WO2011034179A1 - 電解質エマルション及びその製造方法 - Google Patents
電解質エマルション及びその製造方法 Download PDFInfo
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- WO2011034179A1 WO2011034179A1 PCT/JP2010/066227 JP2010066227W WO2011034179A1 WO 2011034179 A1 WO2011034179 A1 WO 2011034179A1 JP 2010066227 W JP2010066227 W JP 2010066227W WO 2011034179 A1 WO2011034179 A1 WO 2011034179A1
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- H01M8/1025—Polymeric electrolyte materials characterised by the chemical structure of the main chain of the ion-conducting polymer having only carbon and oxygen, e.g. polyethers, sulfonated polyetheretherketones [S-PEEK], sulfonated polysaccharides, sulfonated celluloses or sulfonated polyesters
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Definitions
- the present invention relates to an electrolyte emulsion suitable for an electrolyte membrane for a solid polymer electrolyte fuel cell, a method for producing the same, and the like.
- a fuel cell is one that converts the chemical energy of fuel directly into electrical energy by electrochemically oxidizing hydrogen, methanol, etc. in the battery, and is attracting attention as a clean electrical energy supply source. ing.
- solid polymer electrolyte fuel cells are expected to be used as alternative power sources for automobiles, home cogeneration systems, portable generators, and the like because they operate at a lower temperature than others.
- Such a solid polymer electrolyte fuel cell includes at least a membrane electrode assembly in which a gas diffusion electrode in which an electrode catalyst layer and a gas diffusion layer are laminated is bonded to both surfaces of an electrolyte membrane.
- the electrolyte membrane here is a material having a strongly acidic group such as a sulfonic acid group or a carboxylic acid group in the polymer chain and a property of selectively transmitting protons.
- a perfluoro proton exchange membrane represented by Nafion (registered trademark, manufactured by DuPont) having high chemical stability is used.
- fuel for example, hydrogen
- oxidant for example, oxygen or air
- the operation of the fuel cell is realized.
- hydrogen is used as fuel
- hydrogen is oxidized on the anode catalyst to generate protons.
- the protons pass through the electrolyte binder in the anode catalyst layer, then move in the electrolyte membrane, and reach the cathode catalyst through the electrolyte binder in the cathode catalyst layer.
- electrons generated simultaneously with protons by oxidation of hydrogen reach the cathode side gas diffusion electrode through an external circuit.
- the proton and oxygen in the oxidant react to generate water. At this time, electric energy is extracted.
- Solid polymer electrolyte fuel cells are expected to be used for stationary cogeneration systems and in-vehicle power supplies because of their low environmental load and high energy conversion efficiency.
- the vehicle In automobile applications, the vehicle is usually driven at around 80 ° C.
- it is necessary to reduce the size of the radiator and the humidifier to reduce the cost. To that end, it can be applied to operation under high temperature and low humidification conditions (operating temperature 100 to 120 ° C, equivalent to humidity 20 to 50% RH), and wide operating environment (room temperature to 120 ° C / 20 to 100% RH) Therefore, an electrolyte membrane exhibiting high performance is desired.
- Non-Patent Document 1 in order to enable an operating temperature of 100 ° C., a proton conductivity of 0.10 S / cm or higher and an operating temperature of 120 ° C. are enabled at 50% RH. Needs to have a proton conductivity of 0.10 S / cm or more at 20% RH.
- Patent Documents 1 to 3 disclose fluorine-based electrolyte membranes having an equivalent weight (EW), that is, an EW (g / eq) of 670 to 776, which is a dry weight per equivalent of proton exchange groups.
- EW equivalent weight
- Patent Document 4 discloses an electrolyte membrane that hardly dissolves in hot water even with low EW, and an electrolyte membrane of EW698 is exemplified.
- Patent Document 5 discloses a production example of a polymer electrolyte of EW564.
- Patent Document 6 discloses a fluorine-containing polymer electrolyte obtained through a polymerization step in which a radical polymerization initiator composed of a fluorine-containing compound having a molecular weight of 450 or more is used and copolymerized at a polymerization temperature of 0 to 35 ° C. Has been.
- the present inventors can control the ion cluster structure formed in the fluorine electrolyte, and control the ion cluster structure of the electrolyte membrane.
- high conductivity can be expressed even at low humidity.
- This technique discovered by the present inventors provides an electrolyte having high conductivity even under high temperature and low humidification conditions, and enables a higher performance fuel cell.
- the fluorine-based polymer electrolyte having a low equivalent weight is easy to soften and may cause problems in workability, such as absorbing moisture in the air and causing wrinkles on the membrane. Was also found together.
- an object of the present invention is to improve the processability of a fluorine-based polymer electrolyte having a low equivalent weight and high proton conductivity.
- the present invention provides a fluorine-based polymer electrolyte that is improved in workability and easy to manufacture by making the fluorine-based polymer electrolyte into spherical particles having a large particle size and an emulsion in which the particles are dispersed in an aqueous medium.
- Provide material for example
- the present invention is an electrolyte emulsion in which a fluorine-based polymer electrolyte is dispersed in an aqueous medium, and the fluorine-based polymer electrolyte has an SO 3 Z group (Z is an alkali metal, an alkaline earth metal, hydrogen, or NR 1 R 2 R 3 R 4 , R 1 , R 2 , R 3 and R 4 each independently represents an alkyl group having 1 to 3 carbon atoms or hydrogen.
- EW is 250 or more and 700 or less
- a proton conductivity at 110 ° C. and a relative humidity of 50% RH is 0.10 S / cm or more
- a spherical particle having an average particle diameter of 10 to 500 nm (SO 2 F number) / (SO 3 Z group number) is 0 to 0.01.
- the fluoropolymer electrolyte preferably has an equivalent weight (EW) of 250 or more and 650 or less.
- a 1 represents SO 3 Z
- Z represents an alkali metal, an alkaline earth metal, hydrogen, or NR 1 R 2 R 3 R 4 R 1 , R 2 , R 3 and R 4 each independently represents an alkyl group having 1 to 3 carbon atoms or hydrogen.
- k is 0, l is 1, Y 1 is F, n is 0 or 1, Y 2 is F, m is 2 or 4, A It is preferable that 1 is SO 3 H.
- n is preferably 0 and m is preferably 2.
- the fluorine-based polymer electrolyte preferably has a distance between ion clusters of 0.1 nm or more and 2.6 nm or less at 25 ° C. and a relative humidity of 50% RH, which is calculated from the following formula (1) through small-angle X-ray measurement.
- d ⁇ / 2 / sin ( ⁇ m) (1)
- d is a distance between ion clusters
- ⁇ is an incident X-ray wavelength used for small-angle X-ray measurement
- ⁇ m is a Bragg angle indicating a peak.
- the fluorine-based polymer electrolyte is obtained by chemically treating a fluorine-based polymer electrolyte precursor, and the fluorine-based polymer electrolyte precursor is obtained by performing the chemical treatment on SO 3 Z (Z is an alkali metal, an alkaline earth metal, Hydrogen or NR 1 R 2 R 3 R 4 , wherein R 1 , R 2 , R 3 and R 4 each independently represents an alkyl group having 1 to 3 carbon atoms or hydrogen; It is preferable that the melt flow rate is 0.01 to 100 g / 10 min.
- the chemical treatment is preferably a treatment in which the fluorine-based polymer electrolyte precursor and the basic reaction liquid are brought into contact with each other.
- the electrolyte emulsion preferably contains 2 to 80% by mass of a fluorine-based polymer electrolyte.
- the aqueous medium preferably has a water content of more than 50% by mass.
- the present invention includes a step of applying the electrolyte emulsion to a substrate, a step of drying the electrolyte emulsion applied to the substrate to obtain an electrolyte membrane, and a step of peeling the electrolyte membrane from the substrate. It is also a manufacturing method of the electrolyte membrane.
- the present invention also provides an electrolyte membrane obtained by the above-described method for producing an electrolyte membrane.
- the present invention includes a step of preparing an electrode catalyst composition in which composite particles composed of a catalyst metal and a conductive agent are dispersed in the electrolyte emulsion, a step of applying the electrode catalyst composition to a substrate, and a method of applying to the substrate. And a step of obtaining an electrode catalyst layer by drying the electrode catalyst composition.
- the present invention also provides an electrode catalyst layer obtained by the above method for producing an electrode catalyst layer.
- the present invention also provides a membrane electrode assembly comprising the above electrolyte membrane.
- This invention is also a membrane electrode assembly provided with the said electrode catalyst layer.
- the present invention also provides a polymer electrolyte fuel cell comprising the membrane electrode assembly.
- the present invention also provides a copolymerization of an ethylenic fluoromonomer and a vinyl fluoride compound having an SO 2 Z 1 group (Z 1 represents a halogen element) at a polymerization temperature of 0 ° C. or more and 40 ° C. or less.
- a step (2) of obtaining an electrolyte emulsion in which a polymer electrolyte is dispersed The electrolyte emulsion is also a method for producing an electrolyte emulsion, wherein an equivalent weight (EW) is 250 or more and 700 or less.
- EW equivalent weight
- the manufacturing method of the said electrolyte emulsion is what manufactures the electrolyte emulsion of this invention mentioned above.
- the electrolyte emulsion of the present invention has the above-described configuration, for example, when it is processed into an electrolyte membrane, an electrode catalyst layer, etc., it has good processability and is easy to manufacture. Therefore, if the electrolyte emulsion of the present invention is used, a high-power fuel cell can be produced at low cost with high productivity.
- the present invention is an electrolyte emulsion in which a fluorine-based polymer electrolyte is dispersed in an aqueous medium.
- the fluoropolymer electrolyte is a spherical particle having an average particle size of 10 to 500 nm.
- the spherical particles mean particles that are substantially spherical, and “substantially spherical” means that the aspect ratio is 3.0 or less. Normally, the closer the aspect ratio is to 1.0, the closer to a sphere.
- the aspect ratio of the spherical particles is preferably 3.0 or less. A more preferred upper limit is 2.0, and a more preferred upper limit is 1.5.
- the lower limit of the aspect ratio of the spherical particles is, for example, 1.0.
- the emulsion tends to have a high viscosity.
- the viscosity of the electrolyte emulsion is lower than when the particle shape is not spherical, and even if the solid content concentration of the fluoropolymer electrolyte is increased, handling properties are not affected. Therefore, for example, when forming a film by a method such as cast film formation, high productivity can be realized.
- the fluoropolymer electrolyte has an average particle size of 10 to 500 nm. When it is less than 10 nm, when used as an electrode material, active points are covered, and good battery characteristics may not be obtained.
- the upper limit of the average particle diameter can be 500 nm from the viewpoint of the stability of the electrolyte emulsion and the ease of making the precursor emulsion. However, even if the average particle diameter exceeds 500 nm, it does not significantly affect the battery characteristics. Absent.
- the average particle size is within the above-mentioned range, the viscosity of the electrolyte emulsion is low, and the handleability is excellent even when the solid content concentration of the fluorine-based polymer electrolyte is increased, and the productivity is high when forming a film. Can be realized.
- the fluorine-based polymer electrolyte preferably has an average particle size of 10 to 300 nm. A more preferable lower limit of the average particle diameter is 30 nm, and a more preferable upper limit is 160 nm.
- the above-mentioned aspect ratio and average particle diameter are the fluorine-based polymer electrolyte obtained by applying the electrolyte emulsion to the glass substrate with a scanning or transmission electron microscope, atomic force microscope, etc., and then removing the aqueous medium.
- the average ratio of the major axis and minor axis length ratios (major axis / minor axis) measured for 20 or more particles on the obtained image is the aspect ratio, major axis, and minor axis.
- the average value of the shaft length can be obtained as the average particle diameter described later.
- the fluorine-based polymer electrolyte has an equivalent weight (EW), that is, a dry weight per equivalent of ion exchange groups of 250 or more and 700 or less.
- EW equivalent weight
- the upper limit of EW is preferably 650.
- EW exceeds 650 the film forming property may be inferior. More preferably, it is 600, More preferably, it is 550, Most preferably, it is 500.
- the upper limit of EW is preferably 450.
- the ionic conductivity is extremely high, which is particularly suitable as a material for producing an electrolyte membrane or an electrode catalyst layer used in a fuel cell. Therefore, it can be particularly suitably used for various applications that require high ionic conductivity.
- the lower limit of EW is preferably 300, more preferably 350, and even more preferably 390. The smaller the EW, the higher the conductivity and the better. On the other hand, the solubility in hot water may be increased. Therefore, the appropriate range as described above is desirable.
- the fluorine-based polymer electrolyte has a proton conductivity of 0.10 S / cm or more at 110 ° C. and a relative humidity of 50% RH.
- the proton conductivity at 40% RH is 0.10 S / cm or more, more preferably, the proton conductivity at 30% RH is 0.10 S / cm or more, and more preferably, the proton conductivity at 25% RH is 0.10 S / cm. More preferably, the proton conductivity at 23% RH is 0.10 S / cm or more.
- the proton conductivity at 110 ° C. and 50% relative humidity may be 1.0 S / cm or less.
- the electrolyte emulsion of the present invention is applicable to operation under high temperature and low humidification conditions and exhibits high performance in a wide range of operating environments. Electrolyte membranes and electrode catalyst layers can be produced.
- the proton conductivity can be measured as follows using a polymer water content test apparatus (for example, polymer film water content test apparatus MSB-AD-V-FC manufactured by Nippon Bell Co., Ltd.).
- a polymer electrolyte membrane formed to a thickness of 50 ⁇ m is cut into a width of 1 cm and a length of 3 cm and set in a conductivity measuring cell.
- the conductivity measuring cell is set in the chamber of the test apparatus, and the inside of the chamber is adjusted to 110 ° C. and less than 1% RH.
- water vapor generated using ion-exchanged water is introduced into the chamber, and the chamber is humidified in the order of 10% RH, 30% RH, 50% RH, 70% RH, 90% RH, and 95% RH.
- the conductivity at each humidity is measured.
- the fluorine-based polymer electrolyte has a special ion cluster structure. That is, the distance between the ion clusters at 25 ° C. and 50% RH of the fluorine-based polymer electrolyte is preferably 0.1 nm or more and 2.6 nm or less.
- FIG. 1 is a graph plotting the results of Examples and Comparative Examples described later, where the horizontal axis is the intercluster distance and the vertical axis is the ionic conductivity under high temperature and low humidification conditions. The intercluster distance is 2.6 nm. It can be seen that the conductivity rises sharply below.
- the upper limit of the distance between ion clusters is more preferably 2.5 nm.
- the lower limit of the distance between ion clusters may be, for example, 0.5 nm, 1.0 nm, or 2.0 nm.
- the fluorine-based polymer electrolyte has a distance between ion clusters in the above range, it is particularly suitable for operation under high temperature and low humidification conditions, and an electrolyte membrane that exhibits high performance in a wide range of operating environments.
- An electrode catalyst layer can be manufactured.
- An ion cluster is an ion channel formed by aggregating a plurality of proton exchange groups, and a perfluoro proton exchange membrane represented by Nafion is also considered to have such an ion cluster structure (for example, Gierke).
- TD Munn GE, Wilson FC, J. Polymer Sci. Polymer Phys, 1981, 19, 1687).
- the distance d between ion clusters can be measured and calculated by the following method.
- the film is formed by the cast method, it is annealed at 160 ° C. in advance. Further, the terminal group represented by SO 3 Z group fluoropolymer electrolyte is treated to become SO 3 H.
- the sample film is held in an atmosphere of 25 ° C. and 50% RH for 30 minutes or more before measurement, and then measurement is performed.
- the fluorine-based polymer electrolyte has an SO 3 Z group (Z represents an alkali metal, an alkaline earth metal, hydrogen, or NR 1 R 2 R 3 R 4.
- R 1 , R 2 , R 3, and R 4 represent Each independently represents an alkyl group having 1 to 3 carbon atoms or hydrogen).
- the fluorine-based polymer electrolyte has (SO 2 F group number) / (SO 3 Z group number) of 0 to 0.01. “(SO 2 F group number) / (SO 3 Z group number)” is the ratio of the number of SO 2 F groups to the number of SO 3 Z groups of the fluorine-based polymer electrolyte, and is obtained as follows. it can.
- the fluoropolymer electrolyte precursor having a -SO 2 F group if converting process -SO 2 F groups to obtain the fluoropolymer electrolyte, (SO 3 Z contained in fluoropolymer electrolyte radix) is, approximately, - can be regarded as ⁇ (sO 2 F groups contained in the fluoropolymer electrolyte precursor) (sO 2 F groups contained in the fluoropolymer electrolyte) ⁇ .
- the infrared absorption analysis of the (SO 2 F groups contained in the fluorine-based polymer electrolyte) and (SO 2 F groups contained in the fluoropolymer electrolyte precursor) were measured by taking the ratio, The (SO 2 F group number) / (SO 3 Z group number) of the fluorine-based polymer electrolyte can be determined.
- the film of the precursor prepared by heat press or the like was measured by Fourier transform infrared absorption spectroscopy, and the absorption peak intensity (I 0C ) derived from CF 2 near 2364 cm ⁇ 1 and 2704 cm ⁇
- the (SO 2 F group number) / (SO 3 Z group number) of the fluorine-based polymer electrolyte can be calculated as A 1 / A 0 .
- the SO 3 Z group-containing monomer unit is preferably 10 to 95 mol% of the total monomer units.
- total monomer unit indicates all the parts derived from the monomer in the molecular structure of the fluorine-based polymer electrolyte.
- a 1 represents SO 3 Z
- Z represents an alkali metal, an alkaline earth metal, hydrogen
- NR 1 R 2 R 3 R 4 R 1 , R 2 , R 3 and R 4 is derived from SO 3 Z group-containing monomer represented by each independently represent an alkyl group or hydrogen having 1 to 3 carbon atoms.).
- k is more preferably 0, l is more preferably 1, n is more preferably 0 or 1, and n also more preferably, it is 0, Y 2 is F, m is more preferably an integer of 2 ⁇ 6, Y 2 is F, more preferably m is 2 or 4 Y 2 is F and m is particularly preferably 2.
- Y 1 is preferably F, and A 1 is preferably SO 3 H.
- the SO 3 Z group-containing monomer can be used alone or in combination of two or more.
- the fluoropolymer electrolyte includes a repeating unit ( ⁇ ) derived from the SO 3 Z group-containing monomer and a repeating unit ( ⁇ ) derived from an ethylenic fluoromonomer different from the repeating unit ( ⁇ ).
- a polymer is preferred.
- the ethylenic fluoromonomer that constitutes the repeating unit ( ⁇ ) does not have etheric oxygen [—O—] and has a vinyl group.
- the vinyl group is a hydrogen atom by a fluorine atom. Part or all may be substituted.
- etheric oxygen means an —O— structure constituting a monomer molecule.
- Examples of the ethylenic fluoromonomer include tetrafluoroethylene [TFE], hexafluoropropylene [HFP], chlorotrifluoroethylene [CTFE], vinyl fluoride, vinylidene fluoride [VDF], trifluoroethylene, hexafluoroisobutylene.
- TFE tetrafluoroethylene
- HFP hexafluoropropylene
- CTFE chlorotrifluoroethylene
- VDF chlorotrifluoroethylene
- VDF chlorotrifluoroethylene
- VDF chlorotrifluoroethylene
- VDF chlorotrifluoroethylene
- VDF vinyl fluoride
- VDF vinylidene fluoride
- TFE hexafluoroisobutylene.
- Perfluorobutylethylene and the like TFE, VDF, CTFE, trifluoroethylene, vinyl fluoride and HFP are preferred, TFE, CTFE and HFP are more preferred, T
- the fluoropolymer electrolyte has a repeating unit ( ⁇ ) derived from a SO 3 Z group-containing monomer of 10 to 95 mol%, a repeating unit ( ⁇ ) derived from an ethylenic fluoromonomer of 5 to 90 mol%, and a repeating unit.
- a copolymer in which the sum of ( ⁇ ) and repeating units ( ⁇ ) is 95 to 100 mol% of the total monomer units is preferred.
- the repeating unit ( ⁇ ) derived from the SO 3 Z group-containing monomer has a more preferable lower limit of 15 mol%, a further preferable lower limit of 20 mol%, a more preferable upper limit of 60 mol%, and a still more preferable upper limit of 50 mol%. .
- the repeating unit ( ⁇ ) derived from the ethylenic fluoromonomer has a more preferred lower limit of 35 mol%, a still more preferred lower limit of 40 mol%, and a particularly preferred lower limit of 45 mol%.
- the lower limit of the repeating unit ( ⁇ ) is also preferably 50 mol%.
- a more preferred upper limit is 85 mol%, and a still more preferred upper limit is 80 mol%.
- the repeating unit ( ⁇ ) derived from a vinyl ether other than the SO 3 Z group-containing monomer is preferably 0 to 5 mol% as the repeating unit derived from the third component monomer other than the above. More preferably, it may be 4 mol% or less, more preferably 3 mol% or less.
- the polymer composition of the fluorine-based polymer electrolyte can be calculated from, for example, measured values of melt NMR at 300 ° C.
- the vinyl ether other than the SO 3 Z group-containing monomer that constitutes the repeating unit ( ⁇ ) is not particularly limited as long as it does not contain an SO 3 Z group.
- the hydrogen-containing vinyl ether etc. which are represented by these are mentioned.
- 1 type (s) or 2 or more types can be used.
- the electrolyte emulsion preferably contains 2 to 80% by mass (solid content concentration) of the fluorine-based polymer electrolyte. If the amount of the fluorine-based polymer electrolyte is too small, the amount of the aqueous medium increases, and the productivity may decrease when used for film formation. When there are too many fluorine-type polymer electrolytes, a viscosity will become high and handling will become difficult easily. A more preferable lower limit is 5% by mass, and a more preferable upper limit is 60% by mass.
- the aqueous medium may be water alone or, when good dispersibility of the electrolyte emulsion is desired, in addition to water, alcohols such as methanol, ethanol, n-propanol, and isopropanol; N— Nitrogen-containing solvents such as methylpyrrolidone [NMP]; ketones such as acetone; esters such as ethyl acetate; polar ethers such as diglyme and tetrahydrofuran [THF]; polar organic solvents such as carbonates such as diethylene carbonate Of these, one or two or more of them can be used in combination.
- alcohol for improving leveling property polyoxyethylene for improving film forming property Etc. can be used.
- the aqueous medium preferably has a water content of more than 50% by mass. If the water content is too low, the dispersibility tends to deteriorate, which is not preferable from the viewpoint of the environment and the human body.
- a more preferred lower limit is 60% by mass, and a still more preferred lower limit is 70% by mass, preferably 100% by mass.
- the aqueous medium is preferably composed of 70 to 100% by mass of water and 30 to 0% by mass of alcohol.
- the electrolyte emulsion of the present invention can be produced, for example, by the following method.
- an ethylenic fluoromonomer and a vinyl fluoride compound having a SO 2 Z 1 group (Z 1 represents a halogen element) are copolymerized at a polymerization temperature of 0 ° C. or more and 40 ° C.
- EW equivalent weight
- a fluorine-based polymer electrolyte having a low EW has a large amount of proton-exchangeable groups, so that the volume increase due to an organic solvent is significant, and a large amount of alkaline aqueous solution is required or a high concentration of alkali electrolyte is required. It has been found that productivity is lowered, such as requiring an aqueous solution. Moreover, the washing process after hydrolysis is also very complicated. These problems are not found until a polymer electrolyte having a low EW is produced.
- the method for producing an electrolyte emulsion of the present invention solves this problem by adding a basic reaction liquid to the precursor emulsion in the above step (2), and is a fluorine-based polymer having a low EW simply under mild conditions. It has been found that an electrolyte emulsion in which a molecular electrolyte is dispersed can be efficiently produced.
- the above production method is also excellent in productivity because it does not require a step of redispersing or dissolving the electrolyte once coagulated by a complicated operation such as stirring sufficiently while heating.
- the fluoropolymer electrolyte precursor contained in the precursor emulsion obtained in the step (1) is preferably spherical particles having an average particle size of 10 to 500 nm.
- the production method does not include an operation of aggregating particles in the emulsion such as coagulation and drying. Once the particles are aggregated, it is impossible to finally obtain an electrolyte emulsion in which spherical particles having an average particle diameter of 10 to 500 nm are dispersed.
- the fluorine-based polymer electrolyte precursor is subjected to chemical treatment to SO 3 Z (Z represents an alkali metal, an alkaline earth metal, hydrogen, or NR 1 R 2 R 3 R 4.
- R 1 , R 2 , R 3 And R 4 each independently represents an alkyl group having 1 to 3 carbon atoms or a group that can be converted to hydrogen.
- SO 3 Z represents an alkali metal, an alkaline earth metal, hydrogen, or NR 1 R 2 R 3 R 4 by chemical treatment with an ethylenic fluoromonomer.
- R 1 , R 2 , R 3 and R 4 each independently represents a vinyl fluoride compound having an SO 2 Z 1 group (Z 1 represents a halogen element) converted to an alkyl group having 1 to 3 carbon atoms or hydrogen.
- Z 1 represents a halogen element
- Y 1 represents F, Cl or a perfluoroalkyl group
- k represents an integer of 0 to 2
- l represents 0 or 1
- n represents an integer of 0 to 8
- n Y 1 represents Y 2 represents F or Cl
- m represents an integer of 0 to 6.
- a 2 represents SO 2 Z 1
- Z 1 is fluorinated vinyl compound represented by the representative.
- a halogen element are preferred.
- k is preferably 0 and l is preferably 1 from the viewpoint of the synthesis surface and operability.
- n is more preferably 0 or 1
- n is more preferably 0.
- Y 2 is an F
- m is more preferably an integer of 2 ⁇ 6
- Y 2 is an F
- more preferably m is 2 or 4
- Y 2 is an F
- Y 1 is preferably F.
- the said vinyl fluoride compound can be used 1 type or in combination of 2 or more types.
- ethylenic fluoromonomer examples include those described above.
- a third component monomer other than the ethylenic fluoromonomer and the vinyl fluoride compound may be polymerized if desired.
- an aqueous solution of a surfactant is used as a polymerization solvent to finally obtain spherical polymer particles having an average particle diameter of 10 to 500 nm as a polymerization solvent.
- the method must be a method (emulsion polymerization) in which polymerization is carried out by reacting a vinyl fluoride compound and an ethylenic fluoromonomer gas.
- emulsion polymerization In solution polymerization, bulk polymerization, and suspension polymerization, it is impossible to obtain a fluorinated polymer electrolyte as spherical particles having an average particle diameter of 10 to 500 nm.
- EW equivalent weight
- the emulsion polymerization is a method in which an aqueous solution of a co-emulsifier such as a surfactant and alcohol is used, and the polymerization is carried out by reacting a vinyl fluoride compound and an ethylenic fluoromonomer gas in a state where the aqueous solution is filled and emulsified (Mini Emulsion polymerization or microemulsion polymerization). Miniemulsion polymerization and microemulsion polymerization can increase the apparent polymerization rate.
- a co-emulsifier such as a surfactant and alcohol
- the ethylenic fluoromonomer and the vinyl fluoride compound are preferably copolymerized at a polymerization temperature of 0 ° C. or higher and 40 ° C. or lower.
- a process (1) is what obtains a fluorine-type polymer electrolyte precursor emulsion by emulsion polymerization at the polymerization temperature of 0 to 40 degreeC.
- the polymerization temperature is more preferably 5 ° C. or higher, and more preferably 35 ° C. or lower.
- the emulsion polymerization is a method in which a vinyl fluoride compound and a gaseous ethylenic fluoromonomer are radically copolymerized by radicals generated from a polymerization initiator in a surfactant aqueous solution prepared in a pressure vessel.
- the vinyl fluoride compound may be obtained by filling and emulsifying a strong shearing force together with a surfactant and an auxiliary emulsifier such as alcohol.
- the pressure is preferably ⁇ 0.05 MPaG or more and 2.0 MPaG or less.
- the pressure (MPaG) is a pressure gauge value (gauge pressure) with the atmospheric pressure set to 0 MPa.
- a more preferred lower limit is 0.0 MPaG, and a more preferred lower limit is 0.1 MPaG.
- a more preferable upper limit is 1.0 MPaG, and a further preferable upper limit is 0.7 MPaG.
- the gaseous ethylenic fluoromonomer is usually consumed by the progress of the polymerization reaction and the pressure decreases, it is preferable to add the gaseous ethylenic fluoromonomer as appropriate.
- a method of additionally supplying a vinyl fluoride compound that is consumed at the same time is also preferably used.
- the added vinyl fluoride compound may be one obtained by filling and emulsifying a strong shearing force together with a surfactant and an auxiliary emulsifier such as alcohol.
- the vinyl fluoride compound is liquid, a method of press-fitting with a metering pump, a method of press-fitting with an inert gas or the like, and the like are used.
- the fluorine-based polymer electrolyte precursor is preferably melt-flowable.
- a melt flow rate (hereinafter abbreviated as “MFR”) can be used as an index of the degree of polymerization of the fluorine-based polymer electrolyte precursor.
- MFR of the fluoropolymer electrolyte precursor is preferably 0.01 (g / 10 min) or more, more preferably 0.1 (g / 10 min) or more, and 0.3 (g / 10 min). The above is more preferable.
- the upper limit of MFR is preferably 100 (g / 10 min) or less, more preferably 20 (g / 10 min) or less, still more preferably 16 (g / 10 min) or less, and particularly preferably 10 (g / 10 min) or less. If the MFR is smaller than 0.01 (g / 10 min), there is a possibility that molding processing such as film formation will be defective. On the other hand, if the MFR is larger than 100 (g / 10 min), the strength of the film obtained by molding this may be reduced, and the durability when used in a fuel cell may also be reduced.
- MFR 0.01 (g / 10 min) or more and 100 (g / 10 min) or less it is preferable to carry out emulsion polymerization at a temperature of 0 ° C. or more and 40 ° C. or less. If the temperature is higher than 40 ° C., the rate of disproportionation reaction in which the radical at the polymer terminal undergoes ⁇ -rearrangement and the polymerization is stopped increases, and a polymer having a high molecular weight may not be obtained. More preferably, it is 35 degrees C or less, More preferably, it is 30 degrees C or less. On the other hand, when the temperature is lower than 0 ° C., the polymerization becomes very slow, and the productivity may be extremely deteriorated. More preferably, it is 5 degreeC or more, More preferably, it is 10 degreeC or more.
- the polymerization initiator used in step (1) is preferably water-soluble, for example, inorganic peroxides such as persulfuric acid compounds, perboric acid compounds, perchloric acid compounds, perphosphoric acid compounds, percarbonate compounds; And organic peroxides such as succinyl peroxide, t-butyl permaleate, t-butyl hydroperoxide, and the like.
- the inorganic peroxide may be, for example, an ammonium salt, a sodium salt, a potassium salt, or the like.
- a so-called redox initiator in which the water-soluble polymerization initiator and a reducing agent are combined is also preferably used.
- the reducing agent include salts of low-order ions such as sulfite, bisulfite, iron, copper, and cobalt, hypophosphorous acid, hypophosphite, N, N, N ′, N′-tetramethyl
- examples thereof include organic amines such as ethylenediamine, and reducing sugars such as aldose and ketose.
- the polymerization temperature is 30 ° C. or lower, it is preferable to use a redox initiator.
- An azo compound is also the most preferred initiator in the present invention.
- 2,2′-azobis-2-methylpropionamidine hydrochloride, 2,2′-azobis-2,4-dimethylvaleronitrile, 2,2′-azobis- N, N'-dimethyleneisobutylamidine hydrochloride, 2,2'-azobis-2-methyl-N- (2-hydroxyethyl) -propionamide, 2,2'-azobis-2- (2-imidazoline-2 -Yl) -propane and salts thereof, 4,4′-azobis-4-cyanovaleric acid and salts thereof, and the like can be used.
- two or more kinds of the above polymerization initiators can be used in combination.
- the amount of the polymerization initiator is generally 0.001 to 5% by mass with respect to the monomer.
- the polymerization initiator may be charged into the pressure vessel before introducing the ethylenic fluoromonomer, or may be injected as an aqueous solution after introducing the ethylenic fluoromonomer.
- the method of carrying out the additional addition of the polymerization initiator and / or a reducing agent sequentially one by one is preferable.
- the emulsifier that can be used in the step (1) is not particularly limited, but an emulsifier having a low chain transfer property is preferably used.
- an emulsifier represented by RfZ 3 is used.
- Rf is an alkyl group having 4 to 20 carbon atoms, part or all of the hydrogen atoms are replaced with fluorine, may contain etheric oxygen, and can be copolymerized with an ethylenic fluoromonomer. It may have an unsaturated bond.
- Z 3 represents a dissociative polar group, and —COO — B + or —SO 3 — B + is preferably used.
- B + is an alkali metal ion or a monovalent cation such as an ammonium ion or a hydrogen ion.
- Examples of the emulsifier represented by RfZ 3 include Y (CF 2 ) n COO — B + (n represents an integer of 4 to 20, Y represents fluorine or hydrogen), CF 3 —OCF 2 CF 2. —OCF 2 CF 2 COO — B + , CF 3 — (OCF (CF 3 ) CF 2 ) n COO — B + (n represents an integer of 1 to 3) and the like.
- an emulsifier is not specifically limited, 0.01 mass% or more and 10 mass% or less are suitable as aqueous solution. As the emulsifier increases, the number of polymer particles increases, and the apparent polymerization rate tends to increase. If it is less than 0.01% by mass, the emulsified particles may not be stably maintained. When it is more than 10% by mass, cleaning in a subsequent process becomes difficult. A more preferable lower limit is 0.05% by mass, and a still more preferable lower limit is 0.1% by mass. A more preferable upper limit is 5% by mass, and a further preferable upper limit is 3% by mass.
- step (1) in order to increase the number of polymerized particles, so-called “seed polymerization” can be performed in which the dispersion obtained by polymerization using a large amount of emulsifier is diluted and the polymerization is continued.
- the polymerization time is not particularly limited, but is generally 1 to 48 hours.
- the polymerization pH is not particularly limited, but the polymerization may be carried out with pH adjustment as necessary.
- usable pH adjusting agents include alkalizing agents such as sodium hydroxide, potassium hydroxide and ammonia, mineral acids such as phosphoric acid, sulfuric acid and hydrochloric acid, and organic acids such as formic acid and acetic acid.
- a chain transfer agent can also be used for adjusting the molecular weight and molecular weight distribution.
- Preferable chain transfer agents include gaseous hydrocarbons such as ethane and pentane, water-soluble compounds such as methanol, iodine compounds and the like.
- iodine compounds are suitable in that a block polymer can be produced by so-called iodine transfer polymerization.
- the precursor emulsion preferably contains 2 to 80% by mass (solid content concentration) of the fluorine-based polymer electrolyte precursor.
- a more preferable lower limit is 5% by mass, and a more preferable upper limit is 60% by mass.
- the unstable terminal groups of the fluorine-based polymer electrolyte precursor in the precursor emulsion obtained by the step (1) are stabilized. It may be processed.
- the unstable terminal groups possessed by the fluorine-based polymer electrolyte precursor include carboxylic acids, carboxylates, carboxylic esters, carbonates, hydrocarbons, methylols, etc., and polymerization methods, initiators, chain transfer agents, polymerization terminators It depends on the type.
- the method for stabilizing the unstable terminal group of the fluorine-based polymer electrolyte precursor is not particularly limited, and examples thereof include a method for stabilizing by heating decarboxylation to -CF 2 H. it can.
- a fluorine-based polymer electrolyte is obtained by adding a basic reaction liquid to the precursor emulsion obtained in step (1) and chemically treating the fluorine-based polymer electrolyte precursor.
- a step (2) of obtaining a dispersed electrolyte emulsion In step (2), a basic reaction liquid is added to the precursor emulsion, and the fluorine polymer electrolyte precursor and the basic reaction liquid are brought into contact with each other, thereby chemically treating the fluorine polymer electrolyte precursor and subjecting the electrolyte to an electrolyte.
- the chemical treatment include hydrolysis treatment and acid treatment. The hydrolysis treatment can be performed by adding a basic reaction liquid to the precursor emulsion.
- the basic reaction liquid is not particularly limited, but an aqueous solution of an alkali metal or alkaline earth metal hydroxide such as sodium hydroxide or potassium hydroxide is preferred.
- the content of the alkali metal or alkaline earth metal hydroxide is not limited, but is preferably 10 to 30% by mass.
- the reaction liquid preferably contains a swellable organic compound such as methyl alcohol, ethyl alcohol, acetone, DMSO, DMAC, or DMF.
- the content of the swellable organic compound is preferably 1 to 50% by mass.
- the treatment temperature varies depending on the solvent type, solvent composition, etc., but the treatment time can be shortened as the treatment temperature is increased. If the treatment temperature is too high, the polymer electrolyte precursor may be dissolved.
- the treatment is preferably carried out at 20 to 160 ° C.
- the step (2) after the hydrolysis treatment, it is also preferable to obtain a protonated fluorine-based polymer electrolyte by washing with warm water or the like if necessary, and then acid treatment.
- the acid used for the acid treatment is not particularly limited as long as it is a mineral acid such as hydrochloric acid, sulfuric acid or nitric acid, or an organic acid such as oxalic acid, acetic acid, formic acid or trifluoroacetic acid.
- the acid treatment is also preferably for bringing the precursor emulsion or the hydrolyzed precursor emulsion into contact with a cation exchange resin.
- the acid treatment can be performed by passing the precursor emulsion or the precursor emulsion subjected to hydrolysis treatment through a container filled with a cation exchange resin.
- An electrolyte membrane comprising: a step of applying the electrolyte emulsion to a base material; a step of drying the electrolyte emulsion applied to the base material to obtain an electrolyte membrane; and a step of peeling the electrolyte membrane from the base material
- This manufacturing method is also one aspect of the present invention. According to the said manufacturing method, compared with the case where an electrolyte membrane is manufactured from electrolyte solution, an electrolyte membrane with a low moisture content can be manufactured.
- the manufacturing method of the above electrolyte membrane is a method called cast film formation.
- the electrolyte emulsion is developed in a container such as a petri dish, and the solvent is at least partially heated by heating in an oven or the like as necessary. After distilling off, there is a method of obtaining a film-like body by peeling off from the container.
- cast film is formed while controlling the film thickness with a device such as a blade coater, gravure coater or comma coater having a mechanism such as a blade, air knife or reverse roll so that the thickness of the electrolyte emulsion is uniform on a glass plate or film. And it can also be set as a sheet-fed coating film. Further, it can be continuously cast to form a continuous film to form a long film-like film.
- the film is not particularly limited, but includes polyethylene terephthalate (PET), polyethylene butaleate (PBT), polyethylene naphthalate (PEN) and polyesters including liquid crystal polyesters, triacetyl cellulose (TAC), polyarylate, polyether, Polycarbonate (PC), polysulfone, polyethersulfone, cellophane, aromatic polyamide, polyvinyl alcohol, polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polystyrene (PS), acrylonitrile-butadiene-styrene copolymer ( ABS), polymethyl methacrylate (PMMA), polyamide, polyacetal (POM), polyphenylene terephthalate (PPE), polybutylene terephthalate (PBT), polyphenylene sulfide (PPS), polyamideimide (PAI), polyetheramide (PEI), polyetheretherketone (PEEK), polyimide (PI), polymethylpentene (PMP),
- Said electrolyte membrane can be manufactured by the above-mentioned cast film forming method.
- the electrolyte membrane obtained by the above production method is also one aspect of the present invention.
- the thickness of the electrolyte membrane is preferably 1 ⁇ m or more and 500 ⁇ m or less, more preferably 2 ⁇ m or more and 100 ⁇ m or less, and even more preferably 5 ⁇ m or more and 50 ⁇ m or less. If the film thickness is thin, the direct current resistance during power generation can be reduced, while the gas permeation amount may be increased. Therefore, the appropriate range as described above is desirable. Further, it has a porous membrane obtained by stretching a PTFE membrane as described in JP-A-8-162132, and fibrillated fibers described in JP-A-53-149881 and JP-B-63-61337. There may be.
- the electrolyte emulsion of this invention can also be used as the electrolyte binder in an electrode catalyst layer.
- the electrode catalyst layer made of the above electrolyte emulsion is also one aspect of the present invention.
- the electrode catalyst layer is formed by applying and drying an electrode ink (electrode catalyst composition) prepared by adding and mixing an electrode catalyst such as Pt-supported carbon to the fluorine-based polymer electrolyte emulsion of the present invention. It is preferable to obtain.
- the amount of the fluorine-based polymer electrolyte supported with respect to the electrode area is preferably 0.001 to 10 mg / cm 2 , more preferably 0.01 to 5 mg / cm 2 , and still more preferably 0 in the state where the electrode catalyst layer is formed. .1 to 1 mg / cm 2 .
- the electrode catalyst layer is composed of composite particles composed of fine particles of catalyst metal and a conductive agent carrying the catalyst metal, and a polymer electrolyte as a binder, and a water repellent is included as necessary.
- the catalyst metal used for the electrode may be any metal that promotes the oxidation reaction of hydrogen and the reduction reaction of oxygen, such as platinum, gold, silver, palladium, iridium, rhodium, ruthenium, iron, cobalt, nickel, chromium, It is preferably at least one metal selected from the group consisting of tungsten, manganese, vanadium, and alloys thereof, in which platinum is mainly used.
- the conductive agent is not limited as long as it is conductive particles (conductive particles), but is selected from the group consisting of carbon black such as furnace black, channel black, and acetylene black, activated carbon, graphite, and various metals. It is preferable that it is at least 1 type of electroconductive particle.
- the particle size of these conductive agents is preferably 10 angstroms to 10 ⁇ m, more preferably 50 angstroms to 1 ⁇ m, and most preferably 100 to 5000 angstroms.
- the particle diameter of the catalytic metal fine particles (electrode catalyst particles) is not limited, but is preferably 10 to 1000 angstroms, more preferably 10 to 500 angstroms, and most preferably 15 to 100 angstroms.
- the electrocatalyst particles are preferably 1 to 99% by mass, more preferably 10 to 90% by mass, and most preferably 30 to 70% by mass with respect to the conductive particles.
- Pt catalyst-supporting carbon such as TEC10E40E manufactured by Tanaka Kikinzoku Kogyo Co., Ltd. is a suitable example.
- the content of the composite particles is 20 to 95% by mass, preferably 40 to 90% by mass, more preferably 50 to 85% by mass, and most preferably 60 to 80% by mass with respect to the total mass of the electrode catalyst layer. is there.
- the supported amount of the electrode catalyst with respect to the electrode area is preferably 0.001 to 10 mg / cm 2 , more preferably 0.01 to 5 mg / cm 2 , and most preferably 0.1 to 10 mg / cm 2 in a state where the electrode catalyst layer is formed. 1 mg / cm 2 .
- the thickness of the electrode catalyst layer is preferably 0.01 to 200 ⁇ m, more preferably 0.1 to 100 ⁇ m, and most preferably 1 to 50 ⁇ m.
- the porosity of the electrode catalyst layer is not particularly limited, but is preferably 10 to 90% by volume, more preferably 20 to 80% by volume, and most preferably 30 to 60% by volume.
- the electrode catalyst layer of the present invention may further contain polytetrafluoroethylene (hereinafter referred to as PTFE).
- PTFE polytetrafluoroethylene
- the shape of PTFE is not particularly limited, but may be any shape as long as it is regular, preferably in the form of particles or fibers, and these may be used alone or in combination. .
- the PTFE content is preferably 0.001 to 20% by mass, more preferably 0.01 to 10% by mass, and most preferably the total mass of the electrode catalyst layer. 0.1 to 5% by mass.
- the electrode catalyst layer of the present invention may further contain a metal oxide.
- the metal oxide is not particularly limited, but Al 2 O 3 , B 2 O 3 , MgO, SiO 2 , SnO 2 , TiO 2 , V 2 O 5 , WO 3 , Y 2 O 3 , ZrO 2 It is preferably at least one metal oxide selected from the group consisting of Zr 2 O 3 and ZrSiO 4 . Among these, at least one metal oxide selected from the group consisting of Al 2 O 3 , SiO 2 , TiO 2 and ZrO 2 is preferable, and SiO 2 is particularly preferable.
- the content of the metal oxide is preferably 0.001 to 20% by mass, more preferably based on the total mass of the electrode catalyst layer. Is from 0.01 to 10% by weight, most preferably from 0.1 to 5% by weight.
- the metal oxide may be in the form of particles or fibers, but it is particularly desirable that the metal oxide be amorphous.
- amorphous as used herein means that no particulate or fibrous metal oxide is observed even when observed with an optical microscope or an electron microscope. In particular, even when the electrode catalyst layer is magnified up to several hundred thousand times using a scanning electron microscope (SEM), no particulate or fibrous metal oxide is observed.
- the present invention includes a step of preparing an electrode catalyst composition in which composite particles composed of a catalyst metal and a conductive agent are dispersed in the electrolyte emulsion, a step of applying the electrode catalyst composition to a substrate, and a method of applying to the substrate. And a step of obtaining an electrode catalyst layer by drying the electrode catalyst composition.
- the present invention is also an electrode catalyst layer obtained by this production method.
- an electrolyte emulsion is prepared, and an electrode catalyst composition in which the composite particles are dispersed in this electrolyte emulsion is prepared, and this is applied to a polymer electrolyte membrane or another substrate such as a PTFE sheet. After being coated on top, it can be dried and solidified.
- the electrode catalyst composition can be applied by various generally known methods such as a screen printing method and a spray method.
- the electrode catalyst composition includes a fluorine-based polymer electrolyte, composite particles, and an aqueous medium.
- the electrode catalyst composition may be used after further adding a solvent as necessary.
- Solvents that can be used include water, alcohols (ethanol, 2-propanol, ethylene glycol, glycerin, etc.), chlorofluorocarbon and other single solvents or composite solvents.
- the amount of the solvent added is preferably 0.1 to 90% by mass, more preferably 1 to 50% by mass, and most preferably 5 to 20% by mass with respect to the total mass of the electrode catalyst composition. Is desirable.
- a gas diffusion electrode such as ELAT (registered trademark) manufactured by BASF in which a gas diffusion layer and an electrode catalyst layer are laminated
- ELAT registered trademark
- the electrode catalyst layer may be immersed in an inorganic acid such as hydrochloric acid after the electrode catalyst layer is produced.
- the acid treatment temperature is preferably 5 to 90 ° C., more preferably 10 to 70 ° C., and most preferably 20 to 50 ° C.
- a unit in which two types of electrode catalyst layers of an anode and a cathode are bonded to both surfaces of an electrolyte membrane is called a membrane electrode assembly (hereinafter sometimes abbreviated as “MEA”).
- MEA membrane electrode assembly
- a membrane electrode assembly including the electrolyte membrane of the present invention is also one aspect of the present invention.
- the membrane electrode assembly provided with the electrode catalyst layer of the present invention is also one aspect of the present invention.
- a material in which a pair of gas diffusion layers are bonded to the outer side of the electrode catalyst layer so as to face each other is sometimes referred to as MEA.
- the bipolar plate means a composite material of graphite and resin having a groove for flowing a gas such as fuel or oxidant on its surface, or a metal plate.
- the bipolar plate has a function of a flow path for supplying fuel and oxidant to the vicinity of the electrode catalyst.
- a fuel cell is manufactured by inserting and stacking a plurality of MEAs between such bipolar plates.
- the electrolyte emulsion of the present invention is prepared by adding an organic solvent to prepare an electrolyte solution in which the fluoropolymer electrolyte is dissolved, applying the electrolyte solution to a substrate, and drying the electrolyte solution applied to the substrate.
- An electrolyte membrane can also be obtained by forming an electrolyte membrane and peeling the electrolyte membrane from the substrate.
- the polymer electrolyte solution is prepared and then the electrolyte membrane or electrode catalyst layer is produced, a method called cast film formation can be used.
- the polymer electrolyte solution is developed in a container such as a petri dish, and if necessary, There is a method of obtaining a film-like body by, for example, removing the solvent at least partially by heating in an oven or the like and then removing it from the container.
- the polymer electrolyte solution is cast on a glass plate or film while controlling the film thickness with a device such as a blade coater, gravure coater or comma coater having a mechanism such as a blade, air knife or reverse roll so that the thickness is uniform. It is also possible to form a single wafer coating film. Further, it can be continuously cast to form a continuous film to form a long film-like film.
- the film is not particularly limited, but includes polyethylene terephthalate (PET), polyethylene butaleate (PBT), polyethylene naphthalate (PEN) and polyesters including liquid crystal polyesters, triacetyl cellulose (TAC), polyarylate, polyether, Polycarbonate (PC), polysulfone, polyethersulfone, cellophane, aromatic polyamide, polyvinyl alcohol, polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polystyrene (PS), acrylonitrile-butadiene-styrene copolymer ( ABS), polymethyl methacrylate (PMMA), polyamide, polyacetal (POM), polyphenylene terephthalate (PPE), polybutylene terephthalate (PBT), polyphenylene sulfide (PPS), polyamideimide (PAI), polyetheramide (PEI), polyetheretherketone (PEEK), polyimide (PI), polymethylpentene (PMP),
- organic solvent examples include protic organic solvents such as methanol, ethanol, n-propanol, isopropyl alcohol, butanol, and glycerin, and non-protons such as N, N-dimethylformamide, N, N-dimethylacetamide, and N-methylpyrrolidone.
- protic organic solvents such as methanol, ethanol, n-propanol, isopropyl alcohol, butanol, and glycerin
- non-protons such as N, N-dimethylformamide, N, N-dimethylacetamide, and N-methylpyrrolidone.
- An organic solvent can be used alone or in combination of two or more.
- the dissolution method is not particularly limited. For example, first, for example, a mixed solvent of water and a protic organic solvent is added to the electrolyte emulsion under such a condition that the total solid concentration is 1 to 50% by mass. Next, the composition is placed in an autoclave having a glass inner cylinder as necessary, and the air inside is replaced with an inert gas such as nitrogen. Heat and stir for ⁇ 12 hours. Thereby, an electrolyte solution is obtained. The higher the total solid content concentration, the better from the viewpoint of yield. However, if the concentration is increased, undissolved substances may be formed, so 1 to 50% by mass is preferable, more preferably 3 to 40% by mass, and still more preferably 5%. ⁇ 30% by mass.
- the composition ratio of water and the protic organic solvent in the obtained electrolyte solution depends on the dissolution method, dissolution conditions, type of polymer electrolyte, total solid content concentration, dissolution temperature, stirring speed, etc. Although it can be appropriately selected, 10 to 1000 parts by mass of the protic organic solvent is preferable with respect to 100 parts by mass of water, and particularly preferably 10 to 500 parts by mass of the organic solvent with respect to 100 parts by mass of water.
- emulsion liquid particles are dispersed in the liquid as colloid particles or coarser particles to form a milky state
- suspension solid particles in the liquid are colloidal particles or microscope
- colloidal liquid a state in which macromolecules are dispersed
- micellar liquid a lyophilic colloidal dispersion system formed by the association of many small molecules by intermolecular force
- the electrolyte solution can be concentrated.
- the concentration method is not particularly limited. For example, there are a method of heating and evaporating the solvent, a method of concentrating under reduced pressure and the like. If the resulting coating solution has a solid content ratio that is too high, the viscosity may increase and it may be difficult to handle, and if it is too low, the productivity may decrease.
- the fraction is preferably 0.5 to 50% by mass.
- the electrolyte solution is more preferably filtered from the viewpoint of removing coarse particle components.
- the filtration method is not particularly limited, and a general method conventionally performed can be applied. For example, a method of pressure filtration using a filter obtained by processing a filter medium having a normally used rated filtration accuracy is typically mentioned.
- the filter it is preferable to use a filter medium whose 90% collection particle size is 10 to 100 times the average particle size of the particles.
- the filter medium may be filter paper or a filter medium such as a sintered metal filter. Particularly in the case of filter paper, the 90% collection particle size is preferably 10 to 50 times the average particle size of the particles. In the case of a sintered metal filter, the 90% collection particle size is preferably 50 to 100 times the average particle size of the particles.
- Setting the 90% collection particle size to be 10 times or more of the average particle size prevents the pressure necessary for liquid feeding from becoming too high, or the filter is blocked in a short period of time. Can be suppressed.
- setting it to 100 times or less of the average particle diameter is preferable from the viewpoint of satisfactorily removing particle agglomerates and resin undissolved materials that cause foreign matters in the film.
- the evaluation method and measurement method used in this embodiment are as follows.
- the polymer electrolyte membranes were stacked so as to have a thickness of about 0.25 mm, and set in a small-angle X-ray cell capable of humidity control. After maintaining at 25 ° C. and 50% RH for 30 minutes, X-rays were incident on this and scattering was measured. Measurement conditions were an X-ray wavelength of ⁇ 0.154 nm, a camera length of 515 mm, and an imaging plate was used as a detector. The two-dimensional scattering pattern obtained by the imaging plate was subjected to an empty cell scattering correction and a background correction derived from the detector, and then a circular average was performed to obtain a one-dimensional scattering profile.
- H (H2 ⁇ H1) / ( ⁇ 2 ⁇ 1) ⁇ (0.1 ⁇ 1) + H1 (3)
- H2 and ⁇ 2 are the relative humidity and conductivity at the first measurement point where the conductivity exceeds 0.10 S / cm, respectively, and H1 and ⁇ 1 are the highest that the conductivity does not exceed 0.10 S / cm, respectively. Relative humidity and conductivity.
- MFR Melt flow rate
- the polymer composition was calculated from the measured value of melt NMR at 300 ° C.
- NMR a Bruker Fourier transform nuclear magnetic resonance apparatus (FT-NMR) AC300P was used.
- FT-NMR Bruker Fourier transform nuclear magnetic resonance apparatus
- the average particle diameter and aspect ratio were obtained by observing the aggregate of the fluorine-based polymer electrolyte obtained by applying the electrolyte emulsion to aluminum foil or the like with a scanning young electron microscope or the like and then removing the aqueous medium.
- the average ratio of the major axis and minor axis length (major axis / minor axis) measured for 20 or more particles on the image is the aspect ratio, and the average value of the major axis and minor axis length is the average particle diameter.
- the weight of the dried room temperature weighing bottle was precisely weighed, and this was designated as W0. 10 g of the measurement object was put in the measured weighing bottle and precisely weighed to obtain W1.
- the weighing bottle containing the measurement object was dried for 3 hours or more at a temperature of 110 ° C. and an absolute pressure of 0.01 MPa or less using an LV-120 type vacuum dryer manufactured by Espec Co., Ltd., and then cooled in a desiccator containing silica gel to room temperature. After that, it was precisely weighed and set to W2. (W2-W0) / (W1-W0) was expressed as a percentage, measured five times, and the average value was defined as the solid content concentration.
- the polymer electrolyte membrane produced with a thickness of about 50 ⁇ m is stored in a constant temperature and humidity chamber adjusted to 23 ° C. and 50% RH for 1 hour, and then cut into a size of 3 cm in length and 4 cm in width.
- a polytetrafluoroethylene mesh or the like may be superimposed and immersed on the polymer electrolyte membrane so that the polymer electrolyte membrane does not float.
- the polymer electrolyte membrane is taken out of the water, and the water adhering to the surface is wiped off using Whatman filter paper (Cat No. 1441 125).
- the weight MW of the polymer electrolyte membrane with water is measured to a unit of 0.0001 g using an electronic balance GR-202 manufactured by A & D.
- weight measurement is performed within 10 seconds after the membrane is taken out of water.
- the polymer electrolyte membrane is dried at 160 ° C. for 1 hour using a hot air dryer SPH-101 manufactured by ESPEC CORP., And the polymer electrolyte membrane weight MD at the time of drying is measured using the electronic balance. (MW-MD) / MD was expressed as a percentage, and the value was defined as a water content at 25 ° C.
- the solid content concentration of the obtained precursor emulsion was 24.0% by mass.
- 250 g of water was added to 200 g, and nitric acid was added to cause coagulation. After filtering the coagulated polymer, water re-dispersion and filtration were repeated three times, followed by drying in a hot air dryer at 90 ° C. for 24 hours, and subsequently at 120 ° C. for 5 hours. 44.3 g of polymer (fluorine electrolyte precursor) )
- the obtained polymer had an MFR of 0.4 g / 10 min.
- Ultrafiltration is performed while adding an amount of purified water corresponding to the removed filtrate as appropriate to a beaker, and when the electrical conductivity of the filtrate reaches 10 ⁇ S ⁇ cm ⁇ 1 , the addition of pure water is stopped, When 1 L was reached, ultrafiltration was stopped to obtain an aqueous dispersion A.
- a Twin Cond B-173 electrical conductivity meter manufactured by HORIBA, Ltd. was used for the measurement of electrical conductivity. The ultrafiltration treatment time was 5 hours.
- the acid type aqueous dispersion B obtained in the film formation (1.3.2) was spread on a glass petri dish, and 30 ° C. at 80 ° C. using a Neo Hot Plate HI-1000 manufactured by AS ONE Co., Ltd. The solvent was removed by heating and drying for 1 minute. Further, heat treatment was performed at 160 ° C. for 1 hour. Then, it immersed in 25 degreeC ion-exchange water, and peeled from the glass petri dish, and obtained the fluorine-type polymer electrolyte membrane with a film thickness of about 50 micrometers. No wrinkles were observed in the obtained electrolyte membrane. The EW of this fluoropolymer electrolyte membrane was 455.
- Ionic conductivity, intercluster distance, and the fluorine-based polymer electrolyte membrane obtained at 80 ° C. water content (1.4) has a distance between ion clusters of 2.3 nm and an ionic conductivity of 110 ° C. It was 0.10 S / cm at 25% RH and 0.20 S / cm at 110 ° C. and 50% RH. Further, the water content at 25 ° C. was 160%, which was a low water content as compared with the electrolyte membrane of Comparative Example 1 prepared from the fluorine-based polymer electrolyte solution.
- Electrode Catalyst Layer 1 As an electrocatalyst layer, a platinum-supported catalyst TEC10E40E (platinum support rate 40 wt%) manufactured by Tanaka Kikinzoku Kogyo Co., Ltd. was used in 0.4 g, and a fluorine-based polymer electrolyte having an EW of 720 was used. 0.825 g of an electrolyte solution (trade name “SS700C / 20”, manufactured by Asahi Kasei E-Materials Co., Ltd., polymer weight ratio 20.0 wt%, solvent: water) and 8.175 g of ethanol are added, mixed and stirred to obtain an ink.
- an electrolyte solution trade name “SS700C / 20”, manufactured by Asahi Kasei E-Materials Co., Ltd., polymer weight ratio 20.0 wt%, solvent: water
- Electrode Catalyst Layer 2 As the electrocatalyst layer, the platinum supported catalyst TEC10E40E (platinum supported rate 40 wt%) manufactured by Tanaka Kikinzoku Kogyo Co., Ltd. was obtained at (1.3.2).
- a liquid obtained by diluting the acid type aqueous dispersion B with ion-exchanged water and ethanol (polymer weight ratio 5.5 wt%, solvent composition (mass ratio): ethanol / water 50/50) 3.0 g and ethanol 6.0 g
- Amount of platinum supported of the electrode catalyst layer is 0.17 mg / cm 2 at the anode electrode, the cathode electrode is 0.32 mg / cm 2.
- Fuel cell evaluation (MEA1) Using the MEA 1 produced in (1.8), the fuel cell evaluation was performed as described above. As a result, the current density after holding at a voltage of 0.6 V for 20 hours under the conditions of a cell temperature of 80 ° C. and a saturated water vapor pressure of 50 ° C. (corresponding to a humidity of 26% RH) is 0.57 A / cm 2 , which is high. Current density is shown. (1.11) Fuel cell evaluation (MEA2) Using the MEA2 produced in (1.9), the fuel cell evaluation was performed as described above.
- the current density after holding for 20 hours at a voltage of 0.6 V under conditions of saturated water vapor pressure (corresponding to a humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. is 0.49 A / cm 2 , which is high. Current density is shown.
- the treatment of immersing in a 2N hydrochloric acid aqueous solution at 60 ° C. for 1 hour was repeated 5 times by updating the aqueous hydrochloric acid solution every time, and then ion-exchanged water was added and left for 5 hours so that the fluorinated polymer electrolyte did not collapse.
- the operation of removing the supernatant was repeated until the pH of the wastewater reached 5 or higher.
- the fluorine-based polymer electrolyte absorbed about 28.0 times the weight of ion-exchanged water with respect to the dry weight of the fluorine-based electrolyte precursor, and the volume increased significantly.
- the fluorine-based electrolyte treated as described above was carefully collected and then dried to obtain a fluorine-based polymer electrolyte.
- a cast solution having a solid content concentration of 20% by mass obtained by concentrating the fluoropolymer solution under reduced pressure at 80 ° C. was cast on a tetrafluoroethylene film using a doctor blade.
- the solvent is removed by drying at 80 ° C. for 30 minutes, and heat treatment is further performed at 160 ° C. for 1 hour, and a fluorine-based polymer electrolyte having a film thickness of about 50 ⁇ m.
- a membrane was obtained.
- the EW of this fluoropolymer electrolyte membrane was 455, and the distance between ion clusters was 2.3 nm.
- the ionic conductivity was 0.10 S / cm at 110 ° C. and 25% RH, and 0.20 S / cm at 110 ° C. and 50% RH.
- the water content at 25 ° C. was 180%.
- An MEA was prepared and evaluated for a fuel cell in the same manner as in (1.8) of Example 1 except that the fluorine-based polymer electrolyte membrane was used.
- the current density after holding at a voltage of 0.6 V for 20 hours under the conditions of a cell temperature of 80 ° C. and a saturated water vapor pressure (corresponding to a humidity of 26% RH) at 50 ° C. was 0.57 A / cm 2 . .
- An electrode catalyst layer was prepared in the same manner as in (1.7) of Example 1 except that 0.825 g of the fluorine-based polymer electrolyte solution and 8.175 g of ethanol were used instead of the acid type aqueous dispersion B.
- An MEA was produced and evaluated for a fuel cell in the same manner as (1.9) in Example 1 except that this electrode catalyst layer was used.
- the current density after holding for 20 hours at a voltage of 0.6 V under conditions of saturated water vapor pressure (corresponding to a humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. was 0.46 A / cm 2 .
- a high current density was not obtained.
- a fluorine-based electrolyte containing a repeating unit derived from CF 2 ⁇ CF 2 and CF 2 ⁇ CF—O— (CF 2 ) 2 —SO 3 H and having an EW of 720 was produced as follows.
- the gaseous halogenating agent in the reactor is evacuated and evacuated, the gaseous halogenating agent obtained by diluting F 2 gas with nitrogen gas to 20% by mass is introduced until the gauge pressure reaches 0.0 MPaG. And held for 3 hours.
- MFR of the obtained polymer was 3.0 g / 10 minutes, and the repeating unit of the SO 3 H group-containing monomer was 18 mol%.
- a fluorinated polymer electrolyte solution and a fluorinated polymer electrolyte membrane were prepared in the same manner as in Comparative Example 1 except that this fluorinated polymer electrolyte was used, and EW measurement, distance between ion clusters and conductivity measurement were performed. .
- the EW was 720 and the distance between the ion clusters was 3.1 nm. It was 0.06 S / cm at 110 ° C. and 50% RH, and the target high conductivity was not obtained.
- An MEA was produced in the same manner as (1.10) of Example 1 except that the above-described fluorine-based polymer electrolyte membrane was used, and a fuel cell evaluation was performed.
- the current density after holding for 20 hours at a voltage of 0.6 V under conditions of saturated water vapor pressure (corresponding to humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. is 0.25 A / cm 2 , which is high. No current density was obtained.
- an electrode catalyst layer and an MEA were prepared by the same method as (1.11) of Example 1 except that the above-described fluorine-based polymer electrolyte solution was used, and a fuel cell was evaluated.
- the current density after holding for 20 hours at a voltage of 0.6 V under conditions of saturated water vapor pressure (corresponding to humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. is 0.25 A / cm 2 , which is high. No current density was obtained.
- Example 2 A fluorine-based polymer electrolyte emulsion containing a repeating unit derived from CF 2 ⁇ CF 2 and CF 2 ⁇ CF—O— (CF 2 ) 2 —SO 3 H and having an EW of 399 is expressed as CF 2 ⁇ CFOCF 2 CF 2 SO It was prepared in the same manner as in Example 1 except that 1300 g was used instead of 2 F 1150 g, and TFE was added to continue the polymerization so that the internal pressure was maintained at 0.02 MPaG.
- a fluorine-based polymer electrolyte membrane and an electrode catalyst layer were produced.
- the EW of the fluoropolymer electrolyte membrane is 399, the distance between ion clusters is 2.3 nm, and the ionic conductivity is 0.10 S / cm at 110 ° C. and 23% RH, and 0.22 S / cm at 110 ° C. and 50% RH. cm.
- the water content at 25 ° C. was 210%.
- Amount of platinum supported electrocatalyst layer is 0.17 mg / cm 2 at the anode electrode, the cathode electrode was 0.32 mg / cm 2.
- Example (1.11) In the fuel cell evaluation conducted in the same manner as (1.10) in Example 1 except that the above electrolyte membrane was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to humidity 26% RH) at 50 ° C. The current density after holding for 20 hours at a voltage of 0.6 V was 0.61 A / cm 2 . Further, in the fuel cell evaluation conducted in the same manner as in Example (1.11) except that the above electrode catalyst layer was used, the conditions were a saturated water vapor pressure (corresponding to a humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. The current density after holding at a voltage of 0.6 V for 20 hours was 0.51 A / cm 2 .
- Example 3 A fluorine-based electrolyte emulsion containing repeating units derived from CF 2 ⁇ CF 2 and CF 2 ⁇ CF—O— (CF 2 ) 2 —SO 3 H and having an EW of 470 (MFR of 1.8) The temperature was adjusted to 17.5 ° C., and TFE was added in the same manner as in Example 1 except that TFE was added to maintain the internal pressure at 0.09 MPaG and polymerization was continued. 9 hours after the start of the polymerization, when 401 g of TFE was additionally introduced, the TFE was released and the polymerization was stopped to obtain 4664 g of a polymerization solution (precursor emulsion).
- the MFR of the precursor polymer obtained in the same manner as in Example 1 was 1.8 g / 10 minutes.
- the repeating unit of the SO 3 H group-containing monomer of the fluorine-based polymer electrolyte in the fluorine-based polymer electrolyte emulsion was 34.2 mol%.
- the average particle diameter of the fluorine-based polymer electrolyte was 35 nm, and the aspect ratio was 1.0.
- (SO 2 F group number) / (SO 3 Z group number) was 0.
- a fluorine-based polymer electrolyte membrane and an electrode catalyst layer were produced in the same manner as in Example 1 except that the obtained fluorine-based electrolyte emulsion was used.
- the EW of the fluoropolymer electrolyte membrane is 470, the distance between ion clusters is 2.3 nm, and the ionic conductivity is 0.10 S / cm at 110 ° C. and 26% RH, and 0.18 S / cm at 110 ° C. and 50% RH. cm.
- the water content at 25 ° C. was 150%.
- Amount of platinum supported electrocatalyst layer is 0.17 mg / cm 2 at the anode electrode, the cathode electrode was 0.32 mg / cm 2.
- the cell temperature was 80 ° C.
- Example (1.11) the saturated water vapor pressure (corresponding to humidity 26% RH) at 50 ° C.
- the current density after holding for 20 hours at a voltage of 0.6 V was 0.54 A / cm 2 .
- the conditions were a saturated water vapor pressure (corresponding to a humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C.
- the current density after holding at a voltage of 0.6 V for 20 hours was 0.48 A / cm 2 .
- the MFR of the precursor polymer obtained in the same manner as in Example 1 was 16 g / 10 min.
- the repeating unit of the SO 3 H group-containing monomer of the fluorine-based polymer electrolyte in the fluorine-based polymer electrolyte emulsion was 29 mol%.
- the average particle diameter of the fluorine-based polymer electrolyte was 62 nm, and the aspect ratio was 1.0. (SO 2 F group number) / (SO 3 Z group number) was 0.
- a fluorine-based polymer electrolyte membrane and an electrode catalyst layer were produced in the same manner as in Example 1 except that the obtained fluorine-based electrolyte emulsion was used.
- the EW of the fluoropolymer electrolyte membrane is 527, the distance between ion clusters is 2.4 nm, and the ionic conductivity is 0.10 S / cm at 110 ° C. and 30% RH, and 0.14 S / cm at 110 ° C. and 50% RH. cm.
- the water content at 25 ° C. was 100%.
- Amount of platinum supported electrocatalyst layer is 0.17 mg / cm 2 at the anode electrode, the cathode electrode was 0.32 mg / cm 2.
- Example (1.11) In the fuel cell evaluation conducted in the same manner as (1.10) in Example 1 except that the electrolyte membrane was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to 26% RH) at 50 ° C. The current density after holding for 20 hours at a voltage of 0.6 V was 0.51 A / cm 2 . Further, in the fuel cell evaluation conducted in the same manner as in Example (1.11) except that the electrode catalyst layer was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to 26% RH) at 50 ° C. Under the conditions, the current density after holding at a voltage of 0.6 V for 20 hours was 0.46 A / cm 2 .
- Example 5 A fluorine-based polymer electrolyte emulsion containing a repeating unit derived from CF 2 ⁇ CF 2 and CF 2 ⁇ CF—O— (CF 2 ) 2 —SO 3 H and having an EW of 548 is added to 150 g of C 7 F 15 COONH 4 .
- CF 2 CFOCF 2 CF 2 SO 2 F 1150 g instead of 950 g
- the internal temperature is adjusted to 38 ° C.
- TFE is added to maintain the internal pressure at 0.42 MPaG, and the polymerization is continued. Except for this, the same method as in Example 1 was used.
- a polymerization solution (precursor emulsion).
- the MFR of the precursor polymer obtained in the same manner as in Example 1 was 7.2 g / 10 minutes.
- the repeating unit of the SO 3 H group-containing monomer of the fluorine-based polymer electrolyte in the fluorine-based polymer electrolyte emulsion was 27.0 mol%.
- the average particle diameter of the fluorine-based polymer electrolyte was 47 nm, and the aspect ratio was 1.0. (SO 2 F group number) / (SO 3 Z group number) was 0.
- a fluorine-based polymer electrolyte membrane and an electrode catalyst layer were produced in the same manner as in Example 1 except that the obtained fluorine-based electrolyte emulsion was used.
- the EW of the fluorine-based polymer electrolyte membrane is 548, the distance between ion clusters is 2.4 nm, and the ionic conductivity is 0.10 S / cm at 110 ° C. and 35% RH, and 0.13 S / cm at 110 ° C. and 50% RH. cm.
- the water content at 25 ° C. was 90%.
- Amount of platinum supported electrocatalyst layer is 0.17 mg / cm 2 at the anode electrode, the cathode electrode was 0.32 mg / cm 2.
- Example (1.11) In the fuel cell evaluation conducted in the same manner as (1.10) in Example 1 except that the electrolyte membrane was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to 26% RH) at 50 ° C. The current density after holding for 20 hours at a voltage of 0.6 V was 0.49 A / cm 2 . Further, in the fuel cell evaluation conducted in the same manner as in Example (1.11) except that the electrode catalyst layer was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to 26% RH) at 50 ° C. Under the conditions, the current density after holding at a voltage of 0.6 V for 20 hours was 0.45 A / cm 2 .
- a fluorine-based polymer electrolyte membrane and an electrode catalyst layer were produced in the same manner as in Example 1 except that the obtained fluorine-based electrolyte emulsion was used.
- the EW of the fluorine-based polymer electrolyte membrane is 579, the distance between ion clusters is 2.5 nm, and the ionic conductivity is 0.10 S / cm at 110 ° C. and 40% RH, and 0.12 S / cm at 110 ° C. and 50% RH. cm.
- the water content at 25 ° C. was 80%.
- Amount of platinum supported electrocatalyst layer is 0.17 mg / cm 2 at the anode electrode, the cathode electrode was 0.32 mg / cm 2.
- Example (1.11) In the fuel cell evaluation conducted in the same manner as (1.10) in Example 1 except that the electrolyte membrane was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to 26% RH) at 50 ° C. The current density after holding for 20 hours at a voltage of 0.6 V was 0.47 A / cm 2 . Further, in the fuel cell evaluation conducted in the same manner as in Example (1.11) except that the electrode catalyst layer was used, the cell temperature was 80 ° C. and the saturated water vapor pressure (corresponding to 26% RH) at 50 ° C. Under the conditions, the current density after holding at a voltage of 0.6 V for 20 hours was 0.42 A / cm 2 .
- the inside of the system was replaced with nitrogen and then vacuumed, and then TFE was introduced until the internal pressure reached 0.2 MPaG. While stirring at 400 rpm, the temperature was adjusted so that the internal temperature was 48 ° C., CF 4 as an explosion-proof material was introduced to 0.1 MPaG, and then TFE was further introduced so that the internal pressure was 0.70 MPaG.
- MFR of the obtained polymer fluorine polymer electrolyte precursor
- the repeating unit of the SO 3 H group-containing monomer was 19 mol%.
- a fluorinated polymer electrolyte solution and a fluorinated polymer electrolyte membrane were prepared in the same manner as in Comparative Example 1 except that this polymer (fluorinated polymer electrolyte precursor) was used, and EW measurement, distance between ion clusters and conduction were performed. Degree measurement was performed. As a result, EW was 705 and the distance between ion clusters was 2.7 nm. It was 0.08 S / cm at 110 ° C. and 50% RH, and the target high conductivity was not obtained.
- An MEA was produced in the same manner as (1.10) of Example 1 except that the above-described fluorine-based polymer electrolyte membrane was used, and a fuel cell evaluation was performed.
- the current density after holding for 20 hours at a voltage of 0.6 V under conditions of saturated water vapor pressure (corresponding to a humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. is 0.27 A / cm 2 , which is high. No current density was obtained.
- an electrode catalyst layer and an MEA were prepared by the same method as (1.11) of Example 1 except that the above-described fluorine-based polymer electrolyte solution was used, and a fuel cell was evaluated.
- the current density after holding for 20 hours at a voltage of 0.6 V under conditions of saturated water vapor pressure (corresponding to a humidity of 26% RH) at a cell temperature of 80 ° C. and 50 ° C. is 0.26 A / cm 2 , which is high. No current density was obtained.
- the obtained fluorine-based electrolyte emulsion contained a fluorine-based polymer electrolyte having a stable concentration of —SO 3 K having a fluorine-based polymer electrolyte concentration of 43% by mass.
- the fluorine electrolyte emulsion was diluted 100 times with pure water, dropped onto an aluminum plate, and dried at 60 ° C. to prepare a particle shape measurement sample.
- the sample was measured with an atomic force microscope [AFM], and 20 particles in the obtained image were randomly extracted to measure the aspect ratio and average particle diameter, which were 1.0 and 100 nm, respectively. It was.
- a dispersion composition for forming a thin film was obtained by adding a half-volume ethanol-isopropanol mixed solution of the volume of the emulsion to the fluorine-based electrolyte emulsion obtained in (4.3) above.
- the dispersion composition for forming a thin film was applied on a glass plate and then dried at room temperature to obtain a colorless and transparent film.
- the obtained film was fixed by heat treatment at 300 ° C. for 10 minutes, immersed in pure water, and the thin film was peeled off from the glass plate to obtain an electrolyte film.
- the obtained electrolyte membrane had a thickness of 12 to 17 ⁇ m.
- EW was 705.
- MFR of the obtained polymer fluorine polymer electrolyte precursor
- the repeating unit of the SO 3 H group-containing monomer was 19 mol%.
- a fluorinated polymer electrolyte solution and a fluorinated polymer electrolyte membrane were prepared in the same manner as in Comparative Example 1 except that this polymer (fluorinated polymer electrolyte precursor) was used, and EW measurement, distance between ion clusters and conduction were performed. Degree measurement was performed. As a result, EW was 705 and the distance between ion clusters was 2.7 nm. It was 0.08 S / cm at 110 ° C. and 50% RH, and the target high conductivity was not obtained.
- the electrolyte emulsion of the present invention makes it possible to easily and inexpensively provide a fuel cell having high performance even under high temperature and low humidification conditions.
- the electrolyte emulsion of the present invention can be used in various fuel cells including direct methanol fuel cells, water electrolysis, hydrohalic acid electrolysis, salt electrolysis, oxygen concentrators, humidity sensors, gas sensors and the like.
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Abstract
Description
CF2=CF(CF2)k-Ol-(CF2CFY1-O)n-(CFY2)m-A1 (I)
(式中、Y1は、F、Cl又はパーフルオロアルキル基を表す。kは0~2の整数、lは0又は1、nは0~8の整数を表し、n個のY1は、同一でも異なっていてもよい。Y2はF又はClを表す。mは0~6の整数を表す。ただし、m=0の場合は、l=0、n=0である。m個のY2は、同一でも異なっていてもよい。A1はSO3Zを表し、Zはアルカリ金属、アルカリ土類金属、水素、又は、NR1R2R3R4を表す。R1、R2、R3及びR4はそれぞれ独立に炭素数1~3のアルキル基又は水素を表す。)で表されるSO3Z基含有モノマーに由来する繰り返し単位(α)と、前記繰り返し単位(α)とは異なるエチレン性フルオロモノマーに由来する繰り返し単位(β)とを含み、繰り返し単位(α)が10~95モル%、繰り返し単位(β)が5~90モル%、繰り返し単位(α)と繰り返し単位(β)との和が95~100モル%であることが好ましい。
d=λ/2/sin(θm) (1)
(式中、dはイオンクラスター間距離、λは小角X線測定に用いる入射X線波長、θmはピークを示すブラッグ角を表す。)
上記フッ素系高分子電解質が、上記のような範囲のプロトン伝導度を有するため、本発明の電解質エマルションは、高温低加湿条件下での運転に適用可能で、かつ幅広い運転環境で高性能を示す電解質膜や電極触媒層を製造することができる。
イオンクラスター間距離の上限は、より好ましくは2.5nmである。イオンクラスター間距離の下限としては、例えば、0.5nmであってもよいし、1.0nmであってもよいし、また、2.0nmであってもよい。
上記フッ素系高分子電解質が、上記のような範囲のイオンクラスター間距離のものであると、高温低加湿条件下での運転に特に好適であり、かつ幅広い運転環境で高性能を示す電解質膜や電極触媒層を製造することができる。
d=λ/2/sin(θm) (1)
(式中λは入射X線波長)
例えば、-SO2F基を有するフッ素系高分子電解質前駆体の、-SO2F基を変換処理して上記フッ素系高分子電解質を得る場合、(フッ素系高分子電解質に含まれるSO3Z基数)は、近似的に、{(フッ素系高分子電解質前駆体に含まれるSO2F基数)-(フッ素系高分子電解質に含まれるSO2F基数)}とみなすことができる。すなわち、赤外吸光分析により(フッ素系高分子電解質に含まれるSO2F基数)及び(フッ素系高分子電解質前駆体に含まれるSO2F基数)をそれぞれ測定し、その比をとることにより、フッ素系高分子電解質の(SO2F基数)/(SO3Z基数)を求めることができる。
具体的には、ヒートプレス等により作成した上記前駆体のフィルムをフーリエ変換式赤外吸光分光法により測定し、2364cm-1付近のCF2に由来する吸収ピークの強度(I0C)と2704cm-1付近のSO2F基に由来する吸収ピークの強度(I0S)を測定し、その比率A0=I0S/I0Cを求める。次に上記フッ素系高分子電解質をキャスト製膜等によりフィルムを作成し、同様にフーリエ変換式赤外吸光分光法測定して、CF2に由来する吸収ピークの強度(I1C)及びSO2F基に由来する吸収ピークの強度(I1S)を測定し、その比率A1=I1S/I1Cを求める。上記、フッ素系高分子電解質の(SO2F基数)/(SO3Z基数)はA1/A0で計算することができる。
通常、フッ素系高分子電解質に含まれるSO2F基数はSO3Z基数に比べて無視できるほど小さいので、(高分子電解質に含まれるSO3Z基数)=(前駆体に含まれるSO2F基数)とみなすことができる。
CF2=CF(CF2)k-Ol-(CF2CFY1-O)n-(CFY2)m-A1 (I)
(式中、Y1は、F、Cl又はパーフルオロアルキル基を表す。kは0~2の整数、lは0又は1、nは0~8の整数を表し、n個のY1は、同一でも異なっていてもよい。Y2はF又はClを表す。mは0~6の整数を表す。ただし、m=0の場合は、l=0、n=0となる。m個のY2は、同一でも異なっていてもよい。A1はSO3Zを表し、Zはアルカリ金属、アルカリ土類金属、水素、又は、NR1R2R3R4を表す。R1、R2、R3及びR4はそれぞれ独立に炭素数1~3のアルキル基又は水素を表す。)で表されるSO3Z基含有モノマーに由来するものである。
CF2=CF-Rf1 (II)
(式中、Rf1は、F、Cl又は炭素数1~9の直鎖状又は分岐状のフルオロアルキル基を表す。)
で表されるハロエチレン性フルオロモノマー、あるいは下記一般式(III)
CHY3=CFY4 (III)
(式中、Y3はH又はFを表し、Y4はH、F、Cl又は炭素数1~9の直鎖状又は分岐状のフルオロアルキル基を表す。)
で表される水素含有フルオロエチレン性フルオロモノマー等が挙げられる。
なお、フッ素系高分子電解質のポリマー組成は、例えば、300℃における溶融NMRの測定値から算出することができる。
CF2=CF-O-Rf2 (IV)
(式中、Rf2は、炭素数1~9のフルオロアルキル基又は炭素数1~9のフルオロポリエーテル基を表す。)
で表されるフルオロビニルエーテル、より好ましくはパーフルオロビニルエーテル、あるいは下記一般式(V)
CHY5=CF-O-Rf3 (V)
(式中、Y5は、H又はFを表し、Rf3は、炭素数1~9のエーテル基を有していてもよい直鎖状又は分岐状のフルオロアルキル基を表す。)
で表される水素含有ビニルエーテル等が挙げられる。上記ビニルエーテルとしては、1種又は2種以上を用いることができる。
本発明の電解質エマルションは、例えば、下記方法により製造することができる。本発明は、エチレン性フルオロモノマーと、SO2Z1基(Z1はハロゲン元素を表す。)を有するフッ化ビニル化合物と、を0℃以上40℃以下の重合温度で共重合させることにより、フッ素系高分子電解質前駆体を含む前駆体エマルションを得る工程(1)、及び、前記前駆体エマルションに塩基性反応液体を添加し、フッ素系高分子電解質前駆体を化学処理することによって、フッ素系高分子電解質が分散されてなる電解質エマルションを得る工程(2)を含み、電解質エマルションは、当量重量(EW)が250以上700以下であることを特徴とする電解質エマルションの製造方法でもある。
本発明の電解質エマルションの製造方法は、上記工程(2)において、前駆体エマルションに塩基性反応液体を添加することにより、この課題を解決し、温和な条件で簡便に低いEWを有するフッ素系高分子電解質が分散された電解質エマルションを、効率よく製造することができることを見出したものである。
CF2=CF(CF2)k-Ol-(CF2CFY1-O)n-(CFY2)m-A2 (VI)
(式中、Y1は、F、Cl又はパーフルオロアルキル基を表す。kは0~2の整数、lは0又は1、nは、0~8の整数を表し、n個のY1は、同一でも異なっていてもよい。Y2はF又はClを表す。mは0~6の整数を表す。ただし、m=0の場合は、l=0、n=0となる。m個のY2は、同一でも異なっていてもよい。A2はSO2Z1を表し、Z1はハロゲン元素を表す。)で表されるフッ化ビニル化合物が好ましい。
CF2=CFO(CF2)P-SO2F、
CF2=CFOCF2CF(CF3)O(CF2)P-SO2F、
CF2=CF(CF2)P-1-SO2F、
CF2=CF(OCF2CF(CF3))P-(CF2)P-1-SO2F、
(式中、Pは、それぞれ1~8の整数である。)等が挙げられる。
工程(2)は、前駆体エマルションに塩基性反応液体を添加し、フッ素系高分子電解質前駆体と塩基性反応液体とを接触させることで、フッ素系高分子電解質前駆体を化学処理して電解質エマルションを得る工程である。上記化学処理としては、加水分解処理、酸処理等が挙げられる。加水分解処理は、塩基性反応液体を前駆体エマルションに添加することにより行うことができる。
複合粒子としては、導電性粒子に対して電極触媒粒子が、好ましくは1~99質量%、より好ましくは10~90質量%、最も好ましくは30~70質量%であることが好ましい。具体的には、田中貴金属工業株式会社製TEC10E40E等のPt触媒担持カーボンが好適な例として挙げられる。
電極面積に対する電極触媒の担持量としては、電極触媒層を形成した状態で、好ましくは0.001~10mg/cm2、より好ましくは0.01~5mg/cm2、最も好ましくは0.1~1mg/cm2である。電極触媒層の厚みとしては、好ましくは0.01~200μm、より好ましくは0.1~100μm、最も好ましくは1~50μmである。
電極触媒層の空隙率としては特に限定されないが、好ましくは10~90体積%、より好ましくは20~80体積%、最も好ましくは30~60体積%である。
また、撥水性の向上のため、本発明の電極触媒層がさらにポリテトラフルオロエチレン(以下、PTFE)を含有する場合がある。この場合、PTFEの形状としては特に限定されないが、定形性のものであればよく、粒子状、繊維状であることが好ましく、これらが単独で使用されても混合して使用されていてもよい。
上述のような電極触媒層を使用することにより、フラッティングが生じにくく、高い出力を得ることができる。この理由は、含水率を低くすることができ、電極の排水性に優れていることに起因するものと推測される。
次に電極触媒層の製造方法について説明する。本発明は、上記電解質エマルションに、触媒金属及び導電剤からなる複合粒子を分散させた電極触媒組成物を調製する工程と、電極触媒組成物を基材に塗布する工程と、基材に塗布した電極触媒組成物を乾燥させて電極触媒層を得る工程と、を含む電極触媒層の製造方法でもある。本発明は更に、この製造方法により得られた電極触媒層でもある。例えば、電極触媒層は、電解質エマルションを準備し、この電解質エマルション中に、上記複合粒子を分散させた電極触媒組成物を調製し、これを高分子電解質膜上又はPTFEシート等の他の基材上に塗布した後、乾燥、固化して製造することができる。尚、本発明において電極触媒組成物の塗布は、スクリーン印刷法、スプレー法等の一般的に知られている各種方法を用いることが可能である。電極触媒組成物は、フッ素系高分子電解質、複合粒子及び水性媒体を含む。
また一方、ガス拡散層と電極触媒層が積層したBASF社製ELAT(登録商標)のようなガス拡散電極に、上記電極触媒組成物を塗布もしくは浸漬・塗布せしめた後に、乾燥、固化することによっても本発明の電極触媒層を得ることができる。
またさらに、電極触媒層を作製後に塩酸等の無機酸に浸漬を行う場合がある。酸処理の温度としては、好ましくは5~90℃、より好ましくは10~70℃、最も好ましくは20~50℃である。
以下、本実施の形態を実施例によりさらに具体的に説明するが、本実施の形態はこれらの実施例のみに限定されるものではない。
イオン交換基の対イオンがプロトンの状態となっている高分子電解質膜、およそ2~20cm2を、25℃、飽和NaCl水溶液30mlに浸漬し、攪拌しながら30分間放置した。次いで、飽和NaCl水溶液中のプロトンを、フェノールフタレインを指示薬として0.01N水酸化ナトリウム水溶液を用いて中和滴定した。中和後に得られた、イオン交換基の対イオンがナトリウムイオンの状態となっている高分子電解質膜を、純水ですすぎ、更に真空乾燥して秤量した。中和に要した水酸化ナトリウムの物質量をM(mmol)、イオン交換基の対イオンがナトリウムイオンの高分子電解質膜の重量をW(mg)とし、下記式(2)より当量重量EW(g/eq)を求めた。
EW=(W/M)-22 (2)
高分子電解質膜を厚みが0.25mm程度になるよう重ね、湿度制御可能な小角X線用セルにセットした。25℃50%RHの条件で30分保持した後、これに対してX線を入射し、散乱を測定した。測定条件は、X線波長λ0.154nm、カメラ長515mmで、検出器にはイメージングプレートを用いた。イメージングプレートにより得られた2次元散乱パターンに対しては、空セル散乱補正、検出器由来のバックグラウンド補正を施した後、円環平均を行うことで、1次元散乱プロフィールを得た。散乱強度をブラッグ角θに対してプロットした散乱プロフィールにおいて、2θ>1°に存在するクラスター構造由来のピーク位置におけるブラッグ角θmを読み取り、下記式(1)によりイオンクラスター間距離dを算出した。
d=λ/2/sin(θm) (1)
日本ベル株式会社製高分子膜水分量試験装置MSB-AD-V-FCを用いて以下のとおり測定した。50μmの厚みで製膜した高分子電解質膜を幅1cm、長さ3cmに切り出し、伝導度測定用セルにセットする。次いで、伝導度測定用セルを上記試験装置のチャンバー内にセットし、チャンバー内を110℃、1%RH未満に調整する。次いで、チャンバー内にイオン交換水を用いて生成した水蒸気を導入し10%RH、30%RH、50%RH、70%RH、90%RH、95%RHの順序でチャンバー内を加湿しながら上記各湿度での伝導度を測定した。
H=(H2-H1)/(σ2-σ1)×(0.1-σ1)+H1 (3)
(ただし、H2、σ2は、それぞれ伝導度が0.10S/cmを超える最初の測定点の相対湿度と伝導度であり、H1、σ1はそれぞれ伝導度が0.10S/cmを超えない最高の相対湿度とその際の伝導度である。)
フルオロポリマーのMFRの測定は、JIS K 7210に従って270℃、荷重2.16kgの条件下で、MELT INDEXER TYPE C-5059D(日本国東洋精機社製)を用いて測定した。押し出されたポリマーの質量を10分間あたりのグラム数で表した。
ポリマー組成は、300℃における溶融NMRの測定値から算出した。NMRは、ブルカー社製 フーリエ変換核磁気共鳴装置(FT-NMR) AC300Pを用いた。算出には、テトラフルオロエチレンとビニルエーテルに由来する-120ppm付近のピーク強度と、ビニルエーテルに由来する-80ppm付近のピーク強度を用いて、それぞれのピークの積分値から、ポリマーの組成を計算した。
平均粒子径及びアスペクト比は、走査型若電子顕微鏡等で、電解質エマルションをアルミ箔等に塗布したのち水性媒体を除去して得られたフッ素系高分子電解質の集合体を観測し、得られた画像上の20個以上の粒子について測定した長軸及び短軸の長さの比(長軸/短軸)の平均を上記アスペクト比、長軸及び短軸の長さの平均値を平均粒子径として得た。
乾燥した室温の秤量瓶の質量を精秤し、これをW0とした。測定した秤量瓶に測定物を10g入れ、精秤しW1とした。測定物を入れた秤量瓶をエスペック株式会社製LV-120型真空乾燥機を用いて温度110℃、絶対圧0.01MPa以下で3hr以上乾燥した後、シリカゲル入りのデシケーター中で冷却し、室温になった後に精秤しW2とした。 (W2-W0)/(W1-W0)を百分率で表し、5回測定し、その平均値を固形分濃度とした。
前駆体をヒートプレスして作成したフィルムと、得られた電解質エマルションから作成したキャスト膜に対して、IR測定を行い求めた。
約50μmの厚みで作製した高分子電解質膜を23℃50%RHに調節した恒温恒湿室に1時間保管した後、縦3cm、横4cmの大きさに切断する。次いでイオン交換水を満たしたアズワン株式会社製ウォーターバス サーマルロボTR-2Aに、同じくイオン交換水を満たしたSUS304製容器を浸漬し、SUS304製容器内のイオン交換水が25℃になるように温調する。イオン交換水の温度が25℃に達した後、上記の高分子電解質膜を水中に浸漬する。この際、高分子電解質膜が浮き上がらないようポリテトラフルオロエチレン製のメッシュ等を高分子電解質膜に重ねて浸漬してもよい。1時間浸漬した後、水中より高分子電解質膜を取り出して表面に付着した水をワットマン製ろ紙(CatNo.1441 125)を用いてふき取る。次いで、株式会社エーアンドデイ製の電子天秤GR-202を用いて含水時の高分子電解質膜重量MWを0.0001gの単位まで測定する。この際、高分子電解質膜の過度の乾燥を抑制するため、膜を水中から取り出した後10秒以内に重量測定を行うこととする。その後、エスペック株式会社製熱風乾燥機SPH-101を用いて高分子電解質膜を160℃で1時間乾燥し、上記電子天秤にて乾燥時の高分子電解質膜重量MDを測定する。(MW-MD)/MDを百分率で表し、その値を25℃含水率とした。
後述のようにして作製した電極触媒層及び膜電極接合体(MEA)の電池特性(以下「初期特性」という)を調べるため、下記のような燃料電池評価を実施した。
まず、アノード側ガス拡散層とカソード側ガス拡散層とを対向させて、それらの間に下記のようにして作製したMEAを挟み込み、評価用セルに組み込んだ。アノード側及びカソード側のガス拡散層として、カーボンクロス(米国DE NORA NORTH AMERICA社製、ELAT(登録商標)B-1)を用いた。この評価用セルを評価装置(株式会社チノー社製)に設置して80℃に昇温した後、アノード側に水素ガスを300cc/分、カソード側に空気ガスを800cc/分で流した。それらのガスは、予め加湿されたものであり、水バブリング方式により、水素ガス及び空気ガス共に所望の温度で加湿して評価用セルへ供給した。そして、セル温度80℃、所望の加湿度の条件下、評価用セルを0.6Vの電圧で20時間保持した後、電流を測定した。
(1.1)重合工程
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが455のフッ素系電解質エマルションを以下のように作製した。
攪拌翼と温調用ジャケットを備えた内容積6リットルのSUS-316製耐圧容器に、逆浸透膜水2850g、C7F15COONH4 150g、及びCF2=CFOCF2CF2SO2F 1150gを仕込み、系内を窒素で置換した後真空とし、その後TFEを内圧が0.07MPaGになるまで導入した。400rpmで攪拌しながら、内温が10℃になるように温調を行った。(NH4)2S2O8 6gを20gの水に溶解させたものを圧入し、さらにNa2SO3 0.6gを20gの水に溶解させたものを圧入して重合を開始した。その後、内圧が0.07MPaGを維持するようにTFEを追加して重合を継続した。また、Na2SO3 0.6gを20gの水に溶解させたものを、1時間おきに圧入した。
重合開始から11時間後、追加でTFEを400g導入した時点でTFEを放圧し、重合を停止し、4700gの重合液(前駆体エマルション)を得た。得られた前駆体エマルションの固形分濃度は24.0質量%であった。
得られた重合液のうち、200gに水250gを追加し、硝酸を加えて凝析させた。凝析したポリマーを濾過した後、水の再分散と濾過を3回繰り返し、熱風乾燥器で90℃で24時間、引き続き120℃で5時間乾燥し、44.3gのポリマー(フッ素系電解質前駆体)を得た。得られたポリマーのMFRは0.4g/10分であった。
(1.1)で得られた上記重合液(前駆体エマルション)のうち2kgを純水で2倍に希釈し、容積10Lの三口フラスコ中で攪拌し、温度を80℃にして、10質量%の水酸化ナトリウム水溶液を滴下しながらpHを10以上に保持して、含フッ素ポリマーが有する-SO2Fの加水分解を行った。約3時間後にpHの低下がみられなくなったが、加水分解を更に2時間継続し、停止した。この間、含フッ素ポリマーの析出は目視により確認されなかった。
(1.2)で得られた反応液に希硫酸を加えてpHを8に調整し、ミリポア社製限外濾過装置を用いて限外濾過を施した。限外濾過膜は、分画分子量1万のもの(ミリポア社製 Pelicon 2 Filter)を用い、ミリポア社製 ステンレス製ホルダーに挟み込み、限外濾過ユニットを設けた。(1.2)で得られた反応液を、10Lビーカーにいれ、送液ポンプ(ミリポア社製 easy-load MasterFlex 1/P)を用いて上記限外濾過ユニットに供給した。不純物を含む濾液は系外に排出し、処理液はビーカーに戻した。除去した濾液に相当する量の精製水を、適宜ビーカーに加えながら限外濾過を行い、濾液の電気伝導度が10μS・cm-1になった時点で純水の追加を停止し、処理液が1Lになった時点で限外濾過を停止して水性分散体Aを得た。電気伝導度の測定は、堀場製作所社製 Twin Cond B-173電気伝導度計を用いた。限外濾過処理の時間は5時間であった。
ローム&ハース社製のアンバーライトIR120B 200gを、硫酸を用いて酸型に変換した後、純水で十分に洗浄し、硝子製ビュレットに充填した。(1.3.1)で得られた水性分散体200gを、上記ビュレットを1時間かけて通過させ、酸型の水性分散体B(電解質エマルション)を得た。得られた電解質エマルションの固形分濃度は12.5質量%、B型粘度測定器を使用して、25℃でずり速度が20.4s-1で測定した粘度は20.8mPa・sであった。(SO2F基数)/(SO3Z基数)は、0であった。フッ素系高分子電解質の平均粒子径は、42nmであり、アスペクト比は1.0であった。
(1.3.2)で得られた酸型の水性分散体Bをガラスシャーレに展開し、アズワン株式会社製ネオホットプレートHI-1000を用いて80℃にて30分の加熱乾燥を行い溶媒を除去した。さらに160℃で1時間の熱処理を行った。この後、25℃のイオン交換水に浸漬しガラスシャーレから剥離することによって、膜厚約50μmのフッ素系高分子電解質膜を得た。得られた電解質膜に皺は観察されなかった。
このフッ素系高分子電解質膜のEWは455であった。
(1.4)で得られたフッ素系高分子電解質膜のイオンクラスター間距離は2.3nmであり、イオン伝導度は110℃25%RHで0.10S/cm、110℃50%RHで0.20S/cmであった。また、25℃含水率は160%であり、フッ素系高分子電解質溶液から作製した比較例1の電解質膜と比較して低い含水率となった。
電極触媒層としては、田中貴金属工業株式会社製白金担持触媒TEC10E40E(白金担持率40wt%)0.4gに、EWが720であるフッ素系高分子電解質からなる電解質溶液(商品名「SS700C/20」、旭化成イーマテリアルズ株式会社製、ポリマー重量比20.0wt%、溶媒:水)0.825gとエタノール8.175gを添加し、混合、攪拌してインク状にしたものを、PTFEシート上にスクリーン印刷法で塗布した後、大気雰囲気中、160℃で1時間乾燥・固定化したものを使用する。この電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2である。
(1.7)電極触媒層2の作製
電極触媒層としては、田中貴金属工業株式会社製白金担持触媒TEC10E40E(白金担持率40wt%)0.4gに、(1.3.2)で得られた酸型の水性分散体Bをイオン交換水とエタノールで希釈した液体(ポリマー重量比5.5wt%、溶媒組成(質量比):エタノール/水=50/50)3.0gとエタノール6.0gを添加し、混合、攪拌してインク状にしたものを、PTFEシート上にスクリーン印刷法で塗布した後、大気雰囲気中、160℃で1時間乾燥・固定化したものを使用する。この電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2である。
(1.6)で作製したアノード用電極とカソード用電極とを対向させて、(1.4)で作製したフッ素系高分子電解質膜をそれらの間に挟み込み、180℃、面圧0.1MPaの条件でホットプレスを施すことにより、アノード用電極とカソード用電極とを高分子電解質膜に転写、接合してMEA1を作製した。
(1.9)膜電極接合体(MEA2)の作製
(1.7)で作製したアノード用電極とカソード用電極とを対向させて、高分子電解質膜(商品名「Aciplex SF7202」、旭化成イーマテリアルズ株式会社製)をそれらの間に挟み込み、180℃、面圧0.1MPaの条件でホットプレスを施すことにより、アノード用電極とカソード用電極とを高分子電解質膜に転写、接合してMEA2を作製した。
(1.8)で作製したMEA1を用いて、燃料電池評価を上述のようにして行った。その結果、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.57A/cm2となり、高い電流密度を示した。
(1.11)燃料電池評価(MEA2)
(1.9)で作製したMEA2を用いて、燃料電池評価を上述のようにして行った。その結果、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.49A/cm2となり、高い電流密度を示した。
実施例1の(1.1)で得られたフッ素系電解質前駆体を、水酸化カリウム(15質量%)とメチルアルコール(50質量%)を溶解した水溶液中に、80℃で20時間接触させて、加水分解処理を行った。本工程においてフッ素系高分子電解質はフッ素系電解質前駆体乾燥重量に対して約13.7倍の重量の上記水溶液を吸収したため著しく体積増大し、脆く崩れやすい状態になった。その後、60℃水中に5時間浸漬し、フッ素系電解質から上記水溶液を除去した。次に60℃の2N塩酸水溶液に1時間浸漬させる処理を、毎回塩酸水溶液を更新して5回繰り返した後、イオン交換水を投入し、フッ素系高分子電解質が崩れないように5時間静置し、上澄みを除去する操作を、排水のpHが5以上になるまで繰り返した。本工程においてもフッ素系高分子電解質はフッ素系電解質前駆体乾燥重量に対して約28.0倍の重量のイオン交換水を吸収し、著しく体積増大した。上記のとおり処理を行ったフッ素系電解質を注意深く採取した後に乾燥し、フッ素系高分子電解質を得た。
このフッ素系高分子電解質をエタノール水溶液(水:エタノール=50.0:50.0(質量比))とともに5Lオートクレーブ中に入れて密閉し、翼で攪拌しながら160℃まで昇温して5時間保持した。その後、オートクレーブを自然冷却して、固形分濃度5質量%の均一なフッ素系高分子電解質溶液(粘度400mPa・s)を作製した。
このフッ素系高分子溶液を80℃にて減圧濃縮して得た固形分濃度20質量%のキャスト溶液をテトラフルオロエチレンフィルム上にドクターブレードを用いて、キャストした。次に、オーブンに入れて60℃で30分予備乾燥した後、80℃で30分乾燥させて溶媒を除去し、さらに160℃で1時間熱処理を行い、膜厚約50μmのフッ素系高分子電解質膜を得た。
このフッ素系高分子電解質膜のEWは455であり、イオンクラスター間距離は2.3nmであった。イオン伝導度は110℃25%RHで0.10S/cm、110℃50%RHで0.20S/cmであった。また、25℃含水率は180%であった。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが720のフッ素系電解質を以下のように作製した。
攪拌翼と温調用ジャケットを備えた内容積189リットルのSUS-316製耐圧容器に、逆浸透膜水90.5kg、C7F15COONH4 0.945g、及びCF2=CFOCF2CF2SO2F 5.68kgを仕込み、系内を窒素で置換した後真空とし、その後TFEを内圧が0.2MPaGになるまで導入した。189rpmで攪拌しながら、内温が47℃になるように温調を行い、爆発防止材としてのCF4を0.1MPaG導入した後、内圧が0.70MPaGとなるように更にTFEを導入した。(NH4)2S2O8 47gを3Lの水に溶解させたものを系内に導入し、重合を開始した。その後、内圧が0.7MPaGを維持するようにTFEを追加した。TFEを1kg供給する毎に、CF2=CFOCF2CF2SO2Fを0.7kg供給して重合を継続した。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが399のフッ素系高分子電解質エマルションを、CF2=CFOCF2CF2SO2F 1150gに代えて1300gとし、内圧が0.02MPaGを維持するようにTFEを追加して重合を継続すること以外は実施例1と同じ方法で作製した。重合開始から16時間後、追加でTFEを323g導入した時点でTFEを放圧し、重合を停止し、4570gの重合液(前駆体エマルション)を得た。
実施例1同様にして得た前駆体ポリマーのMFRは15.6g/10分であった。
フッ素系高分子電解質エマルション中のフッ素系高分子電解質のSO3H基含有モノマーの繰り返し単位は、45.2mol%であった。フッ素系高分子電解質の平均粒子径は、50nmであり、アスペクト比は1.0であった。(SO2F基数)/(SO3Z基数)は、0であった。
その後、実施例1と同様にして、フッ素系高分子電解質膜、電極触媒層を作製した。フッ素系高分子電解質膜のEWは399であり、イオンクラスター間距離は2.3nmであり、イオン伝導度は110℃23%RHで0.10S/cm、110℃50%RHで0.22S/cmであった。また、25℃含水率は210%であった。電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2であった。上記電解質膜を用いること以外は実施例1の(1.10)と同様に行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.61A/cm2であった。また、上記電極触媒層を用いること以外は実施例の(1.11)と同様に行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.51A/cm2であった。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが470(MFRが1.8)のフッ素系電解質エマルションを、内温を17.5℃に温調し、内圧が0.09MPaGを維持するようにTFEを追加して重合を継続すること以外は実施例1と同じ方法で作製した。重合開始から9時間後、追加でTFEを401g導入した時点でTFEを放圧し、重合を停止し、4664gの重合液(前駆体エマルション)を得た。
実施例1と同様にして得た前駆体ポリマーのMFRは1.8g/10分であった。
フッ素系高分子電解質エマルション中のフッ素系高分子電解質のSO3H基含有モノマーの繰り返し単位は、34.2mol%であった。フッ素系高分子電解質の平均粒子径は、35nmであり、アスペクト比は1.0 であった。(SO2F基数)/(SO3Z基数)は、0であった。
その後、得られたフッ素系電解質エマルションを用いること以外は、実施例1と同様にして、フッ素系高分子電解質膜、電極触媒層を作製した。フッ素系高分子電解質膜のEWは470であり、イオンクラスター間距離は2.3nmであり、イオン伝導度は110℃26%RHで0.10S/cm、110℃50%RHで0.18S/cmであった。また、25℃含水率は150%であった。電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2であった。上記電解質膜を用いること以外は実施例1の(1.10)と同様に行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.54A/cm2であった。また、上記電極触媒層を用いること以外は実施例の(1.11)と同様に行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.48A/cm2であった。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが527のフッ素系高分子電解質エマルションを、C7F15COONH4 150gに代えて60g、CF2=CFOCF2CF2SO2F 1150gに代えて943gとし、内温を38℃に温調し、内圧が0.51MPaGを維持するようにTFEを追加して重合を継続すること以外は実施例1と同じ方法で作製した。重合開始から7時間後、追加でTFEを381g導入した時点でTFEを放圧し、重合を停止し、4260gの重合液(前駆体エマルション)を得た。
実施例1同様にして得た前駆体ポリマーのMFRは16g/10分であった。フッ素系高分子電解質エマルション中のフッ素系高分子電解質のSO3H基含有モノマーの繰り返し単位は、29mol%であった。フッ素系高分子電解質の平均粒子径は、62nmであり、アスペクト比は1.0であった。(SO2F基数)/(SO3Z基数)は、0であった。
その後、得られたフッ素系電解質エマルションを用いること以外は、実施例1と同様にして、フッ素系高分子電解質膜、電極触媒層を作製した。フッ素系高分子電解質膜のEWは527であり、イオンクラスター間距離は2.4nmであり、イオン伝導度は110℃30%RHで0.10S/cm、110℃50%RHで0.14S/cmであった。また、25℃含水率は100%であった。電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2であった。上記電解質膜を用いること以外は実施例1の(1.10)と同様にして行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.51A/cm2であった。また、上記電極触媒層を用いること以外は実施例の(1.11)と同様にして行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.46A/cm2であった。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが548のフッ素系高分子電解質エマルションを、C7F15COONH4 150gに代えて60g、CF2=CFOCF2CF2SO2F 1150gに代えて950gとし、内温を38℃に温調し、内圧が0.42MPaGを維持するようにTFEを追加して重合を継続すること以外は実施例1と同じ方法で作製した。重合開始から5時間後、追加でTFEを381g導入した時点でTFEを放圧し、重合を停止し、4328gの重合液(前駆体エマルション)を得た。
実施例1同様にして得た前駆体ポリマーのMFRは7.2g/10分であった。
フッ素系高分子電解質エマルション中のフッ素系高分子電解質のSO3H基含有モノマーの繰り返し単位は、27.0mol%であった。フッ素系高分子電解質の平均粒子径は、47nmであり、アスペクト比は1.0であった。(SO2F基数)/(SO3Z基数)は、0であった。
その後、得られたフッ素系電解質エマルションを用いること以外は、実施例1と同様にして、フッ素系高分子電解質膜、電極触媒層を作製した。フッ素系高分子電解質膜のEWは548であり、イオンクラスター間距離は2.4nmであり、イオン伝導度は110℃35%RHで0.10S/cm、110℃50%RHで0.13S/cmであった。また、25℃含水率は90%であった。電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2であった。上記電解質膜を用いること以外は実施例1の(1.10)と同様にして行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.49A/cm2であった。また、上記電極触媒層を用いること以外は実施例の(1.11)と同様にして行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.45A/cm2であった。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが579のフッ素系高分子電解質エマルションを、C7F15COONH4 150gに代えて60g、CF2=CFOCF2CF2SO2F 1150gに代えて958gとし、内温を38℃に温調し、内圧が0.53MPaGを維持するようにTFEを追加して重合を継続すること以外は実施例1と同じ方法で作製した。重合開始から5時間後、追加でTFEを383g導入した時点でTFEを放圧し、重合を停止し、4343gの重合液(前駆体エマルション)を得た。
実施例1同様にして得た前駆体ポリマーのMFRは2.8g/10分であった。
フッ素系高分子電解質エマルション中のフッ素系高分子電解質のSO3H基含有モノマーの繰り返し単位は、24.9mol%であった。フッ素系高分子電解質の平均粒子径は、78nmであり、アスペクト比は1.0であった。(SO2F基数)/(SO3Z基数)は、0であった。
その後、得られたフッ素系電解質エマルションを用いること以外は、実施例1と同様にして、フッ素系高分子電解質膜、電極触媒層を作製した。フッ素系高分子電解質膜のEWは579であり、イオンクラスター間距離は2.5nmであり、イオン伝導度は110℃40%RHで0.10S/cm、110℃50%RHで0.12S/cmであった。また、25℃含水率は80%であった。電極触媒層の白金担持量はアノード用電極で0.17mg/cm2、カソード用電極で0.32mg/cm2であった。上記電解質膜を用いること以外は実施例1の(1.10)と同様にして行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.47A/cm2であった。また、上記電極触媒層を用いること以外は実施例の(1.11)と同様にして行った燃料電池評価では、セル温度80℃、50℃の飽和水蒸気圧(湿度26%RHに相当)の条件下、0.6Vの電圧で20時間保持した後の電流密度は0.42A/cm2であった。
CF2=CF2及びCF2=CF-O-(CF2)2-SO3Hに由来する繰り返し単位を含み、EWが705のフッ素系電解質を以下のように作製した。
(4.1)容積3000mlのステンレス製攪拌式オートクレーブに、C7F15COONH4の10%水溶液300gと純水1170gを仕込み、充分に真空、窒素置換を行った。オートクレーブを充分に真空にした後、テトラフルオロエチレン〔TFE〕ガスをゲージ圧力で0.2MPaまで導入し、50℃まで昇温した。その後、CF2=CFOCF2CF2SO2Fを100g注入し、TFEガスを導入してゲージ圧力で0.7MPaまで昇圧した。引き続き0.5gの過硫酸アンモニウム[APS]を60gの純水に溶解した水溶液を注入して重合を開始させた。
重合により消費されたTFEを補給するため、連続的にTFEを供給してオートクレーブの圧力を0.7MPaに保つようにした。更に供給したTFEに対して、質量比で0.53倍に相当する量のCF2=CFOCF2CF2SO2Fを連続的に供給して重合を継続した。供給したTFEが522gになった時点で、オートクレーブの圧力を開放し、重合を停止した。その後室温まで冷却し、フッ素系高分子電解質前駆体を約33質量%含有する、やや白濁した前駆体エマルション2450gを得た。
上記前駆体エマルションの一部をとり、硝酸で凝析させ、水洗し、乾燥した後、溶融NMRを測定したところ、含フッ素ポリマー前駆体中のフルオロビニルエーテル誘導体単位の含有率は19モル%であった。
(4.2)上記(4.1)で得られた前駆体エマルション50mlを純水を用いて5倍に希釈し、容積500mlのビーカー中で攪拌し、温度を55℃にして、10質量%の水酸化ナトリウム水溶液を滴下しながらpHを10以上に保持して、含フッ素ポリマー前駆体が有する-SO2Fの加水分解を行った。約3時間後にpHの低下がみられなくなったが、加水分解を更に2時間継続し、停止した。この間、含フッ素ポリマーの析出は目視により確認されなかった。
(4.3)上記(4.2)で得られた反応液に1規定の塩酸を添加して酸による加水分解を行い、Centriprep YM-10(アミコン社製)を用いて、遠心式限外濾過法により低分子物質の除去及び含フッ素ポリマーの精製濃縮を行った。得られたフッ素系電解質エマルションは、フッ素系高分子電解質の濃度が43質量%であり、安定な-SO3Kを有するフッ素系高分子電解質を含んでいた。
上記フッ素系電解質エマルションを純水で100倍に希釈し、アルミ板の上に滴下し、60℃で乾燥して粒子形状測定用サンプルを作成した。同サンプルを原子間力顕微鏡〔AFM〕で測定し、得られた画像内の粒子の20個を無作為に抽出してアスペクト比、平均粒子径を測定したところ、それぞれ1.0、100nmであった。
(4.4)上記(4.3)で得られたフッ素系電解質エマルションに、エマルションの容積の半量のエタノール-イソプロパノール等容混合液を添加して薄膜形成用分散体組成物を得た。上記薄膜形成用分散体組成物をガラス板上に塗布後、室温で乾燥して無色透明の膜を得た。得られた膜を300℃で10分間熱処理して固定し、純水中に浸漬してガラス板から薄膜を剥離して電解質膜を得た。得られた電解質膜は、膜厚12~17μmであった。得られた電解質膜を用いて、EW測定を行った結果、EWは705であった。
Claims (19)
- フッ素系高分子電解質が水性媒体に分散されてなる電解質エマルションであって、
前記フッ素系高分子電解質は、
SO3Z基(Zはアルカリ金属、アルカリ土類金属、水素、又は、NR1R2R3R4を表す。R1、R2、R3及びR4はそれぞれ独立に炭素数1~3のアルキル基又は水素を表す。)含有モノマー単位を有し、
当量重量(EW)が250以上700以下であり、
110℃相対湿度50%RHにおけるプロトン伝導度が0.10S/cm以上であり、
平均粒子径が10~500nmの球形粒子であり、
(SO2F基数)/(SO3Z基数)が0~0.01である
ことを特徴とする電解質エマルション。 - フッ素系高分子電解質は、当量重量(EW)が250以上650以下である請求項1記載の電解質エマルション。
- フッ素系高分子電解質は、下記一般式(I)
CF2=CF(CF2)k-Ol-(CF2CFY1-O)n-(CFY2)m-A1 (I)
(式中、Y1は、F、Cl又はパーフルオロアルキル基を表す。kは0~2の整数、lは0又は1、nは0~8の整数を表し、n個のY1は、同一でも異なっていてもよい。Y2はF又はClを表す。mは0~6の整数を表す。ただし、m=0の場合は、l=0、n=0である。m個のY2は、同一でも異なっていてもよい。A1はSO3Zを表し、Zはアルカリ金属、アルカリ土類金属、水素、又は、NR1R2R3R4を表す。R1、R2、R3及びR4はそれぞれ独立に炭素数1~3のアルキル基又は水素を表す。)で表されるSO3Z基含有モノマーに由来する繰り返し単位(α)と、前記繰り返し単位(α)とは異なるエチレン性フルオロモノマーに由来する繰り返し単位(β)とを含み、
繰り返し単位(α)が10~95モル%、繰り返し単位(β)が5~90モル%、繰り返し単位(α)と繰り返し単位(β)との和が95~100モル%である
請求項1又は2記載の電解質エマルション。 - フッ素系高分子電解質は、kが0であり、lが1であり、Y1がFであり、nが0又は1であり、Y2がFであり、mが2又は4であり、A1がSO3Hである請求項3記載の電解質エマルション。
- フッ素系高分子電解質は、nが0であり、mが2である請求項4記載の電解質エマルション。
- フッ素系高分子電解質は、小角X線測定を行い下記式(1)から算出される、25℃相対湿度50%RHにおけるイオンクラスター間距離が0.1nm以上2.6nm以下である請求項1、2、3、4又は5記載の電解質エマルション。
d=λ/2/sin(θm) (1)
(式中、dはイオンクラスター間距離、λは小角X線測定に用いる入射X線波長、θmはピークを示すブラッグ角を表す。) - フッ素系高分子電解質は、フッ素系高分子電解質前駆体を化学処理して得られ、
前記フッ素系高分子電解質前駆体は、前記化学処理によってSO3Z(Zはアルカリ金属、アルカリ土類金属、水素、又は、NR1R2R3R4を表す。R1、R2、R3及びR4はそれぞれ独立に炭素数1~3のアルキル基又は水素を表す。)に変換される基を有し、溶融流動可能であり、メルトフローレートが0.01~100g/10分である請求項1、2、3、4、5又は6記載の電解質エマルション。 - 化学処理は、フッ素系高分子電解質前駆体と塩基性反応液体とを接触させる処理である請求項7記載の電解質エマルション。
- 電解質エマルションは、フッ素系高分子電解質を2~80質量%含むものである請求項1、2、3、4、5、6、7又は8記載の電解質エマルション。
- 水性媒体は、水含有率が50質量%を超えるものである請求項1、2、3、4、5、6、7、8又は9記載の電解質エマルション。
- 請求項1、2、3、4、5、6、7、8、9又は10記載の電解質エマルションを基材に塗布する工程と、
基材に塗布した電解質エマルションを乾燥させて電解質膜を得る工程と、
電解質膜を基材から剥離する工程と、
を含むことを特徴とする電解質膜の製造方法。 - 請求項11記載の製造方法により得られたものであることを特徴とする電解質膜。
- 請求項1、2、3、4、5、6、7、8、9又は10記載の電解質エマルションに、触媒金属及び導電剤からなる複合粒子を分散させた電極触媒組成物を調製する工程と、
電極触媒組成物を基材に塗布する工程と、
基材に塗布した電極触媒組成物を乾燥させて電極触媒層を得る工程と、
を含むことを特徴とする電極触媒層の製造方法。 - 請求項13記載の製造方法により得られたものであることを特徴とする電極触媒層。
- 請求項12記載の電解質膜を備えることを特徴とする膜電極接合体。
- 請求項14記載の電極触媒層を備えることを特徴とする膜電極接合体。
- 請求項15又は16記載の膜電極接合体を備えることを特徴とする固体高分子型燃料電池。
- エチレン性フルオロモノマーと、SO2Z1基(Z1はハロゲン元素を表す。)を有するフッ化ビニル化合物と、を0℃以上40℃以下の重合温度で共重合させることにより、フッ素系高分子電解質前駆体を含む前駆体エマルションを得る工程(1)、及び、
前記前駆体エマルションに塩基性反応液体を添加し、フッ素系高分子電解質前駆体を化学処理することによって、フッ素系高分子電解質が分散されてなる電解質エマルションを得る工程(2)、
を含み、
電解質エマルションは、当量重量(EW)が250以上700以下であることを特徴とする電解質エマルションの製造方法。 - 請求項1、2、3、4、5、6、7、8、9又は10記載の電解質エマルションを製造する請求項18記載の電解質エマルションの製造方法。
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JP2012004048A (ja) * | 2010-06-18 | 2012-01-05 | Asahi Kasei E-Materials Corp | 電解質膜並びにその製造方法、電極触媒層並びにその製造方法、膜電極接合体、及び、固体高分子電解質型燃料電池 |
WO2013100079A1 (ja) * | 2011-12-28 | 2013-07-04 | 旭化成イーマテリアルズ株式会社 | レドックスフロー二次電池及びレドックスフロー二次電池用電解質膜 |
WO2013100087A1 (ja) * | 2011-12-28 | 2013-07-04 | 旭化成イーマテリアルズ株式会社 | レドックスフロー二次電池及びレドックスフロー二次電池用電解質膜 |
WO2015002073A1 (ja) | 2013-07-02 | 2015-01-08 | 旭化成イーマテリアルズ株式会社 | 電解質溶液及びその製造方法、連続溶解装置、電解質膜、電極触媒層、膜電極接合体、並びに燃料電池 |
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Also Published As
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US9627702B2 (en) | 2017-04-18 |
EP2479212B1 (en) | 2023-06-07 |
US20160308232A1 (en) | 2016-10-20 |
US20120178017A1 (en) | 2012-07-12 |
CN102498168A (zh) | 2012-06-13 |
US9406958B2 (en) | 2016-08-02 |
US9133316B2 (en) | 2015-09-15 |
EP2479212A4 (en) | 2014-11-05 |
US20150349366A1 (en) | 2015-12-03 |
CN102498168B (zh) | 2014-09-10 |
JP5461566B2 (ja) | 2014-04-02 |
JPWO2011034179A1 (ja) | 2013-02-14 |
EP2479212A1 (en) | 2012-07-25 |
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