WO2023199874A1 - 水素化重合体の製造方法 - Google Patents

水素化重合体の製造方法 Download PDF

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WO2023199874A1
WO2023199874A1 PCT/JP2023/014473 JP2023014473W WO2023199874A1 WO 2023199874 A1 WO2023199874 A1 WO 2023199874A1 JP 2023014473 W JP2023014473 W JP 2023014473W WO 2023199874 A1 WO2023199874 A1 WO 2023199874A1
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Prior art keywords
solvent
producing
hydrogenated polymer
less
aromatic vinyl
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English (en)
French (fr)
Japanese (ja)
Inventor
英之 佐藤
啓克 荒井
裕介 中村
海瑠 松下
宣之 加藤
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Mitsubishi Gas Chemical Co Inc
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Mitsubishi Gas Chemical Co Inc
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Priority to US18/854,584 priority Critical patent/US20250243299A1/en
Priority to KR1020247023571A priority patent/KR20250003466A/ko
Priority to JP2024514948A priority patent/JPWO2023199874A1/ja
Priority to EP23788292.3A priority patent/EP4509531A4/en
Priority to CN202380033030.XA priority patent/CN118984841A/zh
Publication of WO2023199874A1 publication Critical patent/WO2023199874A1/ja
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F8/00—Chemical modification by after-treatment
    • C08F8/04—Reduction, e.g. hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08C—TREATMENT OR CHEMICAL MODIFICATION OF RUBBERS
    • C08C19/00—Chemical modification of rubber
    • C08C19/02—Hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F220/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride ester, amide, imide or nitrile thereof
    • C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
    • C08F220/10—Esters
    • C08F220/12—Esters of monohydric alcohols or phenols
    • C08F220/14—Methyl esters, e.g. methyl (meth)acrylate
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F222/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a carboxyl radical and containing at least one other carboxyl radical in the molecule; Salts, anhydrides, esters, amides, imides, or nitriles thereof
    • C08F222/04—Anhydrides, e.g. cyclic anhydrides
    • C08F222/06—Maleic anhydride
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F297/00—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer
    • C08F297/02—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the anionic type
    • C08F297/04—Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the anionic type polymerising vinyl aromatic monomers and conjugated dienes
    • G—PHYSICS
    • G02—OPTICS
    • G02B—OPTICAL ELEMENTS, SYSTEMS OR APPARATUS
    • G02B1/00—Optical elements characterised by the material of which they are made; Optical coatings for optical elements
    • G02B1/04—Optical elements characterised by the material of which they are made; Optical coatings for optical elements made of organic materials, e.g. plastics
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F212/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
    • C08F212/02—Monomers containing only one unsaturated aliphatic radical
    • C08F212/04—Monomers containing only one unsaturated aliphatic radical containing one ring
    • C08F212/06—Hydrocarbons
    • C08F212/08—Styrene
    • G—PHYSICS
    • G02—OPTICS
    • G02B—OPTICAL ELEMENTS, SYSTEMS OR APPARATUS
    • G02B1/00—Optical elements characterised by the material of which they are made; Optical coatings for optical elements
    • G02B1/04—Optical elements characterised by the material of which they are made; Optical coatings for optical elements made of organic materials, e.g. plastics
    • G02B1/041—Lenses

Definitions

  • the present invention relates to a method for producing a hydrogenated polymer. More specifically, the present invention relates to a method for producing a hydrogenated polymer by hydrogenating the aromatic ring of an aromatic vinyl compound polymer (nuclear hydrogenation).
  • Patent Document 1 is related to the hydrogenation of an aromatic vinyl compound/(meth)acrylate copolymer
  • Patent Document 2 is related to the hydrogenation of an aromatic vinyl compound/(meth)acrylate copolymer.
  • the present invention relates to a method for producing a nuclear hydrogenated polymer.
  • Patent No. 2890748 is related to a method for producing hydrogenated styrene resin
  • Patent No. 4224655 Patent Document 7
  • Patent No. 5007688 Patent Document 8
  • Patent No. 5540703 Japanese Patent Application Publication No. 2014-77044 Patent No. 2890748 Special Publication No. 2001-527095 Special Publication No. 2002-511501 Special table 2002-511508 Patent No. 4224655 Patent No. 5007688
  • nuclear hydrogen additives of styrene and nuclear hydrogen additives of copolymers such as styrene/isoprene cannot be said to have sufficient heat resistance.
  • nuclear hydrogenation it is necessary to conduct the reaction for a long time in order to obtain a high nuclear hydrogenation rate.
  • a method for producing a hydrogenated polymer by hydrogenating an aromatic ring of an aromatic vinyl compound-based polymer comprising: The aromatic vinyl compound-based polymer includes a first monomer unit and a second monomer unit, The method includes: reducing the hydrogenation catalyst before use; Obtaining a hydrogenated polymer by performing a hydrogenation reaction using the aromatic vinyl compound-based polymer, a solvent, and a hydrogenation catalyst after reduction treatment,
  • the solvent is a mixed solvent containing at least one type of first solvent and at least one type of second solvent,
  • the first solvent is a solvent in which the aromatic vinyl compound polymer before hydrogenation is dissolved, the second solvent is a solvent in which the hydrogenated polymer is dissolved;
  • Method for producing hydrogenated polymer comprising: The aromatic vinyl compound-based polymer includes a first monomer unit and a second monomer unit, The method includes: reducing the hydrogenation catalyst before use; Obtaining a hydrogenated polymer by performing a hydrogenation reaction using the aromatic vinyl compound-based polymer, a solvent, and
  • ⁇ 2> The method for producing a hydrogenated polymer according to ⁇ 1>, wherein the at least one first solvent contains one or more selected from the group consisting of methyl acetate, ethyl acetate, butyl acetate, and methyl isobutyrate. .
  • the at least one second solvent is cyclohexane, C9-C10 alkylcyclohexane, C7-C15 monoalkylcyclohexane, C8-C15 dialkylcyclohexane, C9-C15 trialkylcyclohexane, C10-C15 tetraalkylcyclohexane, cyclooctane, C9 ⁇ Contains one or more selected from the group consisting of C15 monoalkylcyclooctane, C10-C15 dialkylcyclooctane, C11-C15 trialkylcyclooctane, C12-C15 tetraalkylcyclooctane, n-octane, and n-decane.
  • ⁇ 1> or ⁇ 2> The method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 3>, wherein the first solvent has a boiling point of 50° C. or higher and an ignition point of 400° C. or higher.
  • ⁇ 5> The method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 4>, wherein the second solvent has a boiling point of 80° C. or higher and an ignition point of 230° C. or higher.
  • ⁇ 6> ⁇ 1> to ⁇ 5>, wherein the first monomer is selected from the group consisting of styrene, ⁇ -methylstyrene, chlorostyrene, 4-methylstyrene, 4-tert-butylstyrene, and 4-methoxystyrene;
  • ⁇ 7> The method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 6>, wherein the second monomer is selected from the group consisting of maleic anhydride, butadiene, cyclopentadiene, and isoprene.
  • ⁇ 8> ⁇ 1> to ⁇ 7 wherein the aromatic vinyl compound-based polymer is selected from the group consisting of a copolymer of styrene and maleic anhydride, a copolymer of styrene and butadiene, and a copolymer of styrene and isoprene.
  • ⁇ 9> The method for producing a hydrogenated polymer according to ⁇ 8>, wherein the aromatic vinyl compound-based polymer is a copolymer of styrene and maleic anhydride.
  • the polymerization ratio (mol %) of the first monomer unit and the second monomer unit is 70:30 or more and less than 100:0, ⁇ 1> to ⁇ 9>.
  • the method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 10> which comprises forming a polymer resin by devolatilization extrusion after the hydrogenation reaction.
  • ⁇ 12> The method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 11>, further comprising a concentration step between the hydrogenation reaction and devolatilization extrusion.
  • ⁇ 13> ⁇ 1> to ⁇ 12, wherein the mass ratio of the at least one first solvent to the at least one second solvent (first solvent: second solvent) is 1:9 to 9:1.
  • ⁇ 14> The method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 13>, wherein the hydrogenation catalyst is a solid catalyst supporting palladium, platinum, ruthenium, rhodium, or nickel.
  • a method for producing an optical material comprising the method for producing a hydrogenated polymer according to any one of ⁇ 1> to ⁇ 14>.
  • ⁇ 16> The method for producing an optical material according to ⁇ 15>, wherein the optical material is an optical lens.
  • the speed of the hydrogenation reaction is improved, resulting in efficiency. It can be manufactured as follows. Furthermore, by shortening the reaction time, it is possible to reduce damage to the polymer, such as a decrease in molecular weight. By the method of the present invention, a hydrogenated polymer having sufficient heat resistance can be obtained.
  • FIG. 1 shows the relationship between hydrogenation reaction time and nuclear hydrogenation rate for Resin 1.
  • a method for producing a hydrogenated polymer by hydrogenating (nuclear hydrogenation) the aromatic ring of an aromatic vinyl compound-based polymer is provided.
  • a method for producing a hydrogenated polymer by hydrogenating the aromatic ring of an aromatic vinyl compound-based polymer includes: The aromatic vinyl compound-based polymer includes a first monomer unit and a second monomer unit, The method includes: reducing the hydrogenation catalyst before use; The method includes obtaining a hydrogenated polymer by carrying out a hydrogenation reaction using the aromatic vinyl compound-based polymer, a solvent, and a hydrogenation catalyst after reduction treatment.
  • the manufacturing method relates to a method of manufacturing a hydrogenated polymer by hydrogenating the aromatic ring of an aromatic vinyl compound-based polymer.
  • aromatic vinyl compound polymer refers to a polymer containing units derived from aromatic vinyl compounds as constitutional units. Therefore, the aromatic vinyl compound-based polymer may be a polymer (homopolymer) consisting of units derived from one type of aromatic vinyl compound, or may include units derived from two or more types of aromatic vinyl compounds as constituent units. Alternatively, it may be a copolymer containing as constituent units a unit derived from one or more aromatic vinyl compounds and a unit derived from one or more compounds other than the aromatic vinyl compound.
  • the unit derived from an aromatic vinyl compound means a unit having a structure in which the C ⁇ C double bond of the vinyl group in the aromatic vinyl compound is opened by polymerization.
  • the aromatic vinyl compound-based polymer includes a first monomer unit and a second monomer unit.
  • aromatic vinyl compound polymer used in the production method according to some embodiments of the present invention is not particularly limited, but aromatic vinyl compound monomers include styrene; ⁇ -methylstyrene, ⁇ -ethylstyrene, o-methyl Alkylstyrene such as styrene, m-methylstyrene, p-methylstyrene, 1,3-dimethylstyrene, p-tert-butylstyrene (the number of carbon atoms in the alkyl group is preferably 1 to 5); p- Hydroxystyrene; alkoxystyrene such as p-methoxystyrene, m-butoxystyrene, p-butoxystyrene (the number of carbon atoms in the alkoxy group is preferably 1 to 5); o-chlorostyrene, m-chlorostyrene, Examples include, but are
  • the first monomer is a monomer derived from an aromatic vinyl compound.
  • said first monomer is selected from the group consisting of styrene, ⁇ -methylstyrene, chlorostyrene, 4-methylstyrene, 4-tertbutylstyrene, and 4-methoxystyrene.
  • the first monomer is styrene.
  • the aromatic vinyl compound-based polymer used in the production method according to some embodiments of the present invention is a polymer using, in addition to the aromatic vinyl compound monomer, a monomer of a compound other than the aromatic vinyl compound.
  • monomers of compounds other than aromatic vinyl compounds include, but are not limited to, (meth)acrylates, dienes, and acid anhydrides.
  • (meth)acrylates include: (Meth)acrylic acid alkyl esters such as methyl (meth)acrylate, ethyl (meth)acrylate, butyl (meth)acrylate, dodecyl (meth)acrylate, and octadecyl (meth)acrylate (number of carbon atoms in the alkyl group) is preferably 1 to 20, more preferably 1 to 10, even more preferably 1 to 5); (Meth)acrylic acid cycloalkyl esters or cyclic saturated hydrocarbon esters such as cyclohexyl (meth)acrylate and isobornyl (meth)acrylate (in each case, the number of ring carbon atoms is preferably 5 to 20, more preferably 5 ⁇ 10); (Meth)acrylic acid hydroxyalkyl esters such as (meth)acrylic acid (2-hydroxyethyl), (meth)acrylic acid (2-hydroxypropyl), (meth)acrylic acid (2-hydroxy-2-methyl)
  • the number of carbon atoms in the alkyl group is preferably 1 to 20, more preferably 1 to 10, and even more preferably 1 to 5.); (Meth)acrylic acid alkoxyalkyl esters such as (meth)acrylic acid (2-methoxyethyl) and (meth)acrylic acid (2-ethoxyethyl) (the number of carbon atoms in the alkyl group is preferably 1 to 20, more preferably is 1 to 10, more preferably 1 to 5.
  • the number of carbon atoms in the alkoxy group is preferably 1 to 10, more preferably 1 to 5, and still more preferably 1 or 2); (meth)acrylic acid phenyl esters such as (meth)acrylic acid phenyl; (Meth)acrylic acid arylalkyl ester such as benzyl (meth)acrylate (The number of carbon atoms in the aryl group site is preferably 6 to 10. Also, the number of carbon atoms in the alkyl group site is preferably 1 to 5. ); Examples include, but are not limited to, (meth)acrylic acid esters having a phospholipid structure such as 2-(meth)acryloyloxyethylphosphorylcholine. One type of (meth)acrylate may be used alone, or two or more types may be used in combination. As the (meth)acrylate, methyl (meth)acrylate is preferred.
  • diene examples include 1,2-butadiene, 1,3-butadiene, 1,2-pentadiene, 1,3-pentadiene, 1,4-pentadiene, 1,2-hexadiene, 1,3-hexadiene, 1, 4-hexadiene, 1,5-hexadiene, 1,3-heptadiene, 1,3-octadiene, 1,3-nonadiene, 1,3-decadiene, isoprene, cyclopentadiene, 1,3-cyclohexadiene and 1,4- Examples include, but are not limited to, cyclohexadiene.
  • the diene one type may be used alone, or two or more types may be used in combination.
  • conjugated dienes are preferred, such as 1,3-butadiene or isoprene.
  • acid anhydrides include, but are not limited to, acid anhydrides such as maleic acid, itaconic acid, citraconic acid, and aconitic acid. Among these, maleic anhydride is preferred as the anhydride.
  • the second monomer is a monomer derived from a conjugated diene compound.
  • said second monomer is selected from the group consisting of maleic anhydride, butadiene, cyclopentadiene, and isoprene.
  • the second monomer is maleic anhydride.
  • the aromatic vinyl compound polymer used in the production method according to some embodiments of the present invention may not contain monomers other than the first monomer and the second monomer as constituent components, as long as the effects of the present invention are not impaired. It's okay to stay.
  • the above-mentioned aromatic vinyl compound-based polymer may contain, for example, 0 to 10% or 0 to 5% of monomer components other than the first monomer and the second monomer in molar ratio based on the total monomer components. good.
  • the aromatic vinyl compound-based polymer is a copolymer of styrene and butadiene (1,2-butadiene, 1,3-butadiene or a combination thereof), a copolymer of styrene and isoprene, It contains one or more selected from the group consisting of a copolymer of styrene and methyl methacrylate, a copolymer of styrene and maleic anhydride, a copolymer of styrene and vinyl acetate, and polystyrene.
  • the aromatic vinyl compound-based polymer is a copolymer of styrene and butadiene (1,2-butadiene, 1,3-butadiene or a combination thereof), a copolymer of styrene and isoprene. It is a type of polymer selected from the group consisting of a copolymer of styrene and methyl methacrylate, a copolymer of styrene and maleic anhydride, a copolymer of styrene and vinyl acetate, and polystyrene. These polymers may be polymerized from each monomer as described below, or commercially available ones may be used. For example, as the polystyrene, "GPPS HF77" manufactured by PS Japan, etc. can be used.
  • the aromatic vinyl compound-based polymer is selected from the group consisting of a copolymer of styrene and maleic anhydride, a copolymer of styrene and butadiene, and a copolymer of styrene and isoprene. Ru.
  • the aromatic vinyl compound-based polymer is a copolymer of styrene and maleic anhydride.
  • Aromatic vinyl compound polymers can be produced by polymerizing various monomers. There are no particular restrictions on the method of polymerizing one or more types of aromatic vinyl compounds or the method of copolymerizing an aromatic vinyl compound with monomers other than aromatic vinyl compound monomers, and radical polymerization methods, ionic polymerization methods, compounding methods, etc. Known methods such as positional polymerization can be used. Industrially, radical polymerization is simple and preferred. As the radical polymerization method, known methods such as bulk polymerization, solution polymerization, emulsion polymerization, and suspension polymerization can be appropriately selected.
  • a monomer composition containing monomer components, a chain transfer agent, and a polymerization initiator (as well as a solvent in the case of solution polymerization) is continuously fed into a complete mixing tank.
  • a continuous polymerization method in which the polymer is supplied and polymerized at 100 to 180°C.
  • solvents used in the solution polymerization method include: Hydrocarbon solvents such as toluene, xylene, cyclohexane, methylcyclohexane; Ester solvents such as ethyl acetate; Ketone solvents such as acetone and methyl ethyl ketone; Ether solvents such as tetrahydrofuran and 1,4-dioxane; Examples include, but are not limited to, alcoholic solvents such as methanol and isopropanol.
  • the reaction mixture after polymerization is extracted from the complete mixing tank and then introduced into a devolatilizing extruder or vacuum devolatilizing tank to distill off the volatile components (monomer components, solvent, etc.), thereby removing the aromatic vinyl compound.
  • a copolymer of a polymer or an aromatic vinyl compound with a monomer other than the aromatic vinyl compound monomer (these may also be collectively referred to simply as an "aromatic vinyl compound polymer”) can be obtained.
  • the polymerization ratio (mol%) of the first monomer unit and the second monomer unit constituting the aromatic vinyl compound polymer is 70:30 or more and 100: It may be less than 0.
  • the polymerization ratio (mol%) of the first monomer unit and the second monomer unit constituting the aromatic vinyl compound polymer is, for example, 70:30 or more, 75:25 or more, 80:20 or more, 85:15 or more, 86:14 or more, 87:13 or more, 88:12 or more, 89:11 or more, 90:10 or more, 91:9 or more, 92:8 or more, It may be 93:7 or more, 94:6 or more, 95:5 or more, 96:4 or more, 97:3 or more, 98:2 or more, 99:1 or more.
  • the polymerization ratio (mol%) of the first monomer unit and the second monomer unit constituting the aromatic vinyl compound polymer is, for example, less than 100:0, 99:1 or less, 98:2 or less, 97:3 or less, 96:4 or less, 95:5 or less, 94:6 or less, 93:7 or less, 92:8 or less, 91:9 or less, 90:10 or less, It may be 89:11 or less, 88:12 or less, 87:13 or less, 86:14 or less, 85:15 or less, 80:20 or less, or 75:25 or less.
  • the polymerization ratio (mol%) of the first monomer unit and the second monomer unit constituting the aromatic vinyl compound polymer is 70:30 or more and 100: It is less than 0.
  • the polymerization ratio (mol%) of the first monomer unit and the second monomer unit constituting the aromatic vinyl compound polymer is, for example, 70:30 or more and less than 100:0, 75:25 or more and less than 100:0, 80:20 or more and less than 100:0, 85:15 or more and less than 100:0, 86:14 or more and less than 100:0, 87:13 or more and less than 100 : Less than 0, 88:12 or more and less than 100:0, 89:11 or more and less than 100:0, 90:10 or more and less than 100:0, 91:9 or more and less than 100:0, 92:8 or more and less than 100:0, 93 : 7 or more and less than 100:0, 94:6 or more and less than
  • the weight average molecular weight of the aromatic vinyl compound polymer used in some embodiments of the present invention is preferably 10,000 to 1,000,000, more preferably 50,000 to 700,000, and more preferably 100,000 to 1,000,000. ⁇ 500,000 is more preferred, and 130,000 ⁇ 250,000 is particularly preferred.
  • polymers with molecular weights less than 10,000 or greater than 1,000,000 can also be hydrogenated by methods according to some embodiments of the present invention, copolymers with weight average molecular weights within the above ranges are preferred. However, it is preferable because it has sufficient mechanical strength and can withstand practical use, has an appropriate viscosity, and is easy to handle.
  • the weight average molecular weight is a value determined in terms of polystyrene by gel permeation chromatography (GPC) using tetrahydrofuran as a solvent.
  • hydrogenation of an aromatic vinyl compound polymer means a reaction in which hydrogen is added to the aromatic ring of an aromatic vinyl compound polymer, for example, a benzene ring is reduced to cyclohexane. . Such hydrogenation is also called nuclear hydrogenation or nuclear hydrogenation.
  • the aromatic vinyl compound-based polymer used in some embodiments of the present invention is dissolved in a suitable solvent and hydrogenated. It is preferable that the polymer has good solubility in both aromatic polymers and hydrogenated polymers, and does not have hydrogenated sites. Furthermore, it is more preferable to use a solvent that allows the reaction to occur quickly. This is because the reaction time is shortened by increasing the rate of hydrogenation, making it possible to reduce damage to the polymer such as a decrease in molecular weight. Further, when assuming devolatilization of solvent components after hydrogenation, it is preferable that the ignition point of the solvent is high. It is preferable if the devolatilizing extrusion step can be performed, since the hydrogenated polymer can be efficiently produced.
  • the solvent used in the manufacturing method in some embodiments of the present invention is a mixed solvent containing at least one type of first solvent and at least one type of second solvent.
  • the first solvent preferably has a high solubility for the polymer before hydrogenation
  • the second solvent preferably has a high solubility for the polymer after hydrogenation.
  • the solubility of polymers in solvents is not easy to predict, and mixing these two types of solvents does not necessarily result in a solvent in which both the polymers before and after the hydrogenation reaction are well dissolved. Do not mean.
  • the solvent is a mixed solvent containing at least one type of first solvent and at least one type of second solvent
  • the first solvent is a solvent in which the aromatic vinyl compound polymer before hydrogenation is dissolved
  • the second solvent is a solvent in which the hydrogenated polymer is dissolved.
  • the at least one first solvent may be an ester solvent.
  • the at least one first solvent includes one or more selected from the group consisting of methyl acetate, ethyl acetate, butyl acetate, and methyl isobutyrate.
  • the first solvent is methyl acetate.
  • the first solvent is ethyl acetate.
  • the first solvent is butyl acetate.
  • the first solvent is methyl isobutyrate.
  • the first solvent is methyl isobutyrate.
  • the first solvent has a boiling point of 50°C or higher and an ignition point of 400°C or higher.
  • a solvent with a high boiling point and a high ignition point the devolatilizing extrusion process can be performed efficiently.
  • solvents include, but are not limited to, methyl isobutyrate, ethyl acetate, and butyl acetate.
  • the at least one second solvent may be a hydrocarbon solvent.
  • the at least one second solvent is cyclohexane, C9-C10 alkylcyclohexane, C7-C15 monoalkylcyclohexane, C8-C15 dialkylcyclohexane, C9-C15 trialkylcyclohexane, C10-C15 From the group consisting of tetraalkylcyclohexane, cyclooctane, C9-C15 monoalkylcyclooctane, C10-C15 dialkylcyclooctane, C11-C15 trialkylcyclooctane, C12-C15 tetraalkylcyclooctane, n-octane, and n-decane Contains one or more selected types.
  • the boiling point of the second solvent is 80°C or higher, and the ignition point is 230°C or higher.
  • solvents include cyclohexane, cyclopentane, methylcyclohexane, n-heptane, 2,2,4-trimethylpentane, cyclooctane, 1,3-dimethylcyclohexane, ethylcyclohexane, 1,2,4-trimethylcyclohexane, decalin. (cis,trans-decahydronaphthalene), and Swaclean 150.
  • the mass ratio (first:second) of the at least one first solvent to the at least one second solvent is 1:9 to 9:1.
  • the mass ratio of at least one first solvent to at least one second solvent (first solvent:second solvent) is, for example, 1:9-9:1, 1:9-8:2, 1:9-7:3, 1:9-6:4, 1:9-5:5, 1:9-4:6, 1: 9-3:7, 1:9-2:8; 2:8-9:1, 2:8-8:2, 2:8-7:3, 2:8-6:4, 2:8-5:5, 2:8-4:6, 2: 8-3:7; 3:7-9:1, 3:7-8:2, 3:7-7:3, 3:7-6:4, 3:7-5:5, 3:7-4:6; 4:6-9:1, 4:6-8:2, 4:6-7:3, 4:6-6:4, 4:6-5:5; 5:5-9:1, 5:5-8:2, 5:5-7:3, 5:5-6:4; 6:
  • the ratio of first solvent to second solvent is preferably 1:9 to 5:5.
  • the ratio of first solvent to second solvent is preferably 3:7 to 7:3.
  • the ratio of first solvent to second solvent is preferably 3:7 to 9:1.
  • the ratio of first solvent to second solvent is preferably 1:9 to 7:3.
  • a metal element having catalytic hydrogenation ability (hereinafter referred to as "specific metal component") can be mentioned.
  • Specific metal components include, but are not limited to, nickel, cobalt, iron, ruthenium, rhodium, palladium, platinum, iridium, copper, silver, molybdenum, tungsten, chromium, and rhenium.
  • the specific metal component may be in a metal state or a cation state as long as it exhibits hydrogenation ability. Among these, the metal state is generally preferable because it has a stronger hydrogenation ability and is stable in a reducing atmosphere.
  • the specific metal components can be used singly or in combination of two or more in a state contained in the solid catalyst.
  • the hydrogenation catalyst is preferably a solid catalyst supporting one or more selected from the group consisting of palladium, platinum, ruthenium, rhodium and nickel, particularly preferably palladium. It is a supported solid catalyst.
  • raw materials for these specific metal components there are no particular restrictions on the raw materials for these specific metal components, and those used as raw materials when preparing catalysts by conventionally known methods can be employed.
  • Such raw materials include, for example, hydroxides, oxides, fluorides, chlorides, bromides, iodides, sulfates, nitrates, acetates, ammine complexes, and carbonyl complexes of the respective metal elements. These may be used alone or in combination of two or more.
  • a specific metal component can be used alone or in combination with a metal that does not have catalytic hydrogenation ability.
  • catalysts such as palladium black and platinum black, which are composed of fine metal powders of specific metal components, and forming alloys of specific metal components, aluminum, and small amounts of additives, and then forming alloys with aluminum and small amounts of additives.
  • a sponge catalyst prepared by partially leaching can be mentioned.
  • lithium, sodium, potassium, rubidium, and cesium as alkali metal elements, magnesium, calcium, strontium, and barium as alkaline earth metal elements, and fluorine as a halogen element.
  • chlorine, bromine and iodine, and a compound of one or more elements selected from the group consisting of mercury, lead, bismuth, tin, tellurium and antimony as auxiliary additive elements (hereinafter abbreviated as specific additive components), It can also be used by being added to the catalyst together with the specific metal components mentioned above.
  • raw materials for these specific additive components there are no particular restrictions on the raw materials for these specific additive components, and those used as raw materials when preparing catalysts by conventionally known methods can be employed.
  • Such raw materials include, for example, hydroxides, oxides, fluorides, chlorides, bromides, iodides, sulfates, nitrates, acetates and ammine complexes of the respective metal elements. These may be used alone or in combination of two or more.
  • the method of adding the specific additive component or the ratio of the specific additive component to the specific metal component there are no particular restrictions on the method of adding the specific additive component or the ratio of the specific additive component to the specific metal component.
  • a specific metal component can also be used in combination with a nonmetallic substance.
  • nonmetallic substances include mainly elements, carbides, nitrides, oxides, hydroxides, sulfates, carbonates, and phosphates (hereinafter referred to as "specific nonmetallic components").
  • Specific examples include graphite, diamond, activated carbon, silicon carbide, silicon nitride, aluminum nitride, boron nitride, boron oxide, aluminum oxide (alumina), silicon oxide (silica), titanium oxide, zirconium oxide, hafnium oxide, Lanthanum oxide, cerium oxide, yttrium oxide, niobium oxide, magnesium silicate, calcium silicate, magnesium aluminate, calcium aluminate, zinc oxide, chromium oxide, aluminosilicate, aluminosilicophosphate, aluminophosphate, borophosphate, magnesium phosphate , calcium phosphate, strontium phosphate, hydroxyapatite (calcium hydroxyphosphate), chlorinated apatite, fluorinated apatite, calcium sulfate, barium sulfate and barium carbonate.
  • the specific nonmetallic components may be used alone or in combination of two or more. When two or more types are used in combination, there are no particular restrictions on the combination, mixing ratio, or form, and they can be used in the form of a mixture of individual compounds, a composite compound, or a double salt.
  • specific nonmetallic components that can be easily obtained at low cost are preferred.
  • Preferred as such specific nonmetallic components are zirconium compounds, aluminum compounds, and apatite compounds, and more preferred are zirconium compounds and apatite compounds. Particularly preferred among them are zirconium oxide and hydroxyapatite (calcium hydroxyphosphate).
  • a part or all of these specific nonmetallic components may be modified or ion-exchanged using the specific additive components described above.
  • specific non-metal component carbides, nitrides, oxides, etc. of specific metal components can also be used.
  • oxides such as nickel oxide, iron oxide, cobalt oxide, molybdenum oxide, tungsten oxide and chromium oxide.
  • a specific metal component may be used alone, or a specific metal component and a specific non-metal component may be used in combination.
  • specific additive components may be included.
  • the method for producing the hydrogenation catalyst used in some embodiments of the present invention is not particularly limited, and conventionally known methods can be used. Examples include a method in which a raw material compound for a specific metal component is impregnated onto a specific non-metal component (support method), a method in which a raw material compound for a specific metal component and a raw material compound for a specific non-metal component are dissolved together in an appropriate solvent.
  • Examples include a method of simultaneously precipitating using an alkali compound or the like (co-precipitation method), and a method of mixing and homogenizing the raw material compound of the specific metal component and the specific non-metal component in an appropriate ratio (kneading method).
  • the specific metal component may be prepared in a cation state and then subjected to a reduction treatment to be converted into a metal state.
  • reducing method and reducing agent for this purpose, conventionally known ones can be used, and there are no particular limitations.
  • Reducing agents include, for example, hydrogen gas, carbon monoxide gas, ammonia, reducing inorganic gases such as hydrazine, phosphine and silane, lower oxygenates such as methanol, formaldehyde and formic acid, sodium borohydride and hydride. Examples include hydrides such as lithium aluminum.
  • the specific metal component is converted into the metal state.
  • the reduction treatment conditions at this time can be set to suitable conditions depending on the type and amount of the specific metal component and reducing agent.
  • This reduction treatment operation may be performed using a separate catalytic reduction device before the hydrogenation reduction in the production method according to some embodiments of the present invention, and the production method according to some embodiments of the present invention It may be carried out before the start of the reaction or simultaneously with the reaction operation in the reactor used for the reaction.
  • the metal content and shape of the hydrogenation catalyst used in some embodiments of the present invention there are no particular limitations on the metal content and shape of the hydrogenation catalyst used in some embodiments of the present invention. Its shape may be powder or molded, and there are no particular restrictions on the shape or molding method. For example, spherical products, tablet molded products, extrusion molded products, and shapes obtained by crushing them into appropriate sizes can be appropriately selected and used.
  • a particularly preferred specific metal component is palladium, and a catalyst using this will be described in detail below.
  • the specific metal component is palladium, considering that palladium is a noble metal, it is economically desirable that the amount used be small and that palladium be used effectively. Therefore, it is preferable to disperse and support palladium on a catalyst carrier.
  • a palladium compound that is soluble in water or an organic solvent is suitable.
  • Such palladium compounds include, for example, palladium chloride, tetrachloropalladium salt, tetraamine palladium salt, palladium nitrate, and palladium acetate.
  • palladium chloride is preferred because it has high solubility in water or organic solvents and is easy to use industrially.
  • Palladium chloride can be used by being dissolved in an aqueous sodium chloride solution, dilute hydrochloric acid, aqueous ammonia, or the like.
  • Palladium or a palladium compound is immobilized on the catalyst carrier by adding a solution of the palladium compound to the catalyst carrier, or by immersing the catalyst carrier in a solution of the palladium compound.
  • Immobilization methods generally include adsorption onto a carrier, crystallization by solvent distillation, and precipitation using a reducing substance and/or basic substance that interacts with the palladium compound, and any suitable method may be used as appropriate. is used.
  • the content of palladium in the hydrogenation catalyst prepared by such a method is preferably 0.01 to 20% by mass, more preferably 0.1 to 20% by mass, based on the total amount of the hydrogenation catalyst, in terms of metal palladium.
  • the content is 10% by mass, more preferably 0.5 to 5% by mass.
  • the palladium content is 0.01% by mass or more, a more sufficient hydrogenation rate can be obtained, and the conversion rate of the aromatic vinyl compound polymer can be further increased.
  • the palladium content is 20% by mass or less, the dispersion efficiency of palladium in the hydrogenation catalyst becomes even higher, so palladium can be used more effectively.
  • palladium may be supported on the carrier in a cationic state rather than in a metallic state.
  • supported cationic palladium for example, present in the form of a palladium compound
  • Reducing agents include, for example, hydrogen gas, carbon monoxide gas, reducing inorganic gases such as ammonia and hydrazine, lower oxygenates such as methanol, formaldehyde and formic acid, carbonized gases such as ethylene, propylene, benzene and toluene.
  • Examples include hydrides such as hydrides, sodium borohydride and lithium aluminum hydride.
  • hydrides such as hydrides, sodium borohydride and lithium aluminum hydride.
  • the conditions for the reduction treatment at this time can be set to suitable conditions depending on the type and amount of the reducing agent.
  • This reduction treatment operation may be performed separately using a catalytic reduction device before the hydrogenation reduction in the production method of this embodiment, or before the start of the reaction or in the reactor used in the production method of this embodiment. It may be carried out simultaneously with the reaction operation.
  • zirconium compound used in some embodiments of the present invention is preferably one selected from the group consisting of zirconium oxide, zirconium hydroxide, zirconium carbonate, alkaline earth zirconate, rare earth zirconate, and zircon. They may be used alone or in combination of two or more.
  • a particularly preferred zirconium compound is zirconium oxide, and there are no particular restrictions on the method for producing it.
  • a commonly known method is to decompose an aqueous solution of a soluble zirconium salt with a basic substance to produce zirconium hydroxide or zirconium carbonate, which is then thermally decomposed.
  • the raw material for the zirconium compound at this time is not limited, and examples thereof include zirconium oxychloride, zirconium oxynitrate, zirconium chloride, zirconium sulfate, zirconium tetraalkoxide, zirconium acetate, and zirconium acetylacetonate.
  • Basic substances used for decomposition include, for example, ammonia, alkyl amines, ammonium carbonate, ammonium hydrogen carbonate, sodium hydroxide, sodium carbonate, sodium hydrogen carbonate, potassium hydroxide, potassium carbonate, potassium hydrogen carbonate. , magnesium hydroxide, calcium hydroxide, lanthanum hydroxide, yttrium hydroxide, and cerium hydroxide, and these may be used alone or in combination of two or more.
  • zirconium oxide As a specific nonmetallic component, there are no particular restrictions on its physical properties or shape. Furthermore, there is no particular restriction on the purity of zirconium oxide, and commercially available zirconium oxides with purity ranging from general purpose to high purity products can be used as appropriate.
  • a specific non-metallic component such as a zirconium compound
  • shape, particle size, physical properties of the carrier such as porosity, or the method of supporting the metal component.
  • shape, carrier physical properties, supporting method, etc. suitable for the reaction method and conditions can be selected and used as appropriate.
  • the hydrogenation catalyst is a hydrogenation catalyst after reduction treatment.
  • the concentration of the copolymer (aromatic polymer + nuclear hydrogenated polymer) in the solution during the nuclear hydrogenation reaction is usually 1 to 50% by mass, preferably 3 to 30% by mass, and more preferably 5 to 25% by mass. It is.
  • the upper limit of the copolymer concentration is set to a predetermined value or less, it is possible to avoid inconvenience in handling due to a decrease in the reaction rate and an increase in solution viscosity.
  • the hydrogenation (hydrogenation) reaction in the production method according to some embodiments of the present invention is carried out using a raw material solution in which an aromatic vinyl compound polymer is dissolved in a solvent. Any of these reactions may be used, and known techniques such as batch reaction and continuous flow reaction may be used.
  • the carrier particle size is usually in the range of 0.1 to 1,000 ⁇ m, preferably 1 to 500 ⁇ m, and more preferably 5 to 200 ⁇ m. Setting the particle size to a predetermined value or more facilitates catalyst separation after the hydrogenation reaction, and setting the upper limit of the particle size to a predetermined value or less prevents the reaction rate from decreasing.
  • Preferred reaction conditions are a temperature of 60 to 250°C, a hydrogen pressure of 3 to 30 MPa, and a reaction time of 3 to 30 hours.
  • the reaction temperature By setting the reaction temperature to a predetermined temperature or higher, the reaction rate becomes faster, and by setting the upper limit of the reaction temperature to a predetermined temperature or lower, side reactions such as polymer decomposition and solvent hydrogenolysis can be suppressed. Further, the reaction rate can be accelerated by setting the hydrogen pressure to a predetermined value or higher, but from an economical point of view, the upper limit is preferably about 30 MPa.
  • a nuclear hydrogenated polymer can be obtained by separating the hydrogenation catalyst and volatile components (solvent, etc.) from the polymer solution after the above hydrogenation reaction. Separation of the catalyst can be performed by known techniques such as filtration or centrifugation. Considering the influence on coloring and mechanical properties, it is desirable to reduce the concentration of residual catalyst metal in the polymer as much as possible, preferably 10 ppm or less, and more preferably 1 ppm or less.
  • the method of purifying the polymer by separating volatile components such as the solvent from the obtained nuclear hydrogenated polymer solution is as follows: 1) Continuously remove the solvent from the polymer solution to form a concentrated liquid, and heat it. 2) A method in which the polymer solution is extruded in a molten state to form pellets (also referred to as "devolatilization extrusion method"), 2) a method in which the solvent is evaporated from the polymer solution to obtain a lump, and then pelletized, 3) a method in which the polymer solution is made into pellets by extrusion in a poor solvent Known methods can be used, such as a method in which a poor solvent is added to a polymer solution, or a poor solvent is added to a polymer solution to precipitate the polymer, followed by pelletization, and 4) a method in which a lump is obtained by contacting with hot water and then pelletized.
  • a manufacturing method includes forming a polymeric resin by devolatilizing extrusion after a hydrogenation reaction.
  • devolatilizing extrusion for example, the polymerization liquid obtained in a polymerization tank is maintained or heated at 120°C to 180°C and introduced into a devolatilizing extruder equipped with a vent port to remove volatile components. It can be done with
  • the manufacturing method according to another preferred embodiment of the present invention further includes a concentration step between the hydrogenation reaction and the devolatilization extrusion.
  • the final hydrogenation rate (“final nuclear hydrogenation rate”, refers to “final nuclear hydrogenation rate”) of the hydrogenated polymer obtained by the method according to some embodiments of the present invention is not particularly limited, but is 90% or more. , 91% or more, 92% or more, 93% or more, 94% or more, 95% or more, 96% or more, 97% or more, 98% or more, 99% or more, 99.9% or more.
  • the final hydrogenation rate of the hydrogenated polymer is 93% or higher.
  • the final hydrogenation rate of the hydrogenated polymer is 95% or greater.
  • the final hydrogenation rate of the hydrogenated polymer is greater than or equal to 96%.
  • the final hydrogenation rate of the hydrogenated polymer is greater than or equal to 97%. In an even more preferred embodiment, the final hydrogenation rate of the hydrogenated polymer is greater than or equal to 98%. In an even more preferred embodiment, the final hydrogenation rate of the hydrogenated polymer is greater than or equal to 99%. In the most preferred embodiment, the final hydrogenation rate of the hydrogenated polymer is greater than or equal to 99.9%.
  • the hydrogenation rate can be determined by measuring UV spectra before and after the hydrogenation reaction, as described in Examples.
  • the initial hydrogenation rate (“initial nuclear hydrogenation rate”, “initial nuclear hydrogenation rate”) of the hydrogenated polymer is not particularly limited, but is 50% or more. , 55% or more, 60% or more, 65% or more, 70% or more, 75% or more, 80% or more, 85% or more, 90% or more, 92% or more, 93% or more, 94% or more, 95% or more, 96 % or more, 97% or more, 98% or more, 99% or more, 99.9% or more.
  • the initial hydrogenation rate of the hydrogenated polymer refers to, for example, 1 hour, 2 hours, 3 hours, 4 hours, 5 hours, 6 hours, and 7 hours after the start of the hydrogenation reaction. This refers to the hydrogenation rate at the time point, 8 hours, 9 hours, 10 hours, 15 hours, and 20 hours, but is not limited thereto.
  • the initial hydrogenation rate of the hydrogenated polymer is the hydrogenation rate 3 hours after the start of the hydrogenation reaction. In one embodiment of the present invention, the initial hydrogenation rate of the hydrogenated polymer is the hydrogenation rate 5 hours after the start of the hydrogenation reaction.
  • the initial hydrogenation rate of the hydrogenated polymer is the hydrogenation rate 20 hours after the start of the hydrogenation reaction.
  • the initial hydrogenation rate of the hydrogenated polymer is 50% or more. In a more preferred embodiment, the hydrogenated polymer has an initial hydrogenation rate of 55% or more. In an even more preferred embodiment, the hydrogenated polymer has an initial hydrogenation rate of 60% or more. In an even more preferred embodiment, the hydrogenated polymer has an initial hydrogenation rate of 65% or more. In an even more preferred embodiment, the hydrogenated polymer has an initial hydrogenation rate of 70% or more. In an even more preferred embodiment, the initial hydrogenation rate of the hydrogenated polymer is 75% or more. In an even more preferred embodiment, the hydrogenated polymer has an initial hydrogenation rate of 80% or more. In an even more preferred embodiment, the initial hydrogenation rate of the hydrogenated polymer is 85% or more. In the most preferred embodiment, the hydrogenated polymer has an initial hydrogenation rate of 90% or more. The hydrogenation rate can be determined by measuring UV spectra before and after the hydrogenation reaction, as described in Examples.
  • a method for producing an optical material including the method for producing the hydrogenated polymer described above.
  • a method for manufacturing an optical material includes: A method for producing a hydrogenated polymer by hydrogenating an aromatic ring of an aromatic vinyl compound-based polymer, the method comprising: The aromatic vinyl compound-based polymer includes a first monomer unit and a second monomer unit, The method includes: reducing the hydrogenation catalyst before use;
  • the present invention includes a method for producing a hydrogenated polymer, which includes obtaining a hydrogenated polymer by performing a hydrogenation reaction using the aromatic vinyl compound-based polymer, a solvent, and a hydrogenation catalyst after reduction treatment. Details of the method for producing the hydrogenated polymer are as explained above.
  • the hydrogenated polymer obtained by the method according to some embodiments of the present invention may be mixed with additives such as antioxidants, colorants, mold release agents, surfactants, antibacterial agents, etc., as appropriate, to form optical materials. It can be a thing. Since the resulting optical material composition has thermoplasticity, it is possible to precisely and economically manufacture optical articles through various thermoforming methods, such as extrusion molding, injection molding, and secondary processing molding of sheet molded bodies. It is. Specific uses of the optical article include, but are not limited to, various light guide plates and light guides, display front panels, plastic lens substrates, optical filters, optical films, lighting covers, illuminated signboards, and the like. In one embodiment of the invention, the optical material is an optical lens.
  • the evaluation method for the resin is as follows.
  • the nuclear hydrogenation rate was determined by UV spectrum measurements before and after the hydrogenation reaction. That is, by dissolving the resin using tetrahydrofuran (THF) as a solvent, measuring the absorption spectrum at 260 nm using a quartz cell, and weighing it using the copolymer resin before the nuclear hydrogenation reaction, the unhydrogenated aromatic ring can be determined. The percentage was calculated.
  • the device used for the measurement was an ultraviolet-visible spectrophotometer "GENESYS 10S" manufactured by Thermo, but it is not particularly limited as long as it is an equivalent device.
  • Weight average molecular weight (Mw) was determined by gel permeation chromatography (GPC).
  • GPC gel permeation chromatography
  • RI differential refractive index
  • THF solvent
  • calibration was performed using standard polystyrene.
  • the device used for the measurement is a high performance liquid chromatography system "Elite LaChrom" manufactured by Shimadzu Science, but is not particularly limited as long as it is an equivalent device.
  • Tgm glass transition point of the resin was determined by differential scanning calorimetry (DSC).
  • the instrument used for the measurement was "DSC7020” manufactured by SII (currently Hitachi High-Tech Science), but there is no particular limitation as long as it is an equivalent instrument.
  • Example 1 0.1 part by mass of 2.0% by mass Pd/ZrO 2 and 1.35 parts by mass of Swaclean 150 (manufactured by Maruzen Petrochemical Co., Ltd., C9C10 alkylcyclohexane mixture, hereinafter referred to as "SWC") were added to a reaction vessel.
  • the nuclear hydrogenation rate of the obtained hydrogenated resin was 84.4% at 3 hours, 92.3% at 5 hours, and 96.9 at 20 hours. %, the final nuclear hydrogenation rate at 44 hours was 98.7%, the weight average molecular weight was 122,000, and the Tg was 145°C.
  • Examples 2 to 7 The catalyst was pre-reduced in the same manner as in Example 1 except that the conditions were changed to those shown in Table 1, and then a hydrogenation reaction was carried out to obtain a hydrogenated polymer.
  • ⁇ Comparative example 1> 5.0 parts by mass of the raw material polymer solution and 0.1 parts by mass of 2.0% by mass Pd/ZrO 2 were charged into a reaction vessel equipped with a stirring device, and heated with hydrogen for 44 hours at a hydrogen pressure of 9.1 MPa and a temperature of 200°C. An addition reaction was performed. After the hydrogenation reaction, the catalyst was removed from the polymer solution by filtration, and then the reaction solution was dropped into excess isopropanol to precipitate the resin. Dry resin powder was obtained by drying the obtained resin powder under reduced pressure. The resulting resin had a nuclear hydrogenation rate of 79.1% at 3 hours, a nuclear hydrogenation rate of 85.0% at 5 hours, and a nuclear hydrogenation rate of 97.9% at 20 hours. The final nuclear hydrogenation rate at 44 hours was 98.3%, the weight average molecular weight was 116,000, and the Tg was 146°C.
  • FIG. 1 shows the relationship between hydrogenation reaction time and nuclear hydrogenation rate for Resin 1. It can be seen that the reaction rate of the hydrogenation reaction can be improved by pre-reducing the hydrogenation catalyst and using it as a hydrogenation catalyst after reduction treatment.
  • the speed of the hydrogenation reaction is improved, thereby efficiently It has been found that it can be manufactured. Furthermore, by shortening the reaction time, it was possible to reduce damage to the polymer, such as a decrease in molecular weight. Furthermore, the hydrogenated polymer obtained by the method of the present invention has sufficient heat resistance and is suitable for use in optical materials.

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