WO2022191288A1 - 重合体の製造方法、ラジカル重合用組成物及びラジカル重合制御剤 - Google Patents
重合体の製造方法、ラジカル重合用組成物及びラジカル重合制御剤 Download PDFInfo
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- WO2022191288A1 WO2022191288A1 PCT/JP2022/010635 JP2022010635W WO2022191288A1 WO 2022191288 A1 WO2022191288 A1 WO 2022191288A1 JP 2022010635 W JP2022010635 W JP 2022010635W WO 2022191288 A1 WO2022191288 A1 WO 2022191288A1
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- QJWFJOSRSZOLKK-UHFFFAOYSA-N prop-2-enamide Chemical compound NC(=O)C=C.NC(=O)C=C QJWFJOSRSZOLKK-UHFFFAOYSA-N 0.000 description 1
- BWJUFXUULUEGMA-UHFFFAOYSA-N propan-2-yl propan-2-yloxycarbonyloxy carbonate Chemical compound CC(C)OC(=O)OOC(=O)OC(C)C BWJUFXUULUEGMA-UHFFFAOYSA-N 0.000 description 1
- 125000004368 propenyl group Chemical group C(=CC)* 0.000 description 1
- 125000002572 propoxy group Chemical group [*]OC([H])([H])C(C([H])([H])[H])([H])[H] 0.000 description 1
- PNXMTCDJUBJHQJ-UHFFFAOYSA-N propyl prop-2-enoate Chemical compound CCCOC(=O)C=C PNXMTCDJUBJHQJ-UHFFFAOYSA-N 0.000 description 1
- 125000004076 pyridyl group Chemical group 0.000 description 1
- 150000004053 quinones Chemical class 0.000 description 1
- 239000007870 radical polymerization initiator Substances 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- XWGJFPHUCFXLBL-UHFFFAOYSA-M rongalite Chemical compound [Na+].OCS([O-])=O XWGJFPHUCFXLBL-UHFFFAOYSA-M 0.000 description 1
- 125000005920 sec-butoxy group Chemical group 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 125000003808 silyl group Chemical group [H][Si]([H])([H])[*] 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 229940079827 sodium hydrogen sulfite Drugs 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000000020 sulfo group Chemical group O=S(=O)([*])O[H] 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000000375 suspending agent Substances 0.000 description 1
- 238000010557 suspension polymerization reaction Methods 0.000 description 1
- 235000002906 tartaric acid Nutrition 0.000 description 1
- 239000011975 tartaric acid Substances 0.000 description 1
- 125000004213 tert-butoxy group Chemical group [H]C([H])([H])C(O*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 1
- NMOALOSNPWTWRH-UHFFFAOYSA-N tert-butyl 7,7-dimethyloctaneperoxoate Chemical compound CC(C)(C)CCCCCC(=O)OOC(C)(C)C NMOALOSNPWTWRH-UHFFFAOYSA-N 0.000 description 1
- ISXSCDLOGDJUNJ-UHFFFAOYSA-N tert-butyl prop-2-enoate Chemical compound CC(C)(C)OC(=O)C=C ISXSCDLOGDJUNJ-UHFFFAOYSA-N 0.000 description 1
- 125000001973 tert-pentyl group Chemical group [H]C([H])([H])C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 1
- 229920003046 tetrablock copolymer Polymers 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 125000003396 thiol group Chemical group [H]S* 0.000 description 1
- KOZCZZVUFDCZGG-UHFFFAOYSA-N vinyl benzoate Chemical compound C=COC(=O)C1=CC=CC=C1 KOZCZZVUFDCZGG-UHFFFAOYSA-N 0.000 description 1
- 229920003169 water-soluble polymer Polymers 0.000 description 1
Images
Classifications
-
- 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
- C08F293/00—Macromolecular compounds obtained by polymerisation on to a macromolecule having groups capable of inducing the formation of new polymer chains bound exclusively at one or both ends of the starting macromolecule
-
- 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
- C08F2/00—Processes of polymerisation
- C08F2/38—Polymerisation using regulators, e.g. chain terminating agents, e.g. telomerisation
-
- 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
- C08F216/00—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 alcohol, ether, aldehydo, ketonic, acetal or ketal radical
- C08F216/02—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 alcohol, ether, aldehydo, ketonic, acetal or ketal radical by an alcohol radical
- C08F216/04—Acyclic compounds
- C08F216/06—Polyvinyl alcohol ; Vinyl alcohol
-
- 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
- C08F218/00—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 acyloxy radical of a saturated carboxylic acid, of carbonic acid or of a haloformic acid
- C08F218/02—Esters of monocarboxylic acids
- C08F218/04—Vinyl esters
- C08F218/08—Vinyl acetate
-
- 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
- C08F8/12—Hydrolysis
Definitions
- the present invention relates to a method for producing a polymer having a polymerization step of polymerizing polymerizable monomers by controlled radical polymerization.
- the present invention also relates to a composition for radical polymerization and a radical polymerization controller used in such a production method.
- Polyvinyl alcohol resin is a crystalline water-soluble polymer material, and its excellent water solubility and film properties (strength, oil resistance, film-forming properties, oxygen gas barrier properties, etc.) can be used as emulsifiers, suspension agents, Widely used as surfactants, fiber processing agents, various binders, paper processing agents, adhesives, films, etc.
- Conventional polyvinyl alcohols with different degrees of saponification and polymerization are used depending on the application.
- various modified polyvinyl alcohols have been proposed in which special functions are imparted by introducing functional groups into polyvinyl alcohol.
- Polyvinyl alcohol is industrially produced by saponifying polyvinyl acetate obtained by radical polymerization of vinyl acetate.
- radical polymerization reaction of vinyl acetate various side reactions such as chain transfer reaction and recombination termination reaction occur simultaneously during polymerization, so the molecular arrangement and terminal structure of the resulting polyvinyl acetate (and polyvinyl alcohol) are precisely controlled. is generally difficult to do.
- Non-Patent Document 1 by polymerizing vinyl acetate in the presence of cobalt (II) acetylacetonate, the number average molecular weight (Mn) is 99,000 and the molecular weight distribution (Mw/Mn) is 1.33. reported the synthesis of polyvinyl acetate.
- polyvinyl alcohol obtained by controlled radical polymerization has a problem of being markedly colored. It is described that polyvinyl alcohol with reduced coloration can be obtained by contacting with an aqueous solution containing a water-soluble ligand to remove the cobalt complex by extraction and then saponifying.
- the polymerization method using such a metal complex has the drawback that it is not easy to completely remove the complex used from the resulting polymer.
- Many transition metals are highly toxic, and the toxicity of transition metals remaining in molded articles using the resulting polymer may pose an environmental problem. ⁇ It was difficult to use it as a medical material.
- the toxicity of complexes that are no longer needed or that are removed from the polymer after the reaction has become an environmental concern.
- a large amount of extract must be used to remove the complex, and the process is complicated, resulting in a problem of high cost.
- metal complexes usually have the problem of being expensive and requiring complicated synthesis.
- a living radical polymerization method that does not require the use of a metal complex is also known.
- methods using nitroxyl-based, iodine-based, or dithioester-based compounds are known.
- these methods have the disadvantage that a special protecting group must be introduced into the growing chain of the polymer, and this protecting group is very expensive.
- the polymerization reaction must be carried out at high temperatures (eg, 110° C. or higher).
- the polymerization controllability of the vinyl ester is insufficient and it is difficult to obtain a high molecular weight product.
- the resulting polymer tends to have undesirable properties, such as being colored or having an odor.
- it is not easy to completely remove the used compounds from the product and there is a risk that residual organic halogen compounds, organic sulfur compounds, and the like may cause health and environmental problems.
- cinnamic acid and its derivatives exist widely in nature and are generally used industrially as food additives and flavoring agents.
- cinnamic acids have unsaturated double bonds, they are difficult to homopolymerize, and it is known that radical polymerization of cinnamic acid monomers proceeds under limited conditions such as copolymerization with fumarate diesters ( Non-Patent Document 2, Patent Document 2).
- Patent Document 3 it is known that by post-adding cinnamic acids to a polyvinyl acetate solution after polymerization, polyvinyl alcohol in which fish eyes and odors are suppressed during molding can be obtained.
- Patent Document 3 there is no known example of using cinnamic acids as control agents for controlled radical polymerization, and such a function has not been assumed academically.
- the present invention has been made to solve the above problems, and provides a method for producing a polymer that is low in toxicity, environmentally friendly, has high polymerization controllability, yields a high molecular weight polymer, and is low in cost.
- Another object of the present invention is to provide a composition for radical polymerization and a radical polymerization controller which are suitably used in such a production method.
- the above problem is a polymerization step of obtaining a polymer by conducting controlled radical polymerization of a monomer (Y) in the presence of an organic compound (A) represented by the following formula (I) and a radical generator (B). and the molar ratio (B/A) of (B) to (A) is 0.5-20.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed.
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- R 1 is preferably an aryl group. It is also preferred that the organic compound (A) is the E form. It is also preferred that the organic compound (A) is represented by the following formula (IV).
- R3 has the same definition as in formula (II) above, and R4 is a hydrogen atom, an alkyl group, an alkoxy group, or a hydroxyl group.
- R4 is preferably a hydrogen atom. It is also preferred that R3 is a methoxy group or a hydroxyl group. It is also preferable that the molar ratio (Y/A) of the monomer (Y) to the organic compound (A) is 300-30,000.
- the monomer (Y) is an olefin, vinyl ester, acrylic acid, acrylic acid ester, acrylamide-based monomer, styrene-based monomer, N-vinylamide-based monomer or dicarboxylic acid-based monomer. is preferably included.
- the production method includes a polymerization step of obtaining a vinyl ester-based polymer by performing controlled radical polymerization of a vinyl ester in the presence of an organic compound (A) and a radical generator (B); It is more preferable to have a saponification step of saponifying the ester polymer to obtain the vinyl alcohol polymer.
- the controlled radical polymerization of the vinyl ester and the controlled radical polymerization of the vinyl ester and a monomer other than the vinyl ester are sequentially performed. It is more preferable to have a polymerization step of obtaining a vinyl ester block copolymer and a saponification step of saponifying the obtained vinyl ester block copolymer to obtain a vinyl alcohol block copolymer.
- the above object includes an organic compound (A) represented by the following formula (I) and a radical generator (B), wherein the molar ratio (B/A) of (B) to (A) is 0.5 to 20. It is also solved by providing a composition for radical polymerization.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed.
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- the composition for radical polymerization further contains the monomer (Y), and the molar ratio (Y/A) of the monomer (Y) to the organic compound (A) is 300 to 30,000.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed.
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- a preferred embodiment of the present invention is a polymer having a terminal structure represented by formula (V) or (VI) below.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed. * indicates a bond.
- R 1 and R 2 have the same definitions as in formula (V) above, and * indicates a bond. ]
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- the organic compound (A) used in the production method of the present invention is highly safe, has high polymerization controllability, and is inexpensive. Therefore, according to the production method, it is possible to synthesize a high-molecular-weight and highly safe polymer while precisely controlling the molecular arrangement, the terminal structure, and the like. Moreover, the production method is low in toxicity, environmentally friendly, does not require a step of removing the organic compound (A), and is low in cost.
- the composition for radical polymerization and the radical polymerization controller of the present invention are suitably used in such a method for producing a polymer.
- FIG. 1 is a graph plotting the number average molecular weight (Mn) against the conversion rate of vinyl acetate in Example 1.
- the present invention comprises a polymerization step of obtaining a polymer by conducting controlled radical polymerization of a monomer (Y) in the presence of an organic compound (A) represented by the following formula (I) and a radical generator (B). and the molar ratio (B/A) of (B) to (A) is 0.5-20.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed.
- a polymer is obtained by conducting controlled radical polymerization of the monomer (Y) in the presence of the organic compound (A) represented by the formula (I) and the radical generator (B).
- the controlled radical polymerization employed in the production method of the present invention is a polymerization reaction in which the reaction proceeds in an equilibrium state between a growing radical terminal (active species) and a covalently bonded species (dormant species) bound to a control agent. That is.
- the organic compound (A) represented by the above formula (I) functions as a control agent.
- Radical polymerization is highly controlled by using the organic compound (A), so that a high-molecular-weight polymer can be obtained while precisely controlling the molecular arrangement, terminal structure, and the like.
- the organic compound (A) is inexpensive, industrially used as a food additive and flavoring agent, and is highly safe, so a step of removing the organic compound (A) is not required. Therefore, the manufacturing method of the present invention is environmentally friendly and excellent in terms of cost.
- R 1 is an alkenyl group or an aryl group, preferably an aryl group.
- the aryl group preferably has 6 to 15 carbon atoms.
- the number of carbon atoms is more preferably 13 or less, more preferably 12 or less, and particularly preferably 10 or less.
- Examples of the aryl group include a phenyl group, a biphenyl group, a naphthyl group, an anthryl group, an indenyl group, a fluorenyl group, a phenanthryl group, an indacenyl group, a phenalenyl group, an azulenyl group, a pyridyl group, and a furyl group, with a phenyl group being preferred. .
- the aryl group may have a substituent as long as the effects of the present invention are not impaired.
- substituents include alkoxy groups, amino groups (including monoalkylamino groups and dialkylamino groups), carboxyl groups, ester groups, silyl groups, sulfanyl groups, cyano groups, nitro groups, sulfo groups, formyl groups, An aryl group, a halogen atom, a hydroxyl group, an ether group, an alkenyl group and the like can be mentioned, and an alkyl group and an alkoxy group are preferred.
- the alkyl group and alkoxy group include those described later as those used as R 3 in formula (II). From the standpoint of being more environmentally friendly and safer, the aryl group preferably has no substituent.
- the alkenyl group preferably has 2 to 10 carbon atoms.
- the carbon number is more preferably 8 or less.
- the number of carbon atoms is more preferably 4 or more.
- the alkenyl group may be a linear or branched alkenyl group, or may be a cyclic cycloalkenyl group.
- alkenyl groups include linear and branched alkenyl groups such as vinyl, allyl, methylvinyl, propenyl, butenyl, pentenyl, and hexenyl; cyclopropenyl, cyclobutenyl, cyclopentenyl, A cycloalkyl group such as a cyclohexenyl group can be mentioned.
- the alkenyl group is preferably a cycloalkenyl group, more preferably a cyclohexenyl group.
- the alkenyl group may have a substituent as long as the effects of the present invention are not impaired. Examples of such substituents include those described above as substituents for the aryl group.
- R 2 is a group represented by formula (II) or (III) below, preferably a group represented by formula (II) below.
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- R3 represents a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group (including monoalkylamino groups and dialkylamino groups), a nitro group, a cyano group, an acetyl is preferably a hydrogen atom, an alkyl group, an aryl group, an alkoxy group, or a hydroxyl group, more preferably an alkyl group, an alkoxy group, or a hydroxyl group, and an alkoxy group or a hydroxyl group. Most preferably there is.
- the number of carbon atoms in the alkyl group is preferably 1-10.
- the number of carbon atoms is more preferably 8 or less, more preferably 6 or less, even more preferably 4 or less, and particularly preferably 2 or less.
- the alkyl group may be a linear or branched alkyl group, or may be a cyclic cycloalkyl group.
- methyl group, ethyl group, n-propyl group, isopropyl group, n-butyl group, isobutyl group, sec-butyl group and tert-butyl group are preferred, and methyl group is more preferred.
- the alkyl group may have a substituent as long as the effects of the present invention are not impaired. Examples of such substituents include those described above as substituents for the aryl group used as R 1 . From the standpoint of being more environmentally friendly and safer, it is preferred that the alkyl group does not have a substituent.
- the aryl group preferably has 6 to 15 carbon atoms.
- the number of carbon atoms is more preferably 13 or less, more preferably 12 or less, and particularly preferably 10 or less.
- Examples of the aryl group include those described above for use as R 1 .
- the alkoxy group preferably has 1 to 10 carbon atoms.
- the number of carbon atoms is more preferably 8 or less, more preferably 6 or less, still more preferably 4 or less, and particularly preferably 1.
- Examples of the alkoxy group include methoxy, ethoxy, propoxy, isopropoxy, butoxy, isobutoxy, sec-butoxy, tert-butoxy, pentyloxy, isopentyloxy, neopentyloxy, and hexyl.
- the alkoxy group may have a substituent as long as it does not impair the effects of the present invention.
- substituents include those described above as substituents for the aryl group used as R 1 . From the standpoint of being more environmentally friendly and safer, it is preferred that the alkoxy group does not have a substituent.
- the organic compound (A) represented by the above formula (I) may be an E-isomer or a Z-isomer, but it should be an E-isomer, that is, an E-isomer organic compound (A) and a radical It is preferred to carry out the controlled radical polymerization of the monomer (Y) in the presence of the generator (B).
- the Z-form organic compound (A) may be present as an optional component.
- the molar ratio of E-form to the total of E-form and Z-form (E/E+Z) is preferably more than 0.5, preferably 0.7 or more. is more preferable, and 0.8 or more is even more preferable.
- the molar ratio (B/E+Z) of the radical generator (B) to the total of the E-isomer and Z-isomer is in the same range as the molar ratio (B/A) described later. It is also preferable that the molar ratio (Y/E+Z) of the monomer (Y) to the sum of the E-isomer and Z-isomer is in the same range as the molar ratio (Y/A) described later.
- organic compound (A) represented by the above formula (I) is represented by the following formula (IV).
- R3 has the same definition as in formula (II) above, and R4 is a hydrogen atom, an alkyl group, an alkoxy group, or a hydroxyl group.
- R4 is a hydrogen atom, an alkyl group, an alkoxy group or a hydroxyl group. Among them, it is preferable that R 4 is a hydrogen atom.
- the bonding position of R4 in the phenyl group is not particularly limited. Examples of the alkyl group and alkoxy group used as R 4 include those described above as those used as R 3 .
- R 1 and R 2 may be linked together to form a ring.
- Examples of the organic compound (A) in which such a ring is formed include those represented by the following formula (VII).
- Azo radical generators include 2,2′-azobisisobutyronitrile, 2,2′-azobis(2,4-dimethylvaleronitrile), 2,2′-azobis(4-methoxy-2,4 -dimethylvaleronitrile) and the like
- peroxide radical generators include peroxydicarbonate compounds such as diisopropyl peroxydicarbonate, di-2-ethylhexyl peroxydicarbonate, and diethoxyethyl peroxydicarbonate; -Perester compounds such as butyl peroxyneodecanate, ⁇ -cumyl peroxyneodecanate, t-butyl peroxyneodecanate; acetylcyclohexylsulfonyl peroxide, diisobutyryl
- a radical generator can be obtained by combining the above radical generator with a peroxide such as potassium persulfate, ammonium persulfate, or hydrogen peroxide.
- Redox radical generators include those obtained by combining the above peroxides with reducing agents such as sodium hydrogen sulfite, sodium hydrogen carbonate, tartaric acid, L-ascorbic acid and Rongalit.
- Examples of polymerization methods include known methods such as bulk polymerization, solution polymerization, suspension polymerization, and emulsion polymerization. Among them, a bulk polymerization method in which polymerization is performed without a solvent or a solution polymerization method in which polymerization is performed in various organic solvents are usually employed. A bulk polymerization method that does not use a solvent or a dispersion medium is preferable from the viewpoint of suppressing the reduction of growing radical terminals due to a chain transfer reaction to a solvent or a dispersion medium. On the other hand, in some cases, solution polymerization is preferable from the viewpoint of adjusting the viscosity of the reaction liquid and controlling the polymerization rate.
- Organic solvents used as solvents for solution polymerization include esters such as methyl acetate and ethyl acetate; aromatic hydrocarbons such as benzene and toluene; lower alcohols such as methanol and ethanol; carbonate esters such as dimethyl carbonate and diethyl carbonate. is mentioned.
- esters, aromatic hydrocarbons, and dimethyl carbonate are preferably used in order to prevent chain transfer.
- the monomer (Y) contains vinyl acetate
- alkali treatment is often performed in methanol after polymerization, and methanol is also preferably used as a polymerization solvent in consideration of processability.
- the amount of solvent to be used may be determined in consideration of the number average molecular weight of the target polymer and the viscosity of the reaction solution. For example, the mass ratio [solvent/monomer (Y)] is selected from the range of 0.01-10.
- radicals generated by decomposition of the radical generator (B) are combined with a small number of monomers (Y) to form short-chain polymer radicals at the growing ends of It combines with the organic compound (A) to produce a dormant species in which the organic compound (A) is covalently bonded to the terminal of the polymer.
- a short-chain polymer is produced and converted to a dormant species, and the increase in molecular weight does not substantially proceed. This period is called an induction period.
- the time required for the polymerization step of the monomer (Y) is usually 0.5 to 30 hours including the induction period and the growth period.
- the amount of the organic compound (A) added to the reaction solution is determined in consideration of the desired number average molecular weight and conversion rate.
- the molar ratio (Y/A) of the monomer (Y) to the organic compound (A) in the polymerization step is preferably 300 or more, more preferably 1000 or more, and 2000 or more. More preferably, 4000 or more is even more preferable, and 6000 or more is particularly preferable.
- the molar ratio (Y/A) is preferably 30,000 or less, more preferably 25,000 or less, and even more preferably 20,000 or less, from the viewpoint of improving the activity rate of growing radical terminals.
- the molar ratio (Y/A) is determined using the total amount of each component.
- the ratio (B/A) of the radical generator (B) to the organic compound (A) in the polymerization step is 0.5-20. If the number of moles of the generated radicals is not greater than the number of moles of the organic compound (A), the polymerization reaction proceeds only by the mechanism of thermal dissociation of the organic compound (A) from the dormant species. becomes extremely small. Therefore, considering that the radical generator (B) generates two radicals, the ratio (B/A) of the radical generator (B) to the organic compound (A) in the polymerization step is 0.5 or more.
- the amount of active radicals supplied from a radical generator generally depends on the efficiency of the radical generator (initiator efficiency), in practice some radical generators are deactivated without being used to form a dormant. Therefore, the molar ratio (B/A) of (B) to (A) is preferably 0.6 or more, more preferably 0.8 or more. On the other hand, if the number of moles of the generated radicals is too much larger than the number of moles of the organic compound (A), the proportion of uncontrolled radical polymerization will increase and the polymerization controllability will decrease.
- the molar ratio (B/A) of (B) to (A) is preferably 15 or less, more preferably 10 or less, and even more preferably 5 or less.
- the molar ratio (B/A) is determined using the total amount of each component.
- the monomer contained in the monomer (Y) used in the polymerization step is not particularly limited as long as it has radical polymerizability, but olefins such as ethylene, propylene and isobutylene; vinyl chloride, vinyl fluoride, Halogenated olefins such as vinylidene chloride and vinylidene fluoride; vinyl formate, vinyl acetate, vinyl trifluoroacetate, vinyl propionate, vinyl valerate, vinyl butyrate, vinyl isobutyrate, vinyl pivalate, vinyl caprate, vinyl laurate, Vinyl esters such as vinyl stearate, vinyl benzoate, vinyl versatate; vinylidene cyanide; acrylic acid; methacrylic acid; methyl acrylate, ethyl acrylate, N-propyl acrylate, i-propyl acrylate, N- acrylate Acrylic esters such as butyl, i-butyl acrylate, t-butyl acrylate, 2-ethyl
- N-vinylamide-based monomers allyl acetate, allyl chloride, 3,4-diacetoxy-1-butene, 2-methylene-1,3-propanediol, 2-methylene-1,3-propanediol diacetate, allyl Allyl-based monomers such as alcohol and dimethylallyl alcohol; Vinyl cyanide-based monomers such as acrylonitrile and methacrylonitrile; vinyl ether monomers such as ether; dicarboxylic acid monomers such as maleic acid, monomethyl maleate, dimethyl maleate, maleic anhydride, itaconic acid, monomethyl itaconate, dimethyl itaconate and itaconic anhydride are preferred, Olefins, vinyl esters, acrylic acid, acrylic acid esters, acrylamide monomers, styrene monomers, N-vinylamide monomers or dicarboxylic acid monomers are more preferable, vinyl ester styrene or N-vinylpyr
- the monomer (Y) may contain one of these monomers, or two or more thereof.
- Monomer (Y) preferably contains one of these monomers as a main component.
- the main component means the monomer contained in the monomer (Y) that has the highest content.
- the content of the monomer that is the main component in the monomer (Y) is preferably 30 mol% or more, more preferably 50 mol% or more, even more preferably 70 mol% or more, and particularly preferably 80 mol% or more.
- vinyl acetate is preferable as the vinyl ester.
- acrylic acid ester methyl acrylate is preferable from an economical point of view.
- the monomer (Y) one type of monomer may be used to obtain a homopolymer, or two or more types of monomers may be used to obtain a copolymer. good too.
- the copolymer may be either a random copolymer or a block copolymer.
- the polymer obtained by the production method of the present invention may be either branched or linear. Preferably.
- the method for mixing the organic compound (A), the radical generator (B) and the monomer (Y) is not particularly limited as long as the method can generate a dormant species and control the increase in the molecular weight of the polymer.
- a method of adding an organic compound (A) and a radical generator (B) to a monomer (Y) a method of mixing an organic compound (A) and a radical generator (B), and then obtaining A method of mixing the mixture and the monomer (Y), a method of mixing the organic compound (A), the radical generator (B) and the monomer (Y) at once, the organic compound (A) and the monomer (Y ), and then mixing the resulting mixture with the radical generator (B).
- the organic compound (A), the radical generator (B), and the monomer (Y) may be divided and mixed. For example, by mixing a part of the monomer (Y) with the organic compound (A) and the radical generator (B), a dormant species in which the organic compound (A) is covalently bonded to the terminal of the short chain polymer is generated. and then the dormant species and the remainder of the monomer (Y) are mixed to increase the molecular weight.
- the dormant species may be isolated as a macroinitiator and then mixed with the rest of the monomer (Y) to increase the molecular weight.
- the polymerization temperature is preferably 0 to 80°C, for example. If the polymerization temperature is lower than 0°C, the polymerization rate will be insufficient and productivity may decrease. From this point of view, the polymerization temperature is more preferably 10° C. or higher, more preferably 20° C. or higher. On the other hand, if the polymerization temperature exceeds 80°C, the controllability of the radical polymerization may deteriorate. From this point of view, the polymerization temperature is more preferably 70° C. or lower, more preferably 65° C. or lower.
- the number average molecular weight (Mn) (measured value) relative to the theoretical number average molecular weight (theoretical Mn) of the polymer when the conversion rate of the monomer (Y) is 5.0%
- the ratio (Mn/theoretical Mn) is preferably 10.0 or less, more preferably 8.0 or less, still more preferably 6.0 or less, even more preferably 5.0 or less, and 4.5 is particularly preferably 4.0 or less, and most preferably 4.0 or less.
- the polymer ratio (Mn/theoretical Mn) when the conversion rate of the monomer (Y) is 5.0% is preferably 0.5 or more, and 0.5%.
- the conversion rate of the monomer (Y) at the end of the polymerization is not particularly limited, and may be adjusted according to the amount of the organic compound (A) and the monomer (Y) added, the desired number average molecular weight, and the like. , usually from 3 to 50%.
- the conversion rate is preferably 10% or more, more preferably 20% or more.
- the number average molecular weight (Mn) (measured value) of the polymer when the conversion rate is 5.0% is obtained as follows. GPC (gel permeation chromatography) measurement of the polymer is performed multiple times from the start of polymerization to the end of polymerization (however, at least once when the conversion rate is 1.0% or more and less than 5.2%).
- the theoretical number average molecular weight (theoretical Mn) of the polymer is determined by the following formula.
- Theoretical Mn molar ratio (Y/A) of monomer (Y) to organic compound (A) ⁇ average molecular weight of monomer (Y) [g/mol] ⁇ (conversion rate [%]/100)
- a block copolymer in the polymerization step, in the presence of the organic compound (A) and the radical generator (B), the controlled polymerization of the monomer (Ya) and the monomer other than the monomer (Ya) ( A block copolymer containing a polymer block (a) containing a monomer (Ya) unit and a polymer block (b) containing a monomer (Yb) unit is obtained by sequentially performing controlled polymerization of Yb) is preferably obtained, in the presence of the organic compound (A) and the radical generator (B), the controlled polymerization of the monomer (Ya) and the controlled polymerization of the monomer (Ya) and the monomer (Yb) By successively performing the Obtaining a copolymer is more preferable.
- the polymerization step will be described below.
- a monomer (Ya), optionally a monomer (Yc) other than the monomer (Ya) and the monomer (Yb), an organic compound (A) and a radical Polymerization of the monomer (Ya) is initiated by mixing the generator (B) by the method described above. Then, after the number average molecular weight of the polymer block (a) containing the monomer (Ya) reaches a target value, the monomer (Yb) is polymerized to convert the monomer (Yb) unit into Synthesis of polymer block (b) containing is carried out.
- the monomer (Yb) is added to the reaction solution and the monomer (Yb) is polymerized to obtain the monomer (Yb ) units may be synthesized.
- the monomer (Yb) is added to the reaction solution without removing the monomer (Ya), and the remaining monomer (Ya) and the monomer (Yb) are copolymerized.
- a copolymer block (ab) comprising monomeric (Ya) units and monomeric (Yb) units may be synthesized.
- an additional monomer (Ya) or another monomer (Yc) may be added as necessary.
- the monomer (Ya), the monomer (Yb), optionally another monomer (Yc), the organic compound (A) and the radical generator (B) are mixed to form a polymer.
- the monomer (Ya), the monomer (Yb), optionally another monomer (Yc), the organic compound (A) and the radical generator (B) are mixed to form a polymer.
- a diblock copolymer may be obtained, and a monomer ( Ya), the monomer (Yb) or another monomer (Yc) may be repeatedly polymerized to obtain a ternary or higher multiblock copolymer.
- the block copolymer is preferably a diblock copolymer, a triblock copolymer or a tetrablock copolymer, and a diblock copolymer or triblock copolymer and more preferably a diblock copolymer.
- the binding form of each block is preferably linear.
- the ratio of the number average molecular weight (Mn) of each block to the number average molecular weight (Mn) of the block copolymer (block Mn/block copolymer Mn ) are preferably from 0.01 to 0.99.
- the ratio (Mn of block/Mn of block copolymer) is more preferably 0.05 or more, further preferably 0.1 or more.
- the ratio (Mn of block/Mn of block copolymer) is more preferably 0.95 or less, further preferably 0.9 or less.
- the content of the monomer (Ya) unit in the polymer block (a) is preferably 50 mol% or more, more preferably 70 mol% or more, even more preferably 80 mol% or more, and particularly preferably 90 mol% or more. .
- the content of the monomer (Yb) units in the polymer block (a) is preferably less than 10 mol%, more preferably less than 5 mol%, even more preferably less than 1 mol%.
- the content of the monomer (Yb) unit in the polymer block (b) is preferably 50 mol% or more, more preferably 70 mol% or more, even more preferably 80 mol% or more, and particularly preferably 90 mol% or more. .
- the content of the monomer (Ya) unit in the polymer block (b) is preferably less than 10 mol%, more preferably less than 5 mol%, even more preferably less than 1 mol%.
- the content of the monomer (Ya) unit in the polymer block (ab) is preferably 1 to 99 mol%, more preferably 5 to 99 mol%, even more preferably 10 to 90 mol%.
- the content of the monomer (Yb) unit in the polymer block (ab) is preferably 1 to 99 mol%, more preferably 5 to 99 mol%, even more preferably 10 to 90 mol%.
- the monomer (Ya), the monomer (Yb), and the other monomer (Yc) are not particularly limited, and those mentioned above as the monomer (Y) can be used in appropriate combination. Among them, it is preferable to use the vinyl ester as one of the monomer (Ya) and the monomer (Yb).
- the other monomer used together with the vinyl ester is not particularly limited as long as it is a monomer other than the vinyl ester, but is preferably the acrylic acid ester, the olefin or the acrylic acid.
- the controlled radical polymerization of the vinyl ester and the controlled radical polymerization of the vinyl ester and a monomer other than the vinyl ester are sequentially performed in the presence of the organic compound (A) and the radical generator (B). Accordingly, it is particularly preferable to obtain a vinyl ester block copolymer containing a vinyl ester polymer block and a polymer block containing a vinyl ester unit and a unit derived from a monomer other than the vinyl ester.
- the polymerization step when the number average molecular weight of the polymer and the conversion rate of the monomer (Y) reach the target values, it is preferable to perform a termination step of adding a polymerization terminator to terminate the polymerization reaction.
- a polymerization terminator include 1,1-diphenylethylene; hydroxyaromatic compounds such as p-methoxyphenol, hydroquinone, cresol, t-butylcatechol and p-nitrosophenol; quinone compounds such as benzoquinone and naphthoquinone; muconic acid and sorbin.
- conjugated carboxylic acids such as acids; thioethers such as phenothiazine, distearylthiodipropionate and dilaurylthiodipropionate; aromatic amines such as p-phenylenediamine and N-nitrosodiphenylamine; nitroxides such as methylpiperidine 1-oxyl and 4-hydroxy-2,2,6,6-tetramethylpiperidine 1-oxyl; transition metal salts such as copper acetate, copper dithiocarbamate and manganese acetate; Among them, 1,1-diphenylethylene, sorbic acid and benzoquinone are preferred, and 1,1-diphenylethylene is more preferred.
- the number of moles of the polymerization terminator to be added is preferably 1 to 100 mol per 1 mol of the added organic compound (A). If the number of moles of the polymerization terminator is too small, the radicals at the ends of the polymer cannot be sufficiently captured, and the resulting polymer may have a poor color tone. On the other hand, if the number of moles of the polymerization terminator is too large, the production cost may increase.
- the temperature of the reaction solution in the termination step may be any temperature at which the polymerization terminator can react with the terminal radicals of the polymer, and is preferably 0 to 80°C.
- the time required for the stopping step is usually 1 minute to 5 hours.
- a removal step for removing the organic compound (A) and the like contained in the obtained polymer may be performed. It is preferable not to perform such a removal step. Since the organic compound (A) is highly safe, the resulting polymer is highly safe even without the removal step.
- the monomer (Y) used in the polymerization step preferably contains a vinyl ester. That is, in the polymerization step, it is preferable to obtain a vinyl ester polymer by performing controlled radical polymerization of vinyl ester in the presence of the organic compound (A) and the radical generator (B).
- the vinyl ester polymer include vinyl ester homopolymers, random copolymers containing vinyl ester units and units derived from monomers other than vinyl ester, and polymer block (a) containing vinyl ester units. , a vinyl ester block copolymer containing a polymer block (b) containing a unit derived from a monomer other than vinyl ester, and the like.
- the vinyl ester polymer thus obtained is suitable for various uses.
- a vinyl alcohol polymer can be obtained by saponifying the vinyl ester polymer dissolved in alcohol.
- the acrylic acid ester units can be converted into acrylic acid units by adjusting the saponification conditions.
- an acrylic acid ester unit or an acrylic acid unit may form a lactone ring with an adjacent vinyl alcohol unit.
- Alcohols used in the saponification reaction include lower alcohols such as methanol and ethanol, and methanol is particularly preferably used. Further, the alcohol may be hydrous alcohol or dehydrated alcohol.
- the alcohol used in the saponification reaction may contain acetone, esters such as methyl acetate and ethyl acetate, and solvents such as toluene.
- the catalyst used in the saponification reaction includes, for example, alkali metal hydroxides such as potassium hydroxide and sodium hydroxide; alkali catalysts such as sodium methylate; and acid catalysts such as mineral acids.
- a suitable temperature for the saponification reaction is, for example, a range of 20 to 80°C. When a gel-like product precipitates as the saponification reaction progresses, the product is pulverized at that time, washed and dried to obtain a vinyl alcohol polymer.
- the degree of saponification of the vinyl alcohol polymer may be adjusted depending on the application, and is not particularly limited, but is usually 50 to 99.99 mol %.
- the degree of saponification refers to the total number of moles of vinyl ester units and vinyl alcohol units (including units derived from vinyl alcohol monomers forming lactone rings) in the vinyl alcohol polymer. It refers to the ratio (mol%) of the total number of moles of vinyl alcohol units (including units derived from vinyl alcohol monomers forming lactone rings).
- the degree of saponification can be determined by 1 H-NMR measurement of the vinyl alcohol polymer.
- the total amount of vinyl ester units and vinyl alcohol units in the vinyl alcohol polymer is preferably 50 mol% or more, more preferably 70 mol% or more, and even more preferably 80 mol% or more.
- a vinyl alcohol block copolymer containing a polymer block (a') containing a vinyl alcohol unit and a polymer block (b') containing a unit derived from a monomer other than a vinyl ester is obtained. Further, the vinyl ester-based block copolymer comprising a polymer block (a) containing a vinyl ester unit and a copolymer block (ab) containing a vinyl ester unit and a unit derived from a monomer other than the vinyl ester.
- the number average molecular weight (Mn) of the polymer obtained by the production method of the present invention is not particularly limited, it is preferably 1,000 or more. According to the production method of the present invention, it is possible to synthesize a high-molecular-weight polymer while precisely controlling the molecular arrangement, terminal structure, and the like. Therefore, the production method is suitably used for producing a polymer having a high number average molecular weight (Mn).
- the number average molecular weight (Mn) of the polymer is more preferably 2,000 or more, more preferably 4,000 or more, even more preferably 10,000 or more, particularly preferably 20,000 or more, most preferably 40,000 or more. preferable.
- the number average molecular weight (Mn) of the polymer is preferably 1,000,000 or less, more preferably 500,000 or less, and even more preferably 300,000 or less.
- the number average molecular weight (Mn) and molecular weight distribution (Mw/Mn) are values measured by GPC using polymethyl methacrylate as a standard substance.
- the column may be appropriately selected in consideration of the solubility of the polymer in the solvent, etc., and a tetrahydrofuran-based column, an HFIP-based column, or the like is preferably used. A specific measuring method is as described in Examples.
- the molecular weight distribution (Mw/Mn) of the polymer obtained by the production method of the present invention is not particularly limited, it is preferably 1.00 to 3.5.
- a polymer with a narrow molecular weight distribution can be obtained by polymerizing by controlled radical polymerization.
- the molecular weight distribution (Mw/Mn) is more preferably 3.4 or less, still more preferably 3.3 or less, and particularly preferably 3.2 or less.
- radical polymerization is highly controlled by using the organic compound (A), so that a high-molecular-weight polymer can be obtained while precisely controlling the molecular arrangement, terminal structure, and the like.
- the organic compound (A) is inexpensive, industrially used as a food additive and flavoring agent, and is highly safe, so a step of removing the organic compound (A) is not required. Therefore, the production method of the present invention is environmentally friendly and excellent in terms of cost.
- the resulting polymer is suitably used in sanitary, daily necessities, construction/civil engineering, industrial, agricultural, medical, food, and other applications by utilizing its properties.
- a preferred embodiment of the present invention comprises an organic compound (A) represented by the following formula (I) and a radical generator (B), wherein the molar ratio (B/A) of (B) to (A) is 0 .5 to 20, the composition for radical polymerization.
- a radical generator B
- the composition for radical polymerization By using the composition, radical polymerization of the monomer (Y) can be carried out with a high degree of control.
- the composition for radical polymerization is highly safe. Therefore, it can be suitably used for radical polymerization of various monomers, including the method for producing the polymer described above.
- Examples of the organic compound (A), radical generator (B) and monomer (Y) used in the composition for radical polymerization include those mentioned above as those used in the method for producing a polymer.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed.
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- composition for radical polymerization preferably further contains a monomer (Y).
- Y molar ratio of the monomer (Y) to the organic compound (A) is preferably 300-30,000.
- a radical polymerization controller comprising an organic compound (A) represented by the following formula (I) is also a preferred embodiment of the present invention.
- the organic compound (A) used as the radical polymerization controller include those described above as those used in the method for producing a polymer.
- the radical generator (B) and the monomer (Y) that are used together with the radical polymerization controller in carrying out the radical polymerization those used in the method for producing a polymer include those mentioned above.
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed.
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- a preferred embodiment of the present invention is a polymer having a terminal structure represented by the following formula (V) or (VI).
- R 1 is an alkenyl group or an aryl group
- R 2 is a group represented by the following formula (II) or (III)
- R 1 and R 2 are A ring may be formed. * indicates a bond.
- R 1 and R 2 have the same definitions as in formula (V) above, and * indicates a bond. ]
- R 3 is a hydrogen atom, a halogen atom, an alkyl group, an aryl group, an alkenyl group, an alkoxy group, an amino group, a nitro group, a cyano group, an acetyl group, a trifluoromethyl group, or a hydroxyl group; indicates a bond.
- R 3 has the same definition as in formula (II) above, and * indicates a bond.
- Theoretical number average molecular weight (theoretical Mn) The theoretical number average molecular weight (theoretical Mn) at a given conversion rate was obtained from the following formula.
- Theoretical Mn molar ratio (Y/A) of monomer (Y) to organic compound (A) ⁇ average molecular weight of monomer (Y) [g/mol] ⁇ (conversion rate [%]/100)
- FIG. 1 is a diagram plotting the number average molecular weight (Mn) against the conversion rate in Example 1.
- FIG. After plotting number average molecular weight (Mn) (horizontal axis, linear scale) against conversion (horizontal axis, linear scale) as shown in FIG.
- the number average molecular weight (Mn) of the polymer when the conversion rate is 5.0% was obtained from a straight line passing through . However, at least one of the two points is the point at which the conversion rate is 1.0% or more and less than 5.2%.
- F (1-Fet)/Fet
- the total amount (Yvac+et) (mol) of VAc and Et in the copolymerization of VAc and Et is determined by the following formula using the amount (Yvac) (mol) and the molar ratio D of VAc in the copolymerization.
- (Yvac+et) (Yvac)+(Yvac)/D
- T is the integrated value (4.8 ppm) of the peak derived from the methine proton (—CH 2 CH (OCOCH 3 )—) of the vinyl acetate monomer unit, and the side chain proton (—CH 2 CH(COOCH 3 )-) is the integrated value (3.6 ppm) of the peak derived from S
- the content (U) (mol%) of the acrylic acid ester monomer unit in the vinyl acetate block copolymer is determined by the following formula: ) was calculated.
- the content of the MA unit in the copolymer block containing the VAc unit and the MA unit was determined.
- (U) (mol %) (S / 3) / (S / 3 + T) ⁇ 100
- T is the integrated value (4.8 ppm) of the peak derived from the methine proton (—CH 2 CH (OCOCH 3 )—) of the vinyl acetate monomer unit, and the methylene proton (—C H 2 CH (OCOCH 3 )-) and main chain protons (-C H 2 CH 2 -) of Et units, and the integrated value (1.0-1.8 ppm) of the peaks derived from the main chain protons (-C H 2 CH 2 -) of the Et unit is defined as Q, and the vinyl acetate system is determined by the following formula.
- the Et unit content (R) (mol %) in the block copolymer was calculated.
- the content of Et units in a copolymer block containing VAc units and Et units was determined using the content (R) and the number average molecular weight (Mn) of each polymer block.
- (R) (mol%) (Q-2T) / 4 / ((Q-2T) / 4 + T) ⁇ 100
- the acrylic acid monomer unit content (O) (mol%) in the vinyl acetate-based block copolymer was obtained by the following method. 1 H-NMR measurement of the vinyl acetate block copolymer was carried out.
- the integrated value (4.8 ppm) of the peak derived from the methine proton (-CH 2 CH (OCOCH 3 )-) of the vinyl acetate monomer unit is T
- the side chain proton of the acrylic acid monomer unit (-CHCH Using the integrated value (12.2 ppm) of the peak derived from COO H )-) as P, the acrylic acid monomer unit content (O) (mol%) in the vinyl acetate block copolymer is calculated by the following formula. did.
- the content (U) and the number average molecular weight (Mn) of each polymer block were used to determine the content of the AA unit in the copolymer block containing the VAc unit and the AA unit.
- (O) (mol %) P / (P + T) x 100
- the N,N-dimethylacrylamide monomer in the vinyl acetate block copolymer is calculated by the following formula.
- the content (M) and the number average molecular weight (Mn) of each polymer block the content (M) of the copolymer block containing the VAc unit and the DMAA unit was calculated.
- DMAA unit content was determined.
- (M) (mol %) (N / 6) / ((N / 6) + T) ⁇ 100
- Example 1 ⁇ Polymerization process> After adding 900 parts by mass of VAc to a reactor equipped with a stirrer, a reflux condenser, and an addition port for a radical generator, nitrogen was introduced into the reactor to perform inert gas replacement. 100 parts by mass of VAc, 0.22 parts by mass of cinnamic acid as an organic compound (A), and 0.45 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced to dissolve Active gas replacement was performed. After the solution in the preparation vessel was added to the reactor, the reactor was heated and stirred so that the internal temperature of the reactor reached 50°C.
- the number average molecular weight (Mn) was 166,900
- the theoretical number average molecular weight (theoretical Mn) was 87,100
- the ratio (Mn/theoretical Mn) was 1.9. rice field.
- the VAc conversion rate reached 22% by mass
- 1.31 parts by mass of 1,1-DPEt was added as a polymerization terminator.
- the number average molecular weight (Mn) was 226,400
- the theoretical number average molecular weight (theoretical Mn) was 149,300
- the ratio (Mn/theoretical Mn) was 1.5
- the molecular weight distribution (Mw/Mn) was 2.57. Met.
- FIG. 1 is a plot of number average molecular weight (Mn) versus conversion of VAc.
- Mn number average molecular weight
- Example 2 A polymerization reaction was carried out in the same manner as in Example 1, except that 0.24 parts by mass of methyl cinnamate was added as the organic compound (A), and the mixture was heated and stirred so that the internal temperature of the reactor reached 50°C. After adding the polymerization terminator, the reactor was connected to a vacuum line, and unreacted VAc was azeotropically removed while adding methanol to obtain a methanol solution of polyvinyl acetate. Details are shown in Table 1.
- the concentration of the methanol solution was adjusted to 1834 parts by mass of methanol per 100 parts by mass of the polyvinyl acetate obtained in the same reactor as above, and then the water bath was heated to bring the internal temperature to 40°C. It was heated and stirred until 66.4 parts by mass of a methanol solution of sodium hydroxide (concentration: 14% by mass, 9.3 parts by mass as sodium hydroxide) was added thereto.
- a saponification reaction was carried out at 65° C. for 1 hour with the methanol solution containing polyvinyl acetate at a concentration of 5% by mass thus prepared.
- a phenolphthalein solution was added to the washing liquid (methanol), and washing was carried out with methanol until no alkaline reaction was observed to remove sodium hydroxide and sodium acetate.
- the solid obtained by centrifugal dehydration was dried in a vacuum dryer at 40°C for 24 hours to obtain white polyvinyl alcohol. The degree of saponification was 99.9%.
- Example 3 ⁇ Polymerization process> 0.15 parts by mass of methyl cinnamate as an organic compound (A) and 0.29 parts by mass of V-70 as a radical generator (B) are added, and the temperature inside the reactor is heated to 45° C., A polymerization reaction was carried out in the same manner as in Example 1 except that 0.84 parts by mass of 1,1-DPEt was added as a terminator to obtain polyvinyl acetate. Details are shown in Table 1.
- Example 4 ⁇ Polymerization process> 0.09 parts by mass of methyl cinnamate as an organic compound (A) and 0.18 parts by mass of V-70 as a radical generator (B) are added, and heated so that the internal temperature of the reactor reaches 40 ° C., A polymerization reaction was carried out in the same manner as in Example 1 except that 0.52 parts by mass of 1,1-DPEt was added as a terminator to obtain polyvinyl acetate. Details are shown in Table 1.
- Example 5 ⁇ Polymerization process> 1.88 parts by mass of methyl cinnamate as the organic compound (A) and 35.81 parts by mass of V-70 as the radical generator (B) are added, and heated so that the reactor internal temperature reaches 45 ° C., A polymerization reaction was carried out in the same manner as in Example 1 except that 10.47 parts by mass of 1,1-DPEt was added as a terminator to obtain polyvinyl acetate. Details are shown in Table 1.
- Example 6 ⁇ Polymerization process> A polymerization reaction was carried out in the same manner as in Example 1, except that 0.24 parts by mass of methyl cinnamate as the organic compound (A) and 0.22 parts by mass of V-70 as the radical generator (B) were added. Vinyl acetate was obtained. Details are shown in Table 1.
- Example 7 ⁇ Polymerization process> A total of 1000 parts by mass of N-vinylpyrrolidone as the monomer (Y), 0.18 parts by mass of methyl cinnamate as the organic compound (A), 0.35 parts by mass of V-70 as the radical generator (B), A polymerization reaction was carried out in the same manner as in Example 1, except for the addition, to obtain polyvinylpyrrolidone.
- Example 8 ⁇ Polymerization process> Example 1 except that 0.24 parts by mass of methyl cinnamate was added as the organic compound (A), the temperature inside the reactor was heated to 65°C, and 0.81 parts by mass of sorbic acid was added as a terminator. A polymerization reaction was carried out in the same manner as above to obtain polyvinyl acetate. Details are shown in Table 1.
- Example 9 ⁇ Polymerization process> 0.24 parts by mass of methyl cinnamate as the organic compound (A) and 25.0 parts of methanol as the solvent were added, and the mixture was heated and stirred so that the internal temperature of the reactor reached 60°C. A polymerization reaction was carried out to obtain polyvinyl acetate. Details are shown in Table 1.
- Example 10 ⁇ Polymerization process> 1000 parts by mass of styrene as the monomer (Y), 0.18 parts by mass of trans-benzalacetone as the organic compound (A), and 0.37 parts by mass of V-70 as the radical generator (B) are added, A polymerization reaction was carried out in the same manner as in Example 1 except that 0.81 parts by mass of sorbic acid was added as a terminator to obtain polystyrene. Details are shown in Table 1.
- Example 11 A polymerization reaction was carried out in the same manner as in Example 1 except that 0.21 parts by mass of trans-benzalacetone was added as the organic compound (A) and the reactor was heated so that the internal temperature of the reactor reached 60° C., and polyvinyl acetate was obtained. got Details are shown in Table 1.
- Example 12 ⁇ Polymerization process> A polymerization reaction was carried out in the same manner as in Example 1, except that 0.21 part by mass of coumarin was added as the organic compound (A), and the reactor was heated and stirred so that the internal temperature of the reactor reached 45° C. to obtain polyvinyl acetate. rice field. Details are shown in Table 1.
- Example 13 ⁇ Polymerization process> A polymerization reaction was carried out in the same manner as in Example 1, except that 0.19 parts by mass of cinnamic alcohol was added as the organic compound (A) and the reactor was heated to a temperature of 60°C. Details are shown in Table 1.
- Example 14 ⁇ Polymerization process> A polymerization reaction was carried out in the same manner as in Example 1, except that 0.28 parts by mass of ⁇ -ionone was added as the organic compound (A) and the temperature inside the reactor was heated to 30° C. to obtain polyvinyl acetate. rice field. Details are shown in Table 1.
- Example 15 ⁇ Polymerization process> After adding 900 parts by mass of VAc to a reactor equipped with a stirrer, a reflux condenser, and an addition port for the radical generator (B), nitrogen was introduced into the reactor to perform inert gas replacement. 100 parts by mass of VAc, 0.24 parts by mass of methyl cinnamate as an organic compound (A), and 0.45 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced. Inert gas replacement was performed. After the solution in the preparation vessel was added to the reactor, the reactor was heated and stirred so that the internal temperature of the reactor reached 45°C.
- the number average molecular weight (Mn) at this time was 233,700.
- the reactor was connected to a vacuum line, and unreacted VAc was azeotropically removed while adding methanol to obtain a methanol solution of a vinyl acetate block copolymer. Details are shown in Table 2.
- the content of MA units in the obtained vinyl acetate block copolymer was 9 mol %, and the content of MA units in the copolymer block containing VAc units and MA units was 25 mol %.
- ⁇ Saponification process> the concentration of the methanol solution was adjusted to 1834 parts by mass of methanol per 100 parts by mass of the obtained vinyl acetate block copolymer in the reactor similar to the above, and then the water bath was heated to increase the internal temperature. was heated and stirred until the temperature reached 40°C. 66.4 parts by mass of a methanol solution of sodium hydroxide (concentration: 14% by mass, 9.3 parts by mass as sodium hydroxide) was added thereto. A saponification reaction was carried out at 65° C. for 1 hour with the thus prepared vinyl acetate block copolymer solution having a concentration of 5% by mass.
- Example 16 ⁇ Polymerization process> After adding 900 parts by mass of VAc to a reactor equipped with a stirrer, a reflux condenser, and an addition port for the radical generator (B), nitrogen was introduced into the reactor to perform inert gas replacement. 100 parts by mass of VAc, 0.24 parts by mass of methyl cinnamate as an organic compound (A), and 0.45 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced. Inert gas replacement was performed. After the solution in the preparation vessel was added to the reactor, the reactor was heated and stirred so that the internal temperature of the reactor reached 45°C.
- the number average molecular weight (Mn) at this time was 203,600.
- the reactor was connected to a vacuum line, and unreacted VAc was azeotropically removed while adding methanol to obtain a methanol solution of a vinyl acetate block copolymer. Details are shown in Table 2.
- the content of Et units in the resulting vinyl acetate block copolymer was 2 mol %, and the content of Et units in the copolymer block containing VAc units and Et units was 12 mol %.
- Example 17 ⁇ Polymerization process> After adding 900 parts by mass of VAc and 180 parts by mass of MA to a reactor equipped with a stirrer, a reflux condenser, and an addition port for the radical generator (B), nitrogen was introduced into the reactor to replace the inert gas. rice field. 100 parts by mass of VAc, 0.63 parts by mass of methyl cinnamate as an organic compound (A), and 3.58 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced. Inert gas replacement was performed. The calculated molar ratio (Y/A) was 3,000.
- Example 18 ⁇ Polymerization process> After adding 900 parts by mass of VAc to a reactor equipped with a stirrer, a reflux condenser, and an addition port for the radical generator (B), nitrogen was introduced into the reactor to perform inert gas replacement. 100 parts by mass of VAc, 0.24 parts by mass of methyl cinnamate as an organic compound (A), and 1.34 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced. Inert gas replacement was performed. After adding the solution in the preparation vessel to the reactor, the reactor was heated and stirred so that the internal temperature of the reactor reached 40°C.
- Example 19 ⁇ Polymerization process> After adding 900 parts by mass of VAc to a reactor equipped with a stirrer, a reflux condenser, and an addition port for the radical generator (B), nitrogen was introduced into the reactor to perform inert gas replacement. 100 parts by mass of VAc, 0.24 parts by mass of methyl cinnamate as an organic compound (A), and 1.34 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced. Inert gas replacement was performed. After adding the solution in the preparation vessel to the reactor, the reactor was heated and stirred so that the internal temperature of the reactor reached 40°C.
- Example 20 ⁇ Polymerization process> After adding 900 parts by mass of VAc to a reactor equipped with a stirrer, a reflux condenser, and an addition port for the radical generator (B), nitrogen was introduced into the reactor to perform inert gas replacement. 100 parts by mass of VAc, 0.24 parts by mass of methyl cinnamate as an organic compound (A), and 1.34 parts by mass of V-70 as a radical generator (B) were added to a preparation vessel, dissolved, and then nitrogen was introduced. Inert gas replacement was performed. After adding the solution in the preparation vessel to the reactor, the reactor was heated and stirred so that the internal temperature of the reactor reached 40°C.
- Example 21 ⁇ Polymerization process> In the polymerization of Example 1, sampling was performed immediately before adding the polymerization terminator, and the polymer was collected by reprecipitation by dropping into hexane. The polymer was dissolved in methanol, added dropwise to hexane again, and dried to obtain polyvinyl acetate. The content (W) of the trans-cinnamic acid-derived structure at the polyvinyl acetate terminal was 0.036 mol%. The content molar ratio (F) of the trans-cinnamic acid-derived structure to the amount of polyvinyl acetate ends was 0.95. Details are shown in Table 2.
- Example 22 ⁇ Polymerization process> In the polymerization of Example 5, sampling was performed immediately before adding the polymerization terminator, and the polymer was recovered by reprecipitation by dropping into hexane. The polymer was dissolved in methanol, added dropwise to hexane again, and dried to obtain polyvinyl acetate.
- the content (W) of the methyl cinnamate-derived structure at the polyvinyl acetate terminal was 0.48 mol %
- the content molar ratio (F) of the methyl cinnamate-derived structure to the polyvinyl acetate terminal was 0.97.
- the ratio (Mn/theoretical Mn) at the initial stage of polymerization was 10.0 or less, and Mn increased as the conversion rate increased, so it was confirmed that the polymerization proceeded in a controlled manner. rice field.
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Abstract
Description
理論Mn=有機化合物(A)に対する単量体(Y)のモル比(Y/A)×単量体(Y)の平均分子量[g/mol]×(転化率[%]/100)
・trans-桂皮酸
・桂皮酸メチル
・trans-ベンザルアセトン
・桂皮アルコール
・4-フェニル-2-ブタノン
・β-イオノン
・クマリン
[ラジカル発生剤(B)]
・[2,2’-アゾビス(4-メトキシ-2,4-ジメチルバレロニトリル)](V-70)
[単量体]
・酢酸ビニル(VAc)
・N-ビニルピロリドン(VP)
・アクリル酸メチル(MA)
・エチレン(Et)
・スチレン(Sty)
・N,N-ジメチルアクリルアミド(DEAA)
・無水マレイン酸(MAn)
[重合禁止剤]
・1,1-ジフェニルエチレン(1,1-DPEt)
株式会社島津製作所製ゲル浸透クロマトグラフィー装置を用い、重合体の数平均分子量(Mn)及び分子量分布(Mw/Mn)を測定した。測定条件は以下のいずれかを採用した。
<条件1>
カラム:昭和電工株式会社製テトラヒドロフラン系カラム「KF-806M」
標準試料:ポリメチルメタクリレート
溶媒及び移動相:テトラヒドロフラン(THF)
流量:1.0mL/min
温度:40℃
試料溶液濃度:0.2質量%(開口径0.45μmフィルターでろ過)
注入量:100μL
検出器:RI
<条件2>
カラム:東ソー株式会社製HFIP系カラム「GMHHR-H(S)」2本直列接続
標準試料:ポリメチルメタクリレート
溶媒及び移動相:トリフルオロ酢酸ナトリウム-HFIP溶液(濃度20mM)
流量:0.2mL/min
温度:40℃
試料溶液濃度:0.1wt%(開口径0.45μmフィルターでろ過)
注入量:10μL
検出器:RI
所定転化率における理論数平均分子量(理論Mn)は以下の式より求めた。
理論Mn=有機化合物(A)に対する単量体(Y)のモル比(Y/A)×単量体(Y)の平均分子量[g/mol]×(転化率[%]/100)
単量体(Y)の転化率が5.0%のときの、重合体の理論数平均分子量(理論Mn)に対する数平均分子量(Mn)(測定値)の比(Mn/理論Mn)が10.0以下を示し、かつ転化率増加に伴いMnが増加するものを制御性に優れると判定した。前記転化率が5.0%のときの重合体の数平均分子量(Mn)(測定値)は、以下のとおり求めた。重合開始から重合終了までの間に複数回(但し、転化率が1.0%以上5.2%未満の間に少なくとも1回)、反応液中の重合体のGPC(ゲルパーミエーションクロマトグラフィー)測定を行うことにより、複数の転化率における、数平均分子量(Mn)を求めた。図1は、実施例1において、転化率に対して、数平均分子量(Mn)をプロットした図である。図1に示されるとおり、転化率(横軸、線形スケール)に対して、数平均分子量(Mn)(横軸、線形スケール)をプロットした後、転化率が5.0%に近い2つの点を通る直線から、前記転化率が5.0%のときの重合体の数平均分子量(Mn)を求めた。但し、2つの点のうち少なくとも1つは、転化率が1.0%以上5.2%未満における点を用いることとした。
VAcに溶存したEt量は以下の通り算出した。Nature Chemistry volume 6, pages179-187(2014)の表1には、Et圧10、25、50[bar]条件下でVAcとEtの共重合を実施し、得られたVAc/Etランダム共重合体に含まれるEtモル分率が各々0.13、0.33、0.54であることが示されている。これに原点(Et圧0のときのEt成分が0)を加えた4点について、Et圧(E)[bar]に対して得られる共重合体に含まれるEtモル分率(Fet)の相関をプロットし、最小二乗法で求めた近似曲線は以下の式で表される。
Fet=0.0108E+0.0208
F=(1-Fet)/Fet
D=(F-1+((1-F)^2+3.6256F)^0.5)/2.06
(Yvac+et)=(Yvac)+(Yvac)/D
酢酸ビニル系ブロック共重合体におけるアクリル酸メチル単量体単位の含有量(U)(モル%)は以下の方法で求めた。酢酸ビニル系ブロック共重合体の1H-NMR測定を行なった。酢酸ビニル単量体単位のメチンプロトン(-CH2CH(OCOCH3)-)に由来するピークの積分値(4.8ppm)をT、アクリル酸メチル単量体単位の側鎖プロトン(-CH2CH(COOCH3)-)に由来するピークの積分値(3.6ppm)をSとして、下記式により酢酸ビニル系ブロック共重合体におけるアクリル酸エステル単量体単位の含有量(U)(モル%)を算出した。また、含有量(U)、各重合体ブロックの数平均分子量(Mn)を用いて、VAc単位とMA単位を含む共重合ブロック中のMA単位の含有量を求めた。
(U)(モル%)=(S/3)/(S/3+T)×100
酢酸ビニル系ブロック共重合体におけるEt単量体単位の含有量(R)(モル%)は以下の方法で求めた。酢酸ビニル系ブロック共重合体の1H-NMR測定を行なった。酢酸ビニル単量体単位のメチンプロトン(-CH2CH(OCOCH3)-)に由来するピークの積分値(4.8ppm)をT、酢酸ビニル単量体単位のメチレンプロトン(-CH 2 CH(OCOCH3)-)およびEt単位の主鎖プロトン(-CH 2 CH 2 -)に由来するピークの積分値(1.0-1.8ppm)をQとして、下記式により酢酸ビニル系ブロック共重合体におけるEt単位の含有量(R)(モル%)を算出した。また、含有量(R)、各重合体ブロックの数平均分子量(Mn)を用いて、VAc単位とEt単位を含む共重合ブロック中のEt単位の含有量を求めた。
(R)(モル%)=(Q-2T)/4/((Q-2T)/4+T)×100
酢酸ビニル系ブロック共重合体におけるアクリル酸単量体単位の含有量(O)(モル%)は以下の方法で求めた。酢酸ビニル系ブロック共重合体の1H-NMR測定を行なった。酢酸ビニル単量体単位のメチンプロトン(-CH2CH(OCOCH3)-)に由来するピークの積分値(4.8ppm)をT、アクリル酸単量体単位の側鎖プロトン(-CH2CH(COOH)-)に由来するピークの積分値(12.2ppm)をPとして、下記式により酢酸ビニル系ブロック共重合体におけるアクリル酸単量体単位の含有量(O)(モル%)を算出した。また、含有量(U)、各重合体ブロックの数平均分子量(Mn)を用いて、VAc単位とAA単位を含む共重合ブロック中のAA単位の含有量を求めた。
(O)(モル%)=P/(P+T)×100
酢酸ビニル系ブロック共重合体におけるN,N-ジメチルアクリルアミド単位の含有量(M)(モル%)は以下の方法で求めた。酢酸ビニル系ブロック共重合体の1H-NMR測定を行なった。酢酸ビニル単量体単位のメチンプロトン(-CH2CH(OCOCH3)-)に由来するピークの積分値(4.8ppm)をT、N,N-ジメチルアクリルアミド単量体単位の側鎖プロトン(-CH2CH(CONH(CH 3)2-)に由来するピークの積分値(3.0ppm)をNとして、下記式により酢酸ビニル系ブロック共重合体におけるN,N-ジメチルアクリルアミド単量体単位の含有量(M)(モル%)を算出した。また、含有量(M)、各重合体ブロックの数平均分子量(Mn)を用いて、VAc単位とDMAA単位を含む共重合ブロック中のDMAA単位の含有量を求めた。
(M)(モル%)=(N/6)/((N/6)+T)×100
酢酸ビニル系ブロック共重合体における無水マレイン酸単位の含有量(J)(モル%)は以下の方法で求めた。酢酸ビニル系ブロック共重合体の1H-NMR測定を行なった。酢酸ビニル単量体単位のメチンプロトン(-CH2CH(OCOCH3)-)に由来するピークの積分値(5.1ppm)をK、無水マレイン酸単量体単位の主鎖プロトン(-CHCH(CO2CO)-)に由来するピークの積分値(3.0ppm)をLとして、下記式により酢酸ビニル系ブロック共重合体における無水マレイン酸単量体単位の含有量(J)(モル%)を算出した。また、含有量(J)、各重合体ブロックの数平均分子量(Mn)を用いて、VAc単位とMAn単位を含む共重合ブロック中のMAn単位の含有量を求めた。
(J)(モル%)=(L/2)/((L/2)+K)×100
重合体における、式(V)または(VI)で表される末端構造単位の含有量(W)(モル%)は以下のように算出した。例としてポリ酢酸ビニル末端に付加した桂皮酸メチルの含有量を定量した。ポリ酢酸ビニルをメタノールに溶解し、ヘキサンで再沈殿を繰り返すことで、ポリ酢酸ビニル末端に付加していない桂皮酸メチルを除去し、回収したポリ酢酸ビニルを真空乾燥機で40℃24時間乾燥させた後に、得られたポリ酢酸ビニルの1H-NMR測定を行なった。酢酸ビニル単量体単位のメチンプロトン(-CH2CH(OCOCH3)-)に由来するピークの積分値(4.8ppm)H、および、桂皮酸メチルの芳香族環に由来する7.1~7.5ppmの範囲に検出される全ピークの積分値Gを算出した。なお、7.1~7.5ppmの積分値を算出する際、ベースラインに傾斜が見られる場合には、その傾斜を考慮して各ピークの面積値を算出した。積分値Hと、積分値Gを芳香族環に結合した水素原子の数で割った値(G/芳香族環に結合した水素原子の数)を用いて、[(G/芳香族環に結合した水素原子の数)/H]から含有量(W)を求めた。
(W)(モル%)=(G/5)/H×100
重合体の鎖数に対する、式(V)または(VI)で表される末端構造の含有モル比(F)は以下の通り算出した。重合体における、式(V)または(VI)で表される末端構造単位の含有量(W)、Mnおよび単量体単位分子量を用いて、[W/(Mn/単量体単位分子量×100)]からモル比(F)を求めた。モル比(F)が1の場合、全ての重合体鎖の片末端に式(V)または(VI)で表される構造単位が導入されていることを示し、1に近いほど制御性に優れるといえる。
(F)=W/(Mn/86×100)
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤の添加口を備えた反応器に、VAc900質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸を0.22質量部、ラジカル発生剤(B)としてV-70を0.45質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。調製容器内の溶液を反応器に添加してから、反応器内温が50℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認した。VAcの転化率が3.9質量%の時点の数平均分子量(Mn)は86,800、理論数平均分子量(理論Mn)は26,800、比(Mn/理論Mn)は3.2であった。VAcの転化率が9.5質量%の時点の数平均分子量(Mn)は132,800、理論数平均分子量(理論Mn)は65,300、比(Mn/理論Mn)は2.0であった。VAcの転化率が12.7質量%の時点の数平均分子量(Mn)は166,900、理論数平均分子量(理論Mn)は87,100、比(Mn/理論Mn)は1.9であった。VAcの転化率が22質量%に到達したところで、重合停止剤として1,1-DPEtを1.31質量部添加した。このときの数平均分子量(Mn)は226,400、理論数平均分子量(理論Mn)は149,300、比(Mn/理論Mn)は1.5、分子量分布(Mw/Mn)は2.57であった。当該溶液から未反応VAcを減圧留去してポリ酢酸ビニルを回収し、真空乾燥機にて40℃で24時間乾燥し、ポリ酢酸ビニルを得た。以上の重合工程の詳細を表1に示す。図1は、VAcの転化率に対して、数平均分子量(Mn)をプロットした図である。図1から求められた、VAcの転化率が5.0%のときの、重合体の理論数平均分子量(理論Mn)に対する数平均分子量(Mn)(測定値)の比(Mn/理論Mn)は3.0であった。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.24質量部添加し、反応器内温が50℃になるように加熱し撹拌した以外は実施例1と同様に重合反応を実施した。重合停止剤添加後に、反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することでポリ酢酸ビニルのメタノール溶液を得た。詳細を表1に示す。
次に、上記と同様の反応器に、得られたポリ酢酸ビニル100質量部に対しメタノール1834質量部となるようにメタノール溶液の濃度を調整した後、水浴を加熱して内温が40℃になるまで加熱撹拌した。ここに水酸化ナトリウムのメタノール溶液(濃度14質量%、水酸化ナトリウムとして9.3質量部)66.4質量部を添加した。こうして調製された濃度5質量%のポリ酢酸ビニルを含むメタノール溶液で65℃にて1時間けん化反応を行った。脱液後、洗液(メタノール)にフェノールフタレイン液を添加し、アルカリ性反応を認めなくなるまでメタノールで洗浄し、水酸化ナトリウム及び酢酸ナトリウムを除去した。遠心脱水して得られた固体を真空乾燥機にて40℃で24時間乾燥することで、白色のポリビニルアルコールを得た。けん化度は99.9%であった。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.15質量部、ラジカル発生剤(B)としてV-70を0.29質量部、添加し、反応器内温が45℃になるように加熱し、停止剤として1,1-DPEtを0.84質量部添加した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.09質量部、ラジカル発生剤(B)としてV-70を0.18質量部、添加し、反応器内温が40℃になるように加熱し、停止剤として1,1-DPEtを0.52質量部添加した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)として桂皮酸メチルを1.88質量部、ラジカル発生剤(B)としてV-70を35.81質量部、添加し、反応器内温が45℃になるように加熱し、停止剤として1,1-DPEtを10.47質量部添加した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を0.22質量部、添加した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
単量体(Y)としてN-ビニルピロリドンを計1000質量部、有機化合物(A)として桂皮酸メチルを0.18質量部、ラジカル発生剤(B)としてV-70を0.35質量部、添加した以外は実施例1と同様に重合反応を実施し、ポリビニルピロリドンを得た。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.24質量部添加し、反応器内温が65℃になるように加熱し、停止剤としてソルビン酸を0.81質量部添加した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.24質量部、溶媒としてメタノールを25.0部添加し、反応器内温が60℃になるように加熱し撹拌した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
単量体(Y)としてスチレンを1000質量部、有機化合物(A)としてtrans-ベンザルアセトンを0.18質量部、ラジカル発生剤(B)としてV-70を0.37質量部添加し、停止剤としてソルビン酸を0.81質量部添加した以外は実施例1と同様に重合反応を実施し、ポリスチレンを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)としてtrans-ベンザルアセトンを0.21質量部添加し、反応器内温が60℃になるように加熱した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)としてクマリンを0.21質量部添加し、反応器内温が45℃になるように加熱し撹拌した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)として桂皮アルコールを0.19質量部添加し、反応器内温が60℃になるように加熱した以外は実施例1と同様に重合反応を実施した。詳細を表1に示す。
<重合工程>
有機化合物(A)としてβ-イオノンを0.28質量部添加し、反応器内温が30℃になるように加熱した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表1に示す。
<重合工程>
有機化合物(A)の代わりに4-フェニル-2-ブタノンを0.22質量部添加し、反応器内温が60℃になるように加熱した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表2に示す。
<重合工程>
有機化合物(A)を添加せず、反応器内温が30℃になるように加熱した以外は実施例1と同様に重合反応を実施し、ポリ酢酸ビニルを得た。詳細を表2に示す。
<重合工程>
有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を0.09質量部、添加した以外は実施例1と同様に重合反応を実施した。5時間後も重合がほぼ進行しなかったため、重合を中止した。詳細を表2に示す。
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤(B)の添加口を備えた反応器に、VAc900質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を0.45質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。調製容器内の溶液を反応器に添加してから、反応器内温が45℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認し、VAcの転化率が8.4質量%に到達したところで、MAを30.00質量部添加した。転化率8.4質量%における重合体の数平均分子量(Mn)は150,700であった。算出したモル比(Y/A)は8240であった。引き続き加熱攪拌を実施し、その固形分濃度から重合の進行を確認するとともに、サンプリングした重合体のGPC測定及び1H-NMR測定を行い、VAcとMAの合計転化率が17.4質量%に到達したところで、重合停止剤として1,1-DPEtを1.31質量部添加した。このときの数平均分子量(Mn)は233,700であった。反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することで酢酸ビニル系ブロック共重合体のメタノール溶液を得た。詳細を表2に示す。得られた酢酸ビニル系ブロック共重合体中のMA単位の含有量は9モル%、VAc単位とMA単位を含む共重合ブロック中のMA単位の含有量は25モル%であった。
次に、上記と同様の反応器に、得られた酢酸ビニル系ブロック共重合体100質量部に対しメタノール1834質量部となるようにメタノール溶液の濃度を調整した後、水浴を加熱して内温が40℃になるまで加熱撹拌した。ここに水酸化ナトリウムのメタノール溶液(濃度14質量%、水酸化ナトリウムとして9.3質量部)66.4質量部を添加した。こうして調製された濃度5質量%の酢酸ビニル系ブロック共重合体溶液で65℃にて1時間けん化反応を行った。脱液して得られたけん化物に水酸化ナトリウム46.5質量部と脱水メタノール2000質量部とイオン交換水210質量部を添加し、65℃でさらに1時間加熱を継続した。脱液後、洗液(メタノール)にフェノールフタレイン液を添加し、アルカリ性反応を認めなくなるまでメタノールで洗浄し、水酸化ナトリウム及び酢酸ナトリウムを除去した。遠心脱水して得られた固体を真空乾燥機にて40℃で24時間乾燥することで、白色のビニルアルコール系ブロック共重合体(ビニルアルコール系重合体ブロック-ビニルアルコール系単量体単位及びアクリル酸系単量体単位を含む共重合体ブロックの二元ブロック共重合体)を得た。けん化度は99.9%であった。詳細を表2に示す。
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤(B)の添加口を備えた反応器に、VAc900質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を0.45質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。調製容器内の溶液を反応器に添加してから、反応器内温が45℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認し、VAcの転化率が10.2質量%に到達したところで、Etを内圧9[bar]となるように圧力調整した。算出したY/Aモル比は9120であった。転化率10.2質量%における重合体の数平均分子量(Mn)は176,600であった。引き続き加熱攪拌を実施し、その固形分濃度から重合の進行を確認するとともに、サンプリングした重合体のGPC測定及び1H-NMR測定を行い、VAcとEtの合計転化率が18.3質量%に到達したところで、重合停止剤として1,1-DPEtを1.31質量部添加した。このときの数平均分子量(Mn)は203,600であった。反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することで酢酸ビニル系ブロック共重合体のメタノール溶液を得た。詳細を表2に示す。得られた酢酸ビニル系ブロック共重合体中のEt単位の含有量は2モル%、VAc単位とEt単位を含む共重合ブロック中のEt単位の含有量は12モル%であった。
次に、実施例2と同様にけん化反応を行い、白色のビニルアルコール系ブロック共重合体(ビニルアルコール系重合体ブロック-ビニルアルコール系単量体単位及びEt単位を含む共重合体ブロックの二元ブロック共重合体)を得た。詳細を表2に示す。
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤(B)の添加口を備えた反応器に、VAc900質量部、MA180質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸メチルを0.63質量部、ラジカル発生剤(B)としてV-70を3.58質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。算出したモル比(Y/A)は3000であった。調製容器内の溶液を反応器に添加してから、反応器内温が40℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認し、VAc及びMAの合計転化率が25.0質量%の時点でMAが完全に消費されたこと[モル比(アクリル酸エステル/ビニルエステル)が0.00001未満]を1H-NMRにより確認した。このときの数平均分子量(Mn)は109,400であった。その直後にVAcを4000.00質量部添加した。このときのVAc及びMAの合計転化率は5.8質量%であり、算出したモル比(Y/A)は13000であった。引き続き加熱攪拌を実施し、その固形分濃度から重合の進行を確認するとともに、サンプリングした重合体のGPC測定及び1H-NMR測定を行い、VAcとMAの合計転化率が20.3質量%に到達したところで、重合停止剤として1,1-DPEtを3.49質量部添加した。このときの数平均分子量(Mn)は195,500であった。反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することで酢酸ビニル系ブロック共重合体のメタノール溶液を得た。詳細を表2に示す。得られた酢酸ビニル系ブロック共重合体中のMA単位の含有量は19モル%、VAc単位とMA単位を含む共重合ブロック中のMA単位の含有量は63モル%であった。
次に、実施例2と同様にけん化反応を行い、白色のビニルアルコール系ブロック共重合体を得た。詳細を表2に示す。
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤(B)の添加口を備えた反応器に、VAc900質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を1.34質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。調製容器内の溶液を反応器に添加してから、反応器内温が40℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認し、VAcの転化率が9.7質量%に到達したところで、AAを83.72質量部添加した。転化率9.7質量%における重合体の数平均分子量(Mn)は104,900であった。算出したモル比(Y/A)は8100であった。引き続き加熱攪拌を実施し、その固形分濃度から重合の進行を確認するとともに、サンプリングした重合体のGPC測定及び1H-NMR測定を行い、VAcとAAの合計転化率が16.2質量%に到達したところで、重合停止剤として1,1-DPEtを1.31質量部添加した。このときの数平均分子量(Mn)は144,400であった。反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することで酢酸ビニル系ブロック共重合体のメタノール溶液を得た。詳細を表2に示す。得られた酢酸ビニル系ブロック共重合体中のAA単位の含有量は8モル%、VAc単位とAA単位を含む共重合ブロック中のAA単位の含有量は20モル%であった。
次に、実施例2と同様にけん化反応を行い、白色のビニルアルコール系ブロック共重合体を得た。詳細を表2に示す。
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤(B)の添加口を備えた反応器に、VAc900質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を1.34質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。調製容器内の溶液を反応器に添加してから、反応器内温が40℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認し、VAcの転化率が8.4質量%に到達したところで、DMAAを115.10質量部添加した。転化率8.4質量%における重合体の数平均分子量(Mn)は114,600であった。算出したモル比(Y/A)は8100であった。引き続き加熱攪拌を実施し、その固形分濃度から重合の進行を確認するとともに、サンプリングした重合体のGPC測定及び1H-NMR測定を行い、VAcとDMAAの合計転化率が19.9質量%に到達したところで、重合停止剤として1,1-DPEtを1.31質量部添加した。このときの数平均分子量(Mn)は145,000であった。反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することで酢酸ビニル系ブロック共重合体のメタノール溶液を得た。詳細を表2に示す。得られた酢酸ビニル系ブロック共重合体中のDMAA単位の含有量は6モル%、VAc単位とDMAA単位を含む共重合ブロック中のDMAA単位の含有量は20モル%であった。
次に、実施例2と同様にけん化反応を行い、白色のビニルアルコール系ブロック共重合体を得た。詳細を表2に示す。
<重合工程>
攪拌機、還流冷却管、ラジカル発生剤(B)の添加口を備えた反応器に、VAc900質量部を添加してから、反応器内に窒素を導入して不活性ガス置換を行った。調製容器にVAc100質量部、有機化合物(A)として桂皮酸メチルを0.24質量部、ラジカル発生剤(B)としてV-70を1.34質量部添加し、溶解した後に窒素を導入して不活性ガス置換を行った。調製容器内の溶液を反応器に添加してから、反応器内温が40℃になるように加熱し撹拌した。適宜サンプリングを行い、その固形分濃度から重合の進行を確認し、VAcの転化率が7.4質量%に到達したところで、MAnを113.95質量部添加した。転化率7.4質量%における重合体の数平均分子量(Mn)は74,400であった。算出したモル比(Y/A)は8100であった。引き続き加熱攪拌を実施し、その固形分濃度から重合の進行を確認するとともに、サンプリングした重合体のGPC測定及び1H-NMR測定を行い、VAcとMAnの合計転化率が18.1質量%に到達したところで、重合停止剤として1,1-DPEtを1.31質量部添加した。このときの数平均分子量(Mn)は100,800であった。反応器を真空ラインに接続し、メタノールを添加しながら未反応のVAcを共沸除去することで酢酸ビニル系ブロック共重合体のメタノール溶液を得た。詳細を表2に示す。得られた酢酸ビニル系ブロック共重合体中のMAn単位の含有量は8モル%、VAc単位とMAn単位を含む共重合ブロック中のMAn単位の含有量は13モル%であった。
次に、実施例2と同様にけん化反応を行い、白色のビニルアルコール系ブロック共重合体を得た。詳細を表2に示す。
<重合工程>
実施例1の重合において、重合停止剤を添加する直前にサンプリングを行い、ヘキサン中に滴下して再沈殿により重合体を回収した。重合体をメタノールに溶解し、再度ヘキサン中に滴下し、乾燥することでポリ酢酸ビニルを得た。ポリ酢酸ビニル末端に有するtrans-桂皮酸由来構造の含有量(W)は0.036モル%であった。ポリ酢酸ビニル末端量に対するtrans-桂皮酸由来構造の含有モル比(F)は0.95であった。詳細を表2に示す。
<重合工程>
実施例5の重合において、重合停止剤を添加する直前にサンプリングを行い、ヘキサン中に滴下して再沈殿により重合体を回収した。重合体をメタノールに溶解し、再度ヘキサン中に滴下し、乾燥することでポリ酢酸ビニルを得た。ポリ酢酸ビニル末端に有する桂皮酸メチル由来構造の含有量(W)は0.48モル%、ポリ酢酸ビニル末端量に対する桂皮酸メチル由来構造の含有モル比(F)は0.97であった。
Claims (15)
- 下記式(I)で表される有機化合物(A)とラジカル発生剤(B)の存在下に、単量体(Y)の制御ラジカル重合を行うことにより重合体を得る重合工程を有し、
(A)に対する(B)のモル比(B/A)が0.5~20である、重合体の製造方法。
- R1がアリール基である、請求項1に記載の重合体の製造方法。
- 有機化合物(A)がE体である、請求項1又は2に記載の重合体の製造方法。
- R4が水素原子である、請求項4に記載の重合体の製造方法。
- R3がメトキシ基又は水酸基である、請求項1~5のいずれかに記載の重合体の製造方法。
- 有機化合物(A)に対する単量体(Y)のモル比(Y/A)が300~30000である、請求項1~6のいずれかに記載の重合体の製造方法。
- 単量体(Y)がオレフィン、ビニルエステル、アクリル酸、アクリル酸エステル、アクリルアミド系単量体、スチレン系単量体、N-ビニルアミド系単量体又はジカルボン酸系単量体を含む、請求項1~7のいずれかに記載の重合体の製造方法。
- 有機化合物(A)とラジカル発生剤(B)の存在下に、ビニルエステルの制御ラジカル重合を行うことによりビニルエステル系重合体を得る重合工程と、得られたビニルエステル系重合体をけん化してビニルアルコール系重合体を得るけん化工程とを有する、請求項8に記載の重合体の製造方法。
- 有機化合物(A)とラジカル発生剤(B)の存在下に、ビニルエステルの制御ラジカル重合と、ビニルエステルとビニルエステル以外の単量体の制御ラジカル重合とを逐次行うことによりビニルエステル系ブロック共重合体を得る重合工程を有する、請求項8に記載の重合体の製造方法。
- 有機化合物(A)とラジカル発生剤(B)の存在下に、ビニルエステルの制御ラジカル重合と、ビニルエステルとビニルエステル以外の単量体の制御ラジカル重合とを逐次行うことによりビニルエステル系ブロック共重合体を得る重合工程と、得られたビニルエステル系ブロック共重合体をけん化してビニルアルコール系ブロック共重合体を得るけん化工程とを有する、請求項10に記載の重合体の製造方法。
- さらに単量体(Y)を含み、有機化合物(A)に対する単量体(Y)のモル比(Y/
A)が300~30000である、請求項12に記載のラジカル重合用組成物。
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US20240174785A1 (en) | 2024-05-30 |
JPWO2022191288A1 (ja) | 2022-09-15 |
TW202244066A (zh) | 2022-11-16 |
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