases significantly if the temperature uniformity of the electrolysis cell is low or if the temperature distribution of the electrolysis cells is large in stacks containing multiple electrolysis cells. Therefore, cooling performance and uniform temperature distribution using cooling methods are effective in improving efficiency.

[0116] Similarly, one method of maintaining a uniform cell temperature is to change the flow rate of the anode solution. However, changes in the flow rate of the anode solution can change the cell output, and if gas components such as oxygen gas generated by the reaction in the anode solution are present in the flow path, a two-layer gas-liquid flow will form, causing pressure loss. This is not preferable because it is difficult to control flow paths with different flow path structures or pressure loss, and differences in flow rate can significantly change the characteristics of the reaction.

[0117] (Second embodiment) 8 is a schematic diagram illustrating a configuration example of an electrolysis device according to a second embodiment. As with the first embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. The following describes only the parts that differ from the first embodiment, and the description of the electrolysis device 1 according to the first embodiment can be applied to the other parts as appropriate.

[0118] The electrolysis device 1 shown in FIG. 8 differs from the electrolysis device 1 shown in FIG. 1 in that it further includes a cooler 403 in the cathode discharge section 400, and does not include the heat exchanger 601 and the circulation flow path P8 in the circulation section 600.

[0119] The cooler 403 is connected to the cathode collector 401. The cooler 403 cools the cathode exhaust separated by the cathode collector 401, thereby condensing the water vapor contained in the cathode exhaust to generate water (cathode condensed water). Carbon products and unreacted substances to be reduced contained in the cathode exhaust are collected in the gaseous state.

[0120] The cooler 403 is connected to the inlet of the cooling channel 141 via a supply channel P9. Cathode condensed water is supplied to the cooling channel 141 as cooling water via the supply channel P9. The supply channel P9 is formed of, for example, piping. Note that, as shown in FIGS. 2 and 3, when the cooling channel 142 and the cooling channel 143 are provided, the same cooling water as that of the cooling channel 141 may be supplied to the cooling channel 142 and the cooling channel 143 connected to the supply channel P9.

[0121] The cooling channels 141, together with the electrolysis cell, form a heat exchange structure that performs heat exchange between the cathode condensate flowing through the cooling channels 141 and the anode solution flowing through the anode channels 112. This allows the anode solution to be cooled and the cathode condensate flowing through the cooling channels 141 to be heated. The heat exchange structure can be formed, for example, by connecting the cooling channels 141 to the anode channels 112 and the cathode channels 122 via channel plates 114 and 124 that function as heat exchange members.

[0122] The heat-exchanged cathode condensed water discharged from the outlet of the cooling flow path 141 flows through a discharge flow path P10 that connects the cooling flow path 141 and the humidifier 302. This allows the cathode condensed water flowing through the discharge flow path P10 to be supplied to the humidifier 302. The discharge flow path P10 is formed of, for example, piping. The flow rate controller 602 can control the flow rate of the cathode condensed water supplied to the humidifier 302. The flow rate controller 602 is not necessarily provided.

[0123] 8, a cooler 403 may be provided midway along a supply flow path P9 that connects the inlet of the cooling flow path 141 and the condensed water collector 502, and anode condensed water may be supplied to the cooling flow path 141 together with cathode condensed water. However, this is not limiting, and the supply flow path P9 does not have to be connected to the condensed water collector 502.

[0124] The electrolysis device of the second embodiment uses a cooler 403 to condense water vapor in the cathode exhaust, which contains gases such as the target substance to be reduced, reduction products, and hydrogen gas resulting from a side reaction, to produce cathode condensed water. The cathode effluent contains the electrolyte components of the anode solution that has moved from the anode flow path 112 to the cathode flow path 122. The cathode condensed water is returned to the humidifier 302, and the cathode effluent is returned to the anode collector 201. This prevents the loss of water from the entire reaction system, and only requires that the humidifier 302 and the anode collector 201 be replenished with water equivalent to the amount of saturated water vapor at the cooled temperature, while maintaining a constant electrolyte concentration.

[0125] The cathode fluid is separated into cathode exhaust and cathode effluent by the cathode collector 401. The cathode exhaust is then cooled to produce cathode condensate. The cathode effluent is returned to the anode collector 201. The cathode condensate does not contain electrolyte components, and when returned to the humidifier 302, the electrolyte components do not get mixed into the humidifier 302, thereby suppressing corrosion of the humidifier 302. In addition, the electrolyte components that move to the cathode flow path 122 are returned to the anode flow path 112, thereby stabilizing the electrolyte concentration. The temperature of the humidifier 302 is operated at a temperature that is approximately 0°C to 20°C lower than the electrolysis cell. Meanwhile, the temperature of the cathode exhaust is also approximately 0°C to 20°C lower than the cell temperature. Although the gas components change due to the electrolysis reaction, there is no significant change in the approximate gas volume, and the amount of discharged water vapor and the amount of water evaporated in humidifier 302 are roughly the same when direct gas-liquid separation of the cathode fluid is performed as in this embodiment. Because the amount of cathode condensed water generated by cooling the cathode exhaust gas and the amount of water reduced in humidifier 302 are roughly the same, changes in the amount of electrolyte components can be prevented, and the electrolyte concentration can be maintained stable.

[0126] As in the first embodiment, the control device 701 transmits control signals to, for example, the flow rate controller 202, the valve 402, and the flow rate controller 602 based on the analysis results of the detection signals, thereby enabling the flow rate controller 202 to adjust the flow rate of the anode solution, the valve 402 to adjust the flow rate of the cathode effluent returned to the anode collector 201, and the flow rate controller 602 to adjust the flow rates of the anode condensed water and the cathode condensed water supplied to the humidifier 302. The control device 701 allows the electrolysis device 1 to be operated by freely setting objectives such as improved cell output, low-cost operation, and long-life operation. Furthermore, the degree of freedom in adjusting the concentration and amount of the electrolyte is improved, enabling stable operation over long periods of time.

[0127] As described above, the electrolysis device of the second embodiment is provided with a cooling channel 141 for cooling the electrolysis cell, and is able to cool the electrolysis cell by supplying cathode condensed water to the cooling channel 141. In this case, the temperature of the anode solution is lower than the temperature of the electrolysis cell. The anode collector 201 separates oxidation products such as oxygen as anode exhaust, but also discharges water equivalent to the saturated water vapor amount of the high-temperature anode solution. With this configuration, the amount of electrolytic solution decreases, which may require the addition of a large amount of water to the anode solution.

[0128] When cooling the electrolytic cell with the anode solution, the amount of water discharged can be reduced by, for example, providing a cooler before the anode collector 201. On the other hand, providing a cooler after the anode collector 201 increases the amount of water vapor discharged, significantly reducing the amount of electrolyte.

[0129] As mentioned above, electrolyte components move from the anode flow channel 112 to the cathode flow channel 122, and the amount of movement increases as the electrolysis reaction proceeds. As a result, the electrolyte concentration decreases as the electrolysis reaction proceeds, increasing cell resistance and gradually reducing reaction efficiency. To optimize the electrolyte concentration, it is preferable to operate the system with a constant stable amount of electrolyte. However, if the cooler is positioned differently or a separate cooling mechanism is installed to cool the cell, the operation can become very unstable due to the electrolyte temperature and the amount of heat being cooled, depending on the operating conditions of the cell.

[0130] In contrast, the electrolysis device of the second embodiment supplies the cathode condensed water to the cooling channel 141 to cool the electrolytic cell, thereby reducing the amount of water lost in the entire reaction system and maintaining a stable amount of electrolyte. Furthermore, by performing heat exchange between the cathode condensed water and the anode solution and returning the heat to the humidifier 302, the electrolytic cell can be cooled and the condensed water can be heated simultaneously, as in the first embodiment, reducing the energy required to cool the cell and the energy input to the humidifier 302 and improving system efficiency.

[0131] This embodiment can be combined with other embodiments as appropriate.

[0132] (Third embodiment) 9 is a schematic diagram illustrating a configuration example of an electrolysis device 1 according to a third embodiment. As with the first embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. Note that, below, only the parts that differ from the first embodiment will be described, and for the other parts, the description of the electrolysis device according to the first embodiment can be used as appropriate.

[0133] The electrolysis device 1 shown in FIG. 9 differs from the electrolysis device 1 shown in FIG. 1 in that it further includes a cooler 403 in the cathode discharge section 400 and does not include the cooling flow path 141 in the electrolysis section.

[0134] The cooler 403 cools the cathode exhaust gas separated by the cathode collector 401, thereby condensing the water vapor contained in the cathode exhaust gas to generate cathode condensed water.

[0135] The cooler 403 is provided midway along the circulation flow path P8. The cathode exhaust gas is cooled using the anode condensed water. The cathode condensed water is supplied to the humidifier 302 together with the anode condensed water via the circulation flow path P8 and the heat exchanger 601, as in the first embodiment.

[0136] As described above, the electrolysis apparatus of the third embodiment condenses water vapor in the cathode exhaust gas using the cooler 403 to generate cathode condensed water. The cathode effluent contains electrolyte components that have moved from the anode flow path 112 to the cathode flow path 122. The cathode condensed water is returned to the humidifier 302 via the circulation flow path P8, and the cathode effluent is returned to the anode collector 201. This prevents water loss from the entire reaction system, and only requires that the humidifier 302 and the anode collector 201 be replenished with water equivalent to the amount of saturated water vapor at the temperature of the cooled anode solution, and the electrolyte concentration can be maintained constant.

[0137] Furthermore, in the electrolysis apparatus of the third embodiment, the anode condensate is used to cool the cathode exhaust gas before heat exchange with the anode effluent in the heat exchanger 601, as in the first embodiment. This is preferable because it further increases the temperature of the anode condensate returned to the humidifier 302. The order of heat exchange in this case may be either the cathode exhaust gas or the anode effluent. For cell cooling, it is preferable to exchange heat with the anode effluent first, but if it is desired to preferentially cool the cathode exhaust gas, it is preferable to exchange heat with the cathode exhaust gas first. The preferred order of these heat exchanges varies depending on the operating temperature and amount of discharged energy of the electrolysis cell, and the priority of cooling the cathode exhaust gas, and is not particularly limited.

[0138] This embodiment can be combined with other embodiments as appropriate.

[0139] (Fourth embodiment) 10 is a schematic diagram illustrating a configuration example of an electrolysis device 1 according to a fourth embodiment. As with the second embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. The following describes only the parts that differ from the second embodiment, and the description of the electrolysis device according to the second embodiment can be applied to the other parts as appropriate.

[0140] The electrolysis device shown in FIG. 10 differs from the electrolysis device shown in FIG. 8 in that the cooler 403 is not directly connected to the cathode collector 401 .

[0141] The cathode collector 401 separates the cathode effluent discharged from the cathode flow channel 122 into cathode effluent and cathode exhaust. The cathode effluent is returned to the anode collector 201 via the circulation flow channel P5. The cathode exhaust may be recovered to the outside as a gas.

[0142] The cooler 403 is provided midway along the supply flow path P9. The cooler 403 cools the anode condensed water supplied from the condensed water collector 502. The cooled anode condensed water is supplied as cooling water to the cooling flow path 141 via the supply flow path P9.

[0143] As in the second embodiment, the cooling channels 141, together with the electrolysis cell, form a heat exchange structure that performs heat exchange between the anode condensate flowing through the cooling channels 141 and the anode solution flowing through the anode channel 112. This allows the anode solution to be cooled and the anode condensate flowing through the cooling channels 141 to be heated. The heat exchange structure can be formed, for example, by connecting the cooling channels 141 and the anode channel 112 via channel plates 114 and 124 that function as heat exchange members.

[0144] The heat-exchanged anode condensed water discharged from the outlet of the cooling flow path 141 flows through a discharge flow path P10 that connects the cooling flow path 141 and the humidifier 302. As a result, the anode condensed water flowing through the discharge flow path P10 is supplied to the humidifier 302. The flow rate controller 602 can control the flow rate of the anode condensed water supplied to the humidifier 302.

[0145] The electrolytic device of the fourth embodiment cools anode condensate and supplies it to the cooling channel 141 as cooling water. This allows the electrolytic cell to be cooled directly rather than by cooling the anode solution, and therefore allows design and operation to be performed solely from the perspective of the cooling performance of the electrolytic cell, without being affected by temperature distribution within the electrolytic cell or changes in the flow rate of the anode solution. Furthermore, the electrolytic cell can be cooled regardless of changes in temperature or heat generation associated with electrolysis. Furthermore, the cooling channel 141 can be freely designed to minimize the temperature distribution within the electrolytic cell. Note that multiple cooling channels may be provided, and the flow rate of cooling water may be changed for each channel to minimize the temperature, heat generation, and temperature distribution of the electrolytic cell.

[0146] Furthermore, the electrolytic device of the fourth embodiment performs heat exchange between the anode condensate and the anode solution, and returns the heat-exchanged anode condensate to the humidifier 302, thereby simultaneously cooling the electrolytic cell and heating the condensate, as in the second embodiment, thereby reducing the energy required for cell cooling and the energy input to the humidifier 302 and improving system efficiency.

[0147] This embodiment can be combined with other embodiments as appropriate.

[0148] (Fifth embodiment) 11 is a schematic diagram illustrating a configuration example of an electrolysis device according to a fifth embodiment. As in the second embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. The following describes only the parts that differ from the second embodiment, and the description of the electrolysis device according to the second embodiment can be applied to the other parts as appropriate.

[0149] The electrolysis device shown in FIG. 11 differs from the electrolysis device shown in FIG. 8 in that the circulation section 600 further includes a valve 603 and a valve 604, and has a circulation flow path P8.

[0150] The condensed water collector 502 has a cooler 512 that cools the anode condensed water contained in the tank, and at least one detector 513 that detects the water level of the anode condensed water contained in the condensed water collector 502 from the bottom of the tank and the temperature of the condensed water collector 502.

[0151] Cooler 501 can cool the anode exhaust using cooled anode condensed water. Cooler 501 has, for example, a double pipe, with the anode exhaust flowing through one pipe and the cooled anode condensed water flowing through the other pipe. The anode condensed water used to cool the anode exhaust is supplied to cooler 403 via cooler 501 and cooled.

[0152] 11 , a cooler 403 may be provided midway along a supply flow path P9 that connects the inlet of the cooling flow path 141 and a condensed water collector 502, and cooled anode condensed water may be supplied to the cooling flow path 141 together with cathode condensed water. However, this is not limiting, and the supply flow path P9 does not need to be connected to the condensed water collector 502.

[0153] The heat-exchanged mixed water of the anode condensed water and the cathode condensed water discharged from the outlet of the cooling flow path 141 flows through an exhaust flow path P10 that connects the outlet of the cooling flow path 141 to the humidifier 302. The exhaust flow path P10 is connected to a circulation flow path P8. The description of the first embodiment can be used as appropriate for the description of the circulation flow path P8.

[0154] Valve 603 is provided midway along circulation flow path P8, which connects discharge flow path P10 and condensed water collector 502. Valve 604 is provided midway along discharge flow path P10, after the connection point between circulation flow path P8 and discharge flow path P10. By opening valve 603 and closing valve 604, the mixed water of anode condensed water and cathode condensed water flowing through discharge flow path P10 can be supplied to and returned from condensed water collector 502. By closing valve 603 and opening valve 604, the mixed water of anode condensed water and cathode condensed water can be supplied from condensed water collector 502 to humidifier 302. Flow rate controller 602 is provided midway along discharge flow path P10. Flow rate controller 602 can control the flow rate of the mixed water of anode condensed water and cathode condensed water supplied to humidifier 302.

[0155] The electrolysis apparatus of the fifth embodiment condenses water vapor in the cathode exhaust gas using a cooler 403 to generate cathode condensed water. The cathode effluent contains electrolyte components that have moved from the anode flow path 112 to the cathode flow path 122. The cathode condensed water is returned to the humidifier 302, and the cathode effluent is returned to the anode collector 201. This prevents water loss from the entire reaction system, and only requires that the humidifier 302 and the anode collector 201 be replenished with water equivalent to the amount of saturated water vapor at the cooled temperature, while maintaining a constant electrolyte concentration.

[0156] As in the first embodiment, the control device 701 transmits control signals to, for example, the flow rate controller 202, the valve 402, the flow rate controller 602, the valve 603, and the valve 604 based on the analysis results of the detection signals, thereby enabling the flow rate controller 202 to adjust the flow rate of the anode solution, the valve 402 to adjust the flow rate of the cathode effluent returned to the anode collector 201, and the flow rate controller 602, the valve 603, and the valve 604 to select the supply destination and adjust the flow rate of the anode condensed water and the cathode condensed water. The control device 701 allows the electrolysis device 1 to be operated by freely setting objectives such as improved cell output, low-cost operation, and long-life operation. Furthermore, the degree of freedom in adjusting the concentration and amount of the electrolyte is improved, enabling stable operation over long periods of time.

[0157] As described above, the electrolysis apparatus of the fifth embodiment uses anode condensed water to cool the anode exhaust gas and as cooling water to cool the cathode exhaust gas and the electrolysis cell, and returns at least a portion of the anode condensed water to the humidifier 302 and at least a portion of the anode condensed water to the condensed water collector 502. Furthermore, by using the detection signals from the detectors 311 and 513 to select the supply destination of the anode condensed water by the control device 701, it is possible to cool the electrolysis cell even if the anode condensed water contained in the anode exhaust gas is small. Furthermore, by adjusting the flow rate of the anode condensed water using the detection signal, it is possible to adjust the cooling efficiency of the electrolysis cell and adjust the temperature of the electrolysis cell. Furthermore, by changing the flow rate of the anode condensed water using the detection signal, it is possible to reduce the temperature distribution inside the electrolysis cell.

[0158] This embodiment can be combined with other embodiments as appropriate.

[0159] (Sixth embodiment) 12 is a schematic diagram illustrating a configuration example of an electrolysis device according to a sixth embodiment. As in the second embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. The following describes only the parts that differ from the second embodiment, and the description of the electrolysis device according to the second embodiment can be applied to the other parts as appropriate.

[0160] The electrolysis apparatus shown in Fig. 12 differs from the electrolysis apparatus shown in Fig. 8 in that the circulation section 600 further includes valves 603 and 604, and includes a circulation flow path P8. The electrolysis apparatus also differs in that the cooling section 500 does not include a cooler 501. The valves 603 and 604 are the same as those in the fifth embodiment, and therefore the description of the fifth embodiment can be used as appropriate. The description of the first embodiment can be used as appropriate for the description of the circulation flow path P8.

[0161] The condensed water collector 502 includes a cooler 512 that cools the anode exhaust gas supplied from the anode collector 201 to condense water vapor contained in the anode exhaust gas to produce anode condensed water, and at least one detector 513 that detects the water level of the anode condensed water contained in the condensed water collector 502 from the bottom surface of the condensed water collector 502, the temperature of the condensed water collector 502, and the concentration of at least one ion contained in the anode exhaust gas.

[0162] The cooler 403 can generate cathode condensed water by cooling the cathode exhaust gas using the anode condensed water. The cathode condensed water is supplied to the cooling flow path 141 via the cooler 403. The anode condensed water is supplied to the cooling flow path 141 together with the cathode condensed water.

[0163] As described above, the electrolysis apparatus of the sixth embodiment produces anode condensed water by directly supplying anode exhaust gas to the condensed water collector 502 for cooling, and also cools cathode condensed water using the anode condensed water. The anode condensed water and cathode condensed water are supplied to the cooling flow path 141, and a portion of the water is returned to the humidifier 302 and the other portion is returned to the condensed water collector 502 for circulation.

[0164] As in the sixth embodiment, by providing coolers 403 and 512, the anode exhaust can be directly cooled, and the temperature of the cooling water can be easily controlled. Furthermore, the temperature of the cooling water can be controlled even when the amount of anode exhaust or water vapor is small, and part of the cooling water can be used to cool the cathode exhaust and the other part can be used to cool the electrolysis cell, so that the respective temperatures can be controlled as desired.

[0165] (Seventh embodiment) 13 is a schematic diagram illustrating a configuration example of an electrolysis device according to a seventh embodiment. As in the sixth embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. The following describes only the parts that differ from the sixth embodiment, and the description of the electrolysis device according to the sixth embodiment can be applied to the other parts as appropriate.

[0166] The electrolysis apparatus shown in FIG. 13 differs from the electrolysis apparatus shown in FIG. 12 in that it includes a supply flow path P11 that supplies cathode condensed water generated by the cooler 403 to the condensed water collector 502.

[0167] The supply flow path P11 connects the cooler 403 and the condensed water collector 502. Cathode condensed water generated by the cooler 403 is stored in the condensed water collector 502, cooled together with anode condensed water by the cooler 403, and supplied to the supply flow path P9. The supply flow path P11 is formed of, for example, piping.

[0168] The cooler 403 can cool the cathode exhaust using the anode condensed water and the cathode condensed water.

[0169] As described above, in the electrolysis device of the seventh embodiment, the cathode effluent is supplied to the anode collector 201, the anode effluent is supplied to the anode collector 201, and the anode exhaust gas is supplied to the condensed water collector 502. The anode condensed water is supplied to the cooler 403 together with the cathode condensed water from the condensed water collector 502. Except for this, similar to the sixth embodiment, the anode condensed water and the cathode condensed water are supplied to the cooling flow path 141 as cooling water. The anode condensed water and the cathode condensed water are used to cool the cathode exhaust gas and the electrolysis cell, and a portion is supplied to the humidifier 302 and another portion is returned to the condensed water collector 502 and circulated. This makes it possible to reduce the amount of water discharged from the entire reaction system of the electrolysis device and circulate it, and the electrolysis device can be operated without supplying water to the electrolysis device from outside.

[0170] This embodiment can be combined with other embodiments as appropriate.

[0171] (Eighth embodiment) 14 is a schematic diagram illustrating a configuration example of an electrolysis device according to an eighth embodiment. As with the first embodiment, the electrolysis device 1 includes an electrolysis unit 100, an anode supply unit 200, a cathode supply unit 300, a cathode discharge unit 400, a cooling unit 500, a circulation unit 600, and a control unit 700. Note that, below, only the parts that differ from the first embodiment will be described, and for the other parts, the description of the electrolysis device according to the first embodiment can be used as appropriate.

[0172] 14 differs from the electrolysis device 1 shown in Fig. 1 in that it further includes a cooler 403 in the cathode discharge section 400, further includes valves 503 and 504 in the cooling section 500, and further includes a flow rate controller 605 and a discharge flow path P10 in the circulation section 600. The explanation of the second embodiment can be used as appropriate for the explanation of the cooler 403 and the circulation flow path P10.

[0173] The flow rate controller 605 is provided midway along the discharge flow path P10. The flow rate controller 605 can control the flow rate of the anode condensed water supplied from the discharge flow path P10 to the humidifier 302. Note that cathode condensed water may also be supplied to the humidifier 302 from the discharge flow path P10 together with the anode condensed water.

[0174] Valve 503 is provided midway through circulation flow path P8, which connects humidifier 302 and condensed water collector 502. Valve 504 is provided midway through supply flow path P9, which connects condensed water collector 502 and an inlet of cooling flow path 141, and upstream of cooler 403. By opening valve 503 and closing valve 504, anode condensed water and / or cathode condensed water can be supplied to heat exchanger 601 to exchange heat with anode wastewater. By closing valve 503 and opening valve 504, anode condensed water and / or cathode condensed water can be supplied to cooling flow path 141 to cool the electrolytic cell or anode solution. Without being limited thereto, anode condensed water and / or cathode condensed water may be supplied to heat exchanger 601 and cooling flow path 141 by opening valves 503 and 504. Furthermore, the configuration is not limited to that shown in FIG. 14, and the anode condensed water may be supplied to the heat exchanger 601 and the cathode condensed water may be supplied to the cooling passage 141.

[0175] As in the first embodiment, the control device 701 transmits control signals to, for example, the flow rate controller 202, the valve 402, the flow rate controller 602, the flow rate controller 605, the valve 503, and the valve 504 based on the analysis results of the detection signals, thereby enabling the flow rate controller 202 to adjust the flow rate of the anode solution, the valve 402 to adjust the flow rate of the cathode effluent returned to the anode collector 201, and the valves 503, 504, the flow rate controller 602, and the flow rate controller 605 to select the supply destination and adjust the flow rate of the anode condensed water and the cathode condensed water. The control device 701 allows the electrolysis device 1 to be operated by freely setting objectives such as improved cell output, low-cost operation, and long-life operation. Furthermore, the degree of freedom in adjusting the concentration and amount of the electrolyte is improved, enabling stable operation over long periods of time.

[0176] As described above, the electrolysis device of the eighth embodiment uses and circulates anode condensed water and / or cathode condensed water for cooling the electrolysis cell and the anode effluent, thereby reducing and circulating the amount of water discharged from the entire reaction system of the electrolysis device, and enabling the electrolysis device to be operated without externally supplying water to the electrolysis device.

[0177] This embodiment can be combined with other embodiments as appropriate. [Example]

[0178] Example 1 The electrolysis device shown in Figure 1 was assembled to investigate the electrolysis performance of carbon dioxide. First, a cathode 121 was prepared by coating carbon particles carrying gold nanoparticles on carbon paper with a porous layer, using the following procedure. A coating solution was prepared by mixing carbon particles carrying gold nanoparticles with pure water, Nafion solution, and ethylene glycol. The average particle size of the gold nanoparticles was 8.7 nm, and the loading amount was 18.9 mass%. This coating solution was filled into an airbrush and spray-coated onto the carbon paper with a porous layer using nitrogen gas. After coating, the carbon paper was washed with running pure water for 30 minutes and then immersed in hydrogen peroxide to oxidize and remove organic substances such as ethylene glycol. This was cut into a 10 cm x 10 cm piece to prepare the cathode 121. The amount of gold coated was approximately 0.4 mg / cm, based on the mixed amount of gold nanoparticles and carbon particles in the coating solution. 2 It was estimated that the anode 111 was an electrode made of Ti mesh coated with IrO2 nanoparticles as an anode catalyst. The IrO2 / Ti mesh electrode was cut into a 10cm x 10cm size and used as the anode 111.

[0179] The electrolysis unit 100 has a catalytic area of ​​100 cm 2 , current density 200mA / cm 2A cooling channel 141 was formed in a stack of 10 electrolysis cells, and an electrolysis reaction was performed. The thickness of one electrolysis cell was 2 mm. The thickness of the channel plate 153 having the cooling channel 141 was 6 mm. The depth of the anode channel 112 was 1.0 mm. The depth of the cooling channel 141 was 5 mm.

[0180] The clamping plate was not provided with a cooling flow channel, and the clamping plate, insulating plate, 1 mm current collecting plate, a stack of flow channel plate 153 with cooling flow channel 141 and electrolytic cell, 1 mm current collecting plate, insulating plate, and clamping plate were stacked in this order.

[0181] An electrolysis device was assembled using the electrolysis unit 100 described above and operated under the following conditions: An electrolyte solution of potassium bicarbonate aqueous solution (concentration: 0.1 M KHCO3) was supplied to the anode flow channel 112 at a flow rate of 10 ccm per electrolysis cell. Current density: 200 mA / cm 2 The electrolytic solution cooled to a temperature of 25° C. was flowed through the anode flow channel 112 at a flow rate of 2.5 ccm / cell to cause a reaction.

[0182] Cooling water was flowed from an external cooling water supply source through the cooling flow path 141 so that the temperature of the electrolytic cell was in the range of 50° C. to 60° C. Water at a temperature of 25° C. was flowed as the cooling water, and the temperature was controlled by adjusting the flow rate.

[0183] Carbon dioxide gas was supplied to the cathode flow path 122 at a flow rate of 500 sccm per electrolysis cell. The carbon dioxide gas was humidified through a humidifier 302. The carbon dioxide gas supplied to the humidifier 302 was humidified by bubbling it into hot water. The entire humidifier 302 was kept warm, and the temperature of the carbon dioxide gas was controlled by the temperature of the humidifier 302 and the hot water before being supplied to the electrolysis unit 100. The temperature of the humidified carbon dioxide gas was controlled to be lower than the temperature of the electrolysis cell, within a range of 40°C to 50°C.

[0184] A first glass bottle with a volume of 1 L was installed as the cathode collector 401, and the liquid (cathode effluent) was separated from the generated CO and unreacted CO gas (cathode exhaust). A portion of the cathode exhaust was collected, and the amount of carbon monoxide or hydrogen gas produced by the carbon dioxide reduction reaction or water reduction reaction was analyzed using a gas chromatograph. The control unit 700 calculated the partial current density of carbon monoxide and hydrogen from the amount of gas produced, as well as the Faraday efficiency, which is the ratio of the total current density to the partial current density. The results are shown in Table 1. Table 1 shows the cell voltage, cell resistance, Faraday efficiency of carbon monoxide (FE(CO)), and Faraday efficiency of hydrogen (FE(H2)). Note that the sum of FE(CO) and FE(H2) may exceed 100% due to measurement errors caused by factors such as flow rate.

[0185] A second glass bottle with a volume of 5 L was installed as an anode collector 201 to separate the anode effluent and the anode exhaust. The separated anode exhaust was cooled, and the water vapor was condensed to generate anode condensed water, which was then captured in a third glass bottle with a volume of 1 L as a condensed water collector 502.

[0186] The third glass bottle was connected to a humidifier 302 via a heat exchanger by piping, and the anode condensed water stored in the third glass bottle was pumped. A heat exchanger was also connected between the anode collector 201 and the electrolysis cell, and heat was exchanged between the anode condensed water in the third glass bottle and the high-temperature anode effluent from the anode collector 201, thereby cooling the anode effluent. The anode condensed water in the third glass bottle was supplied by a pump at regular intervals when the anode condensed water had accumulated. Furthermore, a current of 200 mA / cm 2 The electrolysis device 1 was operated at a current density of 1000 kJ / min.

[0187] During operation of the pump to move the anode condensate from the third vial, the temperature of the third vial is 18°C, and the temperature of the anode condensate supplied to the humidifier 302 ( Flowing through the circulation flow path P8 from the heat exchanger 601 to the humidifier 302 The temperature of the anode condensed water was 35° C. At this time, the flow rate of the cooling water flowing through the cooling flow passage 141 was reduced from an average of about 20 cc / min to 5 cc / min.

[0188] The potassium concentration in the anode effluent in the anode collector 201 and the increase / decrease in the anode effluent were measured at regular intervals. The results of the potassium concentration in the anode effluent and the increase / decrease in the anode effluent are shown in Table 1. As the operation time progressed, the increase / decrease in the anode effluent (increase in the anode effluent) increased, and the reaction could not be operated unless the anode effluent was drained from the anode collector 201, so the reaction was stopped after 400 hours.

[0189] (Comparative Example 1) A cooler was installed between the outlet of the anode flow path 112 of the electrolysis cell and the anode collector 201. A third glass bottle was not installed, and the anode exhaust was discharged directly from the anode collector 201. There was no mechanism for supplying water or electrolyte to the humidifier 302. The rest was the same as in Example 1. The results are shown in Table 1.

[0190] 200mA / cm 2 During operation at a current density of 1000 kJ / s, the temperature of the anode effluent in the anode collector 201 was 55°C. At this time, the flow rate of the cooling water flowing through the cooling flow path 141 was constantly kept at about 20±5 cc / min. Table 1 shows the potassium concentration in the anode effluent and the increase / decrease in the anode effluent. As operation time progressed, the increase / decrease in the anode effluent (increase in the anode effluent) increased, and the system could not operate unless it was drained from the anode collector 201, so the reaction was stopped after 250 hours.

[0191] (Comparative Example 2) A cooler was installed between the outlet of the anode flow path 112 of the electrolysis cell and the anode collector 201. Anode condensed water was supplied from a third glass bottle to the humidifier 302 at regular intervals. The rest of the experiment was the same as in Example 1. The results are shown in Table 1.

[0192] 200mA / cm 2During operation at a current density of 1000 kJ / s, the temperature of the anode effluent in the anode collector 201 was 55°C. At this time, the flow rate of the cooling water flowing through the cooling flow path 141 was constantly kept at about 20±5 cc / min. Table 1 shows the potassium concentration in the anode effluent and the increase / decrease in the anode effluent. As operation time progressed, the increase / decrease in the anode effluent (increase in the anode effluent) increased, and the system could not operate unless it was drained from the anode collector 201, so the reaction was stopped after 250 hours.

[0193] (Comparative Example 3) A cooler was installed midway through the circulation flow path P7, and the anode effluent was cooled to carry out the reaction. The rest of the procedure was the same as in Example 1. The results are shown in Table 1. As operation time progressed, the amount of hot water lost from the humidifier 302 increased, making humidification impossible. Also, the amount of anode effluent increase / decrease increased (anode effluent increased), and operation was not possible unless drainage was carried out from the anode collector 201. Therefore, the reaction was stopped after 210 hours.

[0194] Example 2 The first glass bottle and the second glass bottle were connected by a pipe, and a pump was connected midway through the pipe to move the cathode effluent to the anode collector 201. The rest of the procedure was the same as in Example 1. The results are shown in Table 1.

[0195] When the pump moving the anode condensate from the third glass bottle was operating, the temperature of the third glass bottle was 18°C, and the temperature of the anode condensate supplied to the humidifier 302 was 35°C. At this time, the flow rate of the cooling water flowing through the cooling flow path 141 decreased from an average of approximately 20 cc / min to 5 cc / min. The potassium concentration in the anode effluent in the anode collector 201 and the increase / decrease in the anode effluent were measured at regular intervals. The results of the potassium concentration in the anode effluent and the increase / decrease (increase) in the anode effluent are shown in Table 1. In Example 2, operation could be continued for up to 500 hours.

[0196] Example 3 A cooler was installed to cool the cathode exhaust gas discharged from the first glass bottle, and the water vapor was condensed to produce cathode condensed water, which was captured in a fourth glass bottle with a volume of 1 L. The cooler had a double pipe, with cooling water flowing through the outer pipe and cathode exhaust gas flowing through the inner pipe.

[0197] A fourth glass bottle was connected to the outer pipe of the cooler. Furthermore, the outlet of the outer pipe was connected to the inlet of the cooling channel 141, and cathode condensed water was supplied to the cooling channel 141. The cathode exhaust and the cathode condensed water heated by the electrolysis cell were supplied to the humidifier 302 by a pump at regular intervals. The rest of the procedure was the same as in Example 1. The results are shown in Table 1.

[0198] When the pump moving the anode condensate in the third glass bottle was operating, the temperature of the third glass bottle was 18°C, and the temperature of the anode condensate supplied to the humidifier 302 was 40°C. At this time, the flow rate of the cooling water flowing through the cooling flow path 141 decreased from an average of approximately 20 cc / min to 5 cc / min. The potassium concentration in the anode effluent in the anode collector 201 and the increase / decrease in the anode effluent were measured at regular intervals. The results of the potassium concentration in the anode effluent and the increase / decrease (increase) in the anode effluent are shown in Table 1. In Example 3, operation could be continued for up to 500 hours.

[0199] Example 4 A second glass bottle with a volume of 5 L was installed as an anode collector 201 to separate the anode effluent from the anode exhaust. The anode exhaust was cooled to condense the water vapor to generate anode condensed water, which was then captured in a third glass bottle with a volume of 1 L. A cooler was installed in the third glass bottle to cool the anode condensed water inside. The temperature of the anode condensed water inside was controlled at 18°C ​​± 1°C.

[0200] A first glass bottle with a volume of 5 L was installed as a cathode collector 401 to separate the cathode effluent from the cathode exhaust. The water vapor in the cathode exhaust was condensed using a cooler to produce cathode condensed water, which was captured in a fourth glass bottle with a volume of 1 L. The cooler had a double pipe, with cooling water flowing through the outer pipe and the cathode exhaust flowing through the inner pipe.

[0201] A portion of the anode condensed water stored in the third glass bottle was supplied via piping to the cathode exhaust cooling pipe, and another portion was supplied to the cooling flow path 141. The remainder was supplied to the discharge flow path P10. The three cooling water connections were switchable using valves. When the electrolytic cell temperature was high, more cooling water was supplied to the electrolytic cell, and when the electrolytic cell temperature was low, less cooling water was supplied to the electrolytic cell, controlling the temperature of the electrolytic cell to be between 50°C and 60°C. The cathode exhaust temperature was controlled to approximately 20°C. When both the electrolytic cell and cathode exhaust were high temperatures, the anode condensed water was supplied to the discharge flow path P10. A portion of the anode condensed water was pumped from the discharge flow path P10 to the humidifier 302, and the remainder was supplied to the third glass bottle using piping and a valve. The destination of the anode condensed water was controlled using a water level gauge in the third glass bottle and a water level gauge in the humidifier 302. The rest of the experiment was the same as in Example 1. The results are shown in Table 1.

[0202] The temperature of the anode condensed water supplied to the humidifier 302 was 38°C. At this time, the flow rate of the cooling water flowing through the cooling flow path 141 was constantly about 3±2 cc / min. The potassium concentration in the anode effluent in the anode collector 201 and the increase / decrease (increase) in the anode effluent were measured at regular intervals. The results of the potassium concentration in the anode effluent and the increase / decrease in the anode effluent are shown in Table 1. In Example 4, operation could be continued for up to 500 hours.

[0203] The results of Examples 1, 2, 3, and 4 and Comparative Examples 1, 2, and 3 show that by generating anode condensed water and cathode condensed water and exchanging heat between these condensed waters and the anode solution or anode effluent, it is possible to suppress an increase in the anode effluent and to suppress a decrease in electrolysis efficiency that accompanies an increase in operation time.

[0204] [Table 1]

[0205] The configurations of the above-described embodiments can be applied in combination with each other, and some of them can be replaced with other configurations. Although several embodiments of the present invention have been described herein, these embodiments are presented as examples and are not intended to limit the scope of the invention. These embodiments can be implemented in various other forms, and various omissions, substitutions, modifications, etc. can be made without departing from the spirit of the invention. These embodiments and their modifications are intended to be included within the scope and spirit of the invention, as well as within the scope of the invention and its equivalents as set forth in the claims.

[0206] The above embodiments can be summarized in the following technical solutions. (Technical proposal 1) an anode that oxidizes a first substance to produce an oxidation product; a cathode that reduces a second substance to produce a reduction product; an anode flow channel facing the anode; a cathode flow path facing the cathode; an anode supply flow path connected to an inlet of the anode flow path and supplying an anode solution containing the first substance to the anode flow path; an anode discharge flow path through which an anode fluid containing the anode solution and the oxidation product flows and which is discharged from an outlet of the anode flow path; a cathode gas supply source that supplies a cathode gas containing the second substance; a humidifier for humidifying the cathode gas; a cathode supply flow path connected to an inlet of the cathode flow path and supplying the humidified cathode gas to the cathode flow path; a cathode discharge flow path through which a cathode fluid discharged from an outlet of the cathode flow path and containing the cathode gas and the reduction product flows; an anode collector that separates the anode fluid supplied from the anode discharge flow path into an anode effluent containing the anode solution and an anode exhaust containing the oxidation product; a first cooler that cools the anode exhaust gas supplied from the anode collector to condense first water vapor contained in the anode exhaust gas to generate anode condensed water; a condensate collector for receiving the anode condensate; a first flow path connecting the anode collector and the anode supply flow path, through which the anode solution flows from the anode collector to the anode supply flow path; a second flow path connecting the condensed water collector and the humidifier, through which the anode condensed water flows from the condensed water collector to the humidifier; a first heat exchange structure that performs heat exchange between the anode solution flowing through the first flow path and the anode condensate flowing through the second flow path; An electrolysis device comprising: (Technical proposal 2) an anode that oxidizes a first substance to produce an oxidation product; a cathode that reduces a second substance to produce a reduction product; an anode flow channel facing the anode; a cathode flow path facing the cathode; an anode supply flow path connected to an inlet of the anode flow path and supplying an anode solution containing the first substance to the anode flow path; an anode discharge flow path through which an anode fluid containing the anode solution and the oxidation product flows and which is discharged from an outlet of the anode flow path; a cathode gas supply source that supplies a cathode gas containing the second substance; a humidifier for humidifying the cathode gas; a cathode supply flow path connected to an inlet of the cathode flow path and supplying the humidified cathode gas to the cathode flow path; a cathode discharge flow path through which a cathode fluid discharged from an outlet of the cathode flow path and containing the cathode gas and the reduction product flows; an anode collector that separates the anode fluid supplied from the anode discharge flow path into an anode effluent containing the anode solution and an anode exhaust containing the oxidation product; a first cooler that cools the anode exhaust supplied from the anode collector and condenses first water vapor contained in the anode exhaust to generate anode condensed water; a condensate collector for receiving the anode condensate; a first flow path connecting the anode collector and the anode supply flow path, through which the anode solution flows from the anode collector to the anode supply flow path; a second cooler that cools the anode condensate supplied from the condensate collector; a cooling flow path that is disposed opposite the anode flow path or the cathode flow path and through which the anode condensed water supplied via the second cooler flows; a third flow path that connects an outlet of the cooling flow path and the humidifier, and through which the anode condensed water flows from the cooling flow path to the humidifier; a second heat exchange structure that performs heat exchange between the anode solution flowing through the anode flow path and the anode condensate flowing through the cooling flow path; An electrolysis device comprising: (Technical proposal 3) a cathode collector that separates the cathode fluid supplied from the cathode discharge flow path into a cathode effluent containing the anode solution and a cathode exhaust containing the reduction product, the second cooler cools the cathode exhaust gas to condense second water vapor contained in the cathode exhaust gas to generate cathode condensed water; The electrolysis device according to Technical Solution 2, wherein the cathode condensed water supplied via the second cooler flows through the cooling flow path together with the anode condensed water. (Technical proposal 4) The electrolysis device according to Technical Solution 3 further comprises a fourth flow path through which the cathode wastewater flows and is supplied from the cathode collector to the anode collector. (Technical proposal 5) a fifth flow path through which the anode condensate flows and is supplied from the condensate collector to the second cooler; The electrolysis apparatus according to Technical Scheme 3 or 4, wherein the second cooler cools the cathode exhaust gas using the anode condensate. (Technical proposal 6) the condensate collector has a third cooler that cools the anode condensate, The electrolysis device according to any one of Technical Schemes 1 to 5, wherein the first cooler cools the anode exhaust gas using the anode condensed water cooled by the third cooler. (Technical proposal 7) The electrolysis apparatus according to any one of Technical Schemes 2 to 6, wherein the first cooler is provided in the condensed water collector. (Technical proposal 8) a flow rate controller for controlling the flow rate of the anode condensed water supplied to the humidifier; a first detector that is provided in the humidifier, that is housed in the humidifier, that detects the level of the hot water containing the anode condensate, and that transmits a first detection signal; The electrolysis apparatus according to any one of Technical Solutions 1 to 7, further comprising: a control device that adjusts the flow rate of the anode condensed water supplied to the humidifier by controlling the flow rate controller based on the first detection signal. (Technical proposal 9) a flow rate controller for controlling the flow rate of the anode condensed water supplied to the humidifier; a first detector that is provided in the humidifier, that is housed in the humidifier, that detects the level of the hot water containing the anode condensate, and that transmits a first detection signal; a control device that adjusts the flow rate of the anode condensed water supplied to the humidifier by controlling the flow rate controller based on the first detection signal; a sixth flow path connecting the third flow path and the condensate collector; a first valve provided midway along the sixth flow path; a second valve provided midway along the third flow path; a second detector that detects the water level of the anode condensate contained in the condensate collector and transmits a second detection signal; The electrolysis apparatus according to any one of Technical Solutions 2 to 8, wherein the control device controls the first valve and the second valve based on the second detection signal to select whether the anode condensate is supplied to the humidifier or the condensate collector. (Technical proposal 10) The electrolysis device according to any one of Technical Schemes 1 to 9, further comprising an electrolyte supply source for replenishing the electrolyte in the anode wastewater contained in the anode collector. (Technical proposal 11) The electrolysis device according to any one of Technical Schemes 1 to 10, further comprising a water supply source for supplying water to the humidifier. [Explanation of symbols]

[0207] 1...Electrolysis device, 100...Electrolysis section, 111...Anode, 112...Anode flow path, 113...Anode current collector, 114...Flow path plate, 121...Cathode, 122...Cathode flow path, 123...Cathode current collector, 124...Flow path plate, 131...Separator, 132...Flow path plate, 141...Cooling flow path, 142...Cooling flow path, 143...Cooling flow path, 150...Power supply, 151... Detector, 152...flow path plate, 153...flow path plate, 200...anode supply unit, 201...anode collector, 202...flow rate controller, 204...pressure controller, 205...flow rate controller, 206...heat exchanger, 207...flow rate controller, 211...detector, 212...electrolyte supply source, 300...cathode supply unit, 301...cathode gas supply source, 302...humidifier, 303...water supply source, 304...flow rate controller, 305...pressure controller, 311...detector, 400...cathode discharge section, 401...cathode collector, 402...valve, 403...cooler, 500...cooling section, 501...cooler, 502...condensate collector, 503...valve, 504...valve, 511...detector, 512...cooler, 513...detector, 600...circulation section, 601...heat exchanger, 602...flow rate controller, 603...valve, 604...valve, 605...flow rate controller, 700...control section, 701...control device, P1...anode supply flow path, P2...anode discharge flow path, P3...cathode supply flow path, P4...cathode discharge flow path, P5...circulation flow path, P6...flow path, P7...circulation flow path, P8...circulation flow path, P9...supply flow path, P10...discharge flow path, P11...supply flow path.

Claims

1. an anode that oxidizes a first substance to produce an oxidation product; a cathode that reduces a second material to produce a reduction product; an anode flow channel facing the anode; a cathode flow path facing the cathode; an anode supply flow path connected to an inlet of the anode flow path and configured to supply an anode solution containing the first substance to the anode flow path; an anode discharge flow path through which an anode fluid containing the anode solution and the oxidation product flows and which is discharged from an outlet of the anode flow path; a cathode gas supply source that supplies a cathode gas containing the second substance; a humidifier for humidifying the cathode gas; a cathode supply flow path connected to an inlet of the cathode flow path and supplying the humidified cathode gas to the cathode flow path; a cathode discharge flow path through which a cathode fluid discharged from an outlet of the cathode flow path and containing the cathode gas and the reduction product flows; an anode collector that separates the anode fluid supplied from the anode discharge flow path into an anode effluent containing the anode solution and an anode exhaust containing the oxidation product; a first cooler that cools the anode exhaust gas supplied from the anode collector and condenses first water vapor contained in the anode exhaust gas to generate anode condensed water; a condensate collector for receiving the anode condensate; a first flow path connecting the anode collector and the anode supply flow path, through which the anode effluent flows from the anode collector to the anode supply flow path; a second flow path connecting the condensed water collector and the humidifier, through which the anode condensed water flows from the condensed water collector to the humidifier; a first heat exchange structure that performs heat exchange between the anode solution flowing through the first flow path and the anode condensate flowing through the second flow path; Equipped with An electrolysis device comprising no coolers provided midway along the anode exhaust flow path and midway along the first flow path.

2. an anode that oxidizes a first substance to produce an oxidation product; a cathode that reduces a second material to produce a reduction product; an anode flow channel facing the anode; a cathode flow path facing the cathode; an anode supply flow path connected to an inlet of the anode flow path and configured to supply an anode solution containing the first substance to the anode flow path; an anode discharge flow path through which an anode fluid containing the anode solution and the oxidation product flows and which is discharged from an outlet of the anode flow path; a cathode gas supply source that supplies a cathode gas containing the second substance; a humidifier for humidifying the cathode gas; a cathode supply flow path connected to an inlet of the cathode flow path and supplying the humidified cathode gas to the cathode flow path; a cathode discharge flow path through which a cathode fluid discharged from an outlet of the cathode flow path and containing the cathode gas and the reduction product flows; an anode collector that separates the anode fluid supplied from the anode discharge flow path into an anode effluent containing the anode solution and an anode exhaust containing the oxidation product; a first cooler that cools the anode exhaust gas supplied from the anode collector and condenses first water vapor contained in the anode exhaust gas to generate anode condensed water; a condensate collector for receiving the anode condensate; a first flow path connecting the anode collector and the anode supply flow path, through which the anode effluent flows from the anode collector to the anode supply flow path; a second cooler that cools the anode condensate supplied from the condensate collector; a cooling flow path disposed opposite the anode flow path or the cathode flow path, through which the anode condensed water supplied via the second cooler flows; a third flow path connecting an outlet of the cooling flow path and the humidifier, through which the anode condensed water flows from the cooling flow path to the humidifier; a second heat exchange structure that exchanges heat between the anode solution flowing through the anode flow path and the anode condensate flowing through the cooling flow path; Equipped with An electrolysis device comprising no coolers provided midway along the anode exhaust flow path and midway along the first flow path.

3. a cathode collector that separates the cathode fluid supplied from the cathode discharge flow path into a cathode effluent containing the anode solution and a cathode exhaust containing the reduction product, the second cooler cools the cathode exhaust gas to condense second water vapor contained in the cathode exhaust gas to generate cathode condensed water; The electrolysis device according to claim 2 , wherein the cathode condensed water supplied via the second cooler flows together with the anode condensed water through the cooling flow path.

4. 4. The electrolysis device according to claim 3, further comprising a fourth flow path through which the cathode effluent flows to be supplied from the cathode collector to the anode collector.

5. a fifth flow path through which the anode condensate flows, the anode condensate being supplied from the condensate collector to the second cooler; The electrolysis apparatus according to claim 3 , wherein the second cooler cools the cathode exhaust gas using the anode condensed water.

6. the condensate collector includes a third cooler that cools the anode condensate; 5. The electrolysis device according to claim 1, wherein the first cooler cools the anode exhaust gas by using the anode condensed water cooled by the third cooler.

7. 5. The electrolysis apparatus according to claim 2, wherein the first cooler is provided in the condensed water collector.

8. a flow rate controller for controlling the flow rate of the anode condensed water supplied to the humidifier; a first detector provided in the humidifier, configured to detect a water level of the hot water contained in the humidifier and including the anode condensed water, and to transmit a first detection signal; 5. The electrolysis apparatus according to claim 1, further comprising: a control device that adjusts the flow rate of the anode condensed water supplied to the humidifier by controlling the flow rate controller based on the first detection signal.

9. a flow rate controller for controlling the flow rate of the anode condensed water supplied to the humidifier; a first detector that is provided in the humidifier, that is housed in the humidifier, that detects the level of the hot water containing the anode condensate, and that transmits a first detection signal; a control device that adjusts the flow rate of the anode condensed water supplied to the humidifier by controlling the flow rate controller based on the first detection signal; a sixth flow path connecting the third flow path and the condensate collector; a first valve provided midway along the sixth flow path; a second valve provided midway along the third flow path; a second detector that detects the water level of the anode condensate contained in the condensate collector and transmits a second detection signal; 5. The electrolysis apparatus according to claim 2, wherein the control device controls the first valve and the second valve based on the second detection signal to select whether the anode condensate is supplied to the humidifier or the condensate collector.

10. 5. The electrolysis apparatus according to claim 1, further comprising an electrolyte supply source that replenishes the anode wastewater contained in the anode collector with an electrolyte.

11. 5. The electrolysis device according to claim 1, further comprising a water supply source that supplies water to the humidifier.

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