CN110938834B

CN110938834B - Method for manufacturing electrolytic cell

Info

Publication number: CN110938834B
Application number: CN201910880508.8A
Authority: CN
Inventors: 船川明恭; 角佳典
Original assignee: Asahi Kasei Corp
Current assignee: Asahi Kasei Corp
Priority date: 2018-09-21
Filing date: 2019-09-18
Publication date: 2022-06-07
Anticipated expiration: 2039-09-18
Also published as: JP7173806B2; CN110938834A; JP2020045547A

Abstract

The present invention has been made to solve the above problems, and an object of the present invention is to provide a method for manufacturing an electrolytic cell, which can improve the work efficiency in the electrode renewal in the electrolytic cell. A method for manufacturing a new electrolytic cell by disposing a new laminate including a new electrode for electrolysis and a new separator in an existing electrolytic cell including an anode, a cathode facing the anode, and an existing laminate including an electrode for electrolysis and a separator, the existing laminate being disposed between the anode and the cathode, wherein the method comprises: removing the existing layered body from the existing electrolytic bath; and disposing the new layer between the anode and the cathode.

Description

Method for manufacturing electrolytic cell

Technical Field

The present invention relates to a method for manufacturing an electrolytic cell.

Background

In electrolysis of an aqueous solution of an alkali metal chloride such as a salt solution or electrolysis of water (hereinafter collectively referred to as "electrolysis"), a method using an electrolytic cell provided with a diaphragm, more specifically, an ion exchange membrane or a microporous membrane is used. The electrolytic cell is provided with a large number of electrolytic cells connected in series in its interior in many cases. Electrolysis is performed with a diaphragm interposed between the electrolytic cells. In the electrolytic cell, a cathode chamber having a cathode and an anode chamber having an anode are arranged back to back with a partition wall (back plate) interposed therebetween or pressed by a pressing pressure, a bolt fastening, or the like.

Conventionally, anodes and cathodes used in these electrolytic cells are fixed to anode chambers and cathode chambers of the respective electrolytic cells by welding, sandwiching, or the like, and then stored and transported to customers. On the other hand, the separator is stored in a state in which it is wound around a pipe or the like made of vinyl chloride (polyvinyl chloride) alone, and is transported to a customer. At the customer site, the cell is assembled by arranging the cells on the frame of the cell, sandwiching the membrane between the cells. The manufacturing of the cell and the assembly of the cell at the customer site are carried out in this way. As a structure applicable to such an electrolytic cell, patent documents 1 and 2 disclose a structure in which a separator and an electrode are integrated.

Documents of the prior art

Patent document

Patent document 1: japanese laid-open patent publication No. 58-048686

Patent document 2: japanese laid-open patent publication No. 55-148775

Disclosure of Invention

Technical problem to be solved by the invention

When the electrolysis operation is started and continued, various factors deteriorate the respective members, the electrolysis performance is lowered, and the respective members are replaced at a certain time. The membrane can be relatively simply renewed by withdrawing it from the cell compartment and inserting a new membrane. On the other hand, since the anode and the cathode are fixed to the electrolytic cell, there is a problem that, when the electrode is renewed, the electrolytic cell is taken out from the electrolytic cell, transported to a dedicated renewal plant, fixed by welding or the like, and the old electrode is peeled off, and thereafter, the new electrode is installed, fixed by welding, transported to the electrolysis plant, and returned to the electrolytic cell, thereby causing such a very complicated operation. In the above-described recent development, a structure in which the separator and the electrode are integrated by thermocompression bonding is considered, but the structure can be relatively easily manufactured at a laboratory level, but cannot be easily manufactured according to an actual commercial size of an electrolytic cell (for example, 1.5m in length and 3m in width). In addition, even when this structure is used, the above-mentioned complicated operation cannot be avoided.

The present invention has been made in view of the above problems of the prior art, and an object of the present invention is to provide a method for manufacturing an electrolytic cell, which can improve the operation efficiency in the electrode renewal in the electrolytic cell.

Means for solving the problems

The present inventors have made extensive studies to solve the above-mentioned problems, and as a result, have found that the above-mentioned problems can be solved by removing an existing laminate including an existing electrode and an existing separator in an existing electrolytic cell and disposing a new laminate including a new electrode for electrolysis and a new separator instead of the existing laminate, and have completed the present invention.

That is, the present invention includes the following aspects.

[1]

A method for manufacturing a new electrolytic cell by arranging a new laminate including a new electrode for electrolysis and a new separator in an existing electrolytic cell including an anode, a cathode facing the anode, and an existing laminate including an electrode for electrolysis and a separator, the existing laminate being arranged between the anode and the cathode,

wherein the manufacturing method comprises the following steps:

a step of removing the existing layered body from the existing electrolytic bath, and

And disposing the new layer between the anode and the cathode.

[2]

The method of producing an electrolytic cell as recited in [1], wherein the electrolysis electrode comprises an anode electrolysis electrode (A1) and a cathode electrolysis electrode (B1) in the conventional laminate.

[3]

The method of producing an electrolytic cell according to [1] or [2], wherein the new electrolysis electrode comprises an anode electrolysis electrode (A2) and a cathode electrolysis electrode (B2) in the new laminate.

ADVANTAGEOUS EFFECTS OF INVENTION

According to the method for manufacturing an electrolytic cell of the present invention, the work efficiency in the electrode renewal in the electrolytic cell can be improved.

Drawings

Figure 1 is a schematic cross-sectional view of an electrolytic cell.

Fig. 2 is a schematic sectional view showing a state where two electrolytic cells are connected in series.

FIG. 3 is a schematic view of an electrolytic cell.

FIG. 4 is a schematic perspective view showing an assembly process of the electrolytic cell.

Fig. 5 is a schematic sectional view of a reverse current absorber that the electrolytic cell may be provided with.

FIG. 6 is a schematic cross-sectional view of an electrode for electrolysis in one embodiment of the present invention.

FIG. 7 is a schematic sectional view illustrating one embodiment of an ion exchange membrane.

Fig. 8 is a schematic diagram for explaining the aperture ratio of the reinforcing core material constituting the ion exchange membrane.

FIG. 9 is a schematic view for explaining a method of forming communicating holes of an ion exchange membrane.

Description of the figures

Description of the symbols in FIGS. 1-5

4 … electrolytic cell, 5 … pressurizer, 6 … cathode terminal, 7 … anode terminal,

11 … anode, 12 … anode pad, 13 … cathode pad,

18 … reverse current absorber, 18a … base material, 18b … reverse current absorbing layer, 19 … anode chamber bottom,

21 … cathode, 22 … metal elastomer, 23 … current collector, 24 … support,

A 50 … electrolytic cell, a 60 … anode chamber, a 51 … ion exchange membrane (diaphragm), a 70 … cathode chamber,

80 … partition wall, 90 … cathode structure for electrolysis

Description of symbols for FIG. 6

10 … explanation of the base material of the electrolysis electrode, 20 … covering the first layer of the base material, 30 … second layer, 101 … of the electrolysis electrode with respect to the symbol of FIG. 7

1 … ion exchange membrane, 1a … membrane main body, 2 … carboxylic acid layer, 3 … sulfonic acid layer, 4 … reinforced core material, 11a,11b … coating layer,

Description of symbols for FIG. 8

21a,21b … reinforced core material

Description of symbols (a) and (b) in FIG. 9

52 … reinforcing wire, 504 … communicating hole, 504a … sacrificial wire

Detailed Description

Hereinafter, embodiments of the present invention (hereinafter also referred to as the present embodiments) will be described in detail with reference to the drawings as necessary. The following embodiments are examples for illustrating the present invention, and the present invention is not limited to the following. The drawings show an example of the embodiment, but the embodiment is not limited to this. The present invention can be suitably modified within the scope of the gist thereof. The positional relationship such as up, down, left, right, and the like in the drawings is based on the positional relationship shown in the drawings unless otherwise specified. The dimensions and proportions of the drawings are not limited to those shown.

[ method of manufacturing electrolytic cell ]

A method for manufacturing an electrolytic cell according to the present embodiment is a method for manufacturing a new electrolytic cell by disposing a new laminate including a new electrode for electrolysis and a new separator in an existing electrolytic cell including an anode, a cathode facing the anode, and an existing laminate including an electrode for electrolysis and a separator, the existing laminate being disposed between the anode and the cathode, wherein the method includes: a step of removing the existing layered body from the existing electrolytic bath (hereinafter also simply referred to as "step (a)"); and a step (hereinafter, also simply referred to as "step (B)") of disposing the new laminate between the anode and the cathode.

As described above, according to the method of manufacturing an electrolytic cell of the present embodiment, since the existing electrolytic cell includes the existing laminate including the electrode for electrolysis and the separator as the replaceable component, and the component in the electrolytic cell can be replaced by replacing the laminate itself, it is not necessary to perform complicated operations such as taking out the electrolytic cell, carrying out, removing the old electrode, installing and fixing the new electrode, and transporting and installing the new electrode in the electrolytic cell, and it is possible to improve the work efficiency when the component in the electrolytic cell is replaced.

In the present embodiment, the existing electrolytic cell includes, as constituent members, an anode, a cathode facing the anode, and an existing laminate disposed between the anode and the cathode and including an electrode for electrolysis and a separator, in other words, the existing electrolytic cell includes an electrolytic cell. The existing electrolytic cell is not particularly limited as long as it includes the above-described components, and various known configurations can be applied. In the case where the anode in the existing electrolytic cell is in contact with the electrolysis electrode, the cell substantially functions as a power feeder; when not in contact with the electrolysis electrode, the electrode itself functions as an anode. Similarly, when the cathode in the existing electrolytic cell is in contact with the electrolysis electrode, it substantially functions as a power feeder; when not in contact with the electrolysis electrode, the electrode itself functions as a cathode. Here, the power supply means an electrode that has deteriorated (i.e., an existing electrode), an electrode that is not coated with a catalyst, or the like.

In the present embodiment, the new electrolytic cell is provided with a new laminate including a new electrode for electrolysis and a new separator, in addition to a member that functions as an anode or a cathode in the existing electrolytic cell. That is, the "new electrolysis electrode" provided at the time of manufacturing the new electrolytic cell functions as an anode or a cathode, and is separated from the cathode and the anode in the existing electrolytic cell. In the present embodiment, even when the electrolysis performance of the electrolysis electrode functioning as the anode and/or the cathode deteriorates with the operation of the existing electrolytic cell, the performance of the anode and/or the cathode can be updated by replacing the electrolysis electrode with a new one separate from the former one. Further, since a new separator constituting a new laminate is also provided, the performance of the separator deteriorated with the operation performance can be updated at the same time. The term "renewal performance" as used herein means performance equivalent to or higher than the initial performance of an existing electrolytic cell before operation.

In the present embodiment, the existing electrolytic cell is assumed to be an "electrolytic cell that has already been operated", and the new electrolytic cell is assumed to be an "electrolytic cell that has not been operated". That is, when the electrolytic cell manufactured as a new electrolytic cell is operated, the electrolytic cell becomes "the existing electrolytic cell in the present embodiment", and the electrolytic cell in which the new laminate is disposed in the existing electrolytic cell becomes "the new electrolytic cell in the present embodiment".

Hereinafter, an embodiment of the electrolytic cell will be described in detail by taking a case of performing salt electrolysis using an ion exchange membrane as a diaphragm as an example. However, in the present embodiment, the electrolytic cell is not limited to salt electrolysis, and may be used for water electrolysis or a fuel cell, for example.

In the present description, unless otherwise specified, "electrolytic cell in the present embodiment" is described as including both "existing electrolytic cell in the present embodiment" and "new electrolytic cell in the present embodiment".

The shape, material, and physical properties of the electrolysis electrode in the existing laminate and the new electrolysis electrode in the new laminate may be the same, the shape, material, and physical properties of the separator in the existing laminate and the new separator in the new laminate may be the same, and the shape, material, and physical properties of the existing laminate and the new laminate may be the same. Therefore, unless otherwise specified, the present specification describes the forms of "the electrode for electrolysis in the present embodiment" including "the new electrode for electrolysis in the present embodiment", "the separator in the present embodiment" including "the new separator in the present embodiment", "the laminate in the present embodiment" including "the existing laminate in the present embodiment" and "the new laminate in the present embodiment".

[ electrolytic cell ]

First, an electrolytic cell that can be used as a structural unit of the electrolytic cell in the present embodiment will be described. Figure 1 is a cross-sectional view of an electrolytic cell 50.

The electrolytic cell 50 may be provided with: anode chamber 60, cathode chamber 70, partition 80 provided between anode chamber 60 and cathode chamber 70, anode 11 provided in anode chamber 60, and cathode 21 provided in cathode chamber 70. If necessary, the current collector includes a base material 18a and a reverse current absorbing layer 18b formed on the base material 18a, and may include a reverse current absorber 18 provided in the cathode chamber. The anode 11 and the cathode 21 belonging to 1 electrolytic cell 50 are electrically connected to each other. In other words, the electrolytic cell 50 includes the following cathode structure. The cathode structure 90 includes a cathode chamber 70, a cathode 21 provided in the cathode chamber 70, and a reverse current absorbing body 18 provided in the cathode chamber 70, the reverse current absorbing body 18 includes a base 18a and a reverse current absorbing layer 18b formed on the base 18a as shown in fig. 5, and the cathode 21 is electrically connected to the reverse current absorbing layer 18 b. The cathode chamber 70 further includes a current collector 23, a support 24 for supporting the current collector, and a metal elastic body 22. The metal elastic body 22 is disposed between the current collector 23 and the cathode 21. The support 24 is provided between the current collector 23 and the partition 80. The current collector 23 is electrically connected to the cathode 21 through the metal elastic body 22. The partition 80 is electrically connected to the current collector 23 via the support 24. Therefore, the partition wall 80, the support 24, the current collector 23, the metal elastic body 22, and the cathode 21 are electrically connected. The cathode 21 and the reverse current absorbing layer 18b are electrically connected. The cathode 21 and the reverse current absorbing layer may be directly connected to each other, or may be indirectly connected to each other through a current collector, a support, a metal elastic body, a partition wall, or the like. The entire surface of the cathode 21 is preferably coated with a catalyst layer for reduction reaction. In addition, the electrical connection may be made by: the partition wall 80 is directly attached to the support 24, the support 24 is directly attached to the current collector 23, and the current collector 23 is directly attached to the metal elastic body 22, and the cathode 21 is stacked on the metal elastic body 22. As a method of directly mounting these components to each other, welding and the like are given. The reverse current absorber 18, the cathode 21, and the current collector 23 may be collectively referred to as a cathode structure 90.

FIG. 2 is a cross-sectional view of two adjacent electrolytic cells 50 in the electrolytic bath 4. Figure 3 shows an electrolytic cell 4. Fig. 4 shows an assembly process of the electrolytic cell 4.

As shown in FIG. 2, the electrolytic cell 50, the cation exchange membrane 51, and the electrolytic cell 50 are arranged in series in this order. A cation exchange membrane 51 is disposed between the anode chamber of one 50 and the cathode chamber of the other 50 of the two adjacent electrolytic cells in the electrolytic cell. That is, the anode chamber 60 of the electrolytic cell 50 and the cathode chamber 70 of the electrolytic cell 50 adjacent thereto are separated by the cation exchange membrane 51. As shown in fig. 3, the electrolytic cell 4 is composed of two or more electrolytic cells 50 connected in series via a cation exchange membrane 51. That is, the electrolytic cell 4 is a bipolar type electrolytic cell including two or more electrolytic cells 50 arranged in series and a cation exchange membrane 51 arranged between the adjacent electrolytic cells 50. As shown in fig. 4, the electrolytic cell 4 is assembled by arranging two or more electrolytic cells 50 in series via a cation exchange membrane 51 and connecting them by a pressurizer 5.

The electrolytic cell 4 has an anode terminal 7 and a cathode terminal 6 connected to a power supply. The anode 11 of the electrolytic cell 50 positioned at the endmost portion among two or more electrolytic cells 50 connected in series in the electrolytic cell 4 is electrically connected to the anode terminal 7. The cathode 21 of the electrolytic cell located at the end opposite to the anode terminal 7 among the two or more electrolytic cells 2 connected in series in the electrolytic cell 4 is electrically connected to the cathode terminal 6. The current during electrolysis flows from the anode terminal 7 side to the cathode terminal 6 via the anode and cathode of each electrolytic cell 50. Note that an electrolytic cell having only an anode chamber (anode terminal cell) and an electrolytic cell having only a cathode chamber (cathode terminal cell) may be disposed at both ends of the connected electrolytic cell 50. In this case, the anode terminal 7 is connected to an anode terminal cell disposed at one end thereof, and the cathode terminal 6 is connected to a cathode terminal cell disposed at the other end thereof.

When brine is electrolyzed, brine is supplied to each anode chamber 60, and pure water or a low-concentration sodium hydroxide aqueous solution is supplied to the cathode chamber 70. Each liquid is supplied from an electrolyte supply pipe (not shown) to each electrolytic cell 50 via an electrolyte supply hose (not shown). The electrolyte and the products resulting from the electrolysis are collected by an electrolyte collection tube (not shown). During electrolysis, sodium ions in the brine move from the anode compartment 60 of one cell 50 through the cation exchange membrane 51 and towards the cathode compartment 70 of the adjacent cell 50. Thereby, the current in electrolysis flows in a direction in which the electrolytic cells 50 are connected in series. That is, an electric current flows from anode chamber 60 to cathode chamber 70 through cation exchange membrane 51. With the electrolysis of the brine, chlorine gas is generated on the anode 11 side, and sodium hydroxide (solute) and hydrogen gas are generated on the cathode 21 side.

(Anode case)

The anode chamber 60 has an anode 11 or an anode power supply 11. The power feeder referred to herein means a deteriorated electrode (i.e., an existing electrode), an electrode not coated with a catalyst, or the like. When the electrode for electrolysis in the present embodiment is inserted on the anode side, 11 functions as an anode current-supplying body. When the electrolysis electrode in the present embodiment is not inserted into the anode side, the electrode 11 functions as an anode. In addition, anode chamber 60 preferably has: an anode side electrolyte supply unit for supplying an electrolyte to the anode chamber 60; a baffle plate disposed above the anode-side electrolyte supply unit and substantially parallel to or inclined with respect to the partition wall 80; and an anode-side gas-liquid separation unit disposed above the baffle plate and configured to separate gas from the electrolyte into which the gas is mixed.

(Anode)

In the case where the electrolysis electrode in the present embodiment is not inserted into the anode side, the anode 11 is provided in a frame (i.e., an anode frame) of the anode chamber 60. As the anode 11, a metal electrode such as so-called DSA (registered trademark) can be used. DSA refers to an electrode of a titanium substrate whose surface is coated with an oxide containing ruthenium, iridium, and titanium as components.

As the shape, any of punched metal, nonwoven fabric, foamed metal, expanded metal, metal foil, porous metal foil formed by electroforming, so-called mesh produced by weaving metal wires, and the like can be used.

(Anode power supply body)

When the electrolysis electrode in the present embodiment is inserted into the anode side, the anode feeder 11 is provided in the frame of the anode chamber 60. As the anode current collector 11, a metal electrode such as DSA (registered trademark) or titanium which is not coated with a catalyst may be used. In addition, DSA with a reduced catalyst coating thickness may also be used. In addition, a used anode may be used.

(Anode-side electrolyte supply Unit)

The anode side electrolyte supply unit supplies an electrolyte to the anode chamber 60, and is connected to an electrolyte supply pipe. The anode-side electrolyte supply unit is preferably disposed below the anode chamber 60. As the anode-side electrolyte solution supply unit, for example, a tube (dispersion tube) having an opening formed on the surface thereof can be used. The tube is more preferably arranged parallel to the bottom 19 of the cell along the surface of the anode 11. This pipe is connected to an electrolyte supply pipe (liquid supply nozzle) that supplies electrolyte into the electrolytic cell 50. The electrolytic solution supplied from the liquid supply nozzle is sent into the electrolytic cell 50 through a pipe, and is supplied into the anode chamber 60 from an opening provided on the surface of the pipe. It is preferable to arrange the pipe along the surface of the anode 11 in parallel with the bottom 19 of the electrolytic cell, because the electrolytic solution can be uniformly supplied into the anode chamber 60.

(gas-liquid separator on Anode side)

The gas-liquid separation portion on the anode side is preferably disposed above the baffle plate. In the electrolysis, the anode-side gas-liquid separation section has a function of separating a product gas such as chlorine gas and an electrolytic solution. Unless otherwise specified, the upper direction refers to the upward direction in the electrolytic cell 50 of fig. 1, and the lower direction refers to the downward direction in the electrolytic cell 50 of fig. 1.

During electrolysis, when the generated gas and the electrolytic solution generated in the electrolytic cell 50 are mixed (gas-liquid mixed) and discharged to the outside of the system, vibration may occur due to pressure fluctuation inside the electrolytic cell 50, and physical damage of the ion exchange membrane may be caused. In order to suppress this phenomenon, the electrolytic cell 50 of the present embodiment is preferably provided with an anode-side gas-liquid separation unit for separating gas and liquid. A defoaming plate for defoaming bubbles is preferably provided in the anode-side gas-liquid separation section. When the gas-liquid mixed phase flows through the defoaming plate, bubbles are broken, and the gas-liquid mixed phase can be separated into the electrolyte and the gas. As a result, vibration during electrolysis can be prevented.

(baffle plate)

The baffle plate is preferably disposed above the anode-side electrolyte supply unit and substantially parallel to or inclined with respect to the partition wall 80. The baffle plate is a partition plate that controls the flow of the electrolyte in the anode chamber 60. By providing the baffle plate, the electrolyte (brine, etc.) can be internally circulated in the anode chamber 60, and the concentration thereof can be made uniform. In order to generate the internal circulation, the baffle plate is preferably arranged so as to separate the space near the anode 11 from the space near the partition wall 80. From this point of view, the baffle plate is preferably provided so as to face the respective surfaces of the anode 11 and the partition wall 80. In the space near the anode partitioned by the baffle plate, electrolysis proceeds, whereby the electrolyte concentration (brine concentration) decreases, and a generated gas such as chlorine gas is generated. This causes a difference in specific gravity between the gas and liquid in the space near the anode 11 partitioned by the baffle plate and the space near the partition wall 80. This difference in specific gravity can promote internal circulation of the electrolyte in anode chamber 60, and make the concentration distribution of the electrolyte in anode chamber 60 more uniform.

Although not shown in fig. 1, a current collector may be separately provided inside the anode chamber 60. The current collector may be made of the same material or have the same structure as the current collector of the cathode chamber described later. In the anode chamber 60, the anode 11 itself may function as a current collector.

(next door)

The partition 80 is disposed between the anode chamber 60 and the cathode chamber 70. The partition wall 80 is sometimes called a separator plate, and divides the anode chamber 60 and the cathode chamber 70. As the partition wall 80, a known separator plate for electrolysis can be used, and examples thereof include a partition wall having a cathode side welded with a plate made of nickel and an anode side welded with a plate made of titanium.

(cathode chamber)

In the cathode chamber 70, when the electrode for electrolysis of the present embodiment is inserted on the cathode side, 21 functions as a cathode power supply body; when the electrolysis electrode of the present embodiment is not inserted into the cathode side, 21 functions as a cathode. In the case of having a reverse current absorber, the cathode or cathode power supply 21 is electrically connected to the reverse current absorber. In addition, the cathode chamber 70 also preferably includes a cathode electrolyte supply unit and a cathode gas-liquid separation unit, similarly to the anode chamber 60. Among the parts constituting the cathode chamber 70, the same parts as those constituting the anode chamber 60 are not described.

(cathode)

In the case where the electrolysis electrode of the present embodiment is not inserted into the cathode side, the cathode 21 is provided in the frame (i.e., cathode frame) of the cathode chamber 70. The cathode 21 preferably has a nickel substrate and a catalyst layer coated with the nickel substrate. Examples of the component of the catalyst layer on the nickel base material include metals such as Ru, C, Si, P, S, Al, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Zr, Nb, Mo, Rh, Pd, Ag, Cd, In, Sn, Ta, W, Re, Os, Ir, Pt, Au, Hg, Pb, Bi, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and Lu, and oxides or hydroxides of the metals. Examples of the method for forming the catalyst layer include plating, alloy plating, dispersion-composite plating, CVD, PVD, thermal decomposition, and thermal spraying. These methods may also be combined. The catalyst layer may have two or more layers or two or more elements as necessary. The cathode 21 may be subjected to a reduction treatment as necessary. As the base material of the cathode 21, a base material obtained by plating nickel, a nickel alloy, iron, or stainless steel may be used.

(cathode power supply body)

When the electrode for electrolysis of the present embodiment is inserted into the cathode side, the cathode power supply 21 is provided in the frame of the cathode chamber 70. The cathode power supply body 21 may be coated with a catalyst component. The catalyst component may be a substance that originally used as a cathode and remains. Examples of the component of the catalyst layer include metals such as Ru, C, Si, P, S, Al, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Zr, Nb, Mo, Rh, Pd, Ag, Cd, In, Sn, Ta, W, Re, Os, Ir, Pt, Au, Hg, Pb, Bi, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, and Lu, and oxides or hydroxides of the metals. Examples of the method for forming the catalyst layer include plating, alloy plating, dispersion-composite plating, CVD, PVD, thermal decomposition, and thermal spraying. These methods may also be combined. The catalyst layer may have two or more layers or two or more elements as necessary. Further, a member in which nickel, a nickel alloy, iron, or stainless steel is plated with nickel without being coated with a catalyst may be used. As the base material of the cathode element 21, a base material obtained by plating nickel, a nickel alloy, iron, or stainless steel with nickel may be used.

(reverse current absorbing layer)

As the material of the reverse current absorbing layer, a material having an oxidation-reduction potential lower than that of the element for the catalyst layer of the cathode can be selected. Examples thereof include nickel and iron.

(Current collector)

The cathode chamber 70 preferably includes a current collector 23. This improves the current collecting effect. In the present embodiment, the current collector 23 is preferably a porous plate and is disposed substantially parallel to the surface of the cathode 21.

The current collector 23 is preferably made of a metal having conductivity, such as nickel, iron, copper, silver, or titanium. The current collector 23 may be a mixture, an alloy, or a composite oxide of these metals. The shape of the current collector 23 may be any shape as long as it functions as a current collector, and may be a plate shape or a mesh shape.

(Metal elastomer)

By providing the metal elastic body 22 between the current collector 23 and the cathode 21, each cathode 21 of the two or more electrolytic cells 50 connected in series is pressed against the cation exchange membrane 51, the distance between each anode 11 and each cathode 21 is shortened, and the voltage applied to the entire two or more electrolytic cells 50 connected in series can be reduced. By lowering the voltage, power consumption can be reduced. Further, by providing the metal elastic body 22, when the laminate including the electrolysis electrode in the present embodiment is installed in the electrolytic cell, the electrolysis electrode can be stably maintained at a fixed position by the pressing pressure generated by the metal elastic body 22.

As the metal elastic body 22, a spring member such as a coil spring or a coil, a cushion pad, or the like can be used. As the metal elastic body 22, an appropriate metal elastic body can be suitably used in consideration of stress against the ion exchange membrane and the like. The metal elastic body 22 may be provided on the surface of the current collector 23 on the cathode chamber 70 side, or may be provided on the surface of the partition wall on the anode chamber 60 side. In general, the cathode chamber 70 is divided into two chambers so as to be smaller than the anode chamber 60, and therefore, it is preferable to provide the metal elastic body 22 between the current collector 23 of the cathode chamber 70 and the cathode 21 in terms of the strength of the frame body and the like. The metal elastic body 23 is preferably made of a metal having conductivity, such as nickel, iron, copper, silver, or titanium.

(support)

The cathode chamber 70 preferably includes a support 24 that electrically connects the current collector 23 and the partition 80. This allows a current to flow efficiently.

The support 24 is preferably made of a metal having conductivity, such as nickel, iron, copper, silver, or titanium. The shape of the support 24 may be any shape as long as it can support the current collector 23, and may be a rod, a plate, or a mesh. The support body 24 is, for example, plate-shaped. Two or more supports 24 are disposed between the partition 80 and the current collector 23. The two or more supports 24 are arranged so that their respective surfaces are parallel to each other. The support 24 is disposed substantially perpendicular to the partition 80 and the current collector 23.

(Anode side gasket, cathode side gasket)

The anode gasket 12 is preferably disposed on the surface of a frame constituting the anode chamber 60. The cathode-side gasket 13 is preferably disposed on the surface of the frame constituting the cathode chamber 70. The electrolytic cells are connected to each other so that the cation exchange membrane 51 is sandwiched between the anode-side gasket 12 of one electrolytic cell and the cathode-side gasket 13 of the adjacent electrolytic cell (see fig. 2). These gaskets can provide airtightness to the joint when two or more electrolytic cells 50 are connected in series via the cation exchange membrane 51.

The gasket is a member for sealing between the ion exchange membrane and the electrolytic cell. Specific examples of the gasket include a frame-shaped rubber sheet having an opening formed in the center thereof. The gasket is required to have resistance to corrosive electrolyte, generated gas, and the like, and to be usable for a long time. Therefore, in terms of chemical resistance and hardness, a vulcanized product of ethylene-propylene-diene rubber (EPDM rubber), ethylene-propylene rubber (EPM rubber), a peroxide crosslinked product, or the like is generally used as a gasket. If necessary, a gasket in which a region in contact with a liquid (liquid contact portion) is coated with a fluorine resin such as Polytetrafluoroethylene (PTFE) or tetrafluoroethylene-perfluoroalkyl vinyl ether copolymer (PFA) may be used. The shape of each of these spacers is not particularly limited as long as it has an opening so as not to obstruct the flow of the electrolyte. For example, a frame-shaped gasket is attached with an adhesive or the like along the periphery of each opening of an anode chamber frame constituting the anode chamber 60 or a cathode chamber frame constituting the cathode chamber 70. For example, when 2 electrolytic cells 50 are connected to each other through the cation exchange membrane 51 (see fig. 2), the electrolytic cells 50 to which gaskets are attached may be fastened through the cation exchange membrane 51. This can prevent the electrolyte solution, the alkali metal hydroxide produced by electrolysis, chlorine gas, hydrogen gas, and the like from leaking to the outside of the electrolytic cell 50.

[ layered body ]

The electrode for electrolysis in the present embodiment is used in the form of a laminate with a separator such as an ion exchange membrane or a microporous membrane. That is, the laminate in the present embodiment includes an electrode for electrolysis and a separator. The new laminate in the present embodiment includes the new electrode for electrolysis and the new separator, and as described above, the new laminate is not particularly limited as long as it is separated from the existing laminate in the existing electrolytic cell, and may have the same configuration as the laminate. Specific examples of the electrodes and separators for electrolysis will be described in detail later.

In the step (B) in the present embodiment, a roll body obtained by winding a new laminate is preferably used.

Specific examples of the step using the roll body include, but are not limited to, the following steps: the roll is placed on the electrolytic bath, and then the roll is brought into contact with the state of the roll wound on the electrolytic bath, and a new laminate released from the wound state is placed between the anode and the cathode. In this embodiment, the new laminate may be directly wound to form a wound body, or the new laminate may be wound around a core to form a wound body. The core that can be used here is not particularly limited, and for example, a member having a substantially cylindrical shape and a size corresponding to the new laminate can be used. The new laminate (new electrode for electrolysis and new separator) used as the roll as described above is not particularly limited as long as it can be rolled, and the material, shape, and the like thereof can be appropriately selected in consideration of the step of using the roll, the configuration of the electrolytic cell, and the like in the present embodiment, and the material, shape, and the like thereof are appropriate in terms of the formation of the roll. Specifically, an electrode for electrolysis and a separator of a preferred embodiment described later can be used.

(Process (A))

In the step (a) of the present embodiment, the existing layered body is removed from the existing electrolytic cell. The method of removing is not particularly limited, and for example, the existing layered body can be removed by first releasing the fixing state of the adjacent electrolytic cell and the existing layered body by the pressurizer in the existing electrolytic cell, forming a gap between the electrolytic cell and the existing layered body, and then detaching the existing layered body to be renewed from the existing electrolytic cell.

The temperature condition of the step (a) is not particularly limited, and it is preferably carried out at a temperature at which the separator does not melt. Here, the "temperature at which the separator does not melt" may be determined as the softening point of the separator. The temperature may vary depending on the material constituting the separator, and is preferably 0 to 100 ℃, more preferably 5 to 80 ℃, and still more preferably 10 to 50 ℃.

The pressure conditions in the step (a) are not particularly limited, and the step (a) is preferably carried out under normal pressure.

(Process (B))

In the step (B) of the present embodiment, a new laminate is disposed between the anode and the cathode in the existing electrolytic cell. The temperature condition of the step (B) is not particularly limited, and it is preferably carried out at a temperature at which the separator does not melt. The temperature may vary depending on the material constituting the separator, and is preferably 0 to 100 ℃, more preferably 5 to 80 ℃, and still more preferably 10 to 50 ℃.

The pressure conditions in the step (B) are not particularly limited, and the step (B) is preferably performed under normal pressure.

A new laminate including a new electrode for electrolysis and a new separator may be prepared in advance or at the time of performing the step (B). That is, the method for manufacturing an electrolytic cell according to the present embodiment may include a step of integrating the new electrode for electrolysis and the new separator. The method of integration is not particularly limited, and a preferable example thereof includes a method of integrating an electrode for electrolysis and a separator, which will be described later, with a liquid interposed therebetween by using the surface tension of the liquid.

After the step (B) of the present embodiment is performed, the fixation of each member in the new electrolytic cell can be performed by, but not limited to, connecting each member again by using a pressurizer, for example.

In this embodiment, the laminate may have one of an anode electrolysis electrode (electrolysis electrode functioning as an anode; A1) and a cathode electrolysis electrode (electrolysis electrode functioning as a cathode; B1) as the electrolysis electrode, or may have both A1 and B1. In the case where both a1 and B1 are provided, since both the anode and the cathode exposed after removal of the existing laminate tend to deteriorate the electrode performance, the new laminate used in the step (B) in the present embodiment preferably has an anode electrolysis electrode (electrolysis electrode functioning as an anode; a2) and a cathode electrolysis electrode (electrolysis electrode functioning as a cathode; B2) as new electrolysis electrodes.

[ electrodes for electrolysis ]

In the present embodiment, the electrolysis electrode is not particularly limited as long as it can form a laminate with the separator, that is, can be integrated with the separator as described above. The electrolysis electrode in the present embodiment is preferably used in the form of a wound body. The electrolysis electrode may function as a cathode or as an anode in the electrolytic cell. The material, shape, physical properties, and the like of the electrolysis electrode can be appropriately selected in consideration of the steps (a) and (B) of the present embodiment, the structure of the electrolytic cell, and the like. Preferred embodiments of the electrolysis electrode in the present embodiment will be described below, but these embodiments are merely examples of preferred embodiments in carrying out the steps (a) and (B), and electrodes for electrolysis other than the embodiments described below may be suitably used.

The electrode for electrolysis in the present embodiment can achieve good treatment properties and can be made to intersect with ionsThe force applied per unit mass/unit area is preferably 1.6N/(mg · cm) from the viewpoint of good adhesion of a separator such as a replaced film or a microporous film, a power supply body (a deteriorated electrode and an electrode not coated with a catalyst), and the like ²) Less than 1.6N/(mg. cm) is more preferable²) More preferably less than 1.5N/(mg. cm)²) More preferably 1.2N/mg/cm²The concentration is preferably 1.20N/mg/cm or less²The following. Still more preferably 1.1N/mg-cm²The lower, more preferably 1.10N/mg cm²The lower, particularly preferred is 1.0N/mg-cm²The concentration is preferably 1.00N/mg cm²The following.

From the viewpoint of further improving the electrolytic performance, it is preferably more than 0.005N/(mg. cm)²) More preferably 0.08N/(mg. cm)²) More preferably 0.1N/mg-cm²More preferably 0.14N/(mg. cm)²) The above. From the viewpoint of facilitating the treatment in a large size (for example, a size of 1.5m × 2.5m), more preferably 0.2N/(mg · cm)²) The above.

The above-mentioned applied force can be in the above-mentioned range by appropriately adjusting, for example, the aperture ratio, the thickness of the electrode, the arithmetic average surface roughness, and the like, which will be described later. More specifically, for example, if the opening ratio is increased, the applied force tends to decrease; the applied force tends to increase if the open cell content is reduced.

In addition, good handling properties are obtained; has good adhesive force with a diaphragm such as an ion exchange membrane or a microporous membrane, a deteriorated electrode, a power supply body without being coated with a catalyst, and the like; and from the viewpoint of economy, the mass per unit area is preferably 48mg/cm ²Less than, more preferably 30mg/cm²The concentration is preferably 20mg/cm or less²Hereinafter, from the viewpoint of the combination of handling property, adhesion property and economical efficiency, it is preferably 15mg/cm²The following. The lower limit is not particularly limited, and is, for example, 1mg/cm²Left and right.

The mass per unit area can be in the above range by appropriately adjusting, for example, the aperture ratio and the thickness of the electrode, which will be described later. More specifically, for example, in the case of the same thickness, the mass per unit area tends to decrease as the opening ratio increases; the mass per unit area tends to increase as the open cell content decreases.

The applied force can be measured by the following method (i) or (ii), and the value obtained by the measurement by the method (i) (also referred to as "applied force (1)") and the value obtained by the measurement by the method (ii) (also referred to as "applied force (2)") in the applied force may be the same or different, but in any case, it is preferably less than 1.5N/mg · cm²。

[ method (i) ]

A sample for measurement was obtained by stacking a nickel plate (thickness 1.2mm, 200mm square) obtained by sand blasting using alumina of particle number 320, an ion exchange membrane (170mm square, details of the ion exchange membrane described herein are described in examples) in which inorganic particles and a binder were applied to both surfaces of a membrane of a perfluorocarbon polymer having ion exchange groups introduced, and an electrode sample (130mm square) in this order, sufficiently immersing the stack in pure water, and then removing excess water adhering to the surface of the stack. The nickel plate after the sandblasting has an arithmetic average surface roughness (Ra) of 0.5 to 0.8 μm. The specific calculation method of the arithmetic average surface roughness (Ra) is as described in examples.

Under the conditions of a temperature of 23. + -. 2 ℃ and a relative humidity of 30. + -. 5%, only the electrode sample in the measurement sample was raised by 10 mm/min in the vertical direction by using a tensile compression tester, and the load when the electrode sample was raised by 10mm in the vertical direction was measured. The measurement was performed 3 times, and an average value was calculated.

The average value was divided by the area of the portion of the electrode sample overlapping the ion exchange membrane and the mass of the electrode sample in the portion overlapping the ion exchange membrane to calculate the force (1) (N/mg. cm) applied per unit mass/unit area²)。

The force (1) applied per unit mass and unit area obtained by the method (i) is preferably applied to a separator such as an ion exchange membrane or a microporous membrane in order to obtain good handleabilityThe adhesion between the deteriorated electrode and the catalyst-uncoated power supply body is preferably 1.6N/(mg cm)²) Less than 1.6N/(mg. cm), more preferably less than²) More preferably less than 1.5N/(mg. cm)²) More preferably 1.2N/mg cm²The concentration is preferably 1.20N/mg/cm or less²The following. Still more preferably 1.1N/mg-cm²The lower, more preferably 1.10N/mg cm²The concentration is preferably 1.0N/mg cm or less ²The concentration is preferably 1.00N/mg cm²The following. In addition, from the viewpoint of further improving the electrolytic performance, it is preferably more than 0.005N/(mg. cm)²) More preferably 0.08N/(mg. cm)²) More preferably 0.1N/(mg. cm)²) From the above, it is more preferable that the concentration of the surfactant is 0.14N/(mg. cm) from the viewpoint of facilitating the treatment in a large size (for example, a size of 1.5 m.times.2.5 m)²) More preferably 0.2N/(mg. cm)²) The above.

[ method (ii) ]

A nickel plate (nickel plate having a thickness of 1.2mm, 200mm square, the same as in the above method (i)) obtained by sand blasting using the alumina of grain number 320 and an electrode sample (130mm square) were laminated in this order, and the laminate was sufficiently immersed in pure water, and then excess water adhering to the surface of the laminate was removed, thereby obtaining a sample for measurement. Under the conditions of a temperature of 23. + -. 2 ℃ and a relative humidity of 30. + -. 5%, only the electrode sample in the measurement sample was raised by 10 mm/min in the vertical direction by using a tensile compression tester, and the load when the electrode sample was raised by 10mm in the vertical direction was measured. The measurement was performed 3 times, and an average value was calculated.

The average value was divided by the area of the portion where the electrode sample overlapped the nickel plate and the mass of the electrode sample in the portion where the electrode sample overlapped the nickel plate, and the adhesion force per unit mass per unit area (2) (N/mg cm) was calculated ²)。

The force (2) applied per unit mass and unit area obtained by the method (ii) is not subjected to the catalytic reaction, and is excellent in handling property, and can be applied to a separator such as an ion exchange membrane or a microporous membrane, a deteriorated electrode, or the likeThe electron donor coated with the agent is preferably 1.6N/(mg. cm)²) Less than 1.6N/(mg. cm), more preferably less than²) More preferably less than 1.5N/(mg. cm)²) More preferably 1.2N/mg cm²The concentration is preferably 1.20N/mg/cm or less²The following. Still more preferably 1.1N/mg-cm²The lower, more preferably 1.10N/mg cm²The lower, particularly preferred is 1.0N/mg-cm²The concentration is preferably 1.00N/mg cm²The following. Further, from the viewpoint of further improving the electrolytic performance, it is preferably more than 0.005N/(mg. cm)²) More preferably 0.08N/(mg. cm)²) More preferably 0.1N/(mg. cm)²) From the viewpoint of facilitating the treatment in a large size (for example, a size of 1.5m × 2.5m), it is more preferable that the concentration is 0.14N/(mg · cm)²) The above.

The electrolysis electrode of the present embodiment preferably includes an electrolysis electrode substrate and a catalyst layer. The thickness (gauge thickness) of the electrode base material for electrolysis is not particularly limited, and is preferably 300 μm or less, more preferably 205 μm or less, further preferably 155 μm or less, further preferably 135 μm or less, further preferably 125 μm or less, further preferably 120 μm or less, further preferably 100 μm or less, and further preferably 50 μm or less from the viewpoints of handling properties and economy, in order to obtain good handling properties, and to have good adhesion to a separator such as an ion exchange membrane or a microporous membrane, a deteriorated electrode (power feeder), and an electrode (power feeder) not coated with a catalyst, to be wound in a roll shape suitably, to be bent well, and to be easily handled in a large size (for example, a size of 1.5m × 2.5 m). The lower limit is not particularly limited, but is, for example, 1 μm, preferably 5 μm, and more preferably 15 μm.

In the present embodiment, it is preferable that a liquid is interposed between the separator and the electrolysis electrode from the viewpoint of integrating them. Any liquid may be used as long as it generates surface tension such as water or an organic solvent. The larger the surface tension of the liquid, the larger the force applied between the separator and the electrolysis electrode, and therefore a liquid having a large surface tension is preferable. Examples of the liquid include the following (the value in parentheses is the surface tension of the liquid at 20 ℃).

Hexane (20.44mN/m), acetone (23.30mN/m), methanol (24.00mN/m), ethanol (24.05mN/m), ethylene glycol (50.21mN/m) water (72.76mN/m)

When the liquid has a large surface tension, the separator and the electrode for electrolysis are integrated (laminated), and the electrode tends to be easily replaced. The liquid between the separator and the electrolysis electrode may be in an amount of a degree that the liquid adheres to each other by surface tension, and as a result, the amount of the liquid is small, and therefore, even if the liquid is mixed into the electrolytic solution after the electrolytic cell provided in the laminate, the electrolysis itself is not affected.

From the viewpoint of practicality, it is preferable to use a liquid having a surface tension of 24mN/m to 80mN/m, such as ethanol, ethylene glycol, or water. Particularly, water or an aqueous solution prepared by dissolving sodium hydroxide, potassium hydroxide, lithium hydroxide, sodium hydrogencarbonate, potassium hydrogencarbonate, sodium carbonate, potassium carbonate, or the like in water to obtain an alkali solution is preferable. In addition, these liquids may contain a surfactant to adjust the surface tension. The inclusion of the surfactant changes the adhesiveness between the separator and the electrode for electrolysis, and thus the handleability can be adjusted. The surfactant is not particularly limited, and any of an ionic surfactant and a nonionic surfactant can be used.

The electrode for electrolysis in the present embodiment is not particularly limited, and the ratio measured by the following method (2) is preferably 90% or more, more preferably 92% or more, and further more preferably 95% or more, from the viewpoint of obtaining good handling properties and good adhesion to a separator such as an ion exchange membrane or a microporous membrane, a deteriorated electrode (power feeder), and an electrode (power feeder) not coated with a catalyst, and from the viewpoint of facilitating handling in a large size (for example, a size of 1.5m × 2.5 m). The upper limit is 100%.

[ method (2) ]

An ion exchange membrane (170mm square) and an electrode sample (130mm square) were laminated in this order. The laminate was placed on a curved surface of a polyethylene tube (outer diameter 280mm) so that the electrode sample was located outside the laminate at a temperature of 23. + -. 2 ℃ and a relative humidity of 30. + -. 5%, the laminate and the tube were sufficiently impregnated with pure water to remove excess water adhering to the surface of the laminate and the tube, and after 1 minute, the percentage (%) of the area of the portion where the ion-exchange membrane (170mm square) and the electrode sample were in close contact was measured.

The electrode for electrolysis in the present embodiment is not particularly limited, and is preferably 75% or more, more preferably 80% or more, and is more preferably 90% or more, from the viewpoint of obtaining good handling properties, having good adhesion to a separator such as an ion exchange membrane or a microporous membrane, a deteriorated electrode (power feeder), and an electrode (power feeder) not coated with a catalyst, and being capable of being suitably wound in a roll shape and being suitably bent, as measured by the following method (3), and further from the viewpoint of facilitating handling in a large size (for example, a size of 1.5m × 2.5 m). The upper limit is 100%.

[ method (3) ]

An ion exchange membrane (170mm square) and an electrode sample (130mm square) were laminated in this order. The laminate was placed on a curved surface of a polyethylene tube (outer diameter: 145mm) so that the electrode sample in the laminate was outside at a temperature of 23. + -. 2 ℃ and a relative humidity of 30. + -. 5%, the laminate and the tube were sufficiently impregnated with pure water to remove excess water adhering to the surface of the laminate and the tube, and after 1 minute, the ratio (%) of the area of the portion where the ion exchange membrane (170mm square) and the electrode sample were in close contact was measured.

The electrode for electrolysis in the present embodiment is not particularly limited, and is preferably a porous structure having an open pore ratio or a void ratio of 5 to 90% or less, from the viewpoints of obtaining good handleability, having good adhesion to a separator such as an ion exchange membrane or a microporous membrane, a deteriorated electrode (power feeder), and an electrode (power feeder) not coated with a catalyst, and preventing retention of gas generated during electrolysis. The aperture ratio is more preferably 10 to 80% or less, and still more preferably 20 to 75%.

The open porosity is a ratio of open pores per unit volume. For the opening portion, there are various calculation methods depending on whether even the submicron order or only the opening seen by the eye is considered. In the present embodiment, the open porosity a is calculated by the following equation by calculating the volume V from the values of the gauge thickness, width, and length of the electrode and further actually measuring the weight W.

A＝(1-(W/(V×ρ))×100

ρ is the density (g/cm) of the material of the electrode³). For example 8.908g/cm in the case of nickel³4.506g/cm in the case of titanium³. The adjustment of the open pore ratio is appropriately performed by the following method: if the punched metal is the punched metal, changing the area of the punched metal per unit area; if the metal plate net is the metal plate net, changing the values of SW (short diameter), LW (long diameter) and feeding; if the metal fiber is a net, changing the wire diameter and the mesh number of the metal fiber; if electroforming, changing the pattern of the photoresist used; if the non-woven fabric is used, the diameter and the fiber density of the metal fibers are changed; in the case of the foamed metal, a mold for forming the voids is changed.

In the electrode for electrolysis of the present embodiment, the value measured by the following method (a) is preferably 40mm or less, more preferably 29mm or less, further preferably 10mm or less, and further more preferably 6.5mm or less, from the viewpoint of handling property.

[ method (A) ]

Winding and fixing a sample of a laminated body obtained by laminating an ion exchange membrane and the electrode for electrolysis on the outer diameter under the conditions of a temperature of 23 + -2 ℃ and a relative humidity of 30 + -5%

The electrode for electrolysis was separated and placed on a horizontal plate after standing still for 6 hours on the curved surface of the core material made of vinyl chloride, and the height L in the vertical direction of both ends of the electrode for electrolysis was measured ₁And L₂The average value of these values was used as the measured value.

The electrode for electrolysis in the present embodiment is made to have a size of 50mm × 50mm at a temperature of 24 deg.C, a relative humidity of 32%, a piston speed of 0.2cm/s, andthe ventilation volume is 0.4cc/cm²The aeration resistance (hereinafter also referred to as "aeration resistance 1") in the case of/s (hereinafter also referred to as "measurement condition 1") is preferably 24kPa · s/m or less. The large ventilation resistance means that air is difficult to flow, and means a state of high density. In this state, products generated by electrolysis remain in the electrode, and the reaction substrate is less likely to diffuse into the electrode, so that the electrolytic performance (voltage, etc.) tends to deteriorate. In addition, the concentration on the film surface tends to increase. Specifically, the sodium hydroxide concentration (caustic degrees) on the cathode surface tends to increase, and the saline water supply property on the anode surface tends to decrease. As a result, the product stays at a high concentration at the interface between the separator and the electrolysis electrode, and thus the separator tends to be damaged, and the voltage on the cathode surface tends to increase, the film tends to be damaged, and the film tends to be damaged on the anode surface.

In order to prevent these problems, the ventilation resistance is preferably 24kPa · s/m or less.

From the same points as above, the air flow resistance is more preferably less than 0.19kPa · s/m, still more preferably 0.15kPa · s/m or less, and still more preferably 0.07kPa · s/m or less.

When the gas flow resistance is higher than a certain value, NaOH generated at the electrode tends to stay at the interface between the electrolysis electrode and the separator and become high in concentration in the case of the cathode; in the case of the anode, the saline water supply performance is lowered, the saline water concentration tends to be low, and from the viewpoint of preventing the damage to the separator which may be caused by such retention, it is preferably less than 0.19kPa · s/m, more preferably 0.15kPa · s/m or less, and still more preferably 0.07kPa · s/m or less.

On the other hand, when the gas flow resistance is low, the area of the electrolysis electrode decreases, and therefore the electrolysis area tends to decrease, and the electrolysis performance (voltage, etc.) tends to deteriorate. When the air flow resistance is zero, since no electrolysis electrode is provided, the power feeder functions as an electrode, and the electrolysis performance (voltage, etc.) tends to be significantly deteriorated. From this point of view, the lower limit value determined as the ventilation resistance 1 is not particularly limited, but is preferably greater than 0kPa · s/m, more preferably 0.0001kPa · s/m or more, and still more preferably 0.001kPa · s/m or more.

In addition, in view of the measurement method, it is likely that sufficient measurement accuracy cannot be obtained when the ventilation resistance 1 is 0.07kPa · s/m or less. From this viewpoint, the evaluation of the aeration resistance (hereinafter, also referred to as "aeration resistance 2") of the electrode for electrolysis having an aeration resistance 1 of 0.07kPa · s/m or less can be performed by the following measurement method (hereinafter, also referred to as "measurement condition 2"). That is, the aeration resistance 2 is a value obtained by making the electrode for electrolysis have a size of 50mm X50 mm, and is set at a temperature of 24 ℃, a relative humidity of 32%, a piston velocity of 2cm/s and an aeration amount of 4cc/cm²Ventilation resistance in the case of/s.

The ventilation resistances 1 and 2 can be set to the above ranges by appropriately adjusting, for example, the aperture ratio and the thickness of the electrode, which will be described later. More specifically, for example, if the thickness is the same, the air flow resistances 1 and 2 tend to decrease when the opening ratio is increased, and the air flow resistances 1 and 2 tend to increase when the opening ratio is decreased.

A more specific embodiment of the electrolysis electrode in the present embodiment will be described below.

The electrolysis electrode of the present embodiment preferably includes an electrolysis electrode substrate and a catalyst layer. The catalyst layer may be composed of two or more layers or may have a single-layer structure, as described below.

As shown in fig. 6, the electrolysis electrode 101 of the present embodiment includes an electrolysis electrode base 10 and a pair of first layers 20 covering both surfaces of the electrolysis electrode base 10. The first layer 20 preferably covers the entire electrolytic electrode substrate 10. This makes it easy to improve the catalytic activity and durability of the electrolysis electrode. The first layer 20 may be laminated on only one surface of the electrode base material for electrolysis 10.

In addition, as shown in fig. 6, the surface of the first layer 20 may be coated with the second layer 30. The second layer 30 preferably covers the entirety of the first layer 20. The second layer 30 may be laminated on only one surface of the first layer 20.

(electrode base for electrolysis)

The electrode base material for electrolysis 10 is not particularly limited, and for example, a valve metal typified by nickel, a nickel alloy, stainless steel, or titanium can be used, and preferably contains at least one element selected from nickel (Ni) and titanium (Ti).

When stainless steel is used in a high-concentration alkaline aqueous solution, a substrate containing nickel (Ni) is preferable as the electrode substrate for electrolysis in consideration of elution of iron and chromium and the conductivity of stainless steel being about 1/10 of nickel.

When the electrode base material for electrolysis 10 is used in a chlorine generating atmosphere in a high-concentration saline solution near saturation, the material is preferably titanium having high corrosion resistance.

The shape of the electrode base material for electrolysis 10 is not particularly limited, and may be selected as appropriate according to the purpose. As the shape, any of punched metal, nonwoven fabric, foamed metal, expanded metal, metal foil, porous metal foil formed by electroforming, so-called woven mesh produced by weaving metal wires, and the like can be used. Among them, punched metal or expanded metal is preferable. Electroforming is a technique of combining photolithography and electroplating to form a metal thin film having a precise pattern. In this method, a pattern is formed on a substrate using a photoresist, and a portion not protected by the photoresist is plated to obtain a metal thin film.

The shape of the electrode base material for electrolysis has an appropriate specification depending on the distance between the anode and the cathode in the electrolytic cell. The shape is not particularly limited, and in the case of a so-called zero-gap electrolytic cell in which an ion exchange membrane and an electrode are in contact with each other, a woven mesh, a wire mesh, a foamed metal, a metal nonwoven fabric, a metal lath, a punched metal, a metal porous foil, or the like, which is formed by weaving fine wires, may be used.

Examples of the electrode base material 10 for electrolysis include a porous metal foil, a wire mesh, a metal nonwoven fabric, a punched metal, a metal lath, and a foamed metal.

The sheet material before being processed into a punched metal or a metal lath is preferably a sheet material formed by rolling, an electrolytic foil, or the like. The electrolytic foil is preferably further subjected to plating treatment using the same elements as the base material as a post-treatment to form irregularities on one or both surfaces.

The thickness of the electrode base material for electrolysis 10 is preferably 300 μm or less, more preferably 205 μm or less, further preferably 155 μm or less, further preferably 135 μm or less, further preferably 125 μm or less, further preferably 120 μm or less, further preferably 100 μm or less, and further more preferably 50 μm or less from the viewpoint of handling property and economical efficiency, as described above. The lower limit is not particularly limited, but is, for example, 1 μm, preferably 5 μm, and more preferably 15 μm.

In the electrode base material for electrolysis, it is preferable to relax the residual stress at the time of processing by annealing the electrode base material for electrolysis in an oxidizing atmosphere. In addition, on the surface of the electrode base material for electrolysis, in order to improve adhesion to the catalyst layer coated on the surface, it is preferable to form irregularities by steel grit (スチールグリッド), alumina powder, or the like, and then increase the surface area by acid treatment. Alternatively, the surface area is increased by performing plating treatment preferably using the same element as the base material.

In order to make the first layer 20 adhere to the surface of the electrode base material for electrolysis 10, the electrode base material for electrolysis 10 is preferably subjected to a treatment for increasing the surface area. Examples of the treatment for increasing the surface area include: sand blasting using steel wire particles (カットワイヤ), steel grit, alumina grit, or the like; acid treatment using sulfuric acid or hydrochloric acid; plating treatment with the same element as the base material; and so on. The arithmetic average surface roughness (Ra) of the surface of the substrate is not particularly limited, but is preferably 0.05 to 50 μm, more preferably 0.1 to 10 μm, and still more preferably 0.1 to 8 μm.

Next, a case where the electrolysis electrode of the present embodiment is used as an anode for salt electrolysis will be described.

(first layer)

In fig. 6, the first layer 20 as the catalyst layer contains at least one oxide of ruthenium oxide, iridium oxide, and titanium oxide. Examples of the ruthenium oxide include RuO₂And the like. IrO is an iridium oxide₂And the like. Examples of the titanium oxide include TiO₂And the like. The first layer 20 contains two oxides of ruthenium oxide and titanium oxide, or three oxides of ruthenium oxide, iridium oxide, and titanium oxide. This makes the first layer 20 a more stable layer, and further improves the adhesion to the second layer 30.

When the first layer 20 contains both ruthenium oxide and titanium oxide, the amount of titanium oxide contained in the first layer 20 is preferably 1 to 9 mol, and more preferably 1 to 4 mol, based on 1 mol of ruthenium oxide contained in the first layer 20. By setting the composition ratio of the two oxides in this range, the electrolysis electrode 101 exhibits excellent durability.

When the first layer 20 contains three oxides, i.e., ruthenium oxide, iridium oxide, and titanium oxide, the iridium oxide contained in the first layer 20 is preferably 0.2 to 3 mol, and more preferably 0.3 to 2.5 mol, based on 1 mol of ruthenium oxide contained in the first layer 20. In addition, the titanium oxide contained in the first layer 20 is preferably 0.3 to 8 mol, and more preferably 1 to 7 mol, based on 1 mol of ruthenium oxide contained in the first layer 20. By making the composition ratio of the three oxides in this range, the electrolysis electrode 101 exhibits excellent durability.

In the case where the first layer 20 contains at least two oxides selected from ruthenium oxide, iridium oxide, and titanium oxide, these oxides preferably form a solid solution. By forming an oxide solid solution, the electrode 101 for electrolysis exhibits excellent durability.

In addition to the above-described composition, as long as at least one oxide of ruthenium oxide, iridium oxide, and titanium oxide is contained, substances of various compositions can be used. For example, an oxide coating containing ruthenium, iridium, tantalum, niobium, titanium, tin, cobalt, manganese, platinum, or the like, which is called DSA (registered trademark), may also be used as the first layer 20.

The first layer 20 need not be a single layer, and may include 2 or more layers. For example, the first layer 20 may include a layer containing 3 oxides and a layer containing two oxides. The thickness of the first layer 20 is preferably 0.05 to 10 μm, and more preferably 0.1 to 8 μm.

(second layer)

The second layer 30 preferably comprises ruthenium and titanium. This can further reduce the chlorine overvoltage immediately after the electrolysis.

The second layer 30 preferably comprises palladium oxide, a solid solution of palladium oxide and platinum, or an alloy of palladium and platinum. This can further reduce the chlorine overvoltage immediately after the electrolysis.

When the second layer 30 is thick, the period of time for which the electrolytic performance can be maintained is extended, but from the viewpoint of economy, the thickness is preferably 0.05 to 3 μm.

Next, a case where the electrolysis electrode in the present embodiment is used as a cathode for salt electrolysis will be described.

(first layer)

Examples of the component of the first layer 20 as the catalyst layer include metals such as C, Si, P, S, Al, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Zr, Nb, Mo, Ru, Rh, Pd, Ag, Cd, In, Sn, Ta, W, Re, Os, Ir, Pt, Au, Hg, Pb, Bi, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and oxides or hydroxides of the metals.

At least one of a platinum group metal, a platinum group metal oxide, a platinum group metal hydroxide, and an alloy containing a platinum group metal may or may not be contained.

In the case of containing at least one of platinum group metal, platinum group metal oxide, platinum group metal hydroxide, and platinum group metal-containing alloy, the platinum group metal, platinum group metal oxide, platinum group metal hydroxide, and platinum group metal-containing alloy preferably contains at least one platinum group metal of platinum, palladium, rhodium, ruthenium, and iridium.

As the platinum group metal, platinum is preferably contained.

As the platinum group metal oxide, ruthenium oxide is preferably contained.

As the platinum group metal hydroxide, ruthenium hydroxide is preferably contained.

As the platinum group metal alloy, an alloy containing platinum and nickel, iron, cobalt is preferable.

Further, if necessary, an oxide or hydroxide of a lanthanoid element is preferably contained as the second component. Thus, the electrolysis electrode 101 exhibits excellent durability.

As the oxide or hydroxide of lanthanoid, at least one selected from lanthanum, cerium, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium is preferably contained.

Further, if necessary, an oxide or hydroxide of a transition metal is preferably contained as the third component.

By adding the third component, the electrode 101 for electrolysis exhibits more excellent durability, and the electrolysis voltage can be reduced.

Examples of preferred combinations include alloys of only ruthenium, ruthenium + nickel, ruthenium + cerium, ruthenium + lanthanum + platinum, ruthenium + lanthanum + palladium, ruthenium + praseodymium + platinum, ruthenium + neodymium + platinum, ruthenium + neodymium + manganese, ruthenium + neodymium + iron, ruthenium + neodymium + cobalt, ruthenium + neodymium + zinc, ruthenium + neodymium + gallium, ruthenium + neodymium + sulfur, ruthenium + neodymium + lead, ruthenium + neodymium + nickel, ruthenium + neodymium + copper, ruthenium + samarium + manganese, ruthenium + samarium + iron, ruthenium + samarium + cobalt, ruthenium + samarium + zinc, ruthenium + samarium + gallium, ruthenium + samarium + sulfur, ruthenium + samarium + lead, ruthenium + samarium + nickel, platinum + cerium, platinum + palladium + lanthanum + cerium, platinum + iridium, platinum + palladium, platinum + iridium + palladium, platinum + nickel + ruthenium + platinum, and nickel + platinum, and platinum.

In the case where the catalyst does not contain a platinum group metal, a platinum group metal oxide, a platinum group metal hydroxide, or an alloy containing a platinum group metal, the main component of the catalyst is preferably nickel.

Preferably at least one of nickel metal, oxide, hydroxide.

As the second component, a transition metal may be added. The second component to be added preferably contains at least one element selected from titanium, tin, molybdenum, cobalt, manganese, iron, sulfur, zinc, copper, and carbon.

Preferred combinations include nickel + tin, nickel + titanium, nickel + molybdenum, nickel + cobalt, and the like.

If necessary, an intermediate layer may be provided between the 1 st layer 20 and the electrode substrate 10 for electrolysis. By providing the intermediate layer, the durability of the electrode 101 for electrolysis can be improved.

The intermediate layer preferably has affinity for both the 1 st layer 20 and the electrolytic electrode substrate 10. As the intermediate layer, nickel oxide, platinum group metal oxide, platinum group metal hydroxide are preferable. The intermediate layer may be formed by applying a solution containing the intermediate layer-forming component and firing the solution, or the surface oxide layer may be formed by subjecting the substrate to a heat treatment at a temperature of 300 to 600 ℃ in an air atmosphere. In addition to this, it can be formed by a known method such as a thermal spray method, an ion plating method, or the like.

(second layer)

Examples of the component of the first layer 30 as the catalyst layer include metals such as C, Si, P, S, Al, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Zr, Nb, Mo, Ru, Rh, Pd, Ag, Cd, In, Sn, Ta, W, Re, Os, Ir, Pt, Au, Hg, Pb, Bi, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and oxides or hydroxides of the metals.

At least one of a platinum group metal, a platinum group metal oxide, a platinum group metal hydroxide, and an alloy containing a platinum group metal may or may not be contained. Examples of a preferable combination of elements included in the second layer include the combinations mentioned in the first layer. The combination of the first layer and the second layer may be a combination of the same composition but different composition ratios, or a combination of different compositions.

The thickness of the catalyst layer is preferably 0.01 to 20 μm in total of the thickness of the catalyst layer and the intermediate layer. When the particle size is 0.01 μm or more, the catalyst can exhibit a sufficient function as a catalyst. When the thickness is 20 μm or less, the amount of the catalyst layer is reduced, and a strong catalyst layer can be formed. More preferably 0.05 μm to 15 μm. More preferably 0.1 to 10 μm. More preferably 0.2 to 8 μm.

The thickness of the electrode, i.e., the total thickness of the electrode base material for electrolysis and the catalyst layer, is preferably 315 μm or less, more preferably 220 μm or less, still more preferably 170 μm or less, yet more preferably 150 μm or less, particularly preferably 145 μm or less, still more preferably 140 μm or less, yet still more preferably 138 μm or less, and yet more preferably 135 μm or less, from the viewpoint of handling properties of the electrode. When the particle diameter is 135 μm or less, particularly good handleability can be obtained. Then, from the same viewpoint as above, it is preferably 130 μm or less, more preferably less than 130 μm, still more preferably 115 μm or less, and still more preferably 65 μm or less. The lower limit is not particularly limited, but is preferably 1 μm or more, more preferably 5 μm or more, and still more preferably 20 μm or more from the practical viewpoint. The thickness of the electrode can be determined by measuring with a digital display thickness gauge (Mitutoyo, ltd., minimum display 0.001 mm). The thickness of the electrode base material for electrolysis was measured in the same manner as the electrode thickness. The catalyst layer thickness can be determined by subtracting the thickness of the electrode substrate for electrolysis from the thickness of the electrode.

In the present embodiment, the electrolytic electrode preferably contains at least one catalyst component selected from the group consisting of Ru, Rh, Pd, Ir, Pt, Au, Ti, V, Cr, Mn, Fe, Co, Ni, Cu, Zn, Y, Zr, Nb, Mo, Ag, Ta, W, Re, Os, Al, In, Sn, Sb, Ga, Ge, B, C, N, O, Si, P, S, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, and Dy, from the viewpoint of ensuring sufficient electrolytic performance.

In the present embodiment, when the electrode for electrolysis has a wide elastically deformable region, the thickness of the electrode for electrolysis is preferably 315 μm or less, more preferably 220 μm or less, further preferably 170 μm or less, further more preferably 150 μm or less, particularly preferably 145 μm or less, further preferably 140 μm or less, further more preferably 138 μm or less, further more preferably 135 μm or less, from the viewpoint of obtaining better handleability and better adhesion to a separator such as an ion exchange membrane or a microporous membrane, a deteriorated electrode, a catalyst-uncoated power feeder, and the like. When the particle diameter is 135 μm or less, particularly good handleability is obtained. Further, from the same viewpoint as above, it is preferably 130 μm or less, more preferably less than 130 μm, still more preferably 115 μm or less, and yet more preferably 65 μm or less. The lower limit is not particularly limited, but is preferably 1 μm or more, more preferably 5 μm or more, and still more preferably 20 μm or more from the practical viewpoint. In the present embodiment, the phrase "elastically deformable region is wide" means that the electrode for electrolysis is wound into a roll, and after the wound state is released, warping due to winding is less likely to occur. The thickness of the electrolysis electrode is the thickness of the electrode base material for electrolysis together with the catalyst layer when the catalyst layer described later is included.

(method of manufacturing electrode for electrolysis)

Next, one embodiment of the method for manufacturing the electrolysis electrode 101 will be described in detail.

In the present embodiment, the first layer 20, preferably the second layer 30, is formed on the electrode base material for electrolysis by a method such as baking (thermal decomposition) of the coating film in an oxygen atmosphere, ion plating, or thermal spraying, whereby the electrode 101 for electrolysis can be produced. The production method of the present embodiment can realize high productivity of the electrode 101 for electrolysis. Specifically, the catalyst layer is formed on the electrode base material for electrolysis by a coating step of coating a coating liquid containing a catalyst, a drying step of drying the coating liquid, and a thermal decomposition step of thermally decomposing. Here, the thermal decomposition means that a metal salt as a precursor is heated to be decomposed into a metal or a metal oxide and a gaseous substance. The decomposition products vary depending on the kind of metal used, the kind of salt, the atmosphere in which thermal decomposition is performed, and the like, and many metals tend to form oxides under an oxidizing atmosphere. In the industrial production process of electrodes, thermal decomposition is generally carried out in air, and metal oxides or metal hydroxides are formed in many cases.

(formation of the first layer of the anode)

(coating Process)

The first layer 20 is obtained by applying a solution (first coating liquid) in which a metal salt of at least one of ruthenium, iridium, and titanium is dissolved to an electrode base material for electrolysis, and then thermally decomposing (firing) the solution in the presence of oxygen. The contents of ruthenium, iridium, and titanium in the first coating liquid are substantially equal to those of the first layer 20.

The metal salt may be any of chloride salt, nitrate salt, sulfate salt, metal alkoxide salt, and other salts. The solvent of the first coating liquid may be selected according to the kind of the metal salt, and alcohols such as water and butanol may be used. As the solvent, water or a mixed solvent of water and an alcohol is preferable. The total metal concentration in the first coating liquid in which the metal salt is dissolved is not particularly limited, and is preferably in the range of 10 to 150g/L in view of compatibility with the thickness of the coating film formed by one-time coating.

As a method of applying the first coating liquid to the electrode base material for electrolysis 10, there are used an immersion method of immersing the electrode base material for electrolysis 10 in the first coating liquid, a method of applying the first coating liquid with bristles, a roller method using a sponge roller impregnated with the first coating liquid, an electrostatic coating method of spraying the electrode base material for electrolysis 10 and the first coating liquid with opposite charges, and the like. Among them, a roll method or an electrostatic coating method excellent in industrial productivity is preferable.

(drying step, thermal decomposition step)

The first coating liquid is applied to the electrode base material 100 for electrolysis, dried at a temperature of 10 to 90 ℃, and thermally decomposed in a firing furnace heated to 350 to 650 ℃. During the drying and thermal decomposition, the pre-firing may be performed at 100 to 350 ℃ as required. The drying, pre-firing and thermal decomposition temperatures may be appropriately selected depending on the composition of the first coating liquid and the kind of solvent. The time per thermal decomposition is preferably long, and from the viewpoint of productivity of the electrode, it is preferably 3 to 60 minutes, and more preferably 5 to 20 minutes.

The above cycle of coating, drying, and thermal decomposition is repeated to form the coating (first layer 20) to a predetermined thickness. After the first layer 20 is formed, if necessary, the first layer 20 can be further improved in stability by further baking for a long time and then heating.

(formation of second layer)

The second layer 30 is formed as needed, and is obtained by, for example, applying a solution containing a palladium compound and a platinum compound or a solution containing a ruthenium compound and a titanium compound (second coating liquid) onto the first layer 20, and then thermally decomposing in the presence of oxygen.

(formation of the first layer of the cathode by thermal decomposition)

(coating Process)

The first layer 20 is obtained by applying a solution (first coating liquid) in which metal salts of various combinations are dissolved onto an electrode base material for electrolysis, and then performing thermal decomposition (firing) in the presence of oxygen. The content of the metal in the first coating liquid is substantially equal to that of the first layer 20.

(drying step, thermal decomposition step)

The first coating liquid is applied to an electrode base material 10 for electrolysis, dried at a temperature of 10 to 90 ℃, and thermally decomposed in a firing furnace heated to 350 to 650 ℃. During the drying and thermal decomposition, the pre-firing may be performed at 100 to 350 ℃ as required. The drying, pre-firing and thermal decomposition temperatures may be appropriately selected depending on the composition of the first coating liquid and the kind of solvent. The time per thermal decomposition is preferably long, and from the viewpoint of productivity of the electrode, it is preferably 3 to 60 minutes, and more preferably 5 to 20 minutes.

(formation of intermediate layer)

The intermediate layer is formed as needed, and is obtained by applying a solution (second coating solution) containing a palladium compound or a platinum compound to a substrate and then thermally decomposing the applied solution in the presence of oxygen. Alternatively, the nickel oxide intermediate layer may be formed on the surface of the substrate by simply heating the substrate without applying the solution.

(formation of the first layer of the cathode by ion plating)

The first layer 20 may also be formed using ion plating.

As an example, a method of fixing a substrate in a chamber and irradiating a ruthenium metal target with an electron beam may be mentioned. The evaporated metallic ruthenium particles are positively charged in the plasma in the chamber and accumulate on the negatively charged substrate. The plasma atmosphere was argon and oxygen, and ruthenium was deposited as a ruthenium oxide on the substrate.

(formation of the first layer by means of a plated cathode)

The first layer 20 may be formed by plating.

For example, when electroplating is performed in an electrolytic solution containing nickel and tin using a base material as a cathode, an alloy plating layer of nickel and tin can be formed.

(formation of the first layer by means of a thermally sprayed cathode)

The first layer 20 may also be formed using a thermal spray process.

For example, a catalyst layer in which metallic nickel and nickel oxide are mixed can be formed by plasma-spraying nickel oxide particles onto a substrate.

An ion exchange membrane as one embodiment of the separator will be described in detail below.

[ ion exchange Membrane ]

The ion exchange membrane is not particularly limited as long as it can form a laminate with an electrode for electrolysis, and various ion exchange membranes can be applied. In the present embodiment, it is preferable to use an ion exchange membrane having: comprising a hydrocarbon-based polymer or a fluorine-containing polymer having an ion exchange group A film body of the composition; and a coating layer disposed on at least one face of the film main body. Preferably, the coating layer contains inorganic particles and a binder, and the specific surface area of the coating layer is 0.1 to 10m²(ii) in terms of/g. The ion exchange membrane having such a structure is likely to exhibit stable electrolytic performance with little influence of gas generated during electrolysis on electrolytic performance.

The membrane of the perfluorocarbon polymer having ion exchange groups introduced therein comprises: having ion exchange groups (-SO) derived from sulfo groups₃ ^-A sulfonic acid layer of the group represented, hereinafter also referred to as "sulfonic acid group"), and an ion exchange group (-CO) having a carboxyl group₂ ^-The group represented, hereinafter also referred to as "carboxylic acid group"). From the viewpoint of strength and dimensional stability, it is preferable to further include a reinforcing core material.

The inorganic particles and the binder are described in detail in the description section of the coating layer below.

FIG. 7 is a schematic sectional view showing one embodiment of an ion exchange membrane. The ion exchange membrane 1 has: a membrane main body 1a containing a hydrocarbon-based polymer or a fluorine-containing polymer having an ion exchange group; and

coating layers

11a and 11b formed on both sides of the film main body 1 a.

In the ion exchange membrane 1, the membrane main body 1a includes: having ion exchange groups (-SO) derived from sulfo groups₃ ^-A sulfonic acid layer 3 of a group represented by, hereinafter also referred to as "sulfonic acid group"), and an ion exchange group (-CO) having a group derived from a carboxyl group₂ ^-The group represented, hereinafter also referred to as "carboxylic acid group") 2; and the film main body 1a is reinforced in strength and dimensional stability by the reinforcing core material 4. The ion exchange membrane 1 is provided with a sulfonic acid layer 3 and a carboxylic acid layer 2, and is therefore suitable as a cation exchange membrane.

The ion exchange membrane may have only one of the sulfonic acid layer and the carboxylic acid layer. The ion exchange membrane does not necessarily need to be reinforced by the reinforcing core material, and the arrangement state of the reinforcing core material is not limited to the example of fig. 7.

(film body)

First, the membrane main body 1a constituting the ion exchange membrane 1 will be explained.

The membrane main body 1a has a function of selectively transmitting cations, and may be made of any suitable material, as long as it contains a hydrocarbon-based polymer or fluorine-containing polymer having an ion exchange group.

The hydrocarbon-based polymer or fluorine-containing polymer having an ion exchange group in the membrane main body 1a can be obtained, for example, from a hydrocarbon-based polymer or fluorine-containing polymer having an ion exchange group precursor which can be changed into an ion exchange group by hydrolysis or the like. Specifically, for example, the membrane main body 1a can be obtained by preparing a precursor of the membrane main body 1a using a polymer (hereinafter, referred to as "fluorine-containing polymer (a)" as the case may be) whose main chain is composed of a fluorinated hydrocarbon, which has a group (ion exchange group precursor) that can be converted into an ion exchange group by hydrolysis or the like as a pendant side chain, and which can be melt-processed, and then converting the ion exchange group precursor into an ion exchange group.

The fluorine-containing polymer (a) can be produced, for example, by copolymerizing at least one monomer selected from the following group 1 with at least one monomer selected from the following group 2 and/or the following group 3. The copolymer can also be produced by homopolymerization of one monomer selected from any one of the following

groups

1, 2 and 3.

Examples of the monomer of group 1 include fluorinated vinyl compounds. Examples of the vinyl fluoride compound include ethylene fluoride, tetrafluoroethylene, hexafluoropropylene, vinylidene fluoride, trifluoroethylene, chlorotrifluoroethylene, perfluoroalkyl vinyl ether, and the like. In particular, when an ion exchange membrane is used as the membrane for alkali electrolysis, the vinyl fluoride compound is preferably a perfluoromonomer, preferably a perfluoromonomer selected from the group consisting of tetrafluoroethylene, hexafluoropropylene, and perfluoroalkyl vinyl ether.

Examples of the monomer of group 2 include vinyl compounds having a functional group convertible to a carboxylic acid type ion exchange group (carboxylic acid group). As having functional groups convertible to carboxylic acid groupsExamples of the vinyl compound include CF₂＝CF(OCF₂CYF)_s-O(CZF)_tA monomer represented by-COOR (s is an integer of 0 to 2, t is an integer of 1 to 12, and Y and Z are each independently F or CF) ₃And R represents a lower alkyl group. The lower alkyl group is, for example, an alkyl group having 1 to 3 carbon atoms).

Among these, CF is preferred₂＝CF(OCF₂CYF)_n-O(CF₂)_m-COOR. Wherein n represents an integer of 0 to 2, m represents an integer of 1 to 4, and Y represents F or CF₃R represents CH₃、C₂H₅Or C₃H₇。

When an ion exchange membrane is used as the cation exchange membrane for alkali electrolysis, it is preferable to use at least a perfluoro compound as a monomer, but since the alkyl group of the ester group (see R above) is lost from the polymer at the time of hydrolysis, the alkyl group (R) may not be a perfluoroalkyl group in which all hydrogen atoms are substituted with fluorine atoms.

Among the above, the monomers of group 2 are more preferably those represented below.

CF₂＝CFOCF₂-CF(CF₃)OCF₂COOCH₃、

CF₂＝CFOCF₂CF(CF₃)O(CF₂)₂COOCH₃、

CF₂＝CF[OCF₂-CF(CF₃)]₂O(CF₂)₂COOCH₃、

CF₂＝CFOCF₂CF(CF₃)O(CF₂)₃COOCH₃、

CF₂＝CFO(CF₂)₂COOCH₃、

CF₂＝CFO(CF₂)₃COOCH₃。

Examples of the monomer of group 3 include vinyl compounds having a functional group convertible to a sulfone type ion exchange group (sulfonic acid group). As having a rotaryVinyl compound having functional group substituted with sulfonic acid group, for example, CF is preferable₂＝CFO-X-CF₂-SO₂And F (wherein X represents a perfluoroalkylene group). Specific examples thereof include monomers shown below.

CF₂＝CFOCF₂CF₂SO₂F、

CF₂＝CFOCF₂CF(CF₃)OCF₂CF₂SO₂F、

CF₂＝CFOCF₂CF(CF₃)OCF₂CF₂CF₂SO₂F、

CF₂＝CF(CF₂)₂SO₂F、

CF₂＝CFO[CF₂CF(CF₃)O]₂CF₂CF₂SO₂F、

CF₂＝CFOCF₂CF(CF₂OCF₃)OCF₂CF₂SO₂F。

Among these, CF is more preferable₂＝CFOCF₂CF(CF₃)OCF₂CF₂CF₂SO₂F and CF₂＝CFOCF₂CF(CF₃)OCF₂CF₂SO₂F。

Copolymers obtained from these monomers can be produced by polymerization methods developed for homopolymerization and copolymerization of fluorinated ethylene, particularly by general polymerization methods used for tetrafluoroethylene. For example, in the nonaqueous method, polymerization can be carried out at a temperature of 0 to 200 ℃ and a pressure of 0.1 to 20MPa in the presence of a radical polymerization initiator such as a perfluorocarbon peroxide or an azo compound using an inert solvent such as perfluorocarbon or chlorofluorocarbon.

In the copolymerization, the kind and the ratio of the combination of the monomers are not particularly limited, and are selected and determined according to the kind and the amount of the functional group to be imparted to the resulting fluorine-containing polymer. For example, when a fluorine-containing polymer containing only carboxylic acid groups is produced, at least one monomer selected from the above-mentioned groups 1 and 2 may be copolymerized. In the case of producing a fluorine-containing polymer containing only sulfonic acid groups, at least one monomer selected from the above-mentioned group 1 and group 3 monomers may be copolymerized. In the case of producing a fluorine-containing polymer having a carboxylic acid group and a sulfonic acid group, at least one monomer selected from the group consisting of the monomers of the above-mentioned

groups

1, 2 and 3 may be copolymerized. In this case, the intended fluoropolymer can also be obtained by polymerizing the copolymer composed of the groups 1 and 2 and the copolymer composed of the groups 1 and 3, respectively, and then mixing them. The mixing ratio of the monomers is not particularly limited, and when the amount of the functional group per unit polymer is increased, the ratio of the monomers selected from the above-mentioned

groups

2 and 3 may be increased.

The total ion exchange capacity of the fluorine-containing copolymer is not particularly limited, but is preferably 0.5 to 2.0mg equivalent/g, more preferably 0.6 to 1.5mg equivalent/g. The total ion exchange capacity is an equivalent of an exchange group per unit weight of the dried resin, and can be measured by neutralization titration or the like.

In the membrane body 1a of the ion exchange membrane 1, a sulfonic acid layer 3 containing a fluorine-containing polymer having a sulfonic acid group and a carboxylic acid layer 2 containing a fluorine-containing polymer having a carboxylic acid group are laminated. By forming the membrane main body 1a having such a layer structure, the selective permeability of cations such as sodium ions can be further improved.

When the ion exchange membrane 1 is disposed in an electrolytic cell, it is generally disposed such that the sulfonic acid layer 3 is located on the anode side of the electrolytic cell and the carboxylic acid layer 2 is located on the cathode side of the electrolytic cell.

The sulfonic acid layer 3 is preferably made of a material having low electric resistance, and is preferably thicker than the carboxylic acid layer 2 in terms of film strength. The film thickness of the sulfonic acid layer 3 is preferably 2 to 25 times, more preferably 3 to 15 times that of the carboxylic acid layer 2.

The carboxylic acid layer 2 preferably has a high anion-removing property even if the film thickness is thin. The anion exclusivity as used herein refers to a property of preventing the intrusion or permeation of anions into the ion-exchange membrane 1. In order to improve the anion exclusivity, it is effective to dispose a carboxylic acid layer having a small ion exchange capacity or the like on the sulfonic acid layer.

As the fluorine-containing polymer for the sulfonic acid layer 3, for example, CF is used₂＝CFOCF₂CF(CF₃)OCF₂CF₂SO₂The polymers obtained with F as a monomer of group 3 are suitable.

As the fluorine-containing polymer for the carboxylic acid layer 2, for example, CF is used₂＝CFOCF₂CF(CF₂)O(CF₂)₂COOCH₃The polymers obtained as monomers of group 2 are suitable.

(coating layer)

The ion exchange membrane preferably has a coating layer on at least one face of the membrane main body. As shown in fig. 7, in the ion exchange membrane 1, coating layers 11a and 11b are formed on both surfaces of a membrane main body 1a, respectively.

The coating layer comprises inorganic particles and a binder.

The average particle diameter of the inorganic particles is more preferably 0.90 μm or more. When the average particle diameter of the inorganic particles is 0.90 μm or more, not only gas adhesion but also durability against impurities is remarkably improved. That is, particularly significant effects can be obtained by increasing the average particle diameter of the inorganic particles and satisfying the above-described specific surface area value. In order to satisfy such an average particle diameter and specific surface area, inorganic particles having an irregular shape are preferable. Inorganic particles obtained by melting or inorganic particles obtained by pulverizing raw ore can be used. Preferably, inorganic particles obtained by pulverizing raw ore can be suitably used.

The inorganic particles may have an average particle diameter of 2 μm or less. When the average particle size of the inorganic particles is 2 μm or less, the film can be prevented from being damaged by the inorganic particles. The average particle diameter of the inorganic particles is more preferably 0.90 to 1.2 μm.

Here, the average particle diameter can be measured by using a particle size distribution meter ("SALD 2200 manufactured by Shimadzu corporation").

The shape of the inorganic particles is preferably irregular. The resistance to impurities is further improved. In addition, the particle size distribution of the inorganic particles is preferably broad.

The inorganic particles preferably contain at least one inorganic substance selected from the group consisting of an oxide of a group IV element of the periodic table, a nitride of a group IV element of the periodic table, and a carbide of a group IV element of the periodic table. Particles of zirconia are more preferable from the viewpoint of durability.

The inorganic particles are preferably inorganic particles produced by pulverizing raw ores of the inorganic particles; or raw ore of inorganic particles is melted and purified, and spherical particles having uniform particle diameters are obtained as the inorganic particles.

The raw ore grinding method is not particularly limited, and examples thereof include a ball mill, a bead mill, a colloid mill, a cone mill, a disc mill, an edger, a flour mill, a hammer mill, a pellet mill, a VSI mill, a Wiley mill, a roll mill, and a jet mill. In addition, it is preferable to perform washing after pulverization, and in this case, it is preferable to perform acid treatment as a washing method. This can reduce impurities such as iron adhering to the surface of the inorganic particles.

The coating layer preferably comprises a binder. The binder is a component for forming a coating layer by holding inorganic particles on the surface of the ion exchange membrane. The binder preferably contains a fluorine-containing polymer in view of resistance to an electrolytic solution or a product generated by electrolysis.

The binder is more preferably a fluorine-containing polymer having a carboxylic acid group or a sulfonic acid group, from the viewpoint of resistance to an electrolytic solution or a product generated by electrolysis and adhesion to the surface of the ion exchange membrane. When a coating layer is provided on a layer (sulfonic acid layer) containing a fluoropolymer having sulfonic acid groups, the binder of the coating layer is more preferably a fluoropolymer having sulfonic acid groups. When a coating layer is provided on a layer (carboxylic acid layer) containing a fluoropolymer having carboxylic acid groups, a fluoropolymer having carboxylic acid groups is preferably used as the binder for the coating layer.

In the coating layer, the content of the inorganic particles is preferably 40 to 90% by mass, more preferably 50 to 90% by mass. The content of the binder is preferably 10 to 60% by mass, and more preferably 10 to 50% by mass.

The distribution density of the coating layer in the ion exchange membrane is preferably 1cm per unit ²Is 0.05-2 mg. When the ion exchange membrane has irregularities on the surface, the distribution density of the coating layer is preferably 1cm per 1cm²Is 0.5-2 mg.

The method for forming the coating layer is not particularly limited, and a known method can be used. For example, the following methods can be mentioned: the inorganic particles are dispersed in a solution containing a binder, and the obtained coating liquid is applied by spraying or the like.

(reinforcing core material)

The ion exchange membrane preferably has a reinforcing core material disposed inside the membrane main body.

The reinforcing core material is a member for reinforcing the strength and dimensional stability of the ion exchange membrane. By disposing the reinforcing core material inside the membrane main body, the expansion and contraction of the ion exchange membrane can be controlled particularly within a desired range. The ion exchange membrane does not expand or contract more than necessary during electrolysis and the like, and can maintain excellent dimensional stability for a long time.

The structure of the reinforcing core material is not particularly limited, and for example, a yarn called a reinforcing yarn may be spun to form the reinforcing core material. The reinforcing filaments referred to herein are members constituting a reinforcing core material, and refer to filaments capable of imparting desired dimensional stability and mechanical strength to the ion-exchange membrane and stably existing in the ion-exchange membrane. By using a reinforcing core material obtained by spinning the reinforcing yarn, more excellent dimensional stability and mechanical strength can be imparted to the ion exchange membrane.

The material of the reinforcing core material and the reinforcing filaments used in the reinforcing core material is not particularly limited, but is preferably a material having resistance to acids, alkalis, and the like, and is preferably a fiber composed of a fluorine-containing polymer because heat resistance and chemical resistance are required for a long period of time.

Examples of the fluorine-containing polymer used for reinforcing the core material include Polytetrafluoroethylene (PTFE), tetrafluoroethylene-perfluoroalkyl vinyl ether copolymer (PFA), tetrafluoroethylene-ethylene copolymer (ETFE), tetrafluoroethylene-hexafluoropropylene copolymer, chlorotrifluoroethylene-ethylene copolymer, and vinylidene fluoride Polymer (PVDF). Among these, fibers made of polytetrafluoroethylene are particularly preferably used from the viewpoint of heat resistance and chemical resistance.

The diameter of the reinforcing yarn for reinforcing the core material is not particularly limited, but is preferably 20 to 300 deniers, and more preferably 50 to 250 deniers. The weaving density (the number of beating-up threads per unit length) is preferably 5 to 50 threads/inch. The form of the reinforcing core material is not particularly limited, and for example, woven fabric, nonwoven fabric, knitted fabric, or the like is used, and a woven fabric form is preferable. The thickness of the woven fabric is preferably 30 to 250 μm, more preferably 30 to 150 μm.

The woven fabric or knitted fabric may be monofilament, multifilament, or yarn thereof, or split yarn, and various weaving methods such as plain weaving, leno weaving, knitting, ribbed weaving (コード coated article り), and crepe texture (シャーサッカ) may be used.

The weave and arrangement of the reinforcing core material in the membrane main body are not particularly limited, and may be appropriately set in consideration of the size and shape of the ion exchange membrane, the desired physical properties of the ion exchange membrane, the use environment, and the like.

For example, the reinforcing core material may be arranged along a predetermined one direction of the film main body, but from the viewpoint of dimensional stability, it is preferable to arrange the reinforcing core material along a predetermined first direction and arrange the other reinforcing core material along a second direction substantially perpendicular to the first direction. By arranging two or more reinforcing core members substantially in parallel inside the longitudinal film main body of the film main body, more excellent dimensional stability and mechanical strength can be imparted in multiple directions. For example, it is preferable to weave a reinforcing core material (warp) arranged in the longitudinal direction and a reinforcing core material (weft) arranged in the transverse direction into the surface of the film main body. From the viewpoints of dimensional stability, mechanical strength, and ease of production, more preferred are: a plain weave in which warp yarns and weft yarns are alternately floated and lowered to perform beating-up weaving; a leno weave formed by twisting 2 warps and weaving wefts at the same time; a square plain weave in which 2 or more warps arranged in parallel are laid with the same number of wefts to be woven; and so on.

It is particularly preferable to arrange the reinforcing core material in both the MD direction (traveling direction, longitudinal direction) and the TD direction (vertical direction, transverse direction) of the ion exchange membrane. That is, it is preferable to perform plain weaving in the MD direction and the TD direction. Here, the MD direction refers to a direction (flow direction) in which the membrane main body and various core materials (for example, a reinforcing core material, a reinforcing wire, a sacrificial wire described later) are transported in a process of producing an ion exchange membrane described later, and the TD direction refers to a direction substantially perpendicular to the MD direction. The yarns woven in the MD are referred to as MD yarns, and the yarns woven in the TD are referred to as TD yarns. Generally, many ion exchange membranes used for electrolysis are rectangular, and the longitudinal direction is the MD direction and the width direction is the TD direction. By weaving a reinforcing core material as MD yarns and a reinforcing core material as TD yarns, more excellent dimensional stability and mechanical strength can be imparted in multiple directions.

The arrangement interval of the reinforcing core material is not particularly limited, and may be suitably arranged in consideration of desired physical properties of the ion exchange membrane, use environment, and the like.

The aperture ratio of the reinforcing core material is not particularly limited, but is preferably 30% or more, and more preferably 50% or more and 90% or less. The aperture ratio is preferably 30% or more in terms of electrochemical properties of the ion-exchange membrane, and preferably 90% or less in terms of mechanical strength of the ion-exchange membrane.

The aperture ratio of the reinforcing core material is a ratio (B/a) of the total area (B) of the surfaces through which ions or the like (the electrolyte and cations (for example, sodium ions) contained therein) can pass in the area (a) of any one surface of the membrane main body. The total area (B) of the surface through which ions and other substances can pass is the total area of the region of the ion exchange membrane in which cations, electrolyte, and other substances are not cut by the reinforcing core material and the like included in the ion exchange membrane.

Fig. 8 is a schematic diagram for explaining the aperture ratio of the reinforcing core material constituting the ion exchange membrane. Fig. 8 is an enlarged view of a part of the ion exchange membrane, and only the arrangement of the reinforcing

core materials

21a and 21b in this region is illustrated, and other components are not illustrated.

The total area (B) of the region in which the ion or other substance can pass in the area (a) of the region surrounded by the reinforcing core material 21a arranged in the longitudinal direction and the reinforcing core material 21B arranged in the lateral direction, which is the area including the reinforcing core material, can be obtained by subtracting the total area (C) of the reinforcing core material from the area (a) of the region. That is, the aperture ratio can be obtained by the following formula (I).

(B)/(a) ═ ((a) - (C))/(a) … (I)

In the reinforcing core material, a tape yarn or a highly oriented monofilament containing PTFE is particularly preferable from the viewpoint of chemical resistance and heat resistance. Specifically, the following reinforcing core material is more preferably used: a high-strength porous sheet made of PTFE is cut into tape-like tape yarns or highly oriented monofilaments made of PTFE, and the tape yarns or the highly oriented monofilaments have 50 to 300 deniers and are plain woven with a weaving density of 10 to 50 threads/inch, and have a thickness in the range of 50 to 100 [ mu ] m. The opening ratio of the ion-exchange membrane including the reinforcing core material is more preferably 60% or more.

Examples of the shape of the reinforcing wire include a round wire and a ribbon wire.

(communicating hole)

The ion exchange membrane preferably has communication holes in the interior of the membrane main body.

The communicating hole is a hole that can serve as a flow path for ions and an electrolyte solution generated during electrolysis. The communicating hole is a tubular hole formed in the film body, and is formed by elution of a sacrificial core material (or a sacrificial filament) described later. The shape, the hole diameter, and the like of the communicating hole can be controlled by selecting the shape and the hole diameter of the sacrificial core material (sacrificial wire).

By forming the communicating holes in the ion exchange membrane, the mobility of the electrolytic solution can be ensured during electrolysis. The shape of the communication hole is not particularly limited, and may be a shape of a sacrificial core material used for formation of the communication hole according to a production method described later.

The communication holes are preferably formed so as to alternately pass through the anode side (sulfonic acid layer side) and the cathode side (carboxylic acid layer side) of the reinforcing core material. With this configuration, in the portion of the reinforcing core material where the through holes are formed on the cathode side, ions (for example, sodium ions) transported by the electrolyte filled in the through holes can also flow to the cathode side of the reinforcing core material. As a result, the flow of the cations is not interrupted, and the electric resistance of the ion exchange membrane can be further reduced.

The communication holes may be formed only in a predetermined one direction of the membrane main body constituting the ion exchange membrane, but are preferably formed in both the longitudinal direction and the transverse direction of the membrane main body from the viewpoint of exerting more stable electrolytic performance.

[ production method ]

Examples of a suitable method for producing an ion exchange membrane include a method including the following steps (1) to (6).

(1) The process comprises the following steps: a step of producing a fluorine-containing polymer having an ion exchange group or an ion exchange group precursor which can be hydrolyzed into an ion exchange group.

(2) The process comprises the following steps: and if necessary, weaving at least two or more reinforcing core materials and sacrificial filaments having a property of dissolving in an acid or an alkali and forming communicating holes, thereby obtaining a reinforcing material in which the sacrificial filaments are arranged between the adjacent reinforcing core materials.

(3) The process comprises the following steps: and a step of forming a film of the fluorine-containing polymer having an ion exchange group or an ion exchange group precursor which can be hydrolyzed into an ion exchange group.

(4) The process comprises the following steps: and a step of embedding the reinforcing material in the film as necessary to obtain a film body in which the reinforcing material is arranged.

(5) The process comprises the following steps: and (4) hydrolyzing the film body obtained in step (4) (hydrolysis step).

(6) The process comprises the following steps: and (5) providing a coating layer on the film body obtained in the step (5) (coating step).

The respective steps will be described in detail below.

(1) The process comprises the following steps: process for producing fluorine-containing polymer

In the step (1), the fluorine-containing polymer is produced by using the monomers of the raw materials described in the above-mentioned groups 1 to 3. In order to control the ion exchange capacity of the fluorine-containing polymer, the mixing ratio of the monomers of the raw materials may be adjusted in the production of the fluorine-containing polymer forming each layer.

(2) The process comprises the following steps: process for producing reinforcing material

The reinforcing material is a woven fabric or the like into which reinforcing yarns are woven. The reinforcing core material is formed by embedding a reinforcing material in the film. In the production of an ion exchange membrane having interconnected pores, sacrificial filaments are also woven into the reinforcement material together. In this case, the mixed amount of the sacrificial filaments is preferably 10 to 80% by mass, more preferably 30 to 70% by mass of the entire reinforcing material. By weaving in the sacrificial thread, dislocation of the reinforcing core material can also be prevented.

The sacrificial filaments have solubility in the film production process or the electrolytic environment, and rayon, polyethylene terephthalate (PET), cellulose, polyamide, or the like is used. Further, polyvinyl alcohol having a thickness of 20 to 50 deniers and composed of monofilament or multifilament is also preferable.

In the step (2), the arrangement of the reinforcing core material and the sacrificial wire is adjusted to control the aperture ratio, the arrangement of the through holes, and the like.

(3) The process comprises the following steps: film formation step

In the step (3), the fluoropolymer obtained in the step (1) is formed into a film by an extruder. The film may have a single-layer structure, may have a 2-layer structure of the sulfonic acid layer and the carboxylic acid layer as described above, or may have a multilayer structure of 3 or more layers.

Examples of the method for forming a film include the following methods.

A method of separately forming a film from a fluoropolymer having a carboxylic acid group and a fluoropolymer having a sulfonic acid group.

A method for producing a composite film by coextrusion of a fluoropolymer having a carboxylic acid group and a fluoropolymer having a sulfonic acid group.

The number of the films may be two or more. In addition, coextrusion of different types of films is preferable because it contributes to improvement in the interfacial adhesive strength.

(4) The process comprises the following steps: process for obtaining film body

In the step (4), the reinforcing material obtained in the step (2) is embedded in the film obtained in the step (3), thereby obtaining a film body in which the reinforcing material is present.

Preferred methods for forming the film body include the following: (i) a method in which a fluorine-containing polymer having a carboxylic acid group precursor (for example, a carboxylic acid ester group) on the cathode side (hereinafter, a layer formed of the polymer is referred to as a first layer) and a fluorine-containing polymer having a sulfonic acid group precursor (for example, a sulfonyl fluoride functional group) (hereinafter, a layer formed of the polymer is referred to as a second layer) are formed into a film by a coextrusion method, a heat source and a vacuum source are used as necessary, a heat-resistant release paper having air permeability is laminated on a flat plate or a cylinder having a large number of pores on the surface through a reinforcing material and a second layer/first layer composite film in this order, and air between the layers is removed by reducing the pressure at a temperature at which the polymers are melted to integrate the layers; (ii) separately from the second/first composite films, a fluorine-containing polymer (third layer) having a sulfonic acid group precursor is separately formed into a film in advance, and laminated in this order on a flat plate or a cylinder having a large number of fine pores on the surface thereof via a heat-resistant release paper having air permeability by using a heat source and a vacuum source as necessary, and a composite film composed of the third layer, a reinforcing core material, and the second/first composite films is subjected to pressure reduction at a temperature at which the polymers are melted to remove air between the layers and integrate them at the same time.

Here, when the first layer and the second layer are coextruded, the adhesive strength at the interface can be improved.

In addition, the method of integration under reduced pressure has a feature that the thickness of the third layer on the reinforcing material is increased as compared with the pressure pressing method. Furthermore, since the reinforcing material is fixed to the inner surface of the membrane main body, the reinforcing material has a performance of sufficiently maintaining the mechanical strength of the ion exchange membrane.

The lamination variation described here is merely an example, and an appropriate lamination pattern (for example, a combination of layers or the like) may be appropriately selected in consideration of a desired layer structure of the film body, physical properties, or the like, and then the coextrusion may be performed.

In order to further improve the electrical performance of the ion exchange membrane, a fourth layer made of a fluorine-containing polymer having both a carboxylic acid group precursor and a sulfonic acid group precursor may be interposed between the first layer and the second layer, or a fourth layer made of a fluorine-containing polymer having both a carboxylic acid group precursor and a sulfonic acid group precursor may be used instead of the second layer.

The method for forming the fourth layer may be a method in which the fluorine-containing polymer having a carboxylic acid group precursor and the fluorine-containing polymer having a sulfonic acid group precursor are separately produced and then mixed, or a method in which a monomer having a carboxylic acid group precursor and a monomer having a sulfonic acid group precursor are copolymerized.

When the fourth layer is an ion exchange membrane, the first layer and the fourth layer may be formed by coextrusion, and the third layer and the second layer may be separately formed into a membrane and then laminated by the above method; the 3 layers of the first layer/fourth layer/second layer may also be filmed by coextrusion at once.

In this case, the flow direction of the extruded film is the MD direction. In this way, a membrane main body including a fluorine-containing polymer having an ion exchange group can be formed on the reinforcing material.

The ion exchange membrane preferably has a protruding portion, i.e., a convex portion, made of a fluoropolymer having a sulfonic acid group on the surface side made of the sulfonic acid layer. The method for forming such a convex portion is not particularly limited, and a known method for forming a convex portion on a resin surface can be employed. Specifically, for example, a method of embossing the surface of the film body may be mentioned. For example, when the composite film and the reinforcing material are integrated, the convex portion can be formed by using a release paper which is embossed in advance. When the projections are formed by embossing, the height and arrangement density of the projections can be controlled by controlling the embossing shape (the shape of the release paper) to be transferred.

(5) Hydrolysis step

In the step (5), a step (hydrolysis step) of hydrolyzing the membrane main body obtained in the step (4) and converting the ion exchange group precursor into an ion exchange group is performed.

In the step (5), the sacrificial filaments included in the film body are dissolved and removed with an acid or an alkali, whereby the dissolution holes can be formed in the film body. The sacrificial filaments may remain in the communicating holes without being completely dissolved and removed. The sacrificial filaments remaining in the communicating holes can be dissolved and removed by the electrolytic solution when the ion exchange membrane is subjected to electrolysis.

The sacrificial filaments are soluble to acid or alkali in the ion exchange membrane production process or the electrolytic environment, and the sacrificial filaments are dissolved out to form communicating pores at the positions.

(5) The step (4) may be performed by immersing the film body obtained in the step (4) in a hydrolysis solution containing an acid or an alkali. As the hydrolysis solution, for example, a mixed solution containing KOH and DMSO (dimethyl sulfoxide) may be used.

The mixed solution preferably contains 2.5 to 4.0N KOH and 25 to 35 mass% DMSO.

The hydrolysis temperature is preferably 70 to 100 ℃. The higher the temperature, the more the apparent thickness can be increased. More preferably 75 to 100 ℃.

The hydrolysis time is preferably 10 to 120 minutes. The longer the time, the more the apparent thickness can be increased. More preferably 20 to 120 minutes.

Here, the step of forming the communicating hole by dissolving out the sacrificial thread will be described in more detail. Fig. 9 (a) and (b) are schematic views for explaining a method of forming the communicating holes of the ion exchange membrane.

In fig. 9 (a) and (b), only the communication holes 504 formed by the reinforcing wires 52, the sacrificial wires 504a, and the sacrificial wires 504a are illustrated, and other members such as the membrane main body are not illustrated.

First, the reinforcing filaments 52 constituting the reinforcing core material in the ion exchange membrane and the sacrificial filaments 504a for forming the communication holes 504 in the ion exchange membrane are used as the woven reinforcing material. In the step (5), the sacrificial filaments 504a are eluted to form the communication holes 504.

The method described above can be simply and conveniently used by adjusting the method of knitting the reinforcing filaments 52 and the sacrificial filaments 504a depending on how the reinforcing core material and the communication holes are arranged in the membrane main body of the ion exchange membrane.

Fig. 9 (a) shows a plain-weave reinforcing material in which reinforcing filaments 52 and sacrificial filaments 504a are woven into the paper surface in both the longitudinal direction and the transverse direction, but the arrangement of the reinforcing filaments 52 and the sacrificial filaments 504a in the reinforcing material may be changed as needed.

(6) Coating process

In the step (6), a coating liquid containing inorganic particles obtained by pulverizing or melting raw ore and a binder is prepared, and the coating liquid is applied to the surface of the ion-exchange membrane obtained in the step (5) and dried, whereby a coating layer can be formed.

As the binder, a binder obtained as follows is preferable: hydrolyzing a fluorine-containing polymer having an ion exchange group precursor with an aqueous solution containing dimethyl sulfoxide (DMSO) and potassium hydroxide (KOH), immersing the hydrolyzed polymer in hydrochloric acid, and replacing the counter ion of the ion exchange group with H⁺Thereby obtaining a binder (for example, a fluorine-containing polymer having a carboxyl group or a sulfo group). This is preferable because it is easily dissolved in water or ethanol described later.

The binder was dissolved in a solution obtained by mixing water and ethanol. The preferable volume ratio of water to ethanol is 10:1 to 1:10, more preferably 5:1 to 1:5, and still more preferably 2:1 to 1: 2. The inorganic particles are dispersed in the thus-obtained solution by a ball mill to obtain a coating liquid. In this case, the average particle diameter of the particles may be adjusted by adjusting the time and the rotation speed at which the dispersion is performed. The preferred mixing amounts of the inorganic particles and the binder are as described above.

The concentration of the inorganic particles and the binder in the coating liquid is not particularly limited, and it is preferably a dilute coating liquid. Thereby enabling to coat it uniformly on the surface of the ion exchange membrane.

In addition, when the inorganic particles are dispersed, a surfactant may be added to the dispersion liquid. As the surfactant, nonionic surfactants are preferred, and examples thereof include HS-210, NS-210, P-210, E-212 and the like manufactured by Nichisu oil Co.

The obtained coating liquid was applied to the surface of the ion exchange membrane by spray coating or roll coating, thereby obtaining an ion exchange membrane.

[ microporous film ]

As described above, the microporous membrane of the present embodiment is not particularly limited as long as it can form a laminate with an electrode for electrolysis, and various microporous membranes can be applied.

The porosity of the microporous membrane of the present embodiment is not particularly limited, and may be, for example, 20 to 90, preferably 30 to 85. The porosity can be calculated, for example, by the following equation.

Porosity (1- (weight of film in dry state)/(volume calculated from thickness, width, and length of film, and weight calculated from density of film raw material)) × 100

The average pore diameter of the microporous membrane of the present embodiment is not particularly limited, and may be, for example, 0.01 to 10 μm, preferably 0.05 to 5 μm. The average pore diameter is, for example, observed by cutting the membrane perpendicularly to the thickness direction and observing the cross section by FE-SEM. The average pore diameter can be determined by measuring the diameters of pores observed at about 100 points and averaging the diameters.

The thickness of the microporous membrane of the present embodiment is not particularly limited, and may be, for example, 10 to 1000. mu.m, preferably 50 to 600. mu.m. The thickness can be measured using, for example, a micrometer (manufactured by Mitutoyo corporation).

Specific examples of the microporous membrane include a microporous membrane described in Zirfon Perl UTP500 (also referred to as a Zirfon membrane in this embodiment) manufactured by Agfa, pamphlet of International publication No. 2013-183584, pamphlet of International publication No. 2016-203701, and the like.

In the present embodiment, the separator preferably includes a 1 st ion exchange resin layer and a 2 nd ion exchange resin layer having an EW (ion exchange equivalent weight) different from that of the 1 st ion exchange resin layer. In addition, the separator preferably includes a 1 st ion exchange resin layer and a 2 nd ion exchange resin layer having a functional group different from that of the 1 st ion exchange resin layer. The ion exchange equivalent can be adjusted by the functional group introduced, as described above with respect to the functional group that can be introduced.

(Water electrolysis)

The electrolytic cell of the present embodiment, that is, the electrolytic cell for electrolysis of water, has a structure in which the ion exchange membrane in the electrolytic cell for electrolysis of salt is changed to a microporous membrane. The present invention is different from the above-described electrolytic cell for salt electrolysis in that the raw material to be supplied is water. In the case of other configurations, the electrolytic cell for electrolysis of water may be configured in the same manner as the electrolytic cell for electrolysis of salt. In the case of salt electrolysis, chlorine gas is generated in the anode chamber, and therefore titanium is used as a material for the anode chamber. Examples thereof include nickel. The anode coating is preferably a catalyst coating for oxygen generation. Examples of the catalyst coating include metals, oxides, and hydroxides of platinum group metals and transition metals. For example, elements such as platinum, iridium, palladium, ruthenium, nickel, cobalt, and iron can be used.

[ examples ]

The present embodiment will be described in more detail with reference to the following examples and comparative examples, but the present embodiment is not limited to the following examples.

(diaphragm)

As the separator used for producing the laminate, an ion exchange membrane a produced as follows was used.

As the reinforcing core material, Polytetrafluoroethylene (PTFE) monofilament (hereinafter referred to as PTFE filament) of 90D was used. As the sacrificial yarn, yarn obtained by twisting 35D/6F polyethylene terephthalate (PET) at 200 turns/m (hereinafter referred to as PET yarn) was used. First, in both TD and MD directions, a woven fabric was obtained by plain-weaving PTFE filaments at 24 filaments/inch and sacrificial filaments arranged at 2 filaments between adjacent PTFE filaments. The obtained woven fabric was pressed with a roller to obtain a reinforcing material as a woven fabric having a thickness of 70 μm.

Then, it is prepared as CF₂＝CF₂And CF₂＝CFOCF₂CF(CF₃)OCF₂CF₂COOCH₃Resin A which is a dry resin having an ion exchange capacity of 0.85mg equivalent/g; is CF₂＝CF₂And CF₂＝CFOCF₂CF(CF₃)OCF₂CF₂SO₂F, and resin B having an ion exchange capacity of 1.03mg equivalent/g.

Using these resin A and resin B, a 2-layer film X having a resin A layer thickness of 15 μm and a resin B layer thickness of 84 μm was obtained by a coextrusion T-die method. A single-layer film Y having a thickness of 20 μm was obtained by the T-die method using only the resin B.

Subsequently, a release paper (conical embossing having a height of 50 μm), a film Y, a reinforcing material, and a film X were sequentially laminated on a hot plate having a heating source and a vacuum source inside and having fine holes on the surface thereof, and the release paper was removed after heating and pressure reduction for 2 minutes under conditions of a hot plate surface temperature of 223 ℃ and a vacuum degree of 0.067MPa, thereby obtaining a composite film. The films X are laminated in the following manner as the resin B.

The obtained composite membrane was immersed in an aqueous solution containing 30 mass% of dimethyl sulfoxide (DMSO) and 15 mass% of potassium hydroxide (KOH) at 80 ℃ for 20 minutes, thereby performing saponification. Thereafter, the substrate was immersed in an aqueous solution containing sodium hydroxide (NaOH)0.5N at 50 ℃ for 1 hour to replace the counter ion of the ion exchange group with Na, followed by water washing. Then, the surface of the side of the resin B was polished at a relative speed of 100 m/min and a pressing amount of 2mm, to form an open pore portion, and then dried at 60 ℃.

Further, 20 mass% of zirconia having a 1-order particle diameter of 1 μm was added to a 5 mass% ethanol solution of an acid resin of resin B, and the mixture was dispersed to prepare a suspension, and the suspension was sprayed on both surfaces of the composite film by a suspension spraying method to form a coating layer of zirconia on the surface of the composite film, thereby obtaining an ion-exchange membrane a as a separator.

Measurement of coating density of zirconia by fluorescent X-rayThe degree of the reaction mixture was measured, and the result was 0.5mg/cm². Here, the average particle diameter was measured by a particle size distribution meter ("SALD (registered trademark) 2200", manufactured by shimadzu corporation).

(electrode for electrolysis)

As the electrolysis electrode, the following cathode electrolysis electrode and anode electrolysis electrode were used.

As a base material of the electrode for cathode electrolysis, a nickel foil having a gauge thickness of 22 μm, a length of 95mm and a width of 110mm was prepared.

One surface of the nickel foil is subjected to a surface roughening treatment by nickel plating.

The arithmetic average roughness Ra of the roughened surface was 0.95. mu.m.

For the surface roughness measurement, a stylus-type surface roughness measuring instrument SJ-310 (Mitutoyo Co., Ltd.) was used.

The measurement sample was set on a surface plate parallel to the ground, and the arithmetic average roughness Ra was measured under the following measurement conditions. In the measurement, when 6 times of the measurement were carried out, the average value thereof was recorded.

< shape of contact pin > cone angle 60 °, tip radius 2 μm, and static measurement force 0.75mN

< roughness standard > JIS2001

< evaluation Curve > R

< Filter > GAUSS

< value of sampling length λ c >0.8mm

< sampling length value λ s >2.5 μm

< number of intervals >5

< front walk, rear walk > have

A porous foil was produced by punching a circular hole in the nickel foil. The open pore ratio calculated as follows was 44%.

(measurement of open porosity)

For the electrode for electrolysis, the surface area was uniformly measured at 10 points using a digital thickness gauge (manufactured by Mitutoyo corporation, minimum display 0.001mm), and the average value was calculated. The volume was calculated by using the thickness of the electrode (gauge thickness). The mass is then determined by the ratio of the metals using an electronic balanceHeavy (specific gravity of nickel is 8.908 g/cm)³Specific gravity of titanium is 4.506g/cm³) And calculating the opening rate or the void ratio.

Open pore ratio (porosity) (%) (1- (electrode mass)/(electrode volume × specific gravity of metal)) × 100

The coating liquid for forming the electrode catalyst was prepared in the following order.

A ruthenium nitrate solution (Furuya Metal, K.K.) having a ruthenium concentration of 100g/L and cerium nitrate (Kishida Chemical Co., Ltd.) were mixed so that the molar ratio of the ruthenium element to the cerium element was 1: 0.25. The mixture was sufficiently stirred to prepare a cathode coating solution.

The barrel containing the coating liquid is arranged at the lowest part of the roller coating device. The coating roller was wound around a cylinder made of PVC (polyvinyl chloride) with a rubber (INOAC CORPORATION, E-4088, thickness 10mm) made of foamed EPDM (ethylene-propylene-diene rubber) of a self-contained bubble type, and was set so as to be in constant contact with the coating liquid. On top of this, a coating roll wound with the same EPDM was provided, and further, a roll made of PVC was provided thereon. The electrolytic electrode base material was passed between the 2 nd coating roll and the uppermost PVC roll to apply the coating solution (roll coating method). Thereafter, the resultant was dried at 50 ℃ for 10 minutes, pre-fired at 150 ℃ for 3 minutes, and fired at 350 ℃ for 10 minutes. These operations of coating, drying, pre-firing and firing are repeated until a predetermined coating amount is reached. The thickness of the thus-obtained cathode electrode for electrolysis (length 95mm, width 110mm) was 28 μm. The thickness of the catalyst layer (total thickness of ruthenium oxide and cerium oxide) was 6 μm obtained by subtracting the thickness of the electrode base material for electrolysis from the thickness of the electrode. The catalyst layer was also formed on the surface not roughened.

As an electrode base material for anode electrolysis, a material having a gauge thickness of 100 μm, a titanium fiber diameter of about 20 μm and a weight per unit area of 100g/m was used²And titanium nonwoven fabric with an aperture ratio of 78%.

A coating liquid for forming an electrode catalyst was prepared in the following order. A ruthenium chloride solution (Tahitian noble metal industries, Ltd.) having a ruthenium concentration of 100g/L, iridium chloride (Tahitian noble metal industries, Ltd.) having an iridium concentration of 100g/L, and titanium tetrachloride (Wako pure chemical industries, Ltd.) were added in such a manner that the molar ratio of the ruthenium element, the iridium element and the titanium element was 0.25: 0.25: mixed in the mode of 0.5. The mixed solution was sufficiently stirred to prepare an anode coating solution.

The barrel containing the coating liquid is arranged at the lowest part of the roller coating device. The coating roller was wound around a cylinder made of PVC (polyvinyl chloride) with a rubber (INOAC CORPORATION, E-4088, thickness 10mm) made of foamed EPDM (ethylene-propylene-diene rubber) of a self-contained bubble type, and was set so as to be in constant contact with the coating liquid. On top of this, a coating roll wound with the same EPDM was provided, and further, a roll made of PVC was provided thereon. The electrode base material was passed between the 2 nd coating roll and the uppermost PVC roll to apply the coating solution (roll coating method). After the coating liquid was applied to a porous titanium foil, the foil was dried at 60 ℃ for 10 minutes and baked at 475 ℃ for 10 minutes. After repeating a series of the coating, drying, pre-firing and firing operations, firing was performed at 520 ℃ for 1 hour. The thickness of the obtained electrode for anodic electrolysis (length 95mm, width 110mm) was 114. mu.m.

[ example 1]

(example of Using an electrode-separator laminate for cathode Electrolysis)

A laminate for update (new laminate) is prepared in advance as follows. First, an ion exchange membrane A having a length of 1.5m and a width of 2.5m was prepared by the method described above. In addition, 4 pieces of 0.3m long and 2.4m wide cathode electrolysis electrodes were prepared by the above-described method.

The ion exchange membrane a was immersed in a 2% sodium bicarbonate solution for a day and night, and then the cathode was arranged on the carboxylic acid layer side without any gap, thereby producing a laminate of the electrode for cathode electrolysis and the ion exchange membrane a. When the cathode electrolysis electrode is placed on the ion exchange membrane a, the interface tension is exerted due to contact with the aqueous sodium bicarbonate solution, and the cathode electrolysis electrode and the ion exchange membrane a are integrated by adsorption. When the integration is performed in this manner, no pressure is applied. The temperature during the integration was 23 ℃.

Then, the process of the present invention is carried out,an existing large-sized electrolytic cell (electrolytic cell having the same structure as that of the electrolytic cell shown in FIGS. 3 and 4) already including an existing laminate and the electrolytic cell (described above)Electrode-ion exchange membrane for cathode electrolysisA ofLaminate bodyLaminate of the same configuration) as a component of the electrolytic cell, the fixing state of the adjacent electrolytic cell by the pressurizer is released, and the existing laminate and the adjacent electrolytic cell are brought into a state with a gap therebetween. The existing laminate is taken out and the renewed laminate (new laminate) is transferred to a large-sized electrolytic cell. A new laminate is inserted between electrolytic cells in a large electrolytic cell, and then the electrolytic cells are moved by pressing from a presser so that the new laminate is sandwiched between the adjacent electrolytic cells.

The electrode and the separator can be replaced more easily than before. If a laminate is prepared in advance during the electrolysis operation, it is evaluated that the electrode renewal and the replacement of the separator can be completed in about several tens of minutes per 1 cell.

[ example 2]

(example of Using an electrode-separator laminate for Anode Electrolysis)

A laminate for update (new laminate) is prepared in advance as follows. First, an ion exchange membrane A having a length of 1.5m and a width of 2.5m was prepared by the method described above. In addition, 4 pieces of the electrode for anodic electrolysis having a length of 0.3m and a width of 2.4m were prepared in the manner described above.

The ion exchange membrane a was immersed in a 2% sodium bicarbonate solution for a day and night, and then the anode was arranged on the sulfonic acid layer side without a gap, thereby producing a laminate of an electrode for anode electrolysis and the ion exchange membrane a. When the electrode for anode electrolysis is placed on the ion exchange membrane a, the contact with the aqueous sodium bicarbonate solution exerts an interfacial tension, and the electrode for anode electrolysis and the ion exchange membrane a are integrated by adsorption. When the integration is performed in this manner, no pressure is applied. The temperature during the integration was 23 ℃.

Next, in an existing large electrolytic cell (an existing electrolytic cell having the same structure as in example 1), the fixing state of the adjacent electrolytic cell by the pressurizer was released, and a state was obtained in which a gap was present between the existing layered body and the adjacent electrolytic cell. The existing laminate is taken out and the renewed laminate (new laminate) is transferred to a large-sized electrolytic cell. A new laminate is inserted between electrolytic cells in a large electrolytic cell, and then the electrolytic cells are moved by pressing from a presser to sandwich the new laminate between the adjacent electrolytic cells.

The electrode and the separator are replaced more easily than before. When the laminate was prepared in advance during the electrolysis operation, it was evaluated that the electrode renewal and the replacement of the separator could be completed in about several tens of minutes per 1 cell.

[ example 3]

(example of Using an electrode-separator-electrode laminate for Anode Electrolysis)

A laminate for update (new laminate) is prepared in advance as follows. First, an ion exchange membrane A having a length of 1.5m and a width of 2.5m was prepared by the method described above. In addition, 4 pieces of an electrode for anodic electrolysis and an electrode for cathodic electrolysis each having a length of 0.3m and a width of 2.4m were prepared by the above-mentioned method.

After immersing the ion exchange membrane a in a 2% sodium bicarbonate solution for one day and night, the cathode electrolysis electrode was arranged on the carboxylic acid layer side without a gap, and the anode electrolysis electrode was arranged on the sulfonic acid layer side without a gap, to prepare a laminate of the anode electrolysis electrode, the ion exchange membrane a, and the cathode electrolysis electrode. When the anode electrolysis electrode and the cathode electrolysis electrode are placed on the ion exchange membrane a, the contact with the aqueous sodium bicarbonate solution causes interfacial tension to act, and the anode electrolysis electrode and the cathode electrolysis electrode are integrated with the ion exchange membrane a by adsorption. When the integration is performed in this manner, no pressure is applied. The temperature during the integration was 23 ℃.

Next, the existing large-sized electrolytic cell (electrolytic cell having the same structure as that of the electrolytic cell shown in FIGS. 3 and 4) is already provided with the existing laminate (similar to that described above)Electrode-ion exchange membrane for cathode electrolysisAOf electrodes for anodic electrolysisLaminate of the same constitution) as a component of the electrolytic cell, the fixing state of the adjacent electrolytic cells by the pressurizer is released,the existing laminate and the adjacent electrolytic cell are in a state of having a gap therebetween. The existing laminate is taken out and the renewed laminate (new laminate) is transferred to a large-sized electrolytic cell. A new laminate is inserted between electrolytic cells in a large electrolytic cell, and then the electrolytic cells are moved by pressing from a presser to sandwich the new laminate between the adjacent electrolytic cells.

Comparative example 1

(existing electrode renewal)

In an existing large-sized electrolytic cell (the same electrolytic cell as that shown in fig. 3 and 4) without an existing laminate, the fixation of the adjacent electrolytic cell and the ion exchange membrane a by the pressurizer is released, and the existing ion exchange membrane a is taken out to form a state in which a gap is present between the electrolytic cells. Then the electrolytic cell is hoisted out of the large electrolytic cell by a crane. And (4) conveying the taken electrolytic cell to a factory where welding construction can be performed.

After the anode welded to the rib of the electrolytic cell is peeled off, burrs and the like on the peeled off portion are ground and smoothed by a grinder or the like. The cathode is removed from the portion where the current collector is woven and fixed, and the cathode is peeled off.

Thereafter, a new anode (an anode having the same configuration as that of the anode of the existing electrolytic cell) is provided on the rib of the anode chamber, and the new anode is fixed to the electrolytic cell by spot welding. Similarly, a new cathode (a cathode having the same configuration as that of the cathode of the existing electrolytic cell) is provided on the cathode side, and is folded and fixed into the current collector.

The renewed electrolytic cell is transported to a place of the large electrolytic cell, and the electrolytic cell is returned to the electrolytic cell by a crane.

The time required from releasing the fixation of the electrolytic cell and the ion exchange membrane A to fixing the electrolytic cell again is 1 day or more.

Claims

1. A method for manufacturing an electrolytic cell, comprising arranging a new laminate comprising a new electrode for electrolysis and a new separator functioning as an anode and/or a cathode in an existing electrolytic cell, wherein the existing electrolytic cell comprises an anode, a cathode facing the anode, and an existing laminate comprising an electrode for electrolysis and a separator functioning as an anode and/or a cathode, the existing laminate being arranged between the anode and the cathode,

Wherein the manufacturing method comprises the following steps:

a step A of removing the existing laminate from the existing electrolytic bath by releasing the fixing state of the adjacent electrolytic bath and the existing laminate by a pressurizer to form a gap between the electrolytic bath and the existing laminate and then detaching the existing laminate to be renewed from the existing electrolytic bath,

a step B of disposing the new layer between the anode and the cathode, and

and a step C of fixing the members in the new electrolytic cell by connecting the members in the new electrolytic cell again by the pressurizer.

2. The method of manufacturing an electrolytic cell according to claim 1, wherein the electrolysis electrode comprises an anode electrolysis electrode A1 and a cathode electrolysis electrode B1 in the existing laminate.

3. The method of producing an electrolytic cell according to claim 1 or 2, wherein the new electrolysis electrode comprises an anode electrolysis electrode A2 and a cathode electrolysis electrode B2 in the new laminate.