JP4986298B2 - Method for producing solid electrolyte film and web-like solid electrolyte film - Google Patents

Description

The present invention relates to a method for producing a solid electrolyte film and a web-like solid electrolyte film , and more particularly to a method for producing a solid electrolyte film having a proton conductivity and used in a fuel cell and a web-like solid electrolyte film . is there.

  Fuel cells are attracting attention as next-generation fuels that can improve environmental pollution and energy problems. The fuel cell has a plurality of stacked fuel cells (also referred to as electrode membrane composite (MEA)), and these fuel cells are electrically connected in series. The fuel cell includes an anode electrode and a cathode electrode connected by an external circuit, and a solid electrolyte film sandwiched between these electrodes. A typical process in which the fuel cell generates an electromotive force is as follows. First, when a hydrogen atom-containing substance is supplied to the cathode electrode, the hydrogen atoms become protons in the cathode electrode. Next, this proton passes through the solid electrolyte film and combines with oxygen at the anode electrode, so that an electromotive force can be generated between the two electrodes of the fuel cell.

  Recently, a solid electrolyte film (referred to as an organic polymer film) formed of a polymer has attracted attention among solid electrolytes. Since this organic polymer type film has the characteristics that the operating temperature is low and the size and weight can be reduced, it is expected to be used for a fuel cell for home use or in-vehicle use. Therefore, the organic polymer type film is required to have characteristics such as high proton conductivity, excellent heat resistance, and uniform in-plane characteristics.

  By the way, as a method for forming a polymer into a film, there are a melt film forming method and a solution film forming method as well known. The former can produce a film without using a solvent, but there are problems that the polymer is modified by heating and impurities in the raw polymer remain in the film as they are. On the other hand, although the latter has problems in equipment such as solution production equipment and solvent recovery equipment, the temperature during heating may be low, and it is possible to remove impurities in the polymer in the solution production process. There is. Furthermore, in the latter, there is an advantage that a film excellent in flatness and smoothness can be manufactured as compared with the former film.

  In the solution casting method, a dope containing an organic compound as a raw material and a solvent is cast on a support to form a cast film, and then the cast film is peeled off from the support and further dried by a drying means. This is a method of drying to form a film, and is widely used not only as a method for producing an organic polymer type film but also as a method for producing a polymer film for optical applications. However, the organic polymer film is an organic polymer that satisfies the above-mentioned requirements because it is composed of a polymer compound and is sensitive to temperature and humidity, and it is difficult to adjust the reaction level. It is difficult to produce a mold film.

  Therefore, first, as a method for producing an organic polymer film having excellent quality and heat resistance, for example, a method of producing by a solution film forming method using a dope containing an acidic group-containing polymer (see, for example, Patent Document 1) Alternatively, a method has been proposed in which a dope containing an acidic group-containing polymer is made into a gel film by a solution casting method, and then washed with water and dried to form a film (see, for example, Patent Document 2). In addition, as a method for producing an organic polymer film excellent in high proton conductivity, heat stability, and processability, a film formed by a solution film-forming method is an organic solvent having a boiling point of 100 ° C. or higher. There has been proposed a method of dipping in an aqueous compound solution to cause equilibrium swelling and then drying it (see, for example, Patent Document 3).

  In addition, as a method for producing an organic polymer type film having high proton conductivity and excellent mechanical strength, a dope containing an ionic conductive component is made into a film by a casting method and then immersed in a solvent to dissolve in water. A method of removing the compound and drying it has been proposed (see, for example, Patent Document 4). Further, Patent Documents 5 to 7 propose an organic polymer film having high proton conductivity that is formed from a dope containing a predetermined polyarylene by a solution casting method.

In addition, as a method for producing an organic polymer film having a high proton conductivity, a method of forming a film from a dope containing a polymer having a sulfonic acid group (see, for example, Patent Document 8), or a film was formed from a dope containing a polymer. Thereafter, a method of acid-treating and sulfonating this has been proposed (for example, see Patent Document 9).
JP 2005-232240 A JP 2005-235466 A Japanese Patent Laid-Open No. 2005-248128 JP 2005-310443 A JP 2004-079378 A JP-A-2005-146018 JP 2005-239833 A JP 2005-268144 A JP 2005-268145 A

  Since both methods of Patent Documents 8 and 9 are so-called off-line production methods in which film formation and acid treatment are performed on different production lines, it is difficult to produce a film continuously and in large quantities. Regardless of these methods, Patent Documents 1 to 7 are also manufacturing methods on a small scale, and are not considered methods for mass production. Further, Patent Documents 5 to 7 describe that various organic polymer type films can be produced by a solution casting method, but no specific method is described.

  By the way, after many years of research and development of a method for producing a solid electrolyte film, various methods for producing a solid electrolyte film have been established, and a solid electrolyte film having excellent proton conductivity has been provided to the market. However, the current fuel cell made of a solid electrolyte film cannot sufficiently satisfy the specifications expected from the market as a fuel cell for home use or automobile, particularly the output density. This power density greatly depends on the proton conductivity of the solid electrolyte film. Therefore, in order to meet the demand from the market, further improvement is required for the method for producing the solid electrolyte film from the viewpoint of improving proton conductivity.

  As a result of intensive studies, the present inventor has found that the proton conductivity of the solid electrolyte film is improved by energizing the film-like intermediate in the production process of the solid electrolyte film via the acid-containing liquid. . The present invention provides a solid electrolyte film used for a fuel cell having excellent proton conductivity, a production method capable of continuously and mass-producing the solid electrolyte film, an electrode membrane composite, and a fuel cell. With the goal.

In order to achieve the above object, the present invention has the following features.
(1) In the method for producing a solid electrolyte film of the present invention, a dope containing a polymer, which is a solid electrolyte having a cationic species, and an organic solvent is cast from a casting die on a traveling support. A casting film forming step to be formed; a stripping step of peeling off the casting membrane as a film from the support; an acid treatment step of performing proton substitution on the film; and energizing the film containing the polymer as a solid electrolyte. An energization step, and the energization step is performed continuously after the acid treatment step.
(2) In the energization step, it is preferable to energize the film through a first liquid containing an acid that is a proton donor.
(3) a first electrode that is in contact with the first liquid, and the second electrode that is in contact with the first liquid and disposed so that a distance from the first electrode is 300 mm or less. It is preferable to perform the said electricity supply process using.
(4) In the acid treatment step performed through the second liquid containing an acid that is a proton donor, the proton concentration of the second liquid is preferably 0.05 mol / l or more.
(5) It is preferable that the formula amount of the anion contained in the first liquid or the second liquid is 40 or more and 1000 or less.
(6) The web-like solid electrolyte film of the present invention is produced by the production method described in any one of (1) to ( 5 ) above, and the proton conductivity in water at 25 ° C. is 0.00. It is 080 or more, and the proton conductivity in water at 80 ° C. is 0.17 or more .

According to the method for producing a solid electrolyte film of the present invention, a web-like solid electrolyte film having a high proton conductivity and a uniform proton conductivity is obtained because an energization step of energizing a film containing a polymer that is a solid electrolyte is performed. Can be produced continuously . Further, the membrane electrode assembly using the web-like solid electrolyte film express excellent proton conductivity, a fuel cell using the membrane electrode assembly may exhibit excellent electromotive force.

Hereinafter, embodiments of the present invention will be described in detail. However, the present invention is not limited to the embodiments given here. First, a web-like solid electrolyte film according to the present invention will be described, and then a method for producing the solid electrolyte film will be described.

〔material〕
(First polymer)
In this invention, the compound which has a cation seed | species and a hydrogen atom is used as a polymer component of dope used for the below-mentioned manufacturing method. Among them, a polymer having a cationic species, in particular, a polymer in which the substance X is a cationic species other than a hydrogen atom in Chemical Formula 3 (hereinafter referred to as a first polymer) is a so-called solid electrolyte precursor. A solid electrolyte is produced from the precursor in the precursor film by subjecting the film containing the precursor (hereinafter referred to as a precursor film) to proton substitution. Thus, a film comprising a solid electrolyte (hereinafter referred to as a solid electrolyte film) can be produced from the precursor film by proton substitution.

  In the present specification, proton substitution refers to substitution of a cation species other than a hydrogen atom in a polymer with a hydrogen atom. The cationic species means an atom or an atomic group that generates a cation when ionized. This cationic species need not be monovalent. In the present specification, unless otherwise specified, a cation refers to a cation other than a proton, and a cation species refers to an atom that can be a cation except a hydrogen atom.

  For example, in the case of producing a precursor film, a dope containing a first polymer is produced, the dope is cast on a support, and the cast film formed on the support is peeled off, thereby producing a precursor. Body film can be manufactured. A solid electrolyte film can be produced by proton-substituting this precursor film and substituting H for the substance shown in Chemical Formula 3 contained in the precursor film with H.

  Preferred cations in the substance shown in Chemical Formula 3 are preferably alkali metal cations, alkaline earth metal cations, and ammonium cations, and more preferably calcium ions, barium ions, quaternary ammonium ions, lithium ions, sodium ions, and potassium ions. Even if the film is produced as a cationic species without replacing X in the compound shown in Chemical Formula 3 with H (hydrogen atom), the film functions as a solid electrolyte film. Therefore, in this invention, not only the 2nd polymer mentioned later but 1st polymer can be handled as a solid electrolyte. However, the proton conductivity tends to increase as the ratio of X substituted with H (hereinafter referred to as proton substitution rate) increases. In that sense, X is particularly preferably H. That is, it is preferable that the proton substitution rate is high in proton substitution for producing a solid electrolyte film from a precursor film.

(Second polymer)
As the polymer component of the dope used for the production method described later, a polymer that is a solid electrolyte (hereinafter referred to as a second polymer) can be used in addition to the first polymer described above. This second polymer has proton donating groups. The polymer having a proton donating group is not particularly limited, but a polymer having an acid residue and known as a proton conducting material can be used. Among them, preferred polymers are those having an acid residue, for example, an addition polymerization polymer compound having a sulfonic acid in the side chain, a sulfonated poly (meth) acrylate having a side chain phosphate group, and a polyether ether ketone. Examples include polyether ether ketone, sulfonated polybenzimidazole, sulfonated polysulfone obtained by sulfonated polysulfone, and sulfonated products of heat-resistant aromatic polymer compounds. Examples of the addition polymerization polymer compound having a sulfonic acid in the side chain include perfluorosulfonic acid represented by Nafion (registered trademark), sulfonated styrene, sulfonated polyacrylonitrile styrene, sulfonated polyacrylonitrile butadiene styrene, and the like. Examples of the sulfonated product of the heat resistant aromatic polymer include sulfonated polyimide.

  Preferable examples of perfluorosulfonic acid include substances described in, for example, JP-A-4-366137, JP-A-6-231777, and JP-A-6-342665. Is particularly preferred. However, in Chemical formula 1, m is 100 to 10000, 200 to 5000 is preferable, and 500 to 2000 is more preferable. And n is 0.5-100, and 5-13.5 is especially preferable. X is substantially equivalent to m, and y is substantially equivalent to n.

  Preferred examples of the sulfonated styrene, the sulfonated polyacrylonitrile styrene, and the sulfonated polyacrylonitrile butadiene styrene include the compounds described in JP-A-5-174856 and JP-A-6-111184, and the substances shown in Chemical Formula 2. Can be mentioned.

  Examples of the sulfonated product of the heat-resistant aromatic polymer include, for example, JP-A-6-49302, JP-A-2004-10777, JP-A-2004-34597, JP-A-2005-15541, JP-A-2005-15541. JP 2002-110174 A, JP 2003-100317 A, JP 2003-55457 A, JP 9345818 A, JP 2003-257451 A, JP 2000-510511 A, JP 2002-105200 A. Substances described in the official gazette are mentioned, and among them, a compound of Chemical Formula 3 generated from the first polymer by proton substitution and a substance shown in Chemical Formula 4 below are particularly preferable. Chemical formula 3 is a copolymer composed of each structural unit represented by formulas (I) to (II). X in the formula (I) represents a cationic species.

  The sulfonation reaction in the process of obtaining the above compound can be performed according to various synthetic methods in known literature. As the sulfonating agent, sulfuric acid (concentrated sulfuric acid), fuming sulfuric acid, gaseous or liquid sulfur trisulfide, sulfur trisulfide complex, amidosulfuric acid, chlorosulfonic acid and the like can be used. As the solvent, hydrocarbons (benzene, toluene, nitrobenzene, chlorobenzene, dioxetane, etc.), alkyl halides (methylene chloride, chloroform, dichloroethane, carbon tetrachloride, etc.) and the like can be used. The reaction temperature may be determined in the range of −20 ° C. to 200 ° C. according to the activity of the sulfonating agent. As another method, a mercapto group, a disulfide group, and a sulfinic acid group can be introduced into the monomer in advance, and a sulfonated product can be synthesized by an oxidation reaction with an oxidizing agent. At this time, hydrogen peroxide, nitric acid, bromine water, hypochlorite, hypobromite, potassium permanganate, chromic acid, etc. can be used as the oxidizing agent, and water, acetic acid, Propionic acid or the like can be used. The reaction temperature in this method may be determined in the range of room temperature (for example, 25 ° C.) to 200 ° C. according to the activity of the oxidizing agent. As yet another method, a sulfonated compound may be synthesized by introducing a halogenoalkyl group into the monomer in advance and performing a substitution reaction with sulfite, bisulfite, or the like. In this case, water, alcohols, amides, sulfoxides, sulfones and the like can be used as the solvent. The reaction temperature may be determined in the range of room temperature (for example, 25 ° C.) to 200 ° C. In addition, the solvent in the above sulfonation reaction may be a mixture in which two or more kinds of substances are mixed.

In the reaction step to the sulfonated product, an alkyl sulfonating agent may be used. As a general method, there is a Friedel-Crafts reaction using sultone and AlCl ₃ (Journal of Applied Polymer Science, Vol. 36, 1753-1767, 1988). When an alkyl sulfonating agent is used to perform the Friedel-Crafts reaction, hydrocarbons (benzene, toluene, nitrobenzene, acetophenone, chlorobenzene, trichlorobenzene, etc.), alkyl halides (methylene chloride, chloroform, dichloroethane, Carbon chloride, trichloroethane, dichloroethane, tetrachloroethane, etc.) can be used. The reaction temperature may be determined in the range of room temperature to 200 ° C. Note that the solvent in the reaction may be a mixture of two or more substances.

  About the said 1st and 2nd polymer, the ratio for which a sulfonic acid group accounts among the total weight of a polymer contributes to the hygroscopic expansion coefficient and proton conductivity of a film. If the proportion of sulfonic acid groups in the polymer weight is small, proton conduction paths, so-called proton channels may not be formed sufficiently. Therefore, the obtained film may not exhibit proton conductivity sufficient for practical use. On the other hand, when the proportion of the sulfonic acid group in the polymer weight increases, the moisture absorbability of the film increases, so that the coefficient of expansion due to water content, that is, the dimensional change rate increases, and the film tends to deteriorate.

As solid electrolyte, what has the following various performance is preferable. The ionic conductivity is preferably 0.005 S / cm or more, and more preferably 0.01 S / cm or more, for example, at 25 ° C. and a relative humidity of 70%. Further, the ionic conductivity after being immersed in a 64% by weight aqueous methanol solution at 18 ° C. for one day is preferably 0.003 S / cm or more, more preferably 0.008 S / cm or more, particularly before immersion. What the fall rate of the ionic conductivity after immersion with respect to 20% or less is preferable. The methanol diffusion coefficient is preferably 4 × 10 ⁻⁷ cm ² / s or less, and particularly preferably 2 × 10 ⁻⁷ cm ² / s or less.

  As for strength, those having an elastic modulus of 10 MPa or more are preferred, and those having a modulus of 20 MPa or more are particularly preferred. The method for measuring the elastic modulus is described in detail in paragraph [0138] of JP-A-2005-104148, and the above value of the elastic modulus is a value obtained by a tensile tester manufactured by Toyo Baldwin. Therefore, when obtaining the elastic modulus using another test method or tester, it is preferable to obtain the correlation with the value obtained by the test method or tester in advance.

  As for durability, it is preferable that each change rate of weight, ion exchange capacity, and methanol diffusion coefficient is 20% or less before and after a time-lapse test immersed in a 64 wt% methanol aqueous solution at a constant temperature, and 15% The following are particularly preferred. Further, before and after the time-lapse test in hydrogen peroxide, the rate of change in weight, ion exchange capacity, and methanol diffusion coefficient is preferably 20% or less, and particularly preferably 10% or less. Further, in a 64 wt% aqueous methanol solution, the volume swelling rate at a constant temperature is preferably 10% or less, and particularly preferably 5% or less.

  Further, those having a stable water absorption and water content are preferred. Moreover, it is preferable that it is so small that solubility is substantially negligible with respect to alcohols, water, and a mixed solvent of alcohol and water. Further, it is preferable that the weight loss and the shape change when immersed in the liquid are small enough to be substantially ignored.

  The ionic conduction performance of the solid electrolyte film is expressed by a so-called index which is a ratio between the ionic conductivity and the methanol permeability coefficient. And it can be said that the larger the index in a certain direction, the higher the ion conduction performance in that direction. In the thickness direction of the solid electrolyte film, the ionic conductivity is proportional to the thickness, and the methanol permeability coefficient is inversely proportional to the thickness. Therefore, the ionic conductivity of the solid electrolyte film can be controlled by changing the thickness. In a solid electrolyte film used in a fuel cell, an anode electrode is provided on one side and a cathode electrode is provided on the other side, so that the index in the thickness direction of the solid electrolyte film is larger than the index in the other direction. Is preferred. The thickness of the solid electrolyte film is preferably 10 to 300 μm. For example, in the case of a solid electrolyte in which both ionic conductivity and methanol diffusion coefficient are high, it is particularly preferable to produce a solid electrolyte film so that the thickness is 50 to 200 μm, and both ionic conductivity and methanol diffusion coefficient are In the case of a low solid electrolyte, it is particularly preferable to manufacture the solid electrolyte film so that the thickness is 20 to 100 μm.

  The heat resistant temperature is preferably 200 ° C. or higher, more preferably 250 ° C. or higher, and particularly preferably 300 ° C. or higher. The heat-resistant temperature here means a temperature when heating is performed at a heating rate of 1 ° C./min and weight loss reaches 5%. Note that this weight reduction is calculated excluding the amount of evaporation such as moisture.

Further, when the solid electrolyte film is used for a fuel cell, the solid electrolyte is preferably a solid electrolyte having a maximum output density of 10 mW / cm ² or more.

  By using the first polymer that is the precursor of the solid electrolyte or the second polymer that is the solid electrolyte, a dope suitable for the production of the solid electrolyte film can be produced.

  The dope solvent may be an organic compound that can dissolve the first polymer or the second polymer described above. Examples include aromatic hydrocarbons (eg, benzene, toluene, etc.), halogenated hydrocarbons (eg, dichloromethane, chlorobenzene, etc.), alcohols (eg, methanol, ethanol, n-propanol, n-butanol, diethylene glycol, etc.), Ketones (eg, acetone, methyl ethyl ketone, etc.), esters (eg, methyl acetate, ethyl acetate, propyl acetate, etc.), ethers (eg, tetrahydrofuran, methyl cellosolve, etc.), and nitrogen-containing compounds (N-methylpyrrolidone (NMP)) N, N-dimethylformamide (DMF), N, N′-dimethylacetamide (DMAc) and the like), dimethyl sulfoxide (DMSO) and the like.

  The dope solvent may be a mixture of a plurality of substances. When the solvent is used as a mixture, it is preferable to use a mixture of a good solvent and a poor solvent for the polymer to be a solute.

  The method for determining whether the solvent is a poor solvent or a good solvent for the polymer is that the solvent and the polymer are mixed so that the polymer is 5% by weight of the total weight, and there is an insoluble matter in the mixture. It can be done from whether or not. The good solvent of the polymer, that is, the substance that dissolves the polymer, has a relatively high boiling point among the compounds generally used as the solvent, while the poor solvent has a comparative boiling point among the compounds generally used as the solvent. The lower one. Therefore, by mixing the poor solvent with the good solvent, the efficiency and effect of removing the solvent in the film production process can be enhanced, and in particular, the drying efficiency of the cast film can be greatly improved.

  In a mixture of a good solvent and a poor solvent, the weight ratio of the poor solvent is preferably as large as possible. Specifically, the value of j / (j + k) is preferably 0.1 or more and less than 1. More preferably, the value of j / (j + k) is preferably 0.3 or more and 0.9 or less. Here, j is the weight of the good solvent, and k is the weight of the poor solvent. Thereby, since the ratio of the low boiling-point component in the weight of all the solvents becomes large, the drying efficiency and the drying effect in the manufacturing process of a solid electrolyte film can be improved more.

  As the good solvent component of the first polymer and the second polymer, DMF, DMAc, DMSO, and NMP are preferable. Among them, DMSO is particularly preferable in terms of safety and relatively low boiling point. The poor solvent component of the first polymer and the second polymer is preferably a so-called lower alcohol having 1 to 5 carbon atoms, methyl acetate or acetone, and more preferably a lower alcohol having 1 to 3 carbon atoms. When DMSO is used as a good solvent, methyl alcohol is particularly preferred because of its best compatibility.

  In order to improve various properties of the solid electrolyte film, an additive can be added to the dope. Examples of the additive include an antioxidant, fibers, fine particles, a water absorbing agent, a plasticizer, and a compatibilizer. The addition rate of these additives is preferably in the range of 1% by weight to 30% by weight when the total solid content in the dope is 100% by weight. However, the addition rate and the type of substance do not adversely affect proton conductivity. The additive will be specifically described below.

  Antioxidants include (hindered) phenolic, monovalent or divalent sulfur, trivalent phosphorus, benzophenone, benzotriazole, hindered amine, cyanoacrylate, salicylate, oxalic acid anilide. These compounds are listed as preferred examples. Specific examples thereof include compounds described in JP-A-8-53614, JP-A-10-101873, JP-A-11-114430, and JP-A-2003-151346.

  Preferred examples of the fibers include perfluorocarbon fibers, cellulose fibers, glass fibers, polyethylene fibers, and the like, and specifically, JP-A-10-31815, JP-A-2000-231938, JP-A-2001-307545. And fibers described in JP-A Nos. 2003-317748, 2004-63430, and 2004-107461.

  Examples of the fine particles include titanium oxide, zirconium oxide, and the like. Specific examples include various fine particles described in JP-A Nos. 2003-178777 and 2004-217931.

  Water-absorbing agents, that is, hydrophilic substances include crosslinked polyacrylate, starch-acrylate, poval, polyacrylonitrile, carboxymethylcellulose, polyvinylpyrrolidone, polyglycol dialkyl ether, polyglycol dialkyl ester, synthetic zeolite, titania gel, zirconia gel And yttria gel are preferable examples. Specific examples include water absorbing agents described in JP-A Nos. 7-135033, 8-20716, and 9351857.

  Preferred examples of the plasticizer include phosphate ester compounds, chlorinated paraffins, alkylnaphthalene compounds, sulfone alkylamide compounds, oligoethers, and aromatic nitriles. Examples thereof include plasticizers described in JP-A Nos. 288916 and 2003-317539.

  As the compatibilizer, those having a boiling point or sublimation point of 250 ° C. or higher are preferable, and those having a boiling point or 300 ° C. or higher are more preferable.

  The dope further contains various polymers different from the first polymer and the second polymer for the purpose of (1) increasing the mechanical strength of the film and (2) increasing the acid concentration in the solid electrolyte film. Also good.

  For the purpose of (1) above, it is preferable that the dope contains a polymer having a molecular weight of about 10,000 to 1,000,000 and having good compatibility with the first polymer and the second polymer. Is suitable. For example, perfluorinated polymers, polystyrene, polyethylene glycol, polyoxetane, polyether ketone, polyether sulfone, and polymers containing two or more polymer repeating units are preferred. Moreover, it is preferable to contain these substances in a dope so that it may become the range of 1-30 weight% with respect to the total weight when it is set as a film. In addition, you may improve compatibility with a 1st polymer or a 2nd polymer by using a compatibilizer. As the compatibilizer, those having a boiling point or sublimation point of 250 ° C. or higher are preferable, and those having a boiling point of 300 ° C. or higher are more preferable.

  For the purpose of (2) above, it is preferable to include a polymer having a protonic acid site in the dope. Examples of such a polymer include perfluorosulfonic acid polymers such as Nafion (registered trademark), sulfonated polyetheretherketone having a phosphate group in the side chain, sulfonated polyethersulfone, sulfonated polysulfone, and sulfonated polybenzimidazole. Examples thereof include sulfonated products of heat-resistant aromatic polymer compounds such as Moreover, it is preferable to contain these substances in a dope so that it may become the range of 1-30 weight% with respect to the total weight when it is set as a film.

  Furthermore, when the obtained solid electrolyte film is used in a fuel cell, an active metal catalyst that promotes the oxidation-reduction reaction between the anode fuel and the cathode fuel may be added to the dope. As a result, the fuel that has penetrated from one electrode into the solid electrolyte film is consumed in the solid electrolyte without reaching the other electrode, so that the crossover phenomenon can be prevented. The active metal catalyst is not particularly limited as long as it functions as an electrode catalyst, but platinum or an alloy based on platinum is particularly suitable.

[Dope production]
Below, the dope used for manufacture of the film of this invention is demonstrated. FIG. 1 shows a dope manufacturing facility according to the present invention, which will be described as an example in which a first polymer is used. However, this dope manufacturing equipment is not limited to the case where the first polymer is used, and is applicable to the case where the second polymer is used, for example.

  The dope manufacturing facility 10 includes a solvent tank 11 for storing the solvent 11a, a hopper 12 for supplying the precursor 12a, an additive tank 15 for storing the additive, a solvent 11a and the precursor 12a, A mixing tank 17 that mixes the additive into the mixed solution 16, a heating device 18 that heats the mixed solution 16, a temperature regulator 21 that adjusts the temperature of the heated mixed solution 16, and a temperature A first filtration device 22 that filters the mixed solution 16 exiting the regulator 21 to form a dope 24, a flash device 26 for adjusting the concentration of the dope 24, and a first filter for filtering the concentration-adjusted dope 24. 2 filtration device 27. Further, the dope manufacturing facility 10 is provided with a recovery device 28 for recovering the solvent that volatilizes in the flash device 26 and a regeneration device 29 for regenerating the recovered solvent. The dope manufacturing facility 10 is connected to a film manufacturing facility 33 through a stock tank 32. In addition, although the valves 36-38 for adjusting the amount of liquid feeding and the pumps 41 and 42 for liquid feeding are provided in the dope manufacturing equipment 10, about the increase / decrease in the position and number where these are arrange | positioned It is changed appropriately.

  The process of manufacturing the dope 24 using the dope manufacturing facility 10 will be described below. By opening the valve 37, the solvent 11 a is sent from the solvent tank 11 to the mixing tank 17. Next, the precursor 12 a is sent from the hopper 12 to the mixing tank 17. At this time, the precursor 12a may be continuously fed to the mixing tank 17 by a sending unit that continuously measures and feeds, or the mixing tank 17 is fed by a sending unit that measures and sends a predetermined amount. May be sent intermittently. In addition, the required amount of the additive solution is sent from the additive tank 15 to the mixing tank 17 by opening and closing the valve 36.

  In addition to the method of sending the additive as a solution, for example, when the additive is liquid at room temperature, the additive can be fed into the mixing tank 17 in the liquid state. Further, when the additive is solid, a method of feeding into the mixing tank 17 using a hopper or the like is also possible. When a plurality of types of additives are added, a solution in which a plurality of types of additives are dissolved can be placed in the additive tank 15. Alternatively, it is also possible to use a plurality of additive tanks and put a solution in which the additive is dissolved in each of them and send them to the mixing tank 17 through independent pipes.

  In the above description, the order of putting in the mixing tank 17 is the solvent 11a, the precursor 12a, and the additive, but is not limited to this order. For example, after the precursor 12a is fed into the mixing tank 17, a preferable amount of the solvent 11a can be fed. In addition, the additive is not necessarily limited to mixing the precursor 12a and the solvent 11a in the mixing tank 17, and may be mixed in a mixture of the precursor 12a and the solvent 11a by an in-line mixing method or the like in a later step.

  The mixing tank 17 encloses the outer surface thereof, a jacket 46 supplied with a heat transfer medium between the mixing tank 17, a first stirrer 48 rotated by a motor 47, and a second stirrer 52 rotated by a motor 51, It has. The mixing tank 17 supplies the heat transfer medium to the inside of the jacket 46 and circulates it to adjust the temperature inside. The internal temperature of the mixing tank 17 is preferably in the range of −10 ° C. to 55 ° C. By appropriately selecting and using the types of the first stirrer 48 and the second stirrer 52, the mixed liquid 16 in which the precursor 12a is swollen with the solvent 11a is obtained. The first stirrer 48 preferably has an anchor blade, and the second stirrer 52 is preferably a dissolver type eccentric stirrer.

  Next, the liquid mixture 16 is sent to the heating device 18 by the pump 41. The heating device 18 is preferably a jacketed tube having a tube body (not shown) and a jacket (not shown) for passing a heat transfer medium between the tube body, and further, the mixed liquid 16 is added. It is preferable to have a pressurizing part (not shown) for pressing. By using such a heating device 18, the solid content in the mixed solution 16 can be effectively and efficiently dissolved under heating conditions or pressure heating conditions. Hereinafter, this method of dissolving the solid component in the solvent 11a by heating is referred to as a heating dissolution method. In the heating dissolution method, it is preferable to heat the mixed solution 16 so as to be 60 ° C to 250 ° C.

  Note that the solid component may be dissolved in the solvent 11a by a cooling dissolution method instead of the heating dissolution method. The cooling dissolution method is a method of proceeding dissolution while cooling the mixed solution 16 so that the temperature of the mixed solution 16 is maintained or lower. In the cooling dissolution method, the mixed solution 16 is preferably cooled to a temperature of −100 ° C. to −10 ° C. The precursor 12a can be sufficiently dissolved in the solvent 11a by the heating dissolution method or the cooling dissolution method as described above.

  After the liquid mixture 16 is brought to about room temperature by the temperature controller 21, it is filtered by the first filtration device 22 to remove foreign matters such as impurities and aggregates, thereby obtaining a dope 24. The filter used in the first filtration device 22 preferably has an average pore diameter of 10 μm or less.

  The filtered dope 24 is sent to the stock tank 32 by the valve 38 and temporarily stored, and then used for film production.

  By the way, as described above, the method in which the solid component is once swollen and then dissolved to form a solution increases the time required for the dope production as the concentration of the precursor 12a in the solution increases. May be problematic in terms. In such a case, it is preferable to once make a dope having a concentration lower than the target concentration and then carry out a concentration step to achieve the target concentration. For example, the dope 24 filtered by the first filtration device 22 can be sent to the flash device 26 by the valve 38, and the dope 24 can be concentrated by evaporating a part of the solvent 11 a of the dope 24. . The concentrated dope 24 is extracted from the flash device 26 by the pump 42 and sent to the second filtration device 27. The temperature of the dope 24 during filtration is preferably 0 ° C to 200 ° C. The dope 24 from which foreign matter has been removed by the second filtration device 27 is sent to the stock tank 32 and once stored, and then used for film production. In addition, since the concentrated dope 24 may contain bubbles, it is preferable to perform a bubble removal process before sending it to the second filtration device 27. As the bubble removal method, for example, various known methods such as an ultrasonic irradiation method for irradiating the dope 24 with ultrasonic waves are applied.

  Further, the solvent gas generated by the flash evaporation in the flash device 26 is condensed by the recovery device 28 having a condenser (not shown) and recovered as a liquid. The recovered solvent is regenerated and reused as a solvent for dope production by the regenerator 29. Such recovery and recycling have an advantage in terms of manufacturing cost, and since the manufacturing process of the dope 24 is performed in a closed system, there is an effect of preventing adverse effects on the human body and the environment.

  Further, when impurities such as coarse particles or foreign matters are contained in the dope 24, when the dope 24 is used as a solid electrolyte film, the proton conductivity of the solid electrolyte film is lowered, or the solid electrolyte film itself May deteriorate. Therefore, it is preferable to filter the dope 24 by using a filtering device at least once in the course of manufacturing the dope 24. In addition, the installation number and installation location of the filtration apparatus in the dope manufacturing facility 10 and the frequency | count of filtering dope are not specifically limited, What is necessary is just to determine as needed.

  By the above manufacturing method, the dope 24 in which the concentration of the precursor 12a is 5% by weight or more and 50% by weight or less with respect to the total weight can be manufactured. More preferably, the concentration of the precursor 12a of the dope 24 is in the range of 10 wt% to 40 wt% with respect to the total weight. Further, the concentration of the additive is preferably in the range of 1% by weight to 30% by weight when the entire solid content in the dope is 100% by weight. In the dope 24, whether the solid content is dissolved in the solvent 11 a can be confirmed by illuminating the filtered dope 24 with a fluorescent lamp.

  Even when the solid electrolyte that is the second polymer is used instead of the precursor 12a, the dope can be manufactured using the above-described dope manufacturing facility 10.

[Solid electrolyte film manufacturing process]
Next, the manufacturing method of the solid electrolyte film of this invention is demonstrated. FIG. 2 shows a flow of the solid electrolyte film manufacturing process 60 in the case of using the dope containing the first polymer according to the present invention. In FIG. 2, only the flow of the process will be described briefly, and details of each process will be described with reference to FIG. In the following description, the solid electrolyte film is referred to as a film.

  The solid electrolyte film manufacturing process 60 includes a casting film forming process 63 for forming a casting film 61 from the dope 24, an immersion process 64 for immersing the formed casting film 61 in a liquid to perform solvent substitution, and a support. A stripping process 66 for stripping the casting film 61 to form a precursor film 65, a first drying process 67 for drying the precursor film 65, and a liquid containing an acid as a proton donor in contact with the precursor film 65 Then, an acid treatment step 69 for generating a hydrogen substitution film 68 from the precursor film 65, an energization step 70 for applying a predetermined voltage to the hydrogen substitution film 68 that has undergone the acid treatment step 69, and a hydrogen substitution film 68 after the energization A washing step 71 for washing and a second drying step 73 for drying the hydrogen-substituted film 68 after washing to form a solid electrolyte film 72 are provided.

[Solid electrolyte film production equipment]
FIG. 3 shows a film production facility 33 used in the present embodiment. The film manufacturing facility 33 is a facility designed based on the solid electrolyte film manufacturing process 60. However, this film production facility 33 is an example of the present invention and does not limit the present invention.

  The film production facility 33 includes a casting chamber 80 in which the dope 24 is cast on a support to form a casting film 61, and a drying means while the casting film 61 is transported as the support travels. A transfer chamber 81 for drying the film 61, a casting film 61 is peeled off from the support to form a precursor film 65, a tenter 83 for promoting drying of the precursor film 65, and the precursor film 65 with acid treatment and An acid treatment chamber 84 that performs energization treatment to form a hydrogen-substituted film 68; a drying chamber 85 that further promotes drying of the precursor film 65 to form a film 72; a humidity control chamber 86 that adjusts the humidity of the film 72; A winding chamber 87 for winding the wet film 72 into a roll is provided.

  The film production facility 33 is connected to the dope production facility 10 via the stock tank 32. The stock tank 32 is provided with a stirrer 91 that is rotated by a motor 90. The dope 24 prepared in the dope manufacturing facility 10 is stored in the stock tank 32. Since the stirrer 91 is always rotating, it is possible to keep the dope 24 in a uniform state by suppressing the precipitation and aggregation of solids in the dope 24. In addition, when the dope 24 is stirred in this way, various additives can be appropriately mixed with the dope 24.

The casting chamber 80 includes a casting die 93 that flows out of the dope 24, and a casting band 94 that is a traveling support. As a material of the casting die 93, precipitation hardening type stainless steel is preferable, and its thermal expansion coefficient is preferably 2 × 10 ⁻⁵ (° C. ⁻¹ ) or less. And it has almost the same corrosion resistance as SUS316 in the forced corrosion test with electrolyte aqueous solution, and even if it is immersed in a mixed solution of dichloromethane, methanol and water for 3 months, pitting (opening) occurs at the gas-liquid interface. Those having corrosion resistance that do not occur are preferred. The casting die 93 is preferably produced by grinding a material that has passed for one month or more after casting. As a result, the dope 24 flows uniformly in the casting die 93, and a flow described later. It is possible to prevent streaks or the like from occurring in the spread film 61.

  The so-called wetted surface that is in contact with the dope 24 of the casting die 93 preferably has a finishing accuracy of 1 μm or less in terms of surface roughness and a straightness of 1 μm / m or less in any direction. The slit clearance of the casting die 93 can be adjusted in the range of 0.5 mm to 3.5 mm by automatic adjustment. The chamfer radius R of the corner portion of the liquid contact portion at the tip of the lip of the casting die 93 is constant and 50 μm or less over the entire width of the casting die 93. The casting die 93 is preferably a coat hanger type die.

  The width of the casting die 93 is not particularly limited, but is preferably about 1.1 to 2.0 times the width of the film 72 as the final product. In addition, a temperature controller that controls the temperature of the casting die 93 is preferably attached to the casting die 93 so that the temperature of the dope 24 during film formation is maintained at a predetermined temperature.

  A pump 95 is provided on the upstream side of the casting die 93. Furthermore, it is more preferable that the casting die 93 is provided with a plurality of thickness adjusting bolts (heat bolts) provided at predetermined intervals in the width direction and an automatic thickness adjusting mechanism that adjusts the gap between the slits with the heat bolt. . The heat bolt is preferably subjected to film formation by setting a profile according to the amount of pump 95 (preferably a high precision gear pump) according to a preset program. In order to precisely control the dope feeding amount, the pump 95 is preferably a high-precision gear pump. In addition, a thickness measuring machine such as an infrared thickness meter is provided in the film manufacturing facility 33, and feedback control to the automatic thickness adjusting mechanism is performed by an adjustment program based on the thickness profile and a detection result by the thickness measuring machine. Also good. It is preferable to use a casting die 93 that can adjust the slit interval of the tip lip to be ± 50 μm or less so that the difference in thickness at any two positions excluding both ends of the film 72 as a product is within 1 μm.

It is more preferable that a cured film is formed at the lip end of the casting die 93. The method for forming the cured film is not particularly limited, and examples thereof include ceramic coating, hard chrome plating, and a nitriding method. In the case of using ceramics as the cured film, it is preferable to use a ceramic that can be ground, has a low porosity, is not brittle, has good corrosion resistance, and has no affinity or adhesion to the dope 24. Specific examples include tungsten carbide (WC), Al ₂ O ₃ , TiN, Cr ₂ O _{3 and the} like. Among them, WC is particularly preferable. The WC coating can be performed by a thermal spraying method.

  In order to prevent the dope 24 from locally drying and solidifying at the lip tip of the casting die 93, it is preferable to attach a solvent supply device (not shown) for supplying a solvent to the lip tip in the vicinity of the lip tip. The position where the solvent is supplied is preferably a peripheral portion of a three-phase contact line formed by both ends of the casting bead, both ends of the lip tip, and the outside air. The flow rate of the supplied solvent is preferably 0.1 mL / min to 1.0 mL / min for each side. Thereby, it is possible to prevent foreign matters such as solid components precipitated from the dope 24 and those mixed in the casting bead from the outside from being mixed in the casting film 61. In addition, as a pump which supplies a solvent, it is preferable to use a pulsation rate of 5% or less.

  Further, it is preferable to provide a filtration device 96 on the downstream side of the pump 95. With this filtering device 96, fine particles or foreign matters larger than a predetermined particle size contained in the dope 24, gel-like foreign matters, and the like can be removed.

  A casting band 94 is provided below the casting die 93 so as to span the rotating rollers 97 and 98. The casting band 94 is continuously conveyed by the driving rotation of at least one of the rotating rollers. The casting band 94 is transported endlessly so as to circulate around the casting chamber 80, the transport chamber 81, and a tank described later.

  The width of the casting band 94 is not particularly limited, but it is preferable to use a casting band 94 having a range of 1.1 to 2.0 times the casting width of the dope 24. Further, it is preferable that the length is 20 m to 200 m, the thickness is 0.5 mm to 2.5 mm, and the surface roughness is polished to be 0.05 μm or less.

  The material of the casting band 94 is not particularly limited, and may be an inorganic material such as stainless steel or a plastic film made of an organic material. Examples of the plastic film include non-woven plastic films such as a polyethylene terephthalate (PET) film, a polybutylene terephthalate (PBT) film, a nylon 6 film, a nylon 6,6 film, a polypropylene film, a polycarbonate film, and a polyimide film. It is preferably a long product having chemical stability and heat resistance that can correspond to the solvent to be used and the film forming temperature. In this embodiment, a PET film, which is a plastic film, is used as the casting band 94.

  It is preferable to use a roller having a heat transfer medium attached inside the rotary rollers 97 and 98 so that the surface temperature of the casting band 94 is set to a predetermined value. In the present embodiment, a heat transfer medium flow path (not shown) is formed in the rotation rollers 97 and 98, and the heat transfer medium maintained at a predetermined temperature passes through the flow path to rotate. The temperature of the rollers 97 and 98 is held at a predetermined value. The surface temperature of the casting band 94 is appropriately set according to the type of solvent, the type of solid component, the concentration of the dope 24, and the like.

Instead of the rotating rollers 97 and 98 and the casting band 94, a rotating drum (not shown) can be used as a support. In this case, it is preferable that the rotation can be performed with high accuracy so that the rotation speed unevenness is 0.2% or less. The rotating drum preferably has an average surface roughness of 0.01 μm or less, and preferably has a surface subjected to a hard chrome plating treatment or the like. Thereby, sufficient hardness and durability can be improved. In addition, it is preferable that the surface defects of the rotating drum, the casting band 94, and the rotating rollers 97 and 98 are minimized. Specifically, there is no pinhole of 30 μm or more, and the number of pinholes of 10 μm or more and less than 30 μm is 1 / m ² or less, and the number of pinholes of less than 10 μm is preferably ² / m ² or less.

  In the vicinity of the casting die 93, a decompression chamber is provided to control the pressure on the upstream side in the running direction of the casting band 94 of the ribbon-shaped dope 24, that is, the casting bead formed from the casting die 93 to the casting band 94. (Not shown) is preferably provided. Further, it is preferable to provide a blower (not shown) in the vicinity of the casting band 94 and to blow air to evaporate the solvent of the casting film 61. In addition, it is preferable to provide a wind-shielding plate in the above-described air blower to suppress the wind that disturbs the shape of the casting film 61 from hitting the casting film 61. In addition, the casting chamber 80 is provided with a temperature controller for keeping the internal temperature at a predetermined value, and a condenser (condenser) (both not shown) for condensing and recovering the volatile organic solvent. It is done. This capacitor is preferably in the form of being provided with a recovery device for recovering the condensed organic solvent.

  Inside the transfer chamber 81 is provided a blower (not shown) that sends dry air adjusted to a desired temperature to promote drying of the casting film 61. Moreover, it is preferable that the transfer chamber 81 is divided into a plurality of sections and further adjusted to have different drying temperatures by attaching a drying device in each section. Thereby, since the casting film 61 can be dried gradually, it can suppress that a solvent volatilizes rapidly and shape changes, such as a wrinkle and a twist, generate | occur | produce. The number of compartments in the transfer chamber 81 is not particularly limited, but it is preferable to adjust the drying temperature in the transfer chamber 81 to be in the range of 30 ° C. or more and 60 ° C. or less. Further, the transfer chamber 81 is provided with a condenser (condenser) 99 for recovering the vaporized organic solvent generated when the casting film 61 is dried. The condenser 99 is preferably provided with a recovery device for recovering the condensed and liquefied organic solvent.

  A tank 101 including a peeling roller 100 is provided downstream of the transfer chamber 81. In the tank 101 of this embodiment, an immersion liquid 102 is stored, and the casting film 61 is immersed in the tank 101 together with the casting band 94. In this way, the dipping process 64 is performed in the tank 101. In the dipping process 64, the solvent replacement is performed by dipping the casting film 61 in the dipping solution 102. The immersion liquid 102 has a lower boiling point than the solvent contained in the cast film 61 and is preferably a good organic solvent. When the casting film 61 is immersed in such an immersion liquid 102, the speed at which the organic solvent contained in the casting film 61 is extracted is improved, and the organic solvent remaining in the casting film 61 in the subsequent drying step is increased. It becomes easy to remove.

By this solvent replacement, the cast film 61 develops self-supporting properties. The factors that cause the cast film 61 to exhibit self-supporting properties are as follows.
(1) By replacing the immersion liquid 102 with a part of the solvent contained in the casting film 61, the amount of residual solvent is reduced.
(2) The casting film 61 is solidified by being immersed in the immersion liquid 102 which is a poor solvent for the precursor.
In this way, the casting film 61 having self-supporting property can be easily peeled off as the precursor film 65 by the peeling roller 100, and at the same time, the residual solvent of the precursor film 65 in the subsequent first drying step 67 can be removed. The time required for removal can be shortened.

  It is preferable to use pure water as the immersion liquid 102. The pure water used in the present invention has a specific electric resistance of at least 1 MΩ or more, particularly metal ions such as sodium, potassium, magnesium and calcium are less than 1 ppm, and anions such as chloro and nitric acid are less than 0.1 ppm. Pure water can be easily obtained by a simple substance such as a reverse osmosis membrane, an ion exchange resin, distillation, or a combination thereof.

  In addition, you may perform the immersion process 64 which makes the precursor film 65 contact the immersion liquid 102 in multiple times. When the dipping step 64 is performed a plurality of times, it is preferable to select the dipping solution 102 for each step so that the boiling point becomes lower as the dipping step 64 is followed. The plurality of dipping steps 64 can lower the boiling point of the residual solvent contained in the precursor film 65, so the first drying step 67 and the second drying step 73 performed after the dipping step 64 can be easily performed. can do. The stripping step 66 may be performed while the casting film 61 is immersed in the immersion liquid 102 or may be performed after the casting film 61 is taken out from the immersion liquid 102. Further, instead of the dipping step 64, the cast film 61 is made to have a self-supporting property by applying a dry wind to the cast film 61 in the cast film forming step 63, and the cast film is peeled off. The body film 65 may be used.

  Further, the solvent replacement method of the casting film 61 is not limited to the method of immersing the casting film 61 in the immersion liquid 102. For example, a method of bringing the immersion liquid 102 into contact with the casting film 61 may be used. Specific examples of the method of bringing the immersion liquid 102 into contact include a method of spraying or applying the immersion liquid 102 to the casting film 61 on the support.

  A pair of air knives 103 having an air blowing port directed in the direction of both surfaces of the precursor film 65 is provided downstream of the tank 101 and upstream of the tenter 83. Further, the tenter 83 is provided with a drying device that sends drying air and a number of clips 104 that travel as the chain (not shown) travels. Further, at the downstream side of the tenter 83, an ear clip device 105 for cutting off both end portions (ear portions) of the precursor film 65 is provided. The crusher 105a for finely cutting the scraps at both end portions (called ears) of the cut precursor film 65 is connected to the ear clip device 105.

(Acid treatment room)
In the acid treatment chamber 84, as shown in FIG. 4, an acid immersion tank 110, a current-carrying tank 111, and a water tank 112 are sequentially provided from the upstream side to the downstream side.

(Acid bath)
In the acid immersion tank 110, a liquid (hereinafter referred to as a first liquid) 300 containing an acid as a proton donor is stored. The acid immersion tank 110 is provided with a temperature controller 115. The temperature controller 115 maintains the temperature of the first liquid 300 stored in the acid immersion tank 110 within a predetermined range. Furthermore, the acid immersion tank 110 is provided with rollers 116 and 117. The roller 116 guides the precursor film 65 sent from the ear clip device 105 into the first liquid 300. In this way, the precursor film 65 is subjected to an acid treatment by the contact between the precursor film 65 and the first liquid 300, and the hydrogen-substituted film 68 is generated. The roller 117 guides the hydrogen substitution film 68 out of the first liquid 300. FIG. 4 shows a state in which the rollers 116 and 117 are provided in the acid immersion tank 110. However, the present invention is not limited to this, and one or three or more rollers may be provided in the acid immersion tank 110. .

(First liquid)
As an acid contained in the first liquid 300, for example, sulfuric acid, phosphoric acid, nitric acid, organic sulfonic acid, or the like can be used. Among the acids listed above, when an acid having an anion formula weight of 40 or more and 1000 or less is used, an anion that inhibits proton substitution is less likely to enter the precursor film 65, so that highly efficient proton substitution is performed. Can do. Specific examples include sulfuric acid, phosphoric acid, and nitric acid. Among them, it is preferable to use sulfuric acid having a large anion formula weight. As the 1st liquid 300, what dissolved the acid in water or the mixed solution of the organic solvent and water shown below can be used. As an organic solvent that can be used in the first liquid 300, an organic solvent similar to the second liquid 301 can be used. Details of the organic solvent and the second liquid 301 will be described later.

  The concentration of protons contained in the first liquid 300 (hereinafter referred to as proton concentration) is 0.05 mol / l or more. When the proton concentration of the first liquid 300 is less than 0.05 mol / l, the proton substitution in the precursor film 65 is not sufficiently performed, which is not preferable. The proton concentration is a unit of the same concept as the “normality” conventionally used, and the proton concentration of the first liquid 300 is the hydrogen atom contained in the first liquid 300 and capable of becoming a proton. Represents the concentration.

  The temperature of the first liquid 300 is preferably equal to the glass transition temperature Tg of the precursor film 65 by the temperature controller 115. However, depending on the type of the first liquid 300 to be used, Tg may exceed the boiling point of the first liquid 300. In order to perform stable acid treatment, the temperature is set to a temperature lower than the boiling point of the first liquid 300, preferably less than 90% of the boiling point (° C.), more preferably less than 80% of the boiling point (° C.). In consideration of the environment in which the film production line is installed, the temperature of the first liquid 300 is preferably room temperature or higher, and more preferably adjusted to 30 degrees or higher.

  The glass transition temperature Tg of the polymer can be determined using DTA (differential thermal analysis) or DSC (differential scanning calorimetry). The glass transition temperature Tg can be determined from a DTA curve or a DSC curve. Here, as a method for obtaining the glass transition temperature Tg from the obtained DTA curve or DSC curve, the intermediate glass transition temperature (Tmg), the extrapolated glass transition start temperature (Tig), and the extrapolated glass transition end temperature (Teg). Either may be used. The details of the glass transition temperature Tg measurement method such as DTA and DSC implementation methods are in accordance with JIS K 7121.

  The first liquid 300 is not limited to an acidic aqueous solution, and any liquid that can give protons to the precursor proton acceptor in proton substitution may be used. For example, when the acid is ionized into an anion and a proton, an acid having a higher proton acceptability than the anion may be used as the precursor.

  In this acid treatment step 69, in order to perform high-efficiency proton substitution on the precursor film 65, the residual solvent amount of the precursor film 65 is 1% by weight or more and 100% by weight or less based on the dry weight standard. Is preferred. If the residual solvent amount is reduced to 1% by weight or less with respect to the dry weight standard, the drying time becomes longer, which is not preferable. If this is performed, the porosity of the film increases, which is not preferable. The amount of residual solvent based on this dry amount is a value calculated by {(xy) / y} × 100, where x is the film weight at the time of sampling and y is the weight after drying the sampling film. It is.

  In this acid treatment step 69, the ratio of the precursor of the precursor film 65 substituted with protons (hereinafter referred to as proton substitution rate) is preferably 80 mol% or more, and the proton substitution rate is 90 mol% or more. More preferably. By performing proton substitution with such a high proton substitution rate, a solid electrolyte film 72 having excellent proton conductivity can be produced, and at the same time, the proton conductivity can be further increased in the energization step 70 performed after the acid treatment step 69. It becomes possible to improve.

(Electric tank)
The energization tank 111 stores the second liquid 301 and is provided with an electrode 120, an electrode 121, and rollers 122 and 123. In addition, the energization tank 111 includes a temperature controller 125. The temperature controller 125 keeps the temperature of the second liquid 301 stored in the energization tank 111 within a predetermined range. The electrode 120 is provided on the bottom surface 111 a side inside the energization tank 111. The electrode 121 is provided on the liquid surface 301 a side of the second liquid 301. The electrode 120 and the electrode 121 are connected to a power source 127 through wiring. By operating the power supply 127, a predetermined voltage V <b> 1 is applied between the electrode 120 and the electrode 121. Thus, a current A1 having a predetermined magnitude flows through the second liquid 301 and the hydrogen substitution film 68 between the electrode 120 and the electrode 121. The roller 122 guides the hydrogen substitution film 68 sent from the acid immersion tank 110 into the second liquid 301. Then, after the hydrogen replacement film 68 is guided through the second liquid 301 by the roller 123, it is removed from the second liquid 301 and guided to the water tank 112.

  The distance L1 between the electrode 120 and the electrode 121 is preferably 300 mm or less, more preferably 150 mm or less, and even more preferably 100 mm or less. When the distance L1 is larger than 300 mm, it is difficult to pass a sufficient current through the hydrogen-substituted film 68, resulting in a long processing time, which is not preferable. It is also possible to adjust the magnitude of the current flowing through the hydrogen-substituted film 68 by adjusting the distance L1.

  The power supply 127 includes a current detector (not shown) that detects that a current flows between the electrodes 120 and 121. The energization tank 111 includes a proton concentration controller. The proton concentration controller includes a tank that stores the third liquid, and a pipe and a valve that supply the third liquid stored in the tank to the energization tank 111. This third liquid is a liquid that contains the same or the same acid as the second liquid 301, and has a higher proton concentration than the second liquid 301. A control unit (not shown) is connected to the current detector and the proton concentration controller. The acid concentration regulator can pour the third liquid into the energization tank 111 and adjust the proton concentration of the second liquid 301 in the energization tank 111. When the control unit does not read the detection signal from the current detector, it starts to supply the third liquid to the energizing tank 111. When the controller detects the detection signal from the current detector, the controller supplies the third liquid to the energizing tank 111. Stop supplying. Thus, the energization tank 111 can maintain energization in the hydrogen substitution film 68.

  The shift unit 140 is connected to the electrode 120 and the electrode 121. The shift unit 140 moves the electrode 120 or the electrode 121 to a predetermined position and adjusts the distance L1 between the electrode 120 and the electrode 121 to a desired range. Further, the control unit 141 is connected to the temperature controller 125, the shift unit 140, and the power supply 127. Under the control of the control unit 141, an energization process under a desired condition is performed. The controller 141 preferably adjusts the distance L1, the voltage V1, the current A1, the temperature of the second liquid 301, and the like according to the progress of the energization process.

  The voltage V1 applied between the electrode 120 and the electrode 121 may satisfy the following conditions (hereinafter referred to as energization conditions). (1) The current A1 flows through the hydrogen substitution film 68. (2) No anion is generated from the second liquid 301 by electrolysis.

From (1) above, when a current flows through the hydrogen-substituted film 68, a path through which protons pass in the hydrogen-substituted film 68, that is, a proton channel is formed, and as a result, proton conductivity is improved. Therefore, the current flowing through the hydrogen-substituted film 68 may be a pulsed current in addition to alternating current and direct current. The current density for energizing the hydrogen-substituted film 68 is preferably 0.2 mA / cm ² or more and 100 mA / cm ² or less, and more preferably 1.0 mA / cm ² or more and 20 mA / cm ² or less. When the current density is less than 0.2 mA / cm ² , the proton conductivity is not improved, which is not preferable. On the other hand, if the current density is greater than 100 mA / cm ² , electrolysis of the second liquid occurs and the polymer deteriorates, which is not preferable. Therefore, if the electrolysis of the second liquid 301 in the energization process 70 can be suppressed, the effect of the present invention may be exhibited even if the current density is greater than 100 mA / cm ² .

  On the other hand, (2) is for avoiding a decrease in proton conductivity of the hydrogen-substituted film 68 due to hydroxide ions or the like generated from water molecules. In particular, an anion having a small formula weight such as a hydroxide ion penetrates into the hydrogen-substituted film 68 and binds to protons and hydrogen atoms in the hydrogen-substituted film 68. Conditions for the formula weight of the anion will be described later.

(Second liquid)
As the second liquid 301, a liquid containing an acid can be used. By adjusting the proton concentration of the second liquid 301, the above-described energization conditions can be satisfied. The proton concentration contained in the second liquid 301 is not particularly limited. Note that a liquid containing an acid is preferably used as the second liquid 301.

  Among the liquids containing an acid used as the second liquid 301, when the formula amount of the anion is less than 40, it easily enters the hydrogen-substituted film 68, and when the formula amount of the anion exceeds 1000, the hydrogen substitution Although it is difficult to enter the film 68, once it enters, it tends to remain in the hydrogen-substituted film 68 as it is. This is because the anion remaining in the hydrogen-substituted film 68 causes a decrease in proton conductivity of the hydrogen-substituted film 68. Therefore, it is preferable to use an acid having an anion formula weight of 40 or more and 1000 or less as the second liquid 301 because unnecessary anions do not remain in the hydrogen-substituted film 68 and proton conductivity does not decrease. Specific examples of the second liquid 301 include phosphoric acid, nitric acid, and organic sulfonic acid. Moreover, what dissolved the acid in the liquid mixture of the acid mentioned above in water or the organic solvent and water shown below as the 2nd liquid 301 can be used.

  The organic solvent used as the second liquid 301 may be one kind or a combination of two or more kinds, but it is necessary to select one that does not dissolve or swell the hydrogen-substituted film 68. Examples of the organic solvent used in the present invention include New Edition Solvent Pocket Book (Ohm, published in 1994), but the present invention is not limited thereto. For example, alcohols (methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol, cyclohexanol, benzyl alcohol, fluorinated alcohol), ketones (acetone, methyl ethyl ketone, methyl isobutyl ketone), esters (methyl acetate, Ethyl acetate, butyl acetate), polyhydric alcohols (ethylene glycol, diethylene glycol, propylene glycol, ethylene glycol diethyl ether), N, N-dimethylformamide, perfluorotributylamine, triethylamine, dimethylformamide, dimethyl sulfoxide, methyl cellosolve, etc. Is mentioned.

  In addition, when water is used as the second liquid 301, it is preferable to use pure water. In this case, it is possible to energize the hydrogen substitution film 68 by immersing the hydrogen substitution film 68 after the unwashed acid treatment step, that is, the hydrogen substitution film 68 in which the surplus acid remains in the second liquid 301. it can. When water is used as the second liquid 301, the first liquid 300 used in the immediately preceding acid treatment step 69 needs to satisfy the conditions of the second liquid 301 together with the conditions of the first liquid 300 described above. Moreover, it is preferable that the distance between the acid immersion tank 110 and the energization tank 111 is as small as possible. This is because the energizing process in the energizing tank 111 is performed through the acid remaining in the hydrogen-substituted film 68, and thereby the effect of the present invention is exhibited.

  The temperature of the second liquid 301 is preferably maintained at a temperature at which the proton channel formed in the hydrogen-substituted film 68 is not destroyed or reconstituted by the temperature controller 125. It is preferably 120 ° C. or lower and more preferably 20 ° C. or higher and 80 ° C. or lower.

  A cleaning liquid 305 is stored in the water tank 112. The water tank 112 includes a temperature controller 130. The temperature controller 130 maintains the temperature of the cleaning liquid 305 stored in the water tank 112 within a predetermined range. The water tank 112 includes rollers 131 and 132. The roller 131 guides the hydrogen substitution film 68 sent from the energization tank 111 into the cleaning liquid 305. After the hydrogen replacement film 68 is guided through the cleaning liquid 305 by the roller 132, the hydrogen replacement film 68 is removed from the cleaning liquid 305 and guided to a set of air knives (not shown) arranged downstream of the water tank 112. The In this way, the hydrogen substitution film 68 is washed with water. One set of air knives (not shown) is arranged so as to face the conveyance path of the hydrogen substitution film 68, respectively, and performs a draining process on the hydrogen substitution film 68 passing between the air knives. Thereafter, the hydrogen substitution film 68 is guided to the drying chamber 85.

  It is preferable to use pure water as the cleaning liquid 305. In order to obtain a high effect of washing out the acid, the temperature of the cleaning liquid 305 to be used is preferably 30 ° C. or higher and the boiling point of the cleaning liquid or lower. However, the temperature of the cleaning liquid 305 is not particularly limited as long as it is in a temperature range from approximately room temperature to boiling.

  As a method for rinsing the hydrogen-substituted film 68 in the water-washing step 69, in consideration of carrying out the hydrogen-substituted film 68 while continuously transporting, there are a method of applying the cleaning liquid 305 and a method of spraying the cleaning liquid 305 in addition to the above method. Any of these methods may be used.

The amount of the cleaning liquid 305 used for water washing must be at least an amount exceeding the theoretical dilution rate defined below.
Theoretical dilution factor = application amount of the cleaning liquid 305 [ml / m ² ] ÷ application amount of the first liquid 300 [ml / m ² ]
In other words, the theoretical dilution rate is defined on the assumption that all of the cleaning liquid 305 used for water washing contributed to the dilution and mixing of the first liquid 300. Actually, since complete mixing does not occur, a cleaning liquid amount exceeding the theoretical dilution rate is used. Although it depends on the proton concentration of the first liquid used, the secondary additives, and the type of solvent, it is a cleaning liquid that can be diluted at least 100 to 1000 times, preferably 500 to 10,000 times, more preferably 1000 to 100,000 times. 305 is used.

  In the case of using a predetermined amount of the cleaning liquid 305, the water cleaning method is preferably a batch cleaning method that is applied in several divided portions rather than applying the entire amount at once. That is, the amount of the cleaning liquid 305 is divided into several parts and supplied to a plurality of water washing means installed in tandem in the transport direction of the hydrogen-substituted film 68. An appropriate time (distance) is provided between one water washing means and the next water washing means, and the first liquid 300 is diluted by diffusion. More preferably, if the cleaning liquid 305 on the hydrogen-substituted film 68 flows along the film surface by providing an inclination to the transported hydrogen-substituted film 68, mixed dilution by flow can be obtained in addition to diffusion. It is done. As the most preferable method, by providing a draining means for removing the film of the cleaning liquid 305 on the hydrogen substitution film 68 between the washing means and the washing means, the washing dilution efficiency can be further increased. Specific examples of draining means include a blade used in a blade coater, an air knife used in an air knife coater, a rod used in a rod coater, and a roll used in a roll coater. Although it is advantageous that the number of water washing means arranged in such a tandem is large, 2 to 10 stages, preferably 2 to 5 stages are usually used from the viewpoint of installation space and equipment cost.

  The thickness of the film of the cleaning liquid 305 after the draining means (hereinafter referred to as a water film) is preferably thin, but the thickness of the water film remaining on the hydrogen-substituted film 68 varies depending on the type of the cutting means used. In the method in which a solid is physically brought into contact with the hydrogen-substituted film 68 such as a blade, a rod, or a roll, even if the solid is an elastic body having low hardness such as rubber, the surface of the hydrogen-substituted film 68 is scratched. It is necessary to leave a finite water film as a lubricating fluid because the elastic body is worn away. Usually, a water film of several μm or more, preferably 10 μm or more is left as a lubricating fluid.

  An air knife is preferably used as a draining means that can reduce the thickness of the water film to the limit. By setting a sufficient air volume and pressure, the water film thickness can be brought close to zero. However, if the amount of air blown from the air knife is too large, it may affect the transport stability of the hydrogen-substituted film 68, such as flapping and deviation, so there is a preferable range. Although depending on the original water film thickness on the hydrogen-substituted film 68 and the transport speed of the hydrogen-substituted film 68, the wind speed is usually 10 to 500 m / sec, preferably 20 to 300 m / sec, more preferably 30 to 200 m / sec. Is used. In order to remove the water film uniformly, the air velocity distribution in the width direction of the hydrogen-substituted film 68 is usually within 10%, preferably within 5%, and the air supply to the air knife outlet and the air knife is performed. Adjust the method. As the gap between the surface of the transparent resin film to be transported and the air knife outlet becomes narrower, its draining ability increases. However, the possibility of contact with the hydrogen-substituted film 68 and damage increases, so there is an appropriate range. Usually, an air knife is installed with a gap of 10 μm to 10 cm, preferably 100 μm to 5 cm, more preferably 500 μm to 1 cm. Furthermore, by setting up a backup roll on the opposite side of the water-washing surface of the hydrogen-substituted film 68 so as to face the air knife, the setting of the gap is stabilized, and the influence of fluttering, wrinkles, deformation, etc. of the hydrogen-substituted film 68 is reduced. It is preferable because it can be relaxed.

  Further, by performing the acid treatment step 69 and the water washing step 71 as described above, it is possible to obtain an effect of removing impurities such as inorganic salts in the solid electrolyte contained in the hydrogen-substituted film 68. The deterioration of 72 can also be prevented. In addition, it is preferable that content of the metal contained in the hydrogen-substituted film 68 after the water washing process 71 is 1000 ppm or less by performing the acid treatment process 69 and the water washing process 71, More preferably, it is 100 ppm or less. Examples of the metal include Na, K, Ca, Fe, Ni, Cr, and Zn. The content of these metals can be grasped by, for example, measuring with a commercially available atomic absorption photometer.

  As shown in FIG. 3, the drying chamber 85 includes a number of pass rollers 140, an adsorption recovery device 141 for recovering the volatile solvent inside the drying chamber 85, and a drying device (not shown) for supplying drying air. Is provided. In the drying chamber 85, a drying process is performed in which drying air is applied to the hydrogen-substituted film 68 to remove the solvent contained in the hydrogen-substituted film 68. By subjecting the hydrogen-substituted film 68 to a drying process, a film 72 is generated.

  The humidity control chamber 86 arranged downstream of the drying chamber 85 is provided with the same pass roller 140 as the drying chamber 85, a temperature control device, and a humidity control device (both not shown). A neutralization device (not shown) such as a neutralization bar is provided downstream of the humidity control chamber 86, and the charged voltage of the hydrogen substitution film 68 is adjusted to be within a predetermined range (for example, −3 kV to +3 kV). More preferably, a knurling roller pair (not shown) is provided, and knurling is preferably applied to both end portions of the film 72 by embossing. Inside the take-up chamber 87, a take-up roll 145 for taking up the film 72 and a press roller 146 for controlling the tension during take-up are provided.

  Next, an example of a method for manufacturing the film 72 using the above-described film manufacturing facility 33 will be described.

  As shown in FIG. 3, the dope 24 stored in the stock tank 32 is sent to the filtration device 96 by the pump 95, and is filtered so that fine particles or foreign matters larger than a predetermined particle size contained in the dope 24, and gel-like Remove foreign material.

After the filtered dope 24 is fed into the casting die 93, it is cast on the casting band 94 while forming a casting bead from the casting die 93. In this case, the relative positions of the rotary rollers 97 and 98 and at least one of the rotational speeds are adjusted so that the tension generated in the casting band 94 becomes 10 ³ N / m × 10 ⁶ N / m. Further, the relative speed difference between the casting band 94 and the rotating rollers 97 and 98 is adjusted to be 0.01 m / min or less. At the time of casting, the casting amount of the dope 24 is determined in consideration of the concentration of the dope 24 to be used and the desired thickness of the film product.

  The speed fluctuation of the casting band 94 is preferably 0.5% or less, and the meandering in the width direction that occurs when the casting band 94 makes one round is preferably 1.5 mm or less. In order to suppress the meandering, a detector (not shown) that detects the positions of both ends of the casting band 94 and a position adjustment that adjusts the position of the casting band 94 according to the detection data by the detector. More preferably, a machine (not shown) is provided to feedback control the position of the casting band 94. In addition, it is preferable that the vertical position variation of the casting band 94 immediately below the casting die 93 with the rotation of the rotary rollers 97 and 98 be within 200 μm. The casting chamber 80 is preferably provided with a temperature controller (not shown), so that the temperature is set to -10 ° C to 57 ° C. Solvent evaporated in the casting chamber 80 is recovered by a recovery device (not shown) and then regenerated and reused as a solvent for dope production, which is also preferable for obtaining effects such as reduction in manufacturing cost.

  In order to stabilize the form of the casting bead, it is preferable to control in the decompression chamber so that the upstream area of the bead has a predetermined pressure value. The reduced pressure value by the decompression chamber is preferably −2500 Pa to −10 Pa from the downstream area with respect to the bead. It is preferable to attach a jacket (not shown) to the decompression chamber so that the internal temperature is kept at a predetermined temperature. In order to keep the shape of the casting bead desired, it is preferable to attach a suction device (not shown) to the edge portion of the casting die 93 to suck both sides of the casting bead. The edge suction air volume is preferably in the range of 1 L / min to 100 L / min.

  The casting film 61 on the casting band 94 is transported through the casting chamber 80 and the conveyance chamber 81 by driving the rotary rollers 97 and 98 to drive the casting band 94. In the transfer chamber 81, drying air is supplied from a drying device (not shown) to promote drying of the casting film 61. The capacitor 99 condenses and recovers the volatile solvent inside the transfer chamber 81.

  Subsequently, the casting band 94 on which the casting film 61 is formed is fed into the tank 101 and immersed in the immersion liquid 102. By solvent replacement, the residual solvent amount of the precursor film 65 is reduced, and the cast film 61 exhibits self-supporting properties. Then, the casting film 61 is peeled off from the casting band 94 by the peeling roller 100 to obtain the precursor film 65. The precursor film 65 is guided in a predetermined direction by a guide roller. Further, since the casting band 94 after the casting film 61 has been peeled off travels endlessly as the rotary rollers 97 and 98 are driven, the casting band 94 is fed into the casting chamber 80 again.

  The form in which the casting film 61 is immersed in water in the tank 101 is not particularly limited, but the time for immersing the casting film 61 in the aqueous solution is 1 minute or more and 60 minutes or less. The self-supporting property of the cast film 61 is expressed, and the precursor film 65 can be peeled off from the casting band 94.

  Subsequently, the precursor film 65 is sent out from the tank 101 by the guide roller. Air is blown onto the surface of the precursor film 65 by the air knife 103 to remove moisture adhering to the surface of the precursor film 65. This precursor film 65 is fed into the tenter 83. In the tenter 83, the clip 104 grips both end portions of the precursor film 65 and conveys the chain as the chain travels. During the transfer of the precursor film 65, drying air adjusted to a desired temperature is applied to the precursor film 65 to promote drying of the precursor film 65. However, the clip 104 may be replaced with a pin, and the pin may be transported after being held by being pierced at both end portions of the precursor film 65. At this time, it is preferable to adjust the temperature of the tenter 83 to 80 ° C. or more and 140 ° C. or less by adjusting the temperature of the drying air. In this embodiment, the internal temperature is adjusted to be about 120 ° C. In the present embodiment, it is preferable to divide the inside of the tenter 83 into four temperature zones that differ in the transport direction, and to adjust the drying conditions appropriately for each zone.

  In the tenter 83, the precursor film 65 can be stretched in the width direction. By adjusting the tension in the transport direction applied to the precursor film 65 before being fed into the tenter 83, the precursor film 65 can be stretched in the transport direction. Further, when the precursor film 65 is stretched, at least one of the transport direction and the width direction of the precursor film 65 is stretched so as to have a dimension of 100.5% to 300% with respect to the dimension before stretching. It is preferable to do. Thereby, the molecular orientation of the polymer contained in the precursor film 65 can be adjusted.

  The precursor film 65 is fed into the ear-cutting device 105, where both side ends are cut and removed. Thus, the precursor film 65 excellent in flatness can be obtained by excising the both ends of the precursor film 65 damaged by the clip. In addition, the cut | disconnected both side edge part is sent into the crusher 105a with a cutter blower (not shown), and it grind | pulverizes here, and becomes a chip | tip. When this chip is reused as a polymer raw material for dope production, it is possible to effectively use the raw material or reduce production costs. In addition, although the process of cut | disconnecting the both-ends part of the precursor film 65 can also be abbreviate | omitted, after peeling off from the support body as the precursor film 65, it is preferable to carry out in any one until it winds up as the film 72.

  As shown in FIG. 4, the precursor film 65 guided from the ear clip device 105 is immersed in the first liquid 300 stored in the acid immersion tank 110 by the rollers 116 and 117. By the contact between the precursor film 65 and the first liquid 300, proton substitution is performed on the precursor film 65, and a hydrogen substitution film 68 is generated. The hydrogen substitution film 68 is removed from the first liquid 300 by the roller 117.

  The hydrogen substitution film 68 guided from the acid immersion tank 110 is immersed in the second liquid 301 stored in the energization tank 111 by the rollers 122 and 123 and guided between the electrode 120 and the electrode 121. Since a predetermined voltage is applied between the electrode 120 and the electrode 121, a current is passed between the electrode 120 and the electrode 121 through the second liquid 301 and the hydrogen substitution film 68. Thereafter, the hydrogen substitution film 68 is removed from the first liquid 300 by the rollers 122 and 123 and guided to the energization tank 111.

  Proton conductivity in the hydrogen-substituted film 68 is improved by energizing the hydrogen-substituted film 68 via the acid. It is unclear what process the current conduction through the acid improves the proton conductivity, but it can be estimated as follows. First, the diffusion of protons in the hydrogen-substituted film 68 is promoted by energization. The proton diffusion promotes the proton substitution in the hydrogen-substituted film 68 sufficiently, and at the same time, the energization energy activates the proton substitution. As a result, the proton conductivity of the hydrogen-substituted film 68 is improved. To do.

  The hydrogen substitution film 68 guided from the energization tank 111 is immersed in the cleaning liquid 305 stored in the water tank 112 by the rollers 131 and 132. Thus, the acid remaining in the hydrogen-substituted film 68 can be washed away by the cleaning liquid 305. After sufficiently performing the water washing process, the hydrogen-substituted film 68 is removed from the cleaning liquid 305 by the roller 132 and guided to the drying chamber 85.

  Subsequently, the hydrogen substitution film 68 is fed into the drying chamber 85. In the drying chamber 85, drying air is supplied from a drying device and dried while the hydrogen-substituted film 68 is conveyed while being wound around the pass roller 140. The internal temperature of the drying chamber 85 is not particularly limited, but is determined according to the heat resistance (glass transition point Tg, heat distortion temperature, melting point Tm, continuous use temperature, etc.) of the solid electrolyte, and is Tg or less. In the present invention, the internal temperature of the drying chamber 85 is preferably 80 ° C. or higher and 200 ° C. or lower, and the film 72 is dried until the residual solvent amount of the film 72 is less than 10% by weight with respect to the dry weight standard. Is preferred. The solvent gas generated by the evaporation from the film 72 is adsorbed and recovered by the adsorption / recovery device 141, and after removing the solvent component, is sent again into the drying chamber 85 as the drying air.

  It is more preferable that the drying chamber 85 is divided into a plurality of sections in the transport direction in order to change the blowing temperature. In addition, when a preliminary drying chamber (not shown) is provided between the ear opener 105 and the drying chamber 85 to preliminarily dry the hydrogen-substituted film 68, the temperature of the hydrogen-substituted film 68 is prevented from rapidly rising in the drying chamber 85. Therefore, it is possible to suppress the substantial shape change of the hydrogen-substituted film 68 in the drying chamber 85 and to obtain the film 72 with little shape change.

  The film 72 is carried into the humidity control chamber 86. In the humidity control chamber 86, the humidity is adjusted by adjusting the temperature and the humidity control device to a desired temperature and humidity while the film 72 is conveyed while being wound around the pass roller 140, as in the drying chamber 85. And control its water content. The temperature and humidity in the humidity control chamber 86 are not particularly limited, but the temperature is preferably 20 ° C. or higher and 30 ° C. or lower, and the humidity is preferably 40 RH% or higher and 70 RH% or lower. Thereby, it is possible to suppress the occurrence of curling on the surface of the film 72 and the occurrence of winding failure when winding. In addition, it is preferable to provide a cooling chamber (not shown) between the drying chamber 85 and the humidity control chamber 86 and cool the film 72 to approximately room temperature because it is possible to suppress the shape change of the film 72 due to a temperature change. .

  A static eliminator (not shown) is provided between the humidity control chamber 86 and the winding chamber 87, and the charged voltage is set to a predetermined value while the film 72 is being conveyed. The charged voltage after neutralization is preferably -3 kV to +3 kV. Furthermore, it is preferable that the film 72 is provided with a knurling roller pair to be knurled. In addition, it is preferable that the uneven | corrugated height of the location which provided the knurling is 1 micrometer-200 micrometers.

  Finally, the film 72 is fed into the take-up chamber 87 and taken up on the take-up roll 130 while applying a tension by the press roller 131. Thereby, the roll-shaped film 72 can be obtained, suppressing generation | occurrence | production of wrinkles, a twist, etc. Thus, it is preferable to wind the film while applying a desired tension to the film 72 with the press roller 131, because a roll-shaped film product having excellent flatness can be obtained. In order to prevent excessive winding in the film roll, it is more preferable to gradually change the tension from the start to the end of winding. Further, the width of the film 72 to be wound is preferably 100 mm or more, but the present invention is also applied to the production of a thin film having a thickness of 5 μm to 300 μm.

  According to the method for producing a solid electrolyte film of the present invention, since the hydrogen-substituted film 68 immediately after the acid treatment step 69 is energized, the film 72 having a high proton substitution rate and excellent proton conductivity can be produced.

  In the above embodiment, it is described that the energization process 70 is performed on the hydrogen-substituted film 72 generated by the acid treatment process 69 after the acid treatment process 69 is performed on the precursor film 65. The processing step 69 and the energization step 70 may be performed simultaneously. When the acid treatment process 69 and the energization process 70 are performed simultaneously, the energization tank 111 that stores the first liquid 300 instead of the second liquid 301 described above may be used. Further, this energization process 70 may be performed a plurality of times.

  In the above embodiment, it is described that the energization step 70 is performed by immersing the precursor film 65 in the second liquid 301, but not limited thereto, the energization step 70 is performed by contact between the precursor film 65 and the second liquid 301. You can go. As a method of bringing the precursor film 65 and the second liquid 301 into contact with each other, there is a method of applying the second liquid 301 to the precursor film 65, and through the region where the second liquid 301 is applied on the precursor film 65. The energization process 70 can be performed by applying a voltage. Further, after the precursor film 65 is once immersed in the second liquid 301 and taken out, the energization step is performed by applying a voltage through the region where the second liquid 301 remains on the precursor film 65 without washing. 70 can also be performed.

  In the above embodiment, the acid treatment step 69 is described as being performed by immersing the precursor film 65 in the first liquid 300. However, the present invention is not limited to this, and the acid treatment step is performed by contacting the precursor film 65 and the first liquid 300. 69 may be performed. As a contact method between the first liquid 300 and the precursor film 65 in the acid treatment step 69, (1) the first liquid 300 can be uniformly contacted with the precursor film 65 (2) one side of the precursor film 65 A method that satisfies the requirement that the amount of the first liquid 300 in contact with the electrode is easy to adjust is preferable. As the contact system, a die coater such as extrusion or slide, a roll coater such as a forward roll, a reverse roll or a gravure, a rod coater wound with a thin metal wire, or the like can be preferably used. These contact methods are summarized in Modern Coating and Drying Technology, Edward Cohen and Edgar B. Gutoff, Edits., VCH Publishers, Inc, 1992. Since the first liquid 300 that comes into contact with the precursor film 65 is then removed by washing with water, it is desirable to suppress the coating amount as much as possible when considering waste liquid treatment for environmental protection. From this viewpoint, a rod coater, a gravure coater, and a blade coater that can be stably operated even in a small coating amount region can be preferably used. Furthermore, the acid treatment step 69 can be efficiently performed by using a heating unit that heats the precursor film 65 in contact with the first liquid 300. As the heating means for the precursor film 65, hot air impingement on one surface of the precursor film 65, contact heat transfer with a heating roll, induction heating with a microwave, radiant heat heating with an infrared heater, etc. can be preferably used. In particular, the infrared heater is preferable because it can be performed without contact and without the flow of air, so that the influence of one surface coated with the first liquid 300 can be minimized. As the type of the infrared heater, for example, various far infrared ceramic heaters such as electric type, gas type, oil type and steam type manufactured by Noritake Company Limited can be used. In particular, the oil type and the steam type in which the heat medium uses oil or steam are preferable from the viewpoint of explosion prevention in an atmosphere in which an organic solvent coexists. The temperature of the precursor film 65 is 25 ° C. or higher and lower than 150 ° C., preferably 25 ° C. or higher and lower than 100 ° C., more preferably 40 ° C. or higher and lower than 80 ° C. For the detection of the film temperature, a commercially available non-contact infrared thermometer can be used, and feedback control may be performed on the heating means in order to control the temperature within the above range.

  When heating is performed after the acid is applied to the precursor film 65, a pair of rollers disposed on both side ends of the precursor film 65, holding both side ends of the precursor film 65, and guiding in a predetermined direction is used. Thus, the both end portions of the precursor film 65 may be energized. By using this roller pair, the acid treatment step 69 and the energization step 70 can be performed.

  In the present embodiment, the case where one kind of dope is cast is shown. However, in the present invention, two or more kinds of dopes may be co-cast simultaneously to form a laminated type casting film, or sequentially. Alternatively, a laminated type cast film may be formed by co-casting. In the case where two or more kinds of dopes are co-cast simultaneously, a casting die provided with a feed block may be used, or a multi-manifold casting die may be used. However, as for the film which consists of a multilayer by co-casting, it is preferable that any one of the two layers exposed on the surface is 0.5% to 30% of the total thickness of the film. In addition, when co-casting at the same time, when dope is cast from the die slit to the support, the concentration of each dope is adjusted in advance so that the high-viscosity dope is wrapped and cast by the low-viscosity dope. In the bead formed from the die slit to the support, it is preferable that the dope in contact with the outside world, that is, the exposed dope has a larger proportion of the poor solvent than the inner dope.

  The precursor film is different from the above-described embodiment in that the precursor film is held in the pores of a so-called porous substrate in which a plurality of pores are formed instead of the method described above for producing the precursor film. Can be manufactured. As a method for producing such a precursor film, a method in which a sol-gel reaction liquid containing a precursor is applied onto a porous substrate and the precursor is put into pores, and a precursor is included in the porous substrate. There is a method of immersing in a sol-gel reaction solution to fill the precursor in the pores. Preferable examples of the porous substrate include porous polypropylene, porous polytetrafluoroethylene, porous cross-linked heat-resistant polyethylene, and porous polyimide. Alternatively, the precursor film can be formed by processing the precursor into a fiber shape, filling the voids in the fiber with other polymer compounds, etc., and using the fiber to form a film. In this case, examples of the other polymer compound for filling the void include the substances mentioned as additives in the present specification. About each of these precursor films, the solid electrolyte film excellent in proton conductivity can be manufactured by performing the acid treatment process 69 and the electricity supply process 70 mentioned above.

  In the said embodiment, although the manufacturing method of the solid electrolyte film in case the dope 24 containing a 1st polymer was used was described, this invention is not restricted to this, For example, it replaced with the dope 24 containing a 1st polymer, A solid electrolyte film can be produced using a dope containing a second polymer. Next, a method for producing a solid electrolyte film using a dope containing the second polymer will be described. In addition, the same apparatus, member, process, etc. as embodiment mentioned above are demonstrated using the same code | symbol, and the detailed description is abbreviate | omitted.

  As shown in FIG. 5, in the solid electrolyte film manufacturing process 160, the energization process 70 for energizing the first solid electrolyte film 162 through the second liquid 301 and the second liquid 301 remaining in the first solid electrolyte film 162 are washed away. And a water washing step 71. By the energization process 70 and the water washing process 71, the second solid electrolyte film 163 having higher proton conductivity than the first solid electrolyte film 162 can be generated from the first solid electrolyte film 162. In addition, you may provide a drying process after the water washing process 71 as needed.

  The first solid electrolyte film 162 may be a known solid electrolyte film manufacturing method using a dope containing a second polymer, or a solid electrolyte film manufactured by the above-described solid electrolyte film manufacturing process 60. In the solid electrolyte film manufacturing process 60, the first solid electrolyte film 162 can be made by using a dope using the second polymer instead of the first polymer.

  As the second liquid 301, an acid-containing liquid or water can be used. When a liquid containing an acid is used as the second liquid 301, the same liquid as the second liquid 301 described above can be used. On the other hand, when water is used as the second liquid 301, the energization process 70 may be performed on the first solid electrolyte film 162 brought into contact with a liquid containing an acid of the same quality as the first liquid 301. When the first solid electrolyte film 162 is not sufficiently substituted with protons, the acid treatment step 69 described above may be performed on the first solid electrolyte film 162 together with the energization step 70.

  The method for producing a solid electrolyte film of the present invention includes a so-called on-line method in which each process such as the above-described solid electrolyte film production process 60 and solid electrolyte film production process 160 is continuously performed, and each process is performed one by one. It can also be applied to a so-called offline method. This off-line solid electrolyte film manufacturing method is also performed based on the solid electrolyte film manufacturing process 60 shown in FIG.

  Hereinafter, an outline of the energization process 70 in the off-line solid electrolyte film manufacturing process will be described. In addition, the same apparatus, member, process, etc. as embodiment mentioned above are demonstrated using the same code | symbol, and the detailed description is abbreviate | omitted. The energization device used in the present invention is not limited to the following.

(Energizing device)
In the energization process 70, an energization device 210 shown in FIG. 6 is used. The energization device 210 includes a container 211, a temperature controller 212, an energization holder 214 that holds a hydrogen substitution film 213, and a power source 127. The container 211 stores the second liquid 301. The temperature controller 212 is connected to the container 211 and holds the temperature of the second liquid 301 stored in the container 211 in a desired range. The temperature controller 212 preferably maintains the temperature of the second liquid 301 in the range of 10 ° C. or higher and 120 ° C. or lower. The hydrogen-substituted film 213 is cut out to a predetermined size from the hydrogen-substituted film 68 produced by the above-described solid electrolyte film manufacturing process and the same manufacturing process.

  The energization holder 214 includes a first holder 216 and a second holder 217. As shown in FIG. 7, the first holder 216 includes a support plate 220 that is an insulator, spacers 221 and 222, an electrode 223, and an electrode holder 224. The support plate 220 is formed in a plate shape, and a first fitting surface 220a is formed on one surface and a second fitting surface 220b is formed on the other surface. The support plate 220 has a through hole 220c formed so as to penetrate the first fitting surface 220a and the second fitting surface 220b. The insulating spacers 221 and 222 are formed in a rod shape. The electrode 223 which is a conductor is formed in a plate shape. The electrode holder 224 is formed in a plate shape. One surface 223a of the electrode 223 is fixed to the vicinity of the side end portion of the second fitting surface 220b via the spacers 221 and 222. The other surface 223 b of the electrode 223 is fixed to the one surface 224 a of the electrode holder 224. The spacers 221 and 222 form an opening 216 a between the electrode 223 and the support plate 220.

  Similarly, the second holder 217 includes a support plate 230 that is an insulator, spacers 231 and 232, an electrode 233, and an electrode holder 234. The support plate 230 is formed in a plate shape, and a first fitting surface 230a is formed on one surface and a second fitting surface 230b is formed on the other surface. The support plate 230 has a through hole 230c formed so as to penetrate the first fitting surface 230a and the second fitting surface 230b. The insulating spacers 231 and 232 are formed in a rod shape. The electrode 233 which is a conductor is formed in a plate shape. The electrode holder 234 is formed in a plate shape. One surface 233a of the electrode 233 is fixed to the vicinity of the side end portion of the second fitting surface 230b via the spacers 231 and 232. The other surface 233b of the electrode 233 is fixed to the one surface 234a of the electrode holder 234. The spacers 231 and 232 form an opening 217 a between the electrode 233 and the support plate 230.

  Thus, the energizing holder 214 is formed with a hollow portion composed of the openings 216a and 217a and the through holes 220c and 230c. The hollow portion is filled with a predetermined amount of the second liquid 301. This hollow portion may be either a sealed structure or an open structure. Here, the sealed structure refers to a structure in which the second liquid 301 filled in the hollow part cannot freely move to and from the container 211, and the open structure refers to the second liquid 301 filled in the hollow part freely in the container 211. It refers to the structure that can go to and from.

  The first fitting surface 220a of the first holder 216 and the first fitting surface 230a of the second holder 217 are brought into contact with each other via the hydrogen replacement film 213, and the first holder 216, the hydrogen replacement film 213, and the second holder 217 are contacted. Is fixed with a fixing member such as a screw to form the energization holder 214. At this time, the distance L2 between the electrode 223 and the electrode 233 is preferably 300 mm or less.

  The energizing holder 214 that holds the hydrogen-substituted film 213 is stored in the container 211 and immersed in the second liquid 301 that is maintained at a temperature within a predetermined range. The second liquid 301 contacts the hydrogen substitution film 213 through the openings 216a, 217a, 220c, and 230c. After the electrodes 223 and 233 and the power supply 127 are connected by wiring, a predetermined voltage V1 is applied between the electrode 223 and the electrode 233 by the power supply 127. In this way, current can be passed between the electrode 223 and the electrode 233 via the second liquid 301 and the hydrogen substitution film 213.

  In the above embodiment, the hydrogen substitution film 213 is cut out to a predetermined size from the hydrogen substitution film 68. However, the present invention is not limited to this, and a film piece cut out from the precursor film 65 to a predetermined size is a hydrogen substitution film. It may be used instead of 213. In this case, the film piece is preferably subjected to an acid treatment step together with the energization step, and the acid treatment step is preferably performed before or simultaneously with the energization step.

  The solid electrolyte film of the present invention can be suitably used as a proton conductive membrane for a fuel cell, particularly for a direct methanol fuel cell, and also used as a solid electrolyte film sandwiched between two electrodes of a fuel cell. Can do. Furthermore, as electrolytes, display elements, electrochemical sensors, signal transmission media, capacitors, electrodialysis, electrolytic membranes for electrolysis, gel actuators, salt electrolytic membranes, proton exchange resins in various batteries (redox flow batteries, lithium batteries, etc.) The solid electrolyte film of the present invention can be used.

(Fuel cell)
Hereinafter, an example in which a solid electrolyte film is used for an electrode membrane composite (hereinafter referred to as MEA) and an example in which this electrode membrane composite is used for a fuel cell will be described. However, the form of MEA and fuel cell shown here is an example of the present invention, and the present invention is not limited to this. The solid electrolyte film used in the present embodiment may be either the film 72 or the second solid electrolyte film 163 described above. Hereinafter, taking the case where the film 72 is used as an example, the modes of the MEA and the fuel cell will be described. FIG. 8 is a schematic cross-sectional view of the MEA. The MEA 261 includes a film 72 and an anode electrode 262 and a cathode electrode 263 that are opposed to each other with the film 72 interposed therebetween.

  The anode electrode 262 has a porous conductive sheet 262 a and a catalyst layer 262 b in contact with the film 72, and the cathode electrode 263 has a porous conductive sheet 263 a and a catalyst layer 263 b in contact with the film 72. Examples of the porous conductive sheets 262a and 263a include carbon paper. The catalyst layers 262b and 263b are made of a dispersion in which carbon particles supporting a catalyst metal such as platinum particles are dispersed in a proton conductive material. Examples of the carbon particles include ketjen black, acetylene black, and carbon nanotube. Examples of the proton conductive material include Nafion (registered trademark).

As the manufacturing method of the MEA 261, the following four methods are preferable.
(1) Proton conductive material coating method: A catalyst paste (ink) containing active metal-carrying carbon, proton conductive material, and solvent is directly applied to both surfaces of the film 72, and the porous conductive sheets 262a and 263a are applied to the (thermal) coating layer. A MEA having a five-layer structure is manufactured by pressure bonding.
(2) Porous conductive sheet coating method: After a liquid containing the material of the catalyst layers 262b and 263b, for example, a catalyst paste, is applied to the surfaces of the porous conductive sheets 262a and 263a to form the catalyst layers 262b and 263b. Then, the film 72 is pressure-bonded to produce a MEA 261 having a five-layer structure.
(3) Decal method: After a catalyst paste is applied on PTFE to form catalyst layers 262b and 263b, only the catalyst layers 262b and 263b are applied to the film 72 to form a three-layer structure, which is porous conductive Sheets 262a and 263a are pressure-bonded to form a 5-layer MEA 261.
(4) Post-catalyst loading method: An ink in which a platinum unsupported carbon material is mixed with a proton conductive material is applied to the film 72, the porous conductive sheets 262a, 263a, or PTFE, and then formed into a liquid containing platinum ions. No. 72 is impregnated, and platinum particles are reduced and deposited in a film to form catalyst layers 262b and 263b. After the catalyst layers 262b and 263b are formed, the MEA 261 is manufactured by the methods (1) to (3) described above.

  However, the method of making the MEA is not limited to the above method, and various known methods can be applied. For example, in addition to the above methods (1) to (4), there are the following methods. A coating solution containing the materials of the catalyst layers 262b and 263b is prepared in advance, and this coating solution is applied to a support and dried. The support on which the catalyst layers 262b and 263b are formed is pressure-bonded on the both sides of the film 72 so that the catalyst layers 262b and 263b are in contact with the film 72, respectively. And after peeling a support body, the film 72 in which the catalyst layers 262b and 263b were formed in both surfaces is pinched | interposed with the porous conductive sheets 262a and 263a. And MEA can be manufactured by sticking the porous conductive sheets 262a and 263a and the catalyst layers 262b and 263b.

  FIG. 9 is a schematic view of a fuel cell. The fuel cell 271 includes an MEA 261, a pair of separators 272 and 273 that sandwich the MEA 261, a current collector 276 made of a stainless steel net attached to the separators 272 and 273, and a packing 277. The anode pole side separator 272 is provided with an anode pole side opening 281, and the cathode pole side separator 273 is provided with a cathode pole side opening 282. Gas fuel such as hydrogen and alcohols (such as methanol) or liquid fuel such as an alcohol aqueous solution is supplied from the anode electrode side opening 281, and oxidant gas such as oxygen gas and air is supplied from the cathode electrode side opening 282. Is supplied.

  A catalyst in which active metal particles such as platinum are supported on a carbon material is used for the anode electrode 262 and the cathode electrode 263. Commonly used active metal particle sizes are in the range of 2 to 10 nm. However, the smaller the particle size, the greater the surface area per unit weight and the higher the activity, which is advantageous. However, if it is too small, it is difficult to disperse without agglomeration, so about 2 nm is said to be the small limit. .

  The active polarization in the hydrogen-oxygen fuel cell is larger in the cathode electrode, that is, the air electrode than in the anode electrode, that is, the hydrogen electrode. This is because the rate of the cathode electrode reaction, that is, the oxygen reduction reaction, is slower than that of the anode electrode. For the purpose of improving the activity of the oxygen electrode, various platinum-based binary metals such as Pt—Cr, Pt—Ni, Pt—Co, Pt—Cu, and Pt—Fe can be used. In a direct methanol fuel cell using a methanol aqueous solution as the anode fuel, in order to suppress catalyst poisoning by CO generated during the oxidation process of methanol, Pt—Ru, Pt—Fe, Pt—Ni, Pt—Co, and Pt—Mo are used. Pt-Ru-Mo, Pt-Ru-W, Pt-Ru-Co, Pt-Ru-Fe, Pt-Ru-Ni, Pt-Ru-Cu, Pt-Ru-Sn, etc. A platinum group ternary metal such as Pt—Ru—Au can be used. As the carbon material for supporting the active metal, acetylene black, Vulcan XC-72, ketjen black, carbon nanohorn (CNH), and carbon nanotube (CNT) are preferably used.

The catalyst layers 262b and 263b are formed by (1) transporting fuel to an active metal, (2) providing a field for fuel oxidation (anode electrode) and reduction (cathode electrode) reaction, and (3) oxidation / reduction. And (4) transports protons generated by the reaction to the solid electrolyte, that is, the film 72. For (1), the catalyst layers 262b and 263b are made porous so that liquid and gaseous fuel can permeate deeply. For (2), the active metal catalyst supported on the carbon material is responsible, and (3) is also responsible for the carbon material. In order to fulfill the function (4), a proton conductive material is mixed in the catalyst layers 262b and 263b. The proton conductive material of the catalyst layer is not limited as long as it is a solid having a proton donating group, but a polymer compound having an acid residue, for example, perfluorosulfonic acid represented by Nafion (registered trademark), side chain A sulfonated product of a heat-resistant aromatic polymer such as phosphoric acid group poly (meth) acrylate, sulfonated polyetheretherketone, and sulfonated polybenzimidazole is preferably used. When the solid electrolyte contained in the film 72 is used for the catalyst layers 262b and 263b, the catalyst layers 262b and 263b and the film 72 are made of the same material, so that the electrochemical adhesion between the solid electrolyte and the catalyst layer is increased, and the proton More advantageous in terms of conduction. It is suitable from a viewpoint of battery output and economical efficiency to make the usage-amount of an active metal into the range of 0.03-10 mg / cm < ² >. The amount of the carbon material supporting the active metal is preferably 1 to 10 times the weight of the active metal. The amount of the proton conductive material is preferably 0.1 to 0.7 times the weight of the active metal-carrying carbon.

  The catalyst layers 262b and 263b are also referred to as an electrode base material, a permeable layer, or a backing material, and play a role of collecting current and preventing water accumulation and gas permeation from deteriorating. Usually, carbon paper or carbon cloth can be used, and polytetrafluoroethylene (PTFE) treated for water repellency can be used.

MEA is incorporated into a battery, preferably having an area resistance value of 3Omucm ² below by the AC impedance method in a state filled with fuel, more preferably those of 1 .OMEGA.cm ² or less, and most preferably those 0.5Omucm ² below. The area resistance value is obtained from the product of the actually measured resistance value and the area of the sample.

  What can be used as a fuel of a fuel cell will be described. Examples of the anode fuel include hydrogen, alcohols (such as methanol, isopropanol, and ethylene glycol), ethers (such as dimethyl ether, dimethoxymethane, and trimethoxymethane), formic acid, borohydride complex, and ascorbic acid. Examples of the cathode fuel include oxygen (including oxygen in the atmosphere) and hydrogen peroxide.

In the direct methanol fuel cell, a methanol aqueous solution having a methanol concentration of 3 to 64% by weight is used as the anode fuel. According to the anode reaction formula (CH ₃ OH + H ₂ O → CO ₂ + 6H ⁺ + 6e ⁻ ), 1 mol of water is required for 1 mol of methanol, and the methanol concentration at this time corresponds to 64% by weight. The higher the methanol concentration, there is an advantage that the weight and volume of the battery including the fuel tank with the same energy capacity can be reduced. However, as the methanol concentration is higher, the so-called crossover phenomenon, in which methanol permeates the solid electrolyte film and reacts with oxygen on the cathode side to lower the voltage, becomes more prominent, and the output tends to decrease. Therefore, the optimum concentration is determined by the methanol permeability of the solid electrolyte film to be used. The cathode reaction formula of the direct methanol fuel cell is (3/2) O ₂ + 6H ⁺ + 6e ⁻ → H ₂ O, and oxygen (usually oxygen in the air) is used as the fuel.

  As a method of supplying the anode fuel and the cathode fuel to the respective catalyst layers 262b and 263b, (1) a method of forcibly feeding using an auxiliary device such as a pump (active type), and (2) an auxiliary device There are two methods that are not used, for example, a passive type in which the fuel is exposed to the atmosphere by exposing the catalyst layer to the atmosphere due to capillary action or natural fall when the fuel is a liquid, and ( It is also possible to combine 1) and (2). (1) has the advantage that by extracting the water produced on the cathode side, high-concentration methanol can be used as the fuel, and high output can be achieved by air supply, but a fuel supply system is provided. Therefore, there is a drawback that miniaturization is difficult. Although (2) has the advantage that it can be downsized, it has a drawback that the fuel supply is likely to be rate-limiting and it is difficult to produce a high output.

  Since the single cell voltage of the fuel cell is generally 1 V or less, the single cells are used by stacking in series according to the required voltage of the load. As the stacking method, “planar stacking” in which single cells are arranged on a plane and “bipolar stacking” in which single cells are stacked via separators having fuel flow paths formed on both sides thereof are used. The former is suitable for a small fuel cell because the cathode electrode (air electrode) comes out on the surface, so that air can be easily taken in and can be made thin. In addition to this, a method of applying MEMS technology, performing fine processing on a silicon wafer, and stacking has been proposed.

  Fuel cells are considered for various uses such as for automobiles, homes, and portable devices.In particular, direct methanol fuel cells are advantageous in that they can be reduced in size and weight and do not require charging. It is expected to be used as an energy source for various portable devices and portable devices. For example, mobile devices that can be preferably applied include mobile phones, mobile laptop computers, electronic still cameras, PDAs, video cameras, portable game machines, mobile servers, wearable personal computers, mobile displays, and the like. Examples of portable devices that can be preferably applied include portable generators, outdoor lighting devices, flashlights, and electric (assist) bicycles. Moreover, it can be preferably used as a power source for industrial or household robots or other toys. Furthermore, it is also useful as a power source for charging secondary batteries mounted on these devices.

  Next, examples of the present invention will be described. In the following Examples, Examples 1 to 3 are examples of the embodiment of the present invention, and Examples 4 to 6 are comparative experiments with respect to Examples 1 to 3.

A compound in which X in Chemical Formula 3 is a cationic species other than H was used as a precursor. This precursor is referred to as raw material A. In the compound of Chemical Formula 3 in this example, X is Na, n is 0.4, the number average molecular weight Mn is 50000, and the weight average molecular weight Mw is 120,000. The solvent is a mixture of the solvent component 1 and the solvent component 2. The solvent component 1 is a good solvent for the raw material A, and the solvent component 2 is a poor solvent for the raw material A. The raw material A and the solvent were mixed in a predetermined composition, and the solid content of the raw material A was dissolved in the solvent to produce a dope containing 20% by weight of the precursor based on the total weight. This dope is referred to as dope A in the following description.
-Raw material A; 100 parts by weight-Solvent component 1; 256 parts by weight of dimethyl sulfoxide-Solvent component 2; 171 parts by weight of methanol

[Production of solid electrolyte film]
A casting film 93 is cast from the casting die 93 to the PET film running on the dope A to form a casting film 61. Drying air of 45 ° C./10% RH is blown for 30 minutes through the air duct, and the residual solvent amount is 200 with respect to the dry amount standard. The cast film 61 was dried until the weight percentage was reached. The casting film 61 was immersed in water at 30 ° C. together with the PET film, and the casting film 61 was peeled off from the PET film to obtain a precursor film 65. And the precursor film 65 was immersed in water as it was, and solvent substitution was performed. The peeling time from the PET film and the time required for solvent replacement were 5 minutes. Thus, a precursor film 65 having a self-supporting property and having a residual solvent amount of 150% by weight based on the dry weight basis was obtained. The precursor film 65 was sent to the tenter 83 and conveyed inside the tenter 83 while the clip 104 held its both end portions. In the tenter 83, the precursor film 65 was dried with a drying air at 120 ° C. for 10 minutes. Thus, a precursor film 65 having a residual solvent amount of 10% by weight based on the dry weight standard was obtained. The precursor film 65 was detached from the clip 104 at the outlet of the tenter 83, and both end portions gripped by the clip 104 were cut and removed by the ear clip device 105 provided downstream of the tenter 83.

  Then, the precursor film 65 was immersed in the acid immersion tank 110 in which the first liquid 300 to be boiled is stored for 2 hours, and an acid treatment step 69 was performed. A sulfuric acid aqueous solution (hereinafter referred to as solution A) was used as the first liquid 300. The proton concentration of the first liquid 300 was 0.5 mol / l. By this acid treatment step 69, a hydrogen-substituted film 68 was obtained from the precursor film 65.

The long hydrogen-substituted film 68 produced from the acid treatment step 69 was cut into a substantially rectangular shape (length 100 mm × width 50 mm), and this was used as a piece of hydrogen-substituted film. This hydrogen-substituted film piece was held by the first holder 216 and the second holder 217. The electrode 223 and the electrode 233 were connected to the power source 127 using wiring. The distance L2 between the electrode 223 and the electrode 233 was 10 mm. Next, the hydrogen-substituted film piece was immersed in a container 211 in which the second liquid 301 at approximately 25 ° C. was stored. A p-toluenesulfonic acid aqueous solution (hereinafter referred to as solution B) was used as the second liquid 301. The proton concentration of the second liquid 301 was 6 × 10 ⁻⁴ mol / l. And the DC voltage was applied between the electrode 223 and the electrode 233, and the electricity supply process 70 was performed to the hydrogen substitution film piece. At this time, when the current density Id was obtained based on the current value I read from the current detector built in the power supply 127 and the area S of the hydrogen substitution film 68, the current density Id in this example is It was 6 mA / cm ² . After the energization process 70, the hydrogen-substituted film piece was taken out from the second liquid 301 together with the energization holder 214.

  This hydrogen-substituted film piece was immersed in a water tank in which water having a water temperature of 70 ° C. was stored and washed with water. Further, the hydrogen-substituted film piece was immersed in a water tank in which water having a water temperature of 70 ° C. was stored, and washed again with water. Subsequently, the hydrogen-substituted film piece was drained using an air knife. The drained hydrogen-substituted film piece was sent to a drying chamber and dried at 60 to 120 ° C. Then, a film having a residual solvent amount of less than 5% based on the dry weight standard was obtained. The evaluation results for the obtained film are shown in Table 1.

A film was obtained in the same manner as in Example 1 except that the current density Id in the energization process 70 was 10 mA / cm ² . The evaluation results for the obtained film are shown in Table 1.

A film was obtained in the same manner as in Example 1 except that the current density Id in the energization process 70 was ² mA / cm ² . The evaluation results for the obtained film are shown in Table 1.

  A film was obtained in the same manner as in Example 1 except that the energization step 70 was not performed. The evaluation results for the obtained film are shown in Table 1.

In the energization process, a film was obtained in the same manner as in Example 1 except that a sulfuric acid aqueous solution having a proton concentration of 6 × 10 ⁻⁴ mol / l was used as the second liquid. The evaluation results for the obtained film are shown in Table 1.

In the energization process, a film was obtained in the same manner as in Example 1 except that the current density Id was 0.1 mA / cm ² . The evaluation results for the obtained film are shown in Table 1.

  The characteristics of the obtained solid electrolyte film were evaluated by measuring the following items. The following measurements are common to Examples 1 to 6, and the evaluation results in each Example are summarized in Table 1.

1. Proton conductivity The proton conductivity was measured using a four-terminal AC method according to Journal of the Electronic Society 143, No. 4, 1254-1259 (1996). Specifically, first, a sample obtained by cutting out the solid electrolyte film produced in Examples 1 to 6 to a length of 2 cm and a width of 1 cm was used as a sample. Next, after placing the previous sample on a PTFE plate with four platinum wires fixed at intervals of 5 mm, a PTFE plate was further placed thereon, and these were fixed with screws to form a test cell. Using this test cell and an impedance analyzer combining Solartron 1480 type and 1225B type, proton conductivity was measured in water by the AC impedance method. The proton conductivity measured in water at 25 ° C. was σ _a , and the proton conductivity measured in water at 80 ° C. was σ _b .

  As mentioned above, it turns out that the solid electrolyte film manufactured by Examples 1-3 is equipped with the outstanding proton conductivity compared with Examples 4-6 from the result of each Example. Therefore, the method for producing a solid electrolyte film of the present invention performs a predetermined energization step on the film containing the solid electrolyte, and thus can produce a solid electrolyte film having excellent proton conductivity.

  Moreover, since the manufacturing method of the solid electrolyte film of this invention can be performed by what is called an on-line system, the film of high proton conductivity can be produced in large quantities continuously. Moreover, the solid electrolyte film obtained by this manufacturing method can implement | achieve the outstanding output density, when using as a solid electrolyte layer of a fuel cell.

It is the schematic of an example of the dope manufacturing equipment used by this embodiment. It is a manufacturing-process figure of the 1st solid electrolyte film which concerns on this invention. It is the schematic of an example of the solid electrolyte film manufacturing equipment based on this invention. It is explanatory drawing which shows the outline | summary of the acid treatment chamber which concerns on this invention. It is a manufacturing-process figure of the 2nd solid electrolyte film which concerns on this invention. It is explanatory drawing which shows the outline | summary of the electricity supply apparatus which concerns on this invention. It is sectional drawing which shows the outline | summary of the holder for electricity supply which concerns on this invention. It is sectional drawing of an electrode membrane composite. It is sectional drawing of a fuel cell.

Explanation of symbols

DESCRIPTION OF SYMBOLS 10 Dope manufacturing equipment 11a Solvent 12a Precursor 24 Dope 33 Film manufacturing equipment 60,160 Solid electrolyte film manufacturing process 61 Casting film 63 Casting film formation process 65 Precursor film 66 Stripping process 68, 213 Hydrogen substitution film 69 Acid treatment Process 70 Energizing process 72 Solid electrolyte film 84 Acid treatment chamber 110 Acid dipping tank 111 Current tank 120, 121, 223, 233 Electrode 121 Electrode 127 Power supply 161 First solid electrolysis chamber film 162 Second solid electrolysis chamber film 210 Energization device 214 Energization Holder 261 Electrode membrane composite (MEA)
262 Anode electrode 263 Cathode electrode 271 Fuel cell 276 Current collector 300 First liquid 301 Second liquid 305 Cleaning liquid

Claims (5)

A casting film forming step of casting a dope containing a polymer which is a solid electrolyte having a cationic species and an organic solvent on a traveling support from a casting die to form a casting film;
A stripping step of stripping the cast film as a film from the support;
An acid treatment step of subjecting the film to proton substitution;
An energization step of energizing the film containing the polymer that is a solid electrolyte;
Have
The method for producing a solid electrolyte film, wherein the energization step is continuously performed after the acid treatment step.   2. The method for producing a solid electrolyte film according to claim 1, wherein in the energization step, the film is energized through a first liquid containing an acid which is a proton donor.   Using the first electrode that contacts the first liquid, and the second electrode that contacts the first liquid and is disposed so that the distance from the first electrode is 300 mm or less. The method for producing a solid electrolyte film according to claim 2, wherein the energization step is performed.   4. The solid according to claim 3, wherein the proton concentration in the second liquid is 0.05 mol / l or more in the acid treatment step performed through the second liquid containing an acid which is a proton donor. Manufacturing method of electrolyte film. The method for producing a solid electrolyte film according to any one of claims 2 to 4, wherein the formula amount of anions contained in the first liquid or the second liquid is 40 or more and 1000 or less.

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