WO2008035601A1 - Procédé destiné à produire un copolymère thermoplastique - Google Patents
Procédé destiné à produire un copolymère thermoplastique Download PDFInfo
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- WO2008035601A1 WO2008035601A1 PCT/JP2007/067785 JP2007067785W WO2008035601A1 WO 2008035601 A1 WO2008035601 A1 WO 2008035601A1 JP 2007067785 W JP2007067785 W JP 2007067785W WO 2008035601 A1 WO2008035601 A1 WO 2008035601A1
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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
- 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
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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
- 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
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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
- C08F2/00—Processes of polymerisation
- C08F2/44—Polymerisation in the presence of compounding ingredients, e.g. plasticisers, dyestuffs, fillers
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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
- 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
- C08F220/04—Acids; Metal salts or ammonium salts thereof
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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
- C08F8/44—Preparation of metal salts or ammonium salts
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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
- C08F8/48—Isomerisation; Cyclisation
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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
- 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
- C08F220/04—Acids; Metal salts or ammonium salts thereof
- C08F220/06—Acrylic acid; Methacrylic acid; Metal salts or ammonium salts thereof
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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
- C08F2800/00—Copolymer characterised by the proportions of the comonomers expressed
- C08F2800/20—Copolymer characterised by the proportions of the comonomers expressed as weight or mass percentages
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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
- C08F2810/00—Chemical modification of a polymer
- C08F2810/20—Chemical modification of a polymer leading to a crosslinking, either explicitly or inherently
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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
- C08F2810/00—Chemical modification of a polymer
- C08F2810/30—Chemical modification of a polymer leading to the formation or introduction of aliphatic or alicyclic unsaturated groups
Definitions
- the present invention relates to a method for continuously producing a thermoplastic copolymer containing glutaric anhydride units which are excellent in heat resistance, molding processing characteristics and colorless transparency, and which are particularly free of foreign matters. is there.
- Amorphous resins such as polymethyl methacrylate (hereinafter referred to as PMMA) and polycarbonate (hereinafter referred to as PC) make use of its transparency and dimensional stability to provide optical materials, household electrical equipment, and OA equipment. It is also used in a wide range of fields including parts such as automobiles.
- PMMA polymethyl methacrylate
- PC polycarbonate
- PMMA resin has excellent transparency and weather resistance, it has a problem that heat resistance is not sufficient.
- PC resin is excellent in heat resistance and impact resistance, but optical anisotropy occurs in the molded product having a large birefringence, which is an optical distortion, and it is remarkably excellent in molding processability, scratch resistance, and oil resistance. There was a problem of being inferior.
- maleimide as a heat resistance-imparting component for the purpose of improving the heat resistance of PMMA.
- Resins incorporating a monomer or maleic anhydride monomer have been developed.
- maleic anhydride which is expensive and has low reactivity, has a problem of poor heat stability! /,! //.
- a dartal anhydride unit obtained by subjecting a copolymer containing an unsaturated carboxylic acid monomer unit to a cyclization reaction by heating using an extruder.
- Patent Documents 1 and 2 disclose copolymers containing dartal anhydride units obtained by heat-treating the copolymer using a suspension polymerization method or an emulsion polymerization method. The polymer had a problem that a high degree of colorless transparency could not be obtained due to foreign matters caused by the polymerization method! / ,!
- a copolymer containing the dartal anhydride unit by bulk polymerization or solution polymerization a copolymer containing an unsaturated carboxylic acid alkyl ester unit and an unsaturated carboxylic acid unit is used.
- Bulk polymerization or solution polymerization, followed by heating the resulting polymerization solution to separate and remove unreacted monomers, unreacted monomers and solvent, and further heat-cyclizing the copolymer are disclosed in Patent Documents 3 to 5.
- Patent Documents 4 and 5 disclose a production method in which the copolymer solution (a) obtained by the polymerization reaction is continuously supplied to a devolatilization tank to perform devolatilization and a cyclization reaction. But this In some cases, in order to completely remove the unreacted monomer and solvent under vacuum and complete the cyclization reaction, a long heat treatment is required at a high temperature, which requires a great deal of labor and energy. Furthermore, there is a problem that the copolymer containing the obtained dartal anhydride unit is markedly colored.
- Patent Document 6 discloses a solution polymerization method of a copolymer containing an unsaturated carboxylic acid alkyl ester unit and an unsaturated carboxylic acid unit. However, depolymerization using this polymerization solution is disclosed. For volatilization and cyclization reaction!
- the present inventors produced a copolymer containing a specific unsaturated carboxylic acid unit as in Patent Document 7 under specific polymerization conditions.
- the twin-screw extruder disclosed in Patent Document 4 has been improved.
- Patent Documents 3 to 7 Therefore, there is a demand for a method capable of industrially producing a copolymer containing dartaric anhydride units, which have high colorless transparency and excellent thermal stability, which could not be achieved by the production method disclosed in the above. It was.
- Patent Document 1 JP-A-49-85184 (Page 12, Example)
- Patent Document 2 Japanese Patent Laid-Open No. 01-103612 (Page 12, Example)
- Patent Document 3 Japanese Patent Application Laid-Open No. 58-217501 (Page 12, Example)
- Patent Document 4 Japanese Patent Application Laid-Open No. 60 120707 (Page 12, Example)
- Patent Document 6 Japanese Patent Laid-Open No. 06-049131 (Page 12, Example)
- Patent Document 7 Japanese Patent Application Laid-Open No. 2004-002711 (Page 12, Example)
- the present invention has high heat resistance, excellent molding processing characteristics with excellent colorless transparency, and at the same time, reduces foreign matter present in the copolymer required for the optical material, and It is an object of the present invention to provide a method for industrially producing a thermoplastic copolymer excellent in thermal stability with reduced residual volatile components.
- unsaturated carboxylic acid units and unsaturated carboxylic acid units which are precursors of a thermoplastic copolymer containing a dartal anhydride unit.
- a copolymer containing an acid ester unit bulk polymerization or solution polymerization is performed under specific conditions, followed by devolatilization under specific conditions, thereby allowing unreacted monomers or unreacted monomers and a polymerization solvent.
- the present invention relates to
- a copolymer (A) containing (i) an unsaturated carboxylic acid alkyl ester unit and (ii) an unsaturated carboxylic acid unit is produced, and then the copolymer (A) is heated, B) Dehydration and / or (mouth) by carrying out an intramolecular cyclization reaction by dealcoholization reaction, so that (iii) a dartaric anhydride unit represented by the following general formula (1) and (i) an unsaturated carboxylic acid
- the chain transfer agent is 0.;!
- the raw material mixture containing the initiator is supplied to the polymerization tank, and is continuously polymerized while maintaining the content of the copolymer (A) in the polymerization tank at 20 to 80% by weight. ) And unreacted monomer mixture (a) is continuously produced, and the copolymer solution (a) obtained in the polymerization step is continuously added to a devolatilizer.
- R 2 is the same or different, and is selected from a hydrogen atom and an alkyl group having a carbon number;! To 5! / Represents a deviation
- the raw material mixture contains an organic solvent (C) that dissolves the copolymer (A) with respect to 100 parts by weight of the monomer mixture;! -200 parts by weight.
- thermoplastic copolymer according to claim 1 or 2, wherein the polymerization tank in the polymerization step is a complete mixing type reaction tank.
- the polymerization step includes a complete mixing type reaction vessel according to the above [3] and a tubular reactor having a structure for static mixing arranged in series subsequently to the complete mixing type reaction vessel.
- the copolymer solution (a) is continuously polymerized while maintaining the content of the copolymer (A) at 20 to 55% by weight to continuously produce the copolymer solution (a).
- (A) is continuously extracted by a pump, sent to the tubular reactor having the static mixing structure under pressure, and then radical polymerization is started in the tubular reactor having the static mixing structure.
- Agent The content of the copolymer (A) in the copolymer solution (a) at the outlet of the tubular reactor having the static mixing structure is 50 to 90% by weight.
- a method for producing a thermoplastic copolymer wherein the devolatilizer in the devolatilization step comprises a cylindrical container and a number of stirring elements.
- a supply device having a stirring device attached to one or more rotating shafts, having at least one ventro at the top of the cylinder, and supplying the copolymer solution (a) to one end of the cylinder; [1] to [4] V, the method for producing a thermoplastic copolymer according to any one of the above, characterized in that the apparatus has a discharge port for taking out the devolatilized copolymer (A) at the other end.
- the devolatilization step is a pre-devolatilization step in which devolatilization is performed with a devolatilizer that is heated to a polymerization temperature of 250 ° C or lower and reduced to 200 Torr or lower, followed by a pre-devolatilization step.
- a post-devolatilization step in which devolatilization is performed with a devolatilizer that is heated to a devolatilization temperature of 300 ° C or less and depressurized to 200 Torr or less.
- the cyclization device in the cyclization step has a cylindrical container and a stirring device with a plurality of stirring elements attached to the rotating shaft, and has at least one vent port at the top of the cylindrical portion,
- This is a horizontal stirrer having a supply port for supplying the copolymer (A) at one end of the cylindrical part and a discharge port for taking out the thermoplastic copolymer (B) at the other end.
- the temperature is 250 ° C to 350 ° C.
- thermoplastic copolymer For recycling to the polymerization step from the recovered liquid obtained by recovering the unreacted monomer separated or removed in the devolatilization step or the mixture of the unreacted monomer and the organic solvent (C).
- the addition amount of the chain transfer agent is 0.5 to 1.5 parts by weight with respect to 100 parts by weight of the monomer mixture.
- thermoplastic copolymer In the polymerization step, [1] to [; 11], wherein the addition power of the radical polymerization initiator is 0.001-2.0 parts by weight with respect to 100 parts by weight of the monomer mixture.
- thermoplastic copolymer (B) has a weight average molecular weight of 3 to 150,000.
- the monomer mixture in the polymerization step is 15 to 50% by weight of unsaturated carboxylic acid, 50 to 50% of unsaturated carboxylic acid alkyl ester, with the total of the monomer mixture being 100% by weight.
- thermoplastic copolymer according to any one of the above [1] to [; 13] Production method
- thermoplastic copolymer (B) contains 5 to 50% by weight of (iii) a dartaric anhydride unit.
- thermoplastic resin composition obtained by further blending a rubber-containing polymer (D) with the thermoplastic copolymer obtained by any one of the methods [1] to [; 15],
- thermoplastic resin according to any one of [17] to [; 19] above, wherein the polymer constituting the rubber layer of the multilayer polymer contains an alkyl acrylate unit and an aromatic bulle unit.
- a method for producing a resin composition is provided.
- thermoplastic copolymer excellent in thermal stability in which foreign substances present in a copolymer required for an optical material are reduced and in which residual volatile components are reduced. Became possible.
- FIG. 1 is a schematic process diagram showing an example of a method for producing a thermoplastic copolymer of the present invention.
- FIG. 2 is a schematic process diagram showing another example of the method for producing a thermoplastic copolymer of the present invention.
- FIG. 3 is a schematic process diagram showing another example of the method for producing a thermoplastic copolymer of the present invention.
- FIG. 4 is a schematic process diagram showing another example of the method for producing a thermoplastic copolymer of the present invention.
- FIG. 5 is a schematic process diagram showing another example of the method for producing a thermoplastic copolymer of the present invention. Explanation of symbols
- thermoplastic copolymer (B) of the present invention a method for producing the thermoplastic copolymer (B) of the present invention will be specifically described.
- thermoplastic copolymer (B) of the present invention means (iii) a thermoplastic containing a dartaric anhydride unit represented by the following general formula (1) and (i) an unsaturated carboxylic acid alkyl ester unit. These are copolymers, and these can be used alone or in combination.
- R 2 is the same or different and is selected from a hydrogen atom and an alkyl group having carbon atoms;! To 5! / Represents a deviation
- the method for producing a thermoplastic copolymer containing a dartal anhydride unit represented by the general formula (1) of the present invention is basically produced by the following two steps. That is, an unsaturated carboxylic acid alkyl ester monomer and an unsaturated carboxylic acid monomer that give the dartaric anhydride unit represented by the general formula (1) by the subsequent heating step,
- a process for producing a copolymer solution (a) containing the copolymer (A) by copolymerizing the bulle monomer giving the unit (polymerization process)
- a step of continuously supplying the copolymer solution (a) to a devolatilizer with a pump and heating it under reduced pressure to continuously separate and remove unreacted monomers (a devolatilization step).
- the copolymer (A) obtained in the devolatilization step is further heated and subjected to an intramolecular cyclization reaction by (i) dehydration and / or (mouth) dealcohol.
- a production method comprising a step (cyclization step).
- the copolymer (A) is heated to dehydrate the carboxyl groups of 2 units of (ii) unsaturated carboxylic acid units, or adjacent to (ii) unsaturated carboxylic acid units.
- Removal of the alcohol from the unsaturated carboxylic acid alkyl ester unit produces one unit of the above-mentioned dartaric anhydride unit.
- FIG. 1 shows an example of a schematic process diagram of the production method of the present invention.
- the copolymer solution (a) obtained by the polymerization reaction in the polymerization tank (1) is continuously supplied to the devolatilizer (2) and unreacted monomers or unreacted monomers.
- a mixture of the reaction monomer and the organic solvent (C) (hereinafter sometimes referred to as a volatile component) is removed by devolatilization to obtain a copolymer ( ⁇ ).
- this copolymerization The body (A) is continuously supplied in a molten state to the cyclization unit (3) and cyclized to continuously produce the thermoplastic copolymer (B) containing dartal anhydride units. .
- the unreacted monomer or unreacted single monomer separated and removed in the devolatilization step Fig. 1 shows a specific example of a volatile matter recovery process that is used as a recovered raw material for recovering, separating and purifying a mixture of the product and organic solvent (C) and recycling it to the polymerization process.
- the unreacted monomer separated or removed by the devolatilizer (2) or the mixture of the unreacted monomer and the organic solvent (C) is supplied to the cooling device (4) and used as a recovered raw material. Can be mentioned.
- the devolatilization step and the cyclization step are performed in separate steps, so that the unreacted monomer or the unreacted monomer and the organic solvent (C)
- a mixture hereinafter sometimes referred to as a volatile component
- contamination of water and / or methanol produced as a by-product in the cyclization reaction into the volatile component can be greatly reduced.
- the volatile component In the component recovery step, the volatile component can be easily recovered.
- any unsaturated carboxylic acid monomer that can be copolymerized with other vinyl compounds is not particularly limited.
- unsaturated carboxylic acid monomer the following general formula (2) [0034] [Chemical 3]
- R 3 represents any one selected from hydrogen and an alkyl group having 1 to 5 carbon atoms
- maleic acid and further a hydrolyzate of maleic anhydride.
- Acrylic acid and methacrylic acid are more preferable than methacrylic acid because of the excellent power S, particularly thermal stability. These can be used alone or in combination.
- the unsaturated carboxylic acid monomer represented by the general formula (2) gives an unsaturated carboxylic acid unit having a structure represented by the following general formula (3) when copolymerized.
- R 4 represents any one selected from hydrogen and an alkyl group having 1 to 5 carbon atoms.
- the unsaturated carboxylic acid alkyl ester monomer is not particularly limited, but preferably As a preferable example, one represented by the following general formula (4) can be mentioned.
- R 5 represents any one selected from hydrogen and an alkyl group having 1 to 5 carbon atoms
- R 6 is an unsubstituted or substituted C 1-6 aliphatic hydrocarbon group substituted with a hydroxyl group or halogen
- acrylates and / or methacrylates having an aliphatic or alicyclic hydrocarbon group having 6 to 6 carbon atoms or a hydrocarbon group having a substituent are particularly suitable.
- the unsaturated carboxylic acid alkyl ester monomer represented by the general formula (4) gives an unsaturated carboxylic acid alkyl ester unit having a structure represented by the following general formula (5) when copolymerized.
- R 7 represents any one selected from hydrogen and an alkyl group having 1 to 5 carbon atoms
- R 8 is an aliphatic carbon atom having 1 to 6 carbon atoms which is unsubstituted or substituted with a hydroxyl group or halogen.
- the unsaturated carboxylic acid alkyl ester monomer include methyl acrylate, ethyl acrylate, n-butyl acrylate, t-butyl acrylate, benzyl acrylate, and 2-ethylhexyl acrylate.
- An example is a mer. Of these, methyl methacrylate and ethyl acetate are preferred, and methyl methacrylate is particularly preferred because of its excellent optical properties and thermal stability. These may be used alone or as a mixture of two or more.
- other vinylol monomers may be used as long as the effects of the present invention are not impaired.
- other bulle monomers include fragrances such as styrene, ⁇ -methylstyrene, ⁇ -methylstyrene, ⁇ -methylstyrene, ⁇ -ethylstyrene, ⁇ -ethylstyrene and p-t-butylstyrene.
- Cyanide bur monomers such as acrylonitrile monomers, acrylonitrile, methatalonitrile, etharylonitrile, etc., but aromatic rings in terms of transparency, birefringence and chemical resistance.
- the Monomers that do not contain can be used more preferably. These can be used alone or in combination of two or more.
- thermoplastic copolymer (B) having a high degree of colorless transparency that could not be achieved by conventional techniques.
- the organic solvent (C) used in the present invention is not particularly limited as long as it is an organic solvent soluble in the copolymer (A), but ketones, ethers, amides, One or more selected from alcohols can be preferably used. Specific examples include acetone, methyl ethyl ketone, methyl n-butyl ketone, methyl isobutyl ketone, ethyl isobutyl ketone, jetyl ether, tetrahydrofuran, dioxane, dimethyl.
- the amount of the organic solvent (C) added is 100 parts by weight of the monomer mixture from the viewpoint of the stability of the polymerization reaction, the recoverability in the devolatilization step, and the recyclability to the polymerization step. On the other hand,! To 200 parts by weight is more preferable, 20 to 150 parts by weight is more preferable, and 50 to 150 parts by weight is more preferable. In addition, a bulk polymerization method that does not substantially contain an organic solvent can be preferably used as long as the polymerization reaction can be sufficiently controlled.
- thermoplastic copolymer (B) When the addition amount of the organic solvent (C) exceeds 200 parts by weight, the solvent removal becomes insufficient in the subsequent devolatilization step and the cyclization step, and the amount of gas generated in the thermoplastic copolymer (B) is small. This is not preferable because it increases and thermal stability decreases. On the other hand, in order to reduce the residual solvent in order to reduce the amount of generated gas, the thermoplastic copolymer (B) is remarkably colored because it requires high-temperature and long-time treatment in the devolatilization and cyclization processes. Therefore, it is not preferable.
- the dissolved oxygen concentration of the monomer mixture in the polymerization step is 5 ppm or less. It is preferable to control the temperature below, since the excellent colorless transparency, residence stability and thermal stability of the thermoplastic copolymer (B) after the heat treatment can be achieved. Further, in order to further suppress the coloration after the heat treatment, the preferable range of dissolved oxygen concentration is 0.01 to 3 ppm, and more preferably 0.0;! To 1 ppm. When the dissolved oxygen concentration exceeds 5 ppm, the thermoplastic copolymer (B) after the heat treatment tends to be colored, and the thermal stability of the thermoplastic copolymer (B) is lowered. I can't reach my goal.
- the dissolved oxygen concentration in the present invention is a value obtained by measuring dissolved oxygen in the polymerization solution using a dissolved oxygen meter (for example, DO meter B-505 manufactured by Iijima Electronics Co., Ltd., which is a ganorevani type oxygen sensor). It is.
- a method of passing an inert gas such as nitrogen, argon or helium in the polymerization vessel, a method of directly publishing an inert gas in the polymerization solution, or an inert gas before the start of polymerization A method in which the pressure is charged into the polymerization vessel and then the operation of releasing the pressure is performed once or twice or more.
- the sealed polymerization vessel is deaerated before charging the monomer mixture, and then the inert gas is filled.
- a method of passing an inert gas into the polymerization vessel can be exemplified.
- a desirable ratio of the monomer mixture used in the polymerization step is such that the monomer mixture is 100% by weight, and the unsaturated carboxylic acid monomer is 15 to 50% by weight, more preferably 20%. ⁇ 45% by weight, unsaturated carboxylic acid alkyl ester monomer is preferably 50 to 85% by weight, more preferably 55 to 80% by weight.
- the preferred proportion is 0 to 35% by weight, and the particularly preferred proportion is 0 to 10% by weight.
- the amount of the unsaturated carboxylic acid monomer is less than 15% by weight, the amount of the dartaric anhydride unit represented by the general formula (1) generated by heating the copolymer (A) is There is a tendency for the heat resistance improvement effect to decrease.
- the amount of the unsaturated carboxylic acid monomer exceeds 50% by weight, a large amount of unsaturated carboxylic acid units tend to remain after the cyclization reaction by heating of the copolymer (A), which is colorless. Transparency and retention stability tend to decrease
- the polymerization initiator used in the present invention has a half-life force at the above-described polymerization temperature of 0.;! To 60 minutes, more preferably 1 to 30 minutes, and most preferably 2 to 20 minutes.
- Use agent It is important to use. If this half-life is shorter than 0.1 minute, the radical polymerization initiator decomposes before being uniformly dispersed in the polymerization reaction tank, so that the efficiency (starting efficiency) of the radical polymerization initiator is reduced. The amount used increases, and the thermal stability of the finally obtained thermoplastic copolymer decreases.
- the half-life is longer than 60 minutes, a polymerization lump (scaling) is generated in the polymerization tank, making it difficult to operate the polymerization stably. Furthermore, after the polymerization is completed, it has not reacted in the copolymer solution ⁇ . Since the residual radical polymerization initiator remains, a high degree of colorless transparency cannot be obtained, for example, the subsequent devolatilization or cyclization process or the resin is colored by the residual radical polymerization initiator during molding. In some cases, the purpose of the invention cannot be achieved.
- half-life of radical polymerization initiator is a value described in a known product catalog such as Nippon Oil & Fats Co., Ltd. or Wako Pure Chemical Industries, Ltd.
- radical polymerization initiators examples include tert butyl peroxy 3, 5, 5 trimethinorehexanate, tert butinoreno 1 year xylate, tert butinoreno 1 year old
- the amount of the radical polymerization initiator used is determined based on the polymerization temperature, the polymerization time (average residence time), and the target polymerization rate, preferably 100 parts by weight of the monomer mixture. 0.001 to 2.0 parts by weight, more preferably 0.01 to 2.0 parts by weight, and even more preferably 0.01 to 1.0 parts by weight.
- chain transfer agents such as alkyl mercabtan, carbon tetrachloride, carbon tetrabromide, dimethylacetamide, dimethylformamide, and triethylamine are also used. It is necessary to add 0.;! To 2.0 parts by weight with respect to 100 parts by weight of the monomer mixture.
- alkyl mercaptan used in the present invention include n-octyl mercaptan and n-octadecyl mercaptan. Among them, tododecyl mercaptan and n-dodecyl mercaptan are preferably used.
- the weight average molecular weight (hereinafter also referred to as Mw) of the copolymer (A) is from 30000 to 150000, preferably from 50000-1500. 00, more preferably from 50000 to 130000.
- the weight average molecular weight as used in the field of this invention shows the weight average molecular weight in the absolute molecular weight measured by multi-angle light scattering gel permeation chromatography (GPC-MALLS).
- Mw of 30000 or more is preferable because the thermoplastic copolymer does not become brittle and has good mechanical properties.
- Mw is 150,000 or less, high molecular weight substances that are not sufficiently melted or dissolved in melt-molded or solution-coated products do not remain as foreign matters, so there are no fisheye or repellency defects. So I like it.
- the inventors select a bulk polymerization method or a solution polymerization method as a polymerization step, so that the polymerization reaction proceeds in a substantially homogeneously mixed state, and a uniform molecular weight distribution is obtained. It has been found that a copolymer having the same can be obtained. Therefore, in a preferred embodiment, the copolymer (A) has a molecular weight distribution (weight average molecular weight Mw / number average molecular weight Mn) of 1.5 to 3.0, and in a more preferred embodiment, 1.5 to 2.5. The thing of the range of is obtained.
- the molecular weight distribution (M w / Mn) is a numerical value calculated from the weight average molecular weight (Mw) and the number average molecular weight (Mn) in absolute molecular weight measured by multi-angle light scattering gel permeation chromatography (GPC-MAL LS).
- the polymerization tank (1) used in the present invention is not particularly limited, but from the viewpoint of enabling uniform mixing and obtaining a homogeneous polymerization solution ⁇ , polymerization is performed in each part of the polymerization tank. It is preferable that the composition and temperature of the liquid be a “fully mixed reaction tank” in which the liquid composition and the temperature are maintained substantially equal by the stirring action. Furthermore, the tank reactor is equipped with a stirring device. More preferably, it is a tank reactor equipped with a stirring blade capable of bringing the solution in the tank into a substantially complete mixed state.
- stirring blades such as a double helical blade, a paddle blade, a turbine blade, a propeller blade, a bull margin blade, a multistage blade, an anchor blade, a max blend blade, and a paddle blade are used.
- MIG wings, full zone wings manufactured by Shinko Environmental Solution Co., Ltd., log bone wings, etc. can be preferably exemplified, and more preferable from the viewpoint of obtaining a complete mixing property higher than double helical ribbon wing force.
- the polymerization temperature is controlled by removing heat and optionally heating.
- the temperature control include a jacket, heat transfer heat removal or heating by circulating a heat medium, cooling supply of the monomer mixture, and heating supply.
- the polymerization temperature is preferably in the range of 60 ° C to 160 ° C.
- the polymerization time is determined by the target polymerization rate, polymerization temperature, type of initiator and amount used; however, the range of! To 7 hours is preferable, and more preferably 1 to 6 hours. is there. By setting it within this range, the polymerization control is stabilized and a high-quality methacrylic resin composition can be produced. If the residence time is shorter than 1 hour, it is necessary to increase the amount of radical polymerization initiator used, making it difficult to control the polymerization reaction. Preferably, it is 2 hours or more. More than 6 hours are preferred because productivity decreases after 7 hours Yes
- the average residence time of the copolymer solution (a) in the polymerization tank corresponding to the polymerization time when the production method of the present invention is the above-described continuous polymerization method is similarly set as a target.
- the polymerization rate, the polymerization temperature, and the type of initiator used are determined, but are preferably! To 7 hours, more preferably 1 to 6 hours. By making it within this range, the polymerization control is stabilized even in the continuous polymerization method, and the ability S to produce a high-quality methacrylic resin composition is reduced.
- the polymer content in the resulting copolymer solution (a) can be controlled in the range of 20 to 80% by mass, In a more preferred embodiment, the polymer content is in the range of 30-80% by weight, more preferably 50-70% by weight.
- the polymer content is determined by diluting the copolymer solution (a) with tetrahydrafuran, reprecipitating the diluted solution in ⁇ -hexane, and drying the copolymer (a). It is a value calculated by the following equation after measuring the weight.
- each symbol represents the following number.
- A1 Weight of copolymer (A) after drying (g)
- the solution viscosity of the copolymer solution (a) obtained under the polymerization conditions of the present invention is in the range of 0.;! To 100 Pa's, the polymerization rate ( ⁇ ) is 50 to 80%. Even at a high polymerization rate, it is possible to suppress the acceleration reaction of the polymerization by increasing the viscosity, the so-called gel effect, to perform the polymerization stably, and further, since the solution viscosity is in the above range, it can be easily performed by a pump. In addition, it can be supplied to the devolatilizer in the devolatilization step.
- the copolymer solution (a) in the present invention is a numerical value measured by holding the copolymer solution (a) at 30 ° C using a vibration viscometer (VM-100A manufactured by CBC Materials Co., Ltd.).
- ( ⁇ ) indicates a value calculated from the unreacted monomer quantified by gas chromatography.
- a tubular reactor having a structure for static mixing is arranged in series with the above-described mixed reaction vessel, and the copolymer (A) is mixed in the mixed reaction vessel.
- Continuous polymerization is carried out while maintaining a content of 20 to 55% by weight to continuously produce a copolymer solution (a) (pre-polymerization step), and then the copolymer solution (a) obtained is pumped.
- the content of the copolymer (A) in the copolymer solution (a) at the outlet of the tubular reactor having the structure for static mixing is allowed to pass through the reaction solution to 50 to 90% by weight.
- a method of producing the copolymer solution (a) so as to be (post-polymerization step) can also be preferably used.
- the polymer content in the copolymer solution (a) obtained in the prepolymerization step in the range of 20 to 55% by mass.
- the polymer content is 30 to 55% by mass.
- the content of the polymer is determined by diluting the copolymer solution (a) with tetrahydrafuran, reprecipitating the diluted solution in ⁇ -hexane, and drying the copolymer (a). Is a value calculated by the following equation.
- each symbol represents the following number.
- A1 Weight of copolymer (A) after drying (g)
- the polymer content is 20% by weight or less, in the following devolatilization step and cyclization step, the volatile component is obtained at a higher temperature and longer time than the devolatilization, and the obtained thermoplastic copolymer can be obtained. It is not preferable because it causes coloring of the coalesced (C) and thermal degradation. On the other hand, the polymer content is 80%, and mixing and heat transfer cannot be sufficiently performed, and a stable polymerization reaction cannot be performed. [0076] Further, since the solution viscosity of the copolymer solution (a) obtained under the polymerization conditions of the present invention is in the range of 0.;! To 100 Pa's, the polymerization rate ( ⁇ ) is 50 to 80%.
- the solution viscosity of the copolymer solution (a) in the present invention is the viscosity of the copolymer solution (a) at 30 ° C. using a vibration viscometer (VM-100A manufactured by CBC Materials Co., Ltd.).
- the polymerization rate ( ⁇ ) is a value calculated from the unreacted monomer quantified by gas chromatography.
- the copolymer solution (a) obtained in the pre-polymerization step is continuously used as a tubular reactor (hereinafter referred to as "the present invention") having a static mixing structure (static mixing element) inside. ! /, which is sometimes simply referred to as a “tubular reactor”), and further polymerized.
- the method for supplying the copolymer solution (a) obtained in the prepolymerization step to the tubular reactor is not particularly limited.
- the reaction solution is drawn out from the complete mixing reactor and used for static mixing.
- the operation of feeding the liquid to the tubular reactor having the structural portion can be exemplified by a method preferably performed by a pump.
- a known gear pump can be preferably used.
- the reaction solution can be sent stably to the next step, and the inside of the tubular reactor having the static mixing structure installed subsequently is higher than the vapor pressure of the reaction solution. It is possible to step up the voltage.
- the pressure inside the tubular reactor of the present invention needs to be equal to or higher than the vapor pressure of the reaction solution.
- it is 5 to 40 kg / cm2G and not less than the vapor pressure of the reaction solution.
- the polymerization can be further advanced in the tubular reactor having the static mixing structure, and the final polymer content (polymerization rate) is increased.
- the polymerization rate can be reduced by reducing the polymerization rate to the first-stage mixing reactor by further proceeding with the polymerization through the tubular reactor having the static mixing structure inside.
- the polymerization temperature of the polymer reactor is lowered to reduce the heat distortion temperature and resistance of the polymer. It becomes possible to improve thermal decomposability.
- the inner wall temperature of the tubular reactor it is important to set the inner wall temperature of the tubular reactor to a temperature not lower than the polymerization temperature of the first stage fully mixed reactor and not higher than 250 ° C. is there. If the temperature is lower than the polymerization temperature of the first-stage fully mixed reactor, the viscosity of the reactor wall increases and the reactor becomes clogged, making long-term operation impossible. If the inner wall temperature of the reactor is higher than 250 ° C, the temperature of the reaction solution rises due to heat transfer, so that the radical polymerization initiator is rapidly decomposed and the polymerization rate cannot be sufficiently increased. Preferably, the temperature is 200 ° C or lower.
- the inner wall temperature of the tubular reactor is set by dividing it into two or more temperature regions, and is gradually increased from the reaction liquid inlet. preferable. As a result, it is possible to effectively increase the polymerization rate while suppressing the rapid decomposition of the radical polymerization initiator while suppressing the formation of the dimer.
- the initiation of radical polymerization with a half-life at the reactor inner wall temperature of 0.;!-60 minutes, more preferably 1-30 minutes, most preferably 2-20 minutes It is preferable to add one or more agents. If this half-life exceeds 60 minutes, the polymerization rate increases at the low fluidity portion of the reactor wall surface, and this phenomenon proceeds over a long period of time, which is undesirable. On the other hand, if this half-life is too short, it will not hinder the operation, but the radical polymerization initiator will decompose quickly and the polymerization rate cannot be increased sufficiently. It is not preferable because a copolymer inferior to the above tends to be formed. Therefore, it is preferable to use a radical polymerization initiator having a half-life of 0.1 second or more.
- the “half-life of the radical initiator” is a value described in a known product catalog such as Nippon Oil & Fats Co., Ltd. or Wako Pure Chemical Industries, Ltd.
- radical initiators include tert butyl peroxy 3, 5, 5 trimethylenohexanate, tert butinoleno one-year-old xylaurate, tert-butylenono one-year-old xysopropinore monocarbonate, tert-hexinoleno one-year-old xyisopropinore Monocarbonate, tert butyl peroxyacetate, 1,1 bis (tert butylperoxy) 3,3,5-trimethylenocyclohexane, 1,1 bis (tert butynoleperoxy) cyclohexane Tert-butinoleno 1-year-old xyl-2-ethinorehexanate, tert-butinoleno 1-year-old xyisobutyrate, tert-hexino-leno 1-year-old xyl-2-ethinorehexanate, di-ter
- the amount of the radical initiator used is determined by the polymerization temperature, the polymerization time (average residence time), and the target polymerization rate, but is preferably based on 100 parts by weight of the monomer mixture. 0.001 to 2.0 parts by weight, more preferably 0.001 to 1.0 parts by weight, and even more preferably 0.001 to 0.5 parts by weight.
- the final polymerization rate at the outlet of the tubular reactor is in the range of 50 to 85% by weight.
- the final polymerization rate is less than 50% by weight, it is economically advantageous to produce with one fully mixed reactor, and the effect of the present invention cannot be realized.
- the final polymerization rate exceeds 85% by weight, the fluidity is remarkably lowered, so that it is difficult to transport stably.
- it is 55 to 85 weight%, More preferably, it is 60 to 80 weight%.
- a tubular reactor having a static mixing structure means that there is no movable part! / A tubular reactor in which a plurality of mixing elements are fixed (tubular reactor having a static mixing element). Continuous polymerization in the high polymer concentration range, which cannot be achieved by continuous bulk polymerization or solution polymerization while performing static mixing in the tubular reactor. Became possible.
- the polymerization liquid examples include SMX-type, SMR-type Sulza-type tubular mixers, Kenix-type static mixers, Toray-type tubular mixers, etc.
- SMX-type and SMR-type sulza-type tubular mixers are preferred.
- the average residence time of the reaction liquid in this tubular reactor is preferably in the range of 0.0;! To 60 minutes. If this average transit time is shorter than 0.01 minutes, the polymerization rate cannot be sufficiently increased. On the other hand, if the average transit time is longer than 60 minutes, the thermoplastic copolymer (B) finally obtained is preferably deteriorated in thermal stability and productivity, which is preferable! /.
- the method for adding the radical polymerization initiator used in this tubular reactor is a method of adding a radical polymerization initiator from the side line attached to the tubular reactor inlet, or a serial arrangement at the tubular reactor inlet.
- a method in which a radical polymerization initiator is premixed with a static mixer and passed through the tubular reactor is preferred.
- the radical polymerization initiator can be used as one kind or a mixture of two or more kinds. When two or more types are used, it is preferable to use one having a 10-hour half-life temperature of 5 ° C or more. As a result, the polymerization can proceed efficiently.
- a radical polymerization initiator to the portion immediately before the reaction liquid inlet of the tubular reactor and at least one place inside the reactor in accordance with the temperature rise of the reaction liquid.
- the addition amount of the radical polymerization initiator at this time is preferably 0.0005-1. 0 parts by weight, more preferably 0.001-1. 0 parts by weight per 100 parts by weight of the monomer mixture. Parts, more preferably ⁇ 0.001 to 0.5 parts by weight.
- the polymer content is 50 to 90% by weight. More preferably 60 to 90% by weight, more preferably 60 to 85% by weight of continuous bulk polymerization or This makes it possible to stably carry out continuous solution polymerization, and it is possible to use the force S to produce the copolymer solution (a) more efficiently.
- the feature of the present invention is that the copolymer solution ⁇ obtained by the polymerization step is continuously supplied to the devolatilizer in the subsequent devolatilization step, and the unreacted monomer or the unreacted monomer and the organic
- the mixture comprising the solvent (c) (i) dehydration and / or (mouth) dealcoholization can proceed efficiently in the cyclization step described later, and a bulk polymerization method or a solution polymerization method can be used.
- the present inventors have found that the unreacted monomer and polymerization solvent remaining in the obtained thermoplastic copolymer ( ⁇ ) are reduced, and that the thermal stability is excellent, and the present invention has been achieved.
- the unreacted monomer separated by the devolatilization step or the unreacted monomer and the organic solvent (C) can be recovered separately, and water or methanol produced as a by-product in the cyclization process, and the unreacted monomer or mixture of unreacted monomer and organic solvent (C) can be easily recovered and purified. It can be recycled in the polymerization process.
- the devolatilization temperature in this devolatilization step is not less than the polymerization temperature and less than 300 ° C, more preferably not less than 150 and less than 300 ° C.
- the unreacted monomer or the organic solvent (C) that is the polymerization solvent is not sufficiently removed, and the thermal stability of the resulting thermoplastic copolymer (B) is lowered.
- the temperature is 300 ° C or higher, the resulting thermoplastic copolymer (B) is colored due to thermal degradation of the remaining unreacted monomer and the copolymer (A) which is a precursor polymer. Transparency decreases.
- the pressure is a reduced pressure condition of 200 Torr or less, more preferably lOOTorr or less, and most preferably 50 Torr or less.
- the lower limit of the pressure is not particularly limited, but is practically 0.1 lTorr or more.
- a continuous devolatilizer for performing such devolatilization, it has a cylindrical vessel and a stirring device in which a plurality of stirring elements are attached to a rotating shaft, and at least one vent is provided above the cylindrical portion.
- An apparatus having a port and a supply port for supplying the copolymer solution (a) to one end of the cylindrical portion and a discharge port for taking out the devolatilized copolymer (A) to the other end can be preferably used. .
- the number of rotating shafts is not limited, but usually;! ⁇ 5, more preferably 2-4, more preferably a device having two rotating shafts! / ,.
- the number of stirring elements is preferably 10 to 50, more preferably 20 to 30.
- the shape of the stirring element may be a multi-leaf shape that is not particularly limited (for example, the shape of a clover leaf), or may have irregularities, such as a screw on a ship or a fan blade. Various other applications are possible.
- the stirring element is screw-shaped, the action of sending the reaction product can be obtained, which can be preferably used.
- a continuous biaxial kneader or a batch type melt kneader having a vent is preferred, and a single-screw extruder, twin-screw extruder, twin-screw single-unit equipped with a "unimelt" type screw.
- a continuous biaxial reactor equipped with a plate-shaped paddle is preferably used with a force S.
- the screw diameter of the devolatilizer (D ) And screw length (U ratio (L / D) is preferably 40 or more! /, L / D is short! /, Unreacted unit when using a devolatilizer. Or a mixture of unreacted monomer and organic solvent (C) remains in large quantities, so the reaction proceeds again during the thermoforming process, and there is a tendency for silver and bubbles to appear in the molded product, and the color tone greatly increases during molding retention. This is not preferable.
- each devolatilizer when performing devolatilization using a plurality of devolatilizers is not limited. For example, if devolatilization is performed with two devolatilizers arranged in series, the temperature is preferably higher than the polymerization temperature and lower than 250 ° C. In the devolatilizer connected to the cyclizer, higher than 200 ° C and 300 ° C. It is preferable that the temperature is not higher than ° C.
- the pressure in each devolatilizer when performing devolatilization using a plurality of devolatilizers is, for example, when performing devolatilization with two devolatilizers arranged in series, Volatile components can be efficiently produced by setting 760 Torr (normal pressure condition) to 500 Torr in the devolatilizer connected to the polymerization tank, and then reducing the pressure to 200 Torr or less in the devolatilizer connected to the cyclizer. Can be removed, which is preferable. Further, it is more preferably lOOTorr or less, most preferably 50 Torr or less.
- the lower limit of the pressure is not particularly limited, but is practically 0.1 lTorr or more.
- FIG. 1 An example of devolatilization using a plurality of such devolatilizers will be described with reference to a schematic process diagram shown in FIG.
- two devolatilizers are placed in series in the devolatilization process, connected to the polymerization tank (1), and the devolatilizer is connected to the pre-devolatilization process and cyclization apparatus.
- the devolatilizer be the post-devolatilization process.
- the copolymer solution (a) obtained in the polymerization step is placed in the devolatilizer (2-1) in the pre-devolatilization step where the temperature is raised to the polymerization temperature or higher and 250 ° C or lower.
- the copolymer (A) obtained through the devolatilization step by force has a content of the remaining unreacted monomer or a mixture of the unreacted monomer and the polymerization solvent of 10% by weight or less. In this case, it can be reduced to 5% by weight or less, and (i) dehydration and / or (mouth) dealcoholization can proceed efficiently in the subsequent cyclization step.
- the lower limit of the content of the volatile component in the copolymer (A) after the devolatilization step is not particularly limited, but is substantially 0.1% by weight or more.
- the copolymer (A) after the devolatilization step is introduced as a high-temperature melt into the next cyclization step. Since the cyclization reaction can be carried out continuously as it is, the thermoplastic copolymer (B) can be produced economically advantageously.
- the cyclization step in the present invention that is, the copolymer (A) is heated, and (i) dehydration and / or (mouth) is subjected to intramolecular cyclization reaction by dealcoholization! /, Containing dartal anhydride units
- a thermoplastic copolymer is produced, a continuous kneading extrusion apparatus is used as a cyclization apparatus.
- C more preferably 250-330. It is important to be fi in the C range.
- the pressure condition in the cyclization step is lOOTorr or less, preferably 50 Torr or less, more preferably 30 Torr or less, and most preferably lOTorr or less, so that cyclization proceeds.
- the lower limit of the pressure is not limited, but is usually about 0.1 Torr.
- thermoplastic copolymer (B) when the pressure condition is lOOTorr or higher, the degree of vacuum is insufficient, so the cyclization reaction becomes insufficient, and the thermal stability of the resulting thermoplastic copolymer (B) is reduced.
- the oxygen present in the system is not preferable because the polymer tends to deteriorate during cyclization and become colored. Even if the reaction is carried out in an inert gas atmosphere without using reduced pressure conditions, water and / or alcohol produced as a by-product during cyclization cannot be sufficiently removed, and the resulting thermoplastic copolymer (B ) Is preferable because the thermal stability is reduced!
- the heat treatment time in the cyclization step is preferably 1 minute to 120 minutes, more preferably 20 minutes to 120 minutes, still more preferably 30 minutes to 120 minutes, and most preferably. Is in the range of 30-90 minutes.
- the composition of the thermoplastic copolymer (B) obtained with a low cyclization reaction rate falls within the scope of the present invention.
- the reaction proceeds again during the thermoforming process, and water and / or alcohol by-produced by the cyclization reaction evaporate. Radial silver marks, so-called silver, are generated on the surface of the molded body. Alternatively, bubbles are generated on the surface of the molded body, both of which are not preferable because they cause poor appearance, and are not preferable because of poor thermal stability.
- the cyclization apparatus used for the cyclization reaction is a copolymer supplied from the devolatilization apparatus which is the previous step.
- a device that can continuously cyclize (A) and can satisfy the above-mentioned conditions of temperature, pressure, and time, but a cylindrical container and a plurality of stirring elements are attached to a rotating shaft.
- a supply port for supplying the copolymer (A) to one end of the cylindrical portion, and a thermoplastic copolymer ( A horizontal stirrer having a discharge outlet for taking out B) can be preferably used.
- thermoplastic copolymer (A) As a horizontal stirrer, water / methanol generated as a by-product in the cyclization reaction can be efficiently removed from the molten thermoplastic copolymer (A). It has a container with a jacket for the heating medium around it, has a vent port at least at the top of this container, and supplies a supply port for supplying the copolymer (A) to one end of this container, and the other end. It has a discharge port for taking out the thermoplastic copolymer (B), and has at least two stirring shafts inside the shaft, and a plurality of scraping blades are attached to the shafts, and the shafts are identical.
- the blades When the blades are rotated in different directions or different directions, the blades are attached to each other so that the blades attached to the respective shafts do not collide with each other and are displaced from each other. Rotates while touching the surface with a slight gap , Or the blades attached to each shaft are arranged so as to be aligned on the same plane perpendicular to the axial direction, and the blade tips rotate while contacting the inner surface of the container and the surface of the other blade with a slight gap. Accordingly, it is possible to use a horizontal stirrer having a function of kneading the copolymer (A) in a molten state and constantly updating the surface thereof to advance the cyclization reaction.
- a horizontal type stirring apparatus with good surface renewability shown in Japanese Patent Publication No. 58-11450 and Japanese Patent Publication No. 61-52850 is suitable.
- Hitachi, Ltd. Glasses blade polymerization machine, lattice blade polymerization machine, Mitsubishi Heavy Industries, Ltd. SCR, NSCR reactor, KRC Kneader, SC processor, Sumitomo Heavy Industries, Ltd. BIVOLAK etc. can be illustrated preferably.
- the unreacted monomer separated or removed in the devolatilization step or a mixture of the unreacted monomer and the organic solvent (C) is used as the polymerization step. It is preferable to recycle.
- the unreacted monomer removed in the devolatilization step or the mixture of the unreacted monomer and the organic solvent (C) is recovered and reused in the polymerization step! I like it! /
- the volatile component recovery process will be described in more detail with reference to the schematic process charts shown in FIGS. 1 and 2. Since the volatile components are vaporized in the devolatilizer (2) under reduced pressure and heated conditions, The volatile component is supplied from the device (2) to the cooling device (4), recovered as a liquid, and can be recycled again in the polymerization process.
- the method of supplying the volatile component containing the unreacted monomer separated or removed in the devolatilization process or the mixture of the unreacted monomer and the organic solvent (C) to the cooling device (4) examples thereof include a method using an exhaust device such as an ejector, a blower, and a vacuum pump.
- cooling device (4) for example, a known condenser, a condenser-equipped distiller, etc.
- the volatile components are cooled and agglomerated to form a recovered liquid, which is then returned to the polymerization tank (1). Recycled.
- the recovered liquid obtained in the cooling device (4) is supplied to a purification device (5) such as a flash tower, a demister, a distillation tower, etc., purified and separated, and polymerized.
- a purification device (5) such as a flash tower, a demister, a distillation tower, etc.
- a method of recycling in the tank (1) can also be preferably used.
- the volatile components separated and removed by the devolatilizer (2) are supplied to the refiner (5) without agglomeration and purified and separated, and then the recovered liquid is cooled (
- the method of supplying to 4), cooling, agglomerating, and using it as a recovered material can also be preferably used.
- thermoplastic copolymer (B) economically advantageously by collecting the volatile component in the volatile component collecting step and recycling it to the polymerization tank (1) as a collected raw material.
- the content of the dartaric acid anhydride unit represented by the general formula (1) in the thermoplastic copolymer (B) obtained by force is not particularly limited, but is preferably a thermoplastic copolymer.
- the amount is preferably 5 to 50% by weight, more preferably 10 to 50% by weight, still more preferably 25 to 50% by weight, and particularly preferably 30 to 45% by weight in 100% by weight of the coalescence.
- an infrared spectrophotometer or proton nuclear magnetic resonance (HNMR) measuring instrument is used for quantification of each component unit in the thermoplastic copolymer of the present invention.
- glutaric anhydride unit is 1800Cm- 1 and 1760Cm- 1 absorption characteristic of can this and force distinguish from unsaturated carboxylic acid units and unsaturated carboxylic acid alkyl ester unit.
- NMR method for example, in the case of a copolymer consisting of a dartal anhydride unit, methacrylic acid, and methyl methacrylate, the attribution of the spectrum in the dimethyl sulfoxide heavy solvent is 0.5 to 1.5 ppm.
- the copolymer composition can be determined from the element and the integral ratio of the spectrum.
- hydrogen in the aromatic ring of styrene is found at 6.5 to 7.5 ppm, and the copolymer composition is similarly determined from the spectral ratio. can do.
- thermoplastic copolymer of the present invention includes an unsaturated force rubonic acid unit and / or another copolymerizable bull monomer unit.
- the amount of unsaturated carboxylic acid units contained in the thermoplastic copolymer by sufficiently performing (i) dehydration and / or (mouth) dealcoholization reaction of the copolymer (A). is preferably 10% by weight or less, that is, 0 to 10% by weight, more preferably 0 to 5% by weight.
- the amount of other copolymerizable bur monomer units is preferably 0 to 35% by weight, more preferably 10% by weight or less, that is, 0 to 10% by weight, More preferably, it is 0 to 5% by weight.
- an aromatic bule monomer unit such as styrene is contained, if the content is too large, colorless transparency, optical isotropy, and chemical resistance tend to decrease.
- the thermoplastic copolymer (B) of the present invention has a weight average molecular weight (hereinafter also referred to as Mw) of 30000 to 150,000, preferably ⁇ 50000 to 150000, more preferably ⁇ 50,000 to 130000. It is desirable to have it.
- Mw weight average molecular weight
- the weight average molecular weight as used in the field of this invention shows the weight average molecular weight in the absolute molecular weight measured by multi-angle light scattering gel permeation chromatography (GPC-MALLS).
- the polymerization reaction proceeds in a substantially homogeneously mixed state and has a homogeneous molecular weight distribution.
- a copolymer (A) is obtained, and in a preferred embodiment, the molecular weight distribution (weight average molecular weight Mw / number average molecular weight Mn) of the thermoplastic copolymer (B) is 1.5 to 3.0, In a more preferred embodiment, it has been found that a product in the range of 1.5 to 2.5 can be obtained.
- the molecular weight distribution (Mw / Mn) referred to in the present invention is the weight average molecular weight (Mw) and the number average molecular weight (Mw) in absolute molecular weight measured by multi-angle light scattering gel permeation chromatography (GPC—MALL S). The value calculated from (Mn).
- the thermoplastic copolymer (B) of the present invention obtained by virtue of strength has excellent heat resistance with a glass transition temperature of 120 ° C or higher, and is preferable in terms of practical heat resistance.
- the glass transition temperature is extremely excellent heat resistance of 130 ° C or higher.
- the upper limit is usually about 160 ° C.
- the glass transition temperature mentioned here is a glass transition temperature measured at a heating rate of 20 ° C./min using a differential scanning calorimeter (DSC-7 type manufactured by Perkin Elmer).
- the thermoplastic copolymer (B) produced by the production method of the present invention has a yellowness (Yellowness Index) value of 3 or less, and coloring is further suppressed.
- the embodiment has an extremely high colorless transparency such as 2 or less!
- the yellowness is a value obtained by measuring the YI value of a lmm-thick molded product injection molded at a glass transition temperature of + 140 ° C according to JIS-K7103.
- the lower limit of the yellowness is preferably as low as possible, but is usually around 1.
- thermoplastic copolymer (B) produced by the production method of the present invention is a residual unreacted monomer or a mixture of an unreacted monomer and a polymerization solvent (hereinafter collectively referred to as volatile components).
- Content is 5% by weight or less, preferably! /, In an embodiment! /, 3% by weight or less, and further, 30% at a glass transition temperature of + 130 ° C.
- the weight loss after heating for a minute (hereinafter sometimes referred to as gas generation) is 1.0% by weight or less, in a more preferred embodiment 0.5% by weight, most preferably 0.3% by weight or less. It has a high thermal stability that could not be achieved by conventional methods.
- the lower limit of the content of volatile components and the amount of gas generated is preferably as low as possible, but is usually about 0.1% by weight.
- the thermoplastic copolymer (B) of the present invention has a glass transition temperature + 130 ° C, a melt viscosity force S measured at a shear rate of 12 / sec, in a preferred embodiment, 100 to; lOOOOPa's or less In a more preferred embodiment, it has a high fluidity of 100 to 5000 Pa ′s, and in a most preferred embodiment 100 to 2000 Pa ′s or less, and is excellent in molding processability.
- the melt viscosity here refers to the melt viscosity (Pa's) measured at the above temperature and shear rate using Capillograph Type 1C (die diameter ⁇ 1.0 mm, die length 5.0 mm) manufactured by Toyo Seiki Co., Ltd. It is.
- thermoplastic copolymer (B) of the present invention a hindered phenol, benzotriazole, benzophenone, benzoate, and cyanoacrylate are used within the range not impairing the object of the present invention.
- UV absorbers and antioxidants such as higher alcohols, montanic acid and its salts, its esters, its half esters, stearyl alcohol, stearamide and ethylene Release agents such as waxes, anti-coloring agents such as phosphites and hypophosphites, halogen flame retardants, phosphorus and silicone non-halogen flame retardants, nucleating agents, amines, sulfonic acids, Antistatic agents such as polyethers and colorants such as pigments Any additive may optionally be included. However, it is necessary to add the color so that the color of the additive does not adversely affect the thermoplastic copolymer (B) of the present invention and the transparency is not lowered.
- thermoplastic copolymer (B) produced according to the present invention takes advantage of its excellent heat resistance, colorless transparency, and retention stability to make it an electrical / electronic component, automobile component, mechanical mechanism component, OA device. It can be used for various purposes such as housings for home appliances, their parts, general goods.
- thermoplastic copolymer (B) obtained by the above method is excellent in mechanical properties and molding processability, and can be melt-molded. Therefore, extrusion molding, injection molding, and press molding are possible. It can be used after being formed into a film, sheet, tube, rod, or any other desired shape and size.
- a known method can be used as a method for producing a film made of the thermoplastic copolymer (B). That is, a production method such as an inflation method, a T-die method, a calendar method, a cutting method, a casting method, an emulsion method, or a hot press method can be used. Preferably, an inflation method, a T-die method, a cast method or a hot press method can be used. In the case of the production method using the inflation method or the T-die method, an Estatruder type melt extruder with a single or twin screw can be used.
- the melt extrusion temperature for producing the film of the present invention is preferably 150 to 350 ° C, more preferably 200 to 300 ° C.
- melt kneading using a melt extrusion apparatus it is preferable to use a vent to perform melt kneading under reduced pressure or melt kneading under a nitrogen stream from the viewpoint of suppressing coloring.
- solvents such as tetrahydrofuran, acetone, methyl ethyl ketone, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone can be used.
- Preferred solvents are acetone, methyl ethyl ketone, N methyl pyrrolidone and the like.
- the film is prepared by dissolving the thermoplastic resin composition of the present invention in one or more of the above-mentioned solvents and using the bar coater, T die, T die with bar, die coat, etc., to produce polyethylene terephthalate.
- the thermoplastic copolymer (D) is blended with the thermoplastic copolymer (B) obtained by the above-described method, thereby obtaining a thermoplastic copolymer.
- a thermoplastic resin composition having excellent impact resistance can be obtained without significantly impairing the excellent properties of (B).
- the rubber-containing polymer (D) used in the present invention is composed of a layer containing one or more rubber-like polymers, and one or more layers made of a different polymer, and A multi-layered polymer called a core-shell type with a structure containing one or more rubbery polymers inside, or a monomer mixture consisting of a bull monomer in the presence of a rubbery polymer A graft copolymer obtained by copolymerizing a product can be preferably used.
- the number of layers constituting the core-shell multilayer polymer used in the present invention may be 3 or more, or 4 or more, as long as it is 2 or more. It is preferable that the polymer is a multilayer structure polymer having a rubber layer (core layer) of at least one layer.
- the type of the rubber layer is not particularly limited as long as it is composed of a polymer component having rubber elasticity.
- a polymer component having rubber elasticity for example, attalinole monomers, silicone monomers, styrene monomers, nitrile monomers, conjugation monomers, monomers that form urethane bonds, ethylene monomers, propylene
- examples thereof include rubber composed of a polymer obtained by polymerizing a monomer based on isobutene and the like.
- Preferred rubbers include, for example, acrylate units such as ethyl acrylate units and butyl acrylate units, silicone units such as dimethyl siloxane units and phenylmethyl siloxane units, styrene units and ⁇ -methyl styrene units. It is a rubber composed of a styrene unit, a nitrile unit such as an acrylonitrile unit or a metathalonitrile unit, and a conjugate unit such as a butadiene unit or an isoprene unit. A rubber composed of a combination of two or more of these components is also preferred.
- rubber composed of acrylic units such as ethyl acrylate units and butyl acrylate units, and silicone units such as dimethylsiloxane units and phenylmethylsiloxane units, and (2) ethyl acetate units.
- rubbers composed of acrylic units such as butyl acrylate units and styrene units such as styrene units and ⁇ -methylstyrene units.
- Acrylic units such as ethyl acrylate units and butyl acrylate units and butanegen Rubber composed of conjugation units such as units and isoprene units
- acrylic Examples include acrylic units such as ethenyl units and butyl acrylate units, silicone units such as dimethylsiloxane units and phenylmethylsiloxane units, and rubber composed of styrene units such as styrene units and ⁇ -methylstyrene units. It is done. Of these, the most preferable from the viewpoint of rubber strength transparency and mechanical properties containing an alkyl acrylate unit and a substituted or unsubstituted styrene unit.
- a rubber obtained by crosslinking a copolymer composed of a crosslinkable component such as a dibutenebenzene unit, a aryl arylate unit, or a butylene diol ditalate unit is also preferable.
- the type of layer other than the rubber layer is not particularly limited as long as it is composed of a polymer component having thermoplasticity.
- the glass transition temperature is higher than that of the layer! /, Preferably a polymer component.
- Polymers having thermoplastic properties include unsaturated carboxylic acid alkyl ester units, unsaturated carboxylic acid units, unsaturated glycidyl group-containing units, unsaturated dicarboxylic acid anhydride units, aliphatic bull units, aromatic bull units, and cyanide. Examples thereof include polymers containing one or more units selected from a bull unit, a maleimide unit, an unsaturated dicarboxylic acid unit, and other bull units.
- a polymer containing an unsaturated carboxylic acid alkyl ester unit is preferable, and in addition, one or more units selected from unsaturated glycidyl group-containing units, unsaturated carboxylic acid units and unsaturated dicarboxylic anhydride units are used.
- a polymer to be contained is more preferable.
- the monomer used as the raw material for the unsaturated carboxylic acid alkyl ester unit is not particularly limited. However, acrylic acid alkyl ester or methacrylic acid alkyl ester is preferably used. Specifically, methyl acrylate, methyl methacrylate, ethyl acrylate, ethyl acetate, n-propyl acrylate, n-propyl methacrylate, n-butyl acrylate, n-butyl methacrylate, t-butyl acrylate T-butyl methacrylate, n-hexyl acrylate, n-hexyl methacrylate, 2-ethylhexyl acrylate, 2-ethylhexyl methacrylate, cyclohexyl acrylate, cyclohexyl methacrylate, Stearyl acrylate, stearyl methacrylate, octadecyl acrylate, oct
- Examples of the unsaturated carboxylic acid monomer include acrylic acid, methacrylic acid, maleic acid, and a hydrolyzate of maleic anhydride, which are not particularly limited.
- acrylic acid and methacrylic acid are more preferable because they are excellent in thermal stability, and methacrylolic acid is more preferable. These can be used alone or in combination.
- the monomer used as the raw material for the unsaturated glycidyl group-containing unit is not particularly limited, but is glycidyl acrylate, glycidyl methacrylate, glycidyl itaconate, diglycidyl itaconate, allyl glycidyl ether.
- Styrene 4-glycidyl ether, 4-glycidyl styrene, etc., and glycidyl acrylate or glycidyl methacrylate is preferably used from the viewpoint that the effect of improving impact resistance is great. These units can be used alone or in combination of two or more.
- Examples of monomers used as raw materials for the unsaturated dicarboxylic anhydride unit include maleic anhydride, itaconic anhydride, glutaconic anhydride, citraconic anhydride, and aconitic anhydride, which improve impact resistance.
- Maleic anhydride is preferably used from the viewpoint of great effect. These units can be used alone or in combination of two or more.
- ethylene, propylene, butadiene, and the like can be used as a monomer that is a raw material of the aliphatic bulule unit.
- Monomers that can be used as raw materials for the above aromatic bur units include styrene, ⁇ -methylstyrene, 1-burnaphthalene, and 4-methylstyrene. 4 propyl styrene, 4-cyclohexyl styrene, 4-dodecyl styrene, 2-ethyl benzyl styrene, 4 (phenylbutyl styrene) and halogenated styrene can be used.
- the monomers used as raw materials for the cyanide bulule unit include maleimide, N-methylmaleimide, N-ethylmaleimide, N-propylmaleimide, N-isopropylmaleimide, N-cyclomalemaleimide, N-phenylmaleimide, N— (p Bromophenylenole) maleimide and N- (black phenyl) maleimide can be used.
- maleic acid maleic acid monoethyl ester, itaconic acid, phthalic acid, and the like
- monomers that can be used as raw materials for the above other bulls include acrylamide, methacrylamide, N-methylacrylamide, butoxymethylacryloleamide, N-propylmethacrylamide, N-vinyljetylamine, N-acetylvinylamine, It is possible to use arylamine, methallylamine, N-methylarylamine, p-aminostyrene, 2-isopropenyl-oxazoline, 2-buloloxazoline, 2-alkyleneoxazoline, 2-styrylluoxazoline, etc. it can. These monomers can be used alone or in combination of two or more.
- the type of the outermost layer is, as described above, an unsaturated carboxylic acid alkyl ester unit, an unsaturated carboxylic acid unit, an unsaturated glycidyl group.
- At least one selected from polymers containing an unsaturated carboxylic acid alkyl ester unit, an unsaturated carboxylic acid unit, an unsaturated glycidyl group-containing unit, an unsaturated dicarboxylic acid anhydride unit, and the like is preferable.
- a polymer containing an unsaturated carboxylic acid alkyl ester unit and an unsaturated carboxylic acid unit is used as the rubbery polymer (D) to be subjected to melt-kneading with the thermoplastic copolymer (B). It is most preferable to use a multilayer structure polymer having a coalescence as the outermost layer.
- the outermost layer is a polymer containing an unsaturated carboxylic acid alkyl ester unit and an unsaturated carboxylic acid unit
- thermoplastic copolymer (B) of the present invention by heating, as in the production of the thermoplastic copolymer (B) of the present invention described above, The intramolecular cyclization reaction proceeds to produce a dartal anhydride-containing unit represented by the general formula (1). Therefore, the multilayer outermost polymer having a polymer containing an unsaturated carboxylic acid alkyl ester unit and an unsaturated carboxylic acid unit in the outermost layer is blended with the thermoplastic copolymer (B) and heated when melt-kneaded.
- thermoplastic resin composition of the present invention can exhibit extremely high transparency as well as improved mechanical properties such as impact resistance.
- the monomer used as the raw material for the unsaturated carboxylic acid alkyl ester unit is preferably alkyl acrylate or alkyl methacrylate, more preferably methyl acrylate or methyl methacrylate. used.
- acrylic acid or metataric acid is preferred, and methacrylic acid is more preferred.
- the core layer is a butyl acrylate / styrene copolymer
- the outermost layer is a methyl methacrylate / the above general one.
- the core layer is a butyl acrylate / styrene copolymer
- the outermost layer is methyl methacrylate / the above general formula (1)
- the unit is a unit containing phthalic anhydride / methacrylic acid copolymer
- the core layer is dimethylsiloxane / butyl acrylate copolymer and the outermost layer is methyl methacrylate polymer
- the core layer is butadiene / Examples thereof include styrene copolymers whose outermost layer is a methyl methacrylate polymer and those whose core layer is a butyl acrylate polymer and whose outermost layer is a methyl methacrylate polymer.
- a preferable example is one in which either one or both of the rubber layer and the outermost layer is a polymer containing a glycidyl methacrylate unit.
- the layer is a butyl acrylate / styrene polymer
- the outermost layer is a methyl methacrylate / copolymer composed of a unit containing dartaric acid anhydride represented by the general formula (1)
- the core layer is an acrylic acid.
- a continuous phase is a butyl / styrene copolymer whose outermost layer is methyl methacrylate / a unit containing phthalic anhydride represented by the general formula (1) / methacrylic acid polymer. It is possible to approximate the refractive index with the thermoplastic copolymer (B) and to obtain a good dispersion state in the resin composition, and the transparency that can satisfy the demands that have become more sophisticated in recent years. Since it is expressed, it can be used preferably.
- the weight ratio of the core to the shell is preferably 50% by weight or more and 90% by weight or less of the core layer with respect to the entire multilayer structure polymer. 60% by weight or more and 80% by weight or less is more preferable!
- the primary particle diameter of the multilayer structure polymer used in the present invention can be appropriately controlled by the particle diameter of the rubber used for the core layer and the amount of the thermoplastic polymer used for the shell layer.
- the multilayer structure polymer of the present invention a commercially available product that satisfies the above-described conditions may be used. Alternatively, it may be prepared by a known method.
- Examples of commercially available products of the multilayer structure polymer include "Metaprene (registered trademark)” manufactured by Mitsubishi Rayon Co., Ltd., “Kaneace (registered trademark)” manufactured by Kaneka Chemical Industry Co., Ltd. Registered trademark) ”,“ Atariroid (registered trademark) ”manufactured by Rohm and Haas,“ Staffroid® (registered trademark) ”manufactured by Gantz Kasei Kogyo, and“ Parapet (registered trademark) SA ”manufactured by Kuraray Co., Ltd. May be used alone or in combination of two or more.
- rubber-containing graft copolymer used as the rubber-containing polymer (D) of the present invention include an unsaturated carboxylic acid ester monomer in the presence of the rubber polymer.
- Examples of the rubbery polymer used in the graft copolymer include Gen rubber, acrylic rubber, and ethylene rubber. Specific examples include polybutadiene, styrene-butadiene copolymer, styrene-butadiene block copolymer, acrylonitrile butadiene.
- Copolymer butyl acrylate copolymer, polyisoprene, butadiene-methyl methacrylate copolymer, butyl acrylate-methyl methacrylate copolymer, butadiene-ethyl acrylate copolymer, ethylene propylene
- examples thereof include a copolymer, an ethylene propylene copolymer, an ethylene isoprene copolymer, and an ethylene-methyl acrylate copolymer.
- These rubber polymers can be used alone or in a mixture of two or more.
- the graft copolymer in the present invention contains the above monomer (mixture) in the presence of 10 to 80% by weight, preferably 20 to 70% by weight, more preferably 30 to 60% by weight of a rubbery polymer. ) It is obtained by copolymerizing 20 to 90% by weight, preferably 30 to 80% by weight, more preferably 40 to 70% by weight. When the ratio of the rubbery polymer is less than the above range or exceeds the above range, impact strength and surface appearance may be deteriorated.
- the graft copolymer may contain an ungrafted copolymer that is produced when the monomer mixture is graft copolymerized with the rubber polymer.
- the graft ratio is preferably 10 to 100%.
- the graft ratio is a weight ratio of the grafted monomer mixture to the rubbery polymer.
- the intrinsic viscosity of the ungrafted copolymer measured at 30 ° C in the methylethylketone solvent is 0.;! ⁇ 0.6 dl / g of strength S, impact strength and moldability. It is preferably used from the viewpoint of balance.
- the intrinsic viscosity of the graft copolymer according to the present invention measured at 30 ° C in the methyl ethyl ketone solvent is not particularly limited, but is 0.2 to; Is preferably used from the viewpoint of the balance between moldability and moldability, and more preferably 0.3 to 0.7 dl / g.
- the method for producing the graft copolymer in the present invention can be obtained by a known polymerization method such as bulk polymerization, solution polymerization, suspension polymerization, and emulsion polymerization without particular limitation.
- the primary particle size of the graft copolymer used in the present invention can be appropriately controlled by the particle size of the rubbery polymer and the amount of the monomer mixture to be copolymerized.
- thermoplastic resin composition having excellent transparency can be obtained. I like it. Specifically, it is more preferable that the difference in refractive index between the two is 0.05 or less. Is preferably 0.02 or less, more preferably 0.01 or less. In order to satisfy such a refractive index condition, a method of adjusting the composition ratio of each monomer unit of the thermoplastic copolymer (B) and / or the rubber-containing polymer (D) is used. And a method for preparing a rubbery polymer or monomer composition.
- the refractive index difference referred to here is a value measured by the following method.
- the thermoplastic resin composition of the present invention is sufficiently dissolved under appropriate conditions to obtain a cloudy solution, which is separated from the solvent-soluble portion by an operation such as centrifugation. Separate into insoluble parts.
- the measured refractive index 23 ° C, measured wave
- the difference in length 550 nm is defined as the difference in refractive index.
- the copolymer composition of the thermoplastic copolymer (B) and the rubber-containing polymer (D) in the resin composition is obtained after the separation operation of the soluble component and the insoluble component by the solvent described above. Analyze each component individually.
- the weight ratio of the thermoplastic polymer (B) and the rubber-containing polymer (D) is preferably in the range of 99 / ;! to 50/50. More preferably, it is in the range of / ;! to 60/40, and most preferably in the range of 99 / ;! to 70/30.
- thermoplastic resin composition of the present invention When the thermoplastic resin composition of the present invention is produced, a method in which the thermoplastic polymer (A) and the rubber-containing polymer (B) are heated and melt-mixed under an appropriate shearing field. Use.
- the thermoplastic polymer (A) and the rubbery-containing polymer (B) are mixed by heating and mixing the thermoplastic polymer (A) and other optional components in advance. Thereafter, a method of uniformly melting and kneading with a single-screw or twin-screw extruder is preferably used from the viewpoint of dispersibility and productivity.
- melt kneading is performed at a relatively low temperature and at a low rotational speed so that a shearing force is not so much applied.
- Force S is preferred.
- the resin temperature in the needing zone is T
- the 1% decomposition temperature of the rubber-containing polymer (B) is defined as 100-45 using a differential thermal weight simultaneous measurement apparatus (TG / DTA-200, manufactured by Seiko Denshi Kogyo Co., Ltd.) in nitrogen. This is the temperature when the weight reduction rate reaches 1% when the weight before heating is 100% in the heating test conducted in the temperature range of 0 ° C at a rate of temperature increase of 20 ° C / min.
- the resin temperature is lower than the range of the present invention, the melt viscosity becomes extremely high, and melt kneading is practically impossible, which is not preferable.
- the resin temperature is higher than the range of the present invention, reaggregation and coloring of the rubber-containing polymer (B) become remarkable, which is not preferable.
- N exceeds 150, the coloring due to the decomposition and re-aggregation of the dispersed rubber-containing polymer (B) due to the action of shearing force and the accompanying heat generation becomes unfavorable.
- the value of N is smaller than 10, the dispersion of the rubber-containing polymer (B) with insufficient shearing force will be insufficient, leading to deterioration of surface smoothness, impact strength and heat resistance. Therefore, it is not preferable.
- the screw length in the melting zone and the needing zone of the extruder used in the melt-kneading is preferably not too long as compared with the screw diameter.
- the melting zone refers to the area between the resin when the resin is supplied to the screw and reaches the first needing zone, and the position where the resin is completely melted is the start point and the position of the discharge port is the end point.
- the needing zone is composed of a needing disc 'inverted full flight disc. The zone is for kneading and staying of the resin. If there are two or more locations, the zone is the combined region.
- Lm / D ⁇ 30 and Lk / D ⁇ 5 are preferred, where Lm is the screw length in the melting zone, Lk is the screw length in the needing zone, and D is the screw diameter. 25 and Lk / D ⁇ 4.5 are more preferable than force S, and more preferably Lm / D ⁇ 20 and Lk / D ⁇ 4.
- the lower limit is Lm / D ⁇ 10, Lk / D ⁇ 3 from the viewpoint of dispersibility of rubber by shear force It is preferable that When the Lm / D value exceeds 30 and the Lk / D value exceeds 5, the cutting force becomes too strong, and the dispersed rubbery polymer (B) is colored by decomposition and re-aggregation. It is not preferable.
- the dispersion of the rubber-containing polymer (B) becomes insufficient, the surface smoothness deteriorates, and the impact strength decreases the heat resistance. It is easy to cause.
- thermoplastic polymer and thermoplastic resin composition of the present invention are not limited to other thermoplastic resins, for example, polyethylene, polypropylene, acrylic resin, polyamide, and polyester, within the range not impairing the object of the present invention.
- Thermosetting resins such as disulfide resin, polyether ether ketone resin, polyester, polysulfone, polyphenylene oxide, polyacetal, polyimide, polyester terimide, such as phenol resin, melamine resin, polyester resin, silicone resin, epoxy resin
- the power S can further contain one or more selected types.
- hindered phenol, benzotriazole, benzophenone, benzoate, and cyanoacrylate UV absorbers and antioxidants higher fatty acids, acid esters and acid amides, and higher alcohol and other lubricants.
- additives such as phosphorus and silicone non-halogen flame retardants, nucleating agents, amines, sulfonic acids, polyethers and other antistatic agents, pigments, dyes, fluorescent brighteners and other colorants You may make it contain.
- the color of the additive does not adversely affect the thermoplastic polymer, and transparency is not lowered! /.
- thermoplastic resin composition of the present invention is excellent in mechanical properties and molding processability, and can be melt-molded. Therefore, it can be subjected to extrusion molding, injection molding, press molding, and the like. It can be used by molding into pipes, rods, and other molded products having any desired shape and size.
- a known method is used as a method for producing a film comprising the thermoplastic resin composition of the present invention. Power to use s. That is, a production method such as an inflation method, a T-die method, a calendar method, a cutting method, a casting method, an emulsion method, or a hot press method can be used.
- a production method such as an inflation method, a T-die method, a calendar method, a cutting method, a casting method, an emulsion method, or a hot press method can be used.
- T-die method cast method or hot press method
- an Estatruder type melt extruder with a single or twin screw can be used.
- the melt extrusion temperature for producing the film of the present invention is preferably 150 to 350 ° C, more preferably 200 to 300 ° C. Further, when melt kneading using a melt extrusion apparatus, it is preferable to use a vent to perform melt kneading under reduced pressure or melt kneading under a nitrogen stream from the viewpoint of suppressing coloring.
- solvents such as tetrahydrofuran, acetone, methyl ethyl ketone, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone can be used.
- Preferred solvents are acetone, methyl ethyl ketone, N methyl pyrrolidone and the like.
- the film is prepared by dissolving the thermoplastic resin composition of the present invention in one or more of the above-mentioned solvents and using the bar coater, T die, T die with bar, die coat, etc., to produce polyethylene terephthalate. By using a dry method that evaporates and removes the solvent, or a wet method that solidifies the solution with a coagulating liquid. Can be manufactured.
- Machine-related parts such as, optical equipment such as microscopes, binoculars, cameras and watches, precision machine-related parts; alternator terminals, alternator connectors, IC regulators, various valves such as exhaust gas valves, and fuel related exhaust System 'intake pipes, air intake nozzle snorkel, intake hold, fuel pump, engine coolant joint, carburetor main body, carburetor spacer, exhaust gas sensor, coolant sensor, oil temperature sensor, brake Patwaresen Sir, Slot Nore Position Sensor 1, Crankshaft Position Sensor, Air Flow Meter, Thermostat Base for Air Conditioner, Heating Hot Air Flow Control Valve, Radiator Motor Brush Honoreder, Water Pump Impeller, Turbine Vane, Wiper Motor Related Parts, Dust Rejuvenator 1.
- various valves such as exhaust gas valves, and fuel related exhaust System 'intake pipes, air intake nozzle snorkel, intake hold, fuel pump, engine coolant joint, carburetor main body, carburetor spacer, exhaust gas sensor, coolant sensor, oil temperature sensor, brake Patwaresen Sir
- Starter switches Starter switches, starter relays, wire harnesses for transmissions, window washer nozzles, air conditioner panel switch boards, coils for fuel-related solenoid valves, connectors for fuses, horn terminals, electrical component insulation plates, steps.
- optical discs VD, CD, DVD, MD, LD, etc.
- various discs as optical recording / optical communication related components such as photographic lenses such as LA, VTR, projection TV, viewfinder, filter, prism, Fresnel lens, etc.
- Substrate protective film, optical disk player pick-up lens, optical fiber, optical switch, optical connector, and other information equipment related components such as liquid crystal display, flat panel display, plasma display light guide plate, Fresnel lens, polarizing plate, polarizing plate protection Film, retardation film, light diffusion film Tail lamp lenses, parts for transportation equipment such as automobiles, such as viewing angle widening films, reflection films, antireflection films, antiglare films, brightness enhancement films, prism sheets, pickup lenses, light guide films for touch panels, covers, etc.
- Headlamp lens inner lens, amber cap, reflector, extension, side mirror, room mirror
- medical equipment related parts such as glazing typified by a glass, side visor, instrument needle, instrument cover, and window glass
- building material related parts such as eyeglass lenses, eyeglass frames, contact lenses, endoscopes, optical cells for analysis, etc. It can also be applied to lighting windows, road translucent plates, lighting covers, signboards, translucent sound insulation walls, nostab materials, etc., and is extremely useful for these various applications.
- A1 Weight of copolymer (A) after drying (g)
- the unreacted monomer concentration (% by weight) in the copolymer solution (a) and the charged raw material solution was quantified by gas chromatography and calculated from the following equation.
- Ml concentration of unreacted monomer (% by weight) in copolymer solution (a)
- Copolymer (A) before being introduced into the cyclization step and thermoplastic copolymer after cyclization (B) Each lg is dissolved in 20 g of tetrahydrofuran, and unreacted monomer and / or organic remaining by gas chromatography. The solvent (C) was quantified, and the content of volatile components was calculated from the following formula. Volatile content (wt%) ⁇ ( «+ ⁇ ) / ⁇ 1 ⁇ X 100
- composition of each copolymer unit was determined by measuring 1 H-NMR in deuterated dimethyl sulfoxide at 30 ° C.
- thermoplastic copolymer obtained was injection molded at a glass transition temperature of + 140 ° C, and the total light transmittance (%) at 23 ° C of the resulting 1 mm thick molded product was manufactured by Toyo Seiki Co., Ltd. Transparency was evaluated by measuring using a direct reading haze meter.
- thermoplastic copolymer was injection-molded at a glass transition temperature of + 140 ° C, and the YI value of the resulting 1 mm-thick molded product was SM color computer (manufactured by Suga Test Instruments Co., Ltd.) according to JIS K7103. And measured.
- thermoplastic copolymer pellets were dissolved in methyl ethyl ketone at a concentration of 25% by weight with stirring at room temperature for 24 hours, and the obtained thermoplastic copolymer solution was cast into a glass plate shape
- the film was dried at 50 ° C. for 20 minutes and then at 80 ° C. for 30 minutes to produce a film having a thickness of 100 ⁇ 5 mm. This film was observed with an optical microscope, and the number of foreign matters over 20 m per 1 mm square unit area was counted. This was observed at 10 force points per sample at random, and the count of the number of foreign objects was repeated. The average value was evaluated as the number of foreign objects per lmm square unit area (pieces / mm 2 ).
- thermoplastic copolymer (B) pellets 5 g were pre-dried at 80 ° C for 12 hours, and the weight before and after being heat-treated for 30 minutes in a heating furnace adjusted to a glass transition temperature of + 130 ° C.
- the weight reduction rate calculated by the following equation was evaluated as the amount of gas generated during residence.
- Weight loss rate (% by weight) ⁇ (W0— W1) / W0 ⁇ X 100
- W0 weight of thermoplastic copolymer (B) before heat treatment (g)
- W1 Weight of thermoplastic copolymer (B) after heat treatment (g)
- thermoplastic copolymer (B) pellets were pre-dried at 80 ° C for 12 hours, and glass transition temperature + 130 ° C using a Toyo Seiki Co., Ltd.
- Capillograph Type 1C die diameter ⁇ lmm, die length 5 mm Measured at a shear rate of 12 / sec.
- a stainless steel autoclave with a capacity of 20 liters and a double helical stirring blade was continuously supplied at a rate of 8 kg / h with a monomer mixture of the following formulation bubbled with 20 L / min of nitrogen gas for 15 min.
- the mixture was stirred at 50 rpm, the internal temperature was controlled at 130 ° C, and continuous polymerization was carried out with an average residence time of 3 hours.
- the obtained copolymer solution (a) was sampled and analyzed. As a result, the polymerization rate was 60%, and the content of the copolymer (A) in the copolymer solution (a), ie, solid The minute was 60% by weight. Further, the solution viscosity of the obtained copolymer solution (a) was measured at 30 ° C. and found to be 60 Pa ′s. 30 parts by weight methacrylic acid
- the copolymer (A) obtained in the devolatilization process was driven by a gear pump, and the glasses blade was turned into a horizontal twin-shaft agitator (“Hitachi Glasses Blade Polymerizer (trade name)” manufactured by Hitachi, Ltd., capacity 24 L, vent part: 1 place) at a feed rate of 4.7 kg / h, continuously rotating at a screw speed of 10 rpm, a cylinder temperature of 300 ° C, depressurizing from the vent, and performing a cyclization reaction at the pressure lOTorr. And a thermoplastic copolymer (B-1) was produced at a rate of 4.6 kg / h. The average residence time of the cyclizer at this time was 60 minutes.
- the vent part of the twin screw extruder in the pre-devolatilization step was connected to a cooler, and volatile components were recovered at 2.8 kg / h. Subsequently, the recovered liquid obtained was supplied to a distillation column and distilled under reduced pressure at 90 ° C. and 400 Torr, and the recovered liquid was continuously purified to obtain 97% as a recovered raw material. The recovered raw material obtained was recycled as a raw material mixture in the polymerization process.
- thermoplastic copolymer (B — 2) to (B— Production of 7) and recovery of unreacted monomer and organic solvent (C) were carried out.
- Table 3 shows the evaluation results of the obtained thermoplastic copolymer (B).
- a stainless steel autoclave with a capacity of 20 liters and a double helical stirring blade was continuously fed at a rate of 8 kg / h at a rate of 8 kg / h with a raw material mixture of the following formulation published with nitrogen gas at 20 L / min for 15 minutes.
- the mixture was stirred, the internal temperature was controlled at 130 ° C, and continuous polymerization was carried out with an average residence time of 3 hours.
- the polymerization rate was 77%, and the content of copolymer (A) in the copolymer solution (a), that is, solid The minute was 50% by weight. Further, the solution viscosity of the obtained copolymer solution (a) was measured at 30 ° C. and found to be 50 Pa ′s.
- the copolymer (A) obtained in the devolatilization process was driven by a gear pump, and the glasses blade was turned into a horizontal twin-shaft agitator (“Hitachi Glasses Blade Polymerizer (trade name)” manufactured by Hitachi, Ltd., capacity 24 L, vent part: 1 point) at a feed rate of 3.8kg / h, screw rotation speed 10rpm, cylinder temperature 300 ° C, decompression from the vent, cyclization reaction at pressure lOTorr, strand cut And the thermoplastic copolymer (B-8) was produced at a rate of 3.6 kg / h. The average residence time of the cyclizer at this time was 60 minutes.
- the recovered liquid obtained was supplied to a distillation column and distilled under reduced pressure at 90 ° C. and 400 Torr, and the recovered liquid was continuously purified to obtain 97% as a recovered raw material.
- the recovered raw material obtained was recycled as a raw material mixture in the polymerization process.
- a stainless steel autoclave with a capacity of 20 liters and a double helical stirring blade was continuously fed at a rate of 8. Okg / h with a raw material mixture of the following formulation bubbled with nitrogen gas at 20 L / min for 15 minutes, Stirring was performed at 50 rpm, the internal temperature was controlled at 130 ° C, and continuous polymerization was performed with an average residence time of 3 hours.
- the obtained copolymer solution (a) was sampled and analyzed. As a result, the polymerization rate was 77%, and the content of the copolymer (A) in the copolymer solution (a), that is, the solid content was It was 50% by weight. Further, the solution viscosity of the obtained copolymer solution (a) was measured at 30 ° C. and found to be 50 Pa ′s.
- the copolymer (A) obtained in the pre-devolatilization step was further subjected to 44 mm by a gear pump.
- the copolymer (A) obtained in the devolatilization process was driven by a gear pump, and the glasses blade was turned into a horizontal twin-shaft agitator (“Hitachi Glasses Blade Polymerizer (trade name)” manufactured by Hitachi, Ltd., capacity 24 L, vent part: 1 point) at a feed rate of 3.8kg / h, screw speed 10rpm, cylinder temperature 300 ° C, decompression from the vent, cyclization reaction at pressure lOTorr, strand cutter And a thermoplastic copolymer (B-14) was produced at a rate of 3.6 kg / h. The average residence time of the cyclizer at this time was 60 minutes.
- thermoplastic copolymer (B — Production of 15) to (B 19) and recovery of unreacted monomers and organic solvent (C) were carried out.
- Table 3 shows the evaluation results of the obtained thermoplastic copolymer (B).
- MAA Methacrylic acid 1, 1 1 bis 1 t-Butyl carboxycyclohexane ST: Styrene) Lauroyl peroxide
- EGMA Ethylene glycol monomethyl ether
- EGMA Ethylene glycol monomethyl ether
- MAA methacrylic brewer
- EGMA Ethylene glycol monomethyl ether
- MMA Methyl methacrylate
- MAA Methacrylic acid
- MMA Methyl methacrylate
- MAA Methacrylic acid
- a methyl methacrylate / acrylamide copolymer suspension (prepared by the following method) in a stainless steel clave with a capacity of 20 liters and equipped with a baffle and a fudra-type stirring blade.
- 20 parts by weight of methyl methacrylate, acrylamide 80 parts by weight, 0.3 parts by weight of potassium persulfate, 1500 parts by weight of ion-exchanged water are charged into the reactor and maintained at 70 ° C. while the reactor is replaced with nitrogen gas.
- the solution is obtained as an aqueous solution of methyl acrylate and acrylamide copolymer. (The obtained aqueous solution was used as a suspending agent.) 2.
- the copolymer (A) had a polymerization rate of 98% and a weight average molecular weight of 70,000.
- a stainless steel autoclave with a capacity of 20 liters and a double helical stirrer blade is supplied with a total of 10 kg of the monomer mixture of the following formulation with a plunger pump. Publish with 15 minutes of nitrogen gas for 15 minutes. Next, when nitrogen gas was flowed at a flow rate of 5 L / min and the reaction system was stirred, the temperature was raised to 100 ° C. and polymerization was started. At 160 minutes from the start of polymerization, polymerization runaway occurred, Stirring was stopped, making it difficult to continue polymerization.
- Methacrylic acid 25 parts by weight
- a copolymer solution (a) was obtained by the production method disclosed in Patent Document 2 and Example 7.
- the copolymer solution (a) was sampled from the outlet of the polymerization tank and analyzed, and the properties of the obtained copolymer solution (a) and copolymer ( ⁇ ⁇ ⁇ ) are shown in Table 1.
- the copolymer solution (a) obtained in the polymerization step was continuously supplied to a high-temperature vacuum chamber heated to 250 ° C, and the pressure was 50 Torr for 60 minutes. Then, devolatilization and cyclization reaction were performed, and the bulk product was pulverized to obtain a thermoplastic copolymer (B-21). The resulting powder of (B-21) was dried at 100 ° C for 8 hours, and each copolymer component composition and various characteristics evaluation results determined by ifi-NMR are shown in Table 4.
- a copolymer solution (a) was obtained by the production method disclosed in Patent Document 3 and Example 2.
- the copolymer solution (a) was sampled from the outlet of the polymerization tank and analyzed, and the properties of the obtained copolymer solution (a) and copolymer ( ⁇ ⁇ ⁇ ) are shown in Table 1.
- a copolymer solution (a) was obtained by the production method disclosed in Patent Document 4 and Example 17.
- the copolymer solution (a) was sampled from the outlet of the polymerization tank and analyzed, and the properties of the obtained copolymer solution (a) and copolymer ( ⁇ ) are shown in Table 1.
- the copolymer solution (a) obtained in the polymerization step was supplied to a devolatilization tank heated to 260 ° C, and the pressure was 20 Torr for 30 minutes. Volatilization and cyclization were performed to obtain a pellet-shaped thermoplastic copolymer (B-23).
- the resulting powder of (B-23) was dried at 100 ° C for 8 hours, and the composition of each copolymer component and various properties evaluated by NMR are shown in Table 3.
- Example 8 Continuous polymerization was carried out under the same conditions as in Example 8 to produce a copolymer solution (a).
- the obtained copolymer solution (a) was sampled and analyzed.
- the polymerization rate was 80%
- the copolymer ( ⁇ ) content in the copolymer solution (a) that is, the solid content was 40%. % By weight.
- the solution viscosity of the obtained copolymer solution (a) was measured at 30 ° C. and found to be 30 Pa ⁇ s.
- the copolymer solution (a) obtained in the polymerization step is continuously supplied to a high-temperature vacuum chamber heated to 250 ° C., and at a pressure of 50 Torr for 60 minutes. Volatilization and cyclization were performed, and the bulk product was pulverized to obtain a thermoplastic copolymer (B-24). The resulting powder of (B-24) was dried at 100 ° C for 8 hours, and the composition of each copolymer component and various characteristics evaluated by ifi-NMR are shown in Table 3. [Comparative Example 7]
- Example 8 Continuous polymerization was carried out under the same conditions as in Example 8 to produce a copolymer solution (a).
- the obtained copolymer solution (a) was sampled and analyzed.
- the polymerization rate was 80%
- the copolymer ( ⁇ ) content in the copolymer solution (a) that is, the solid content was 40%. % By weight.
- the solution viscosity of the obtained copolymer solution (a) was measured at 30 ° C. and found to be 30 Pa ⁇ s.
- the copolymer solution (a) obtained in the polymerization step is supplied to a devolatilization tank heated to 260 ° C. and devolatilized at a pressure of 20 Torr for 30 minutes.
- a cyclization reaction was performed to obtain a pellet-shaped thermoplastic copolymer (B-25).
- the obtained powder (B-25) was dried at 100 ° C for 8 hours, and the composition of each copolymer component and the results of various characteristic evaluations determined by NMR are shown in Table 3.
- thermoplastic copolymer (B) From the examples;! To 19 and the comparative examples;! To 7, the production method of the present invention is subjected to bulk polymerization or solution polymerization under a specific polymerization condition in the polymerization step, and further from the obtained polymerization solution. After devolatilization to remove the reactive monomer, a cyclization reaction is performed under specific conditions. Excellent, especially with few foreign substances! / The ability to produce thermoplastic copolymer (B)
- the copolymer solution (a) obtained in the pre-polymerization step was continuously withdrawn, and a 2.5-inch inner diameter tubular reactor (SMX type static mixer manufactured by Gebrüter's Zultour, Switzerland) After adding premixed with the copolymer solution (a) by adding 0.005 parts by weight of 1,1-ji-t-butylperoxycyclohexane in the piping part with 30 built-in mixing elements) , Continuously fed to another 2.5-inch tubular reactor installed in series (Gebrütter, Switzerland, Sultour Co., Ltd., SMX static mixer, 30 static mixing elements built-in) to conduct polymerization reaction It was.
- SMX type static mixer manufactured by Gebrüter's Zultour, Switzerland
- the inner wall temperature of the tubular reactor at this time was 130 ° C, and the half-life of the radical polymerization initiator at this inner wall temperature was 12 minutes.
- the average residence time in the tubular reactor was 60 minutes.
- the internal pressure was 25 kg / cm 2 G.
- the polymerization rate was 80%, and the solution viscosity (30 ° C.) of the copolymer solution (a) was 70 Pa ′s.
- this copolymer solution (a) was dissolved in 40 g of tetrahydrofuran and reprecipitated in 500 mL of hexane to obtain 4.0 g of a powdery copolymer (A-26). From this, the polymer content (solid content) was calculated to be 80% by weight. The weight average molecular weight of this copolymer (A-26) was 85000, and the amount of methacrylic acid units in the copolymer (A) was 30% by weight.
- the copolymer (A) obtained in the devolatilization step was rotated by a gear pump, Supply continuously to a shaft agitator (Hitachi Glasses Blade Polymerizer (trade name), manufactured by Hitachi, Ltd., capacity 24L, vent: 1 location) at a supply speed of 3.8kg / h, screw speed 10rpm, The temperature was reduced from the vent at 300 ° C, the cyclization reaction was performed at the pressure lOTorr, pelletized with a strand cutter, and a thermoplastic copolymer (B-8) was produced at a rate of 3.6 kg / h. . The average residence time of the cyclizer at this time was 60 minutes.
- the vent part of the twin screw extruder in the pre-devolatilization step was connected to a cooler, and volatile components were recovered at 4.2 kg / h. Subsequently, the recovered liquid obtained was supplied to a distillation column and distilled under reduced pressure at 90 ° C. and 400 Torr, and the recovered liquid was continuously purified to obtain 97% as a recovered raw material. The recovered raw material obtained was recycled as a raw material mixture in the polymerization process.
- a stainless steel autoclave with a capacity of 20 liters and a double helical stirring blade was continuously supplied at a rate of 5 kg / h with a monomer mixture of the following formulation bubbled with nitrogen gas at 20 L / min for 15 minutes, The mixture was stirred at 50 rpm, the internal temperature was controlled at 130 ° C, and continuous polymerization was carried out with an average residence time of 5 hours.
- the polymerization rate was 40%, and the solution viscosity of the copolymer solution (a) was measured at 30 ° C., and as a result, it was 20 Pa ′s.
- the copolymer solution (a) obtained in the pre-polymerization step was continuously withdrawn, and a 2.5-inch inner diameter tubular reactor (SMX type static mixer manufactured by Gebrüter's Zultour, Switzerland) With 30 internal mixing elements)
- SMX type static mixer manufactured by Gebrüter's Zultour, Switzerland
- the inner wall temperature of the tubular reactor at this time was 130 ° C, and the half-life of the radical polymerization initiator at this inner wall temperature was 12 minutes.
- the average residence time in the tubular reactor was 60 minutes.
- the internal pressure was 25 kg / cm 2 G.
- the polymerization rate was 80%, and the solution viscosity (30 ° C.) of the copolymer solution (a) was 50 Pa ′s.
- this copolymer solution (a) was dissolved in 40 g of tetrahydrofuran and reprecipitated in 500 mL of hexane to obtain 4.0 g of a powdery copolymer (A-27). From this, the polymer content (solid content) was calculated to be 80% by weight. The weight average molecular weight of this copolymer (A-27) was 85000, and the amount of methacrylic acid units in the copolymer (A) was 20% by weight.
- the copolymer (A) obtained in the devolatilization process is driven by a gear pump, and the glasses blade is turned into a horizontal biaxial agitator (Hitachi Glasses Blade Polymerizer (trade name) manufactured by Hitachi, Ltd., capacity 24L, vent: 1 point) at a feed rate of 3.8kg / h, screw speed 10rpm, cylinder temperature 300 ° C, decompression from the vent, cyclization reaction at pressure lOTorr, strand cutter And a thermoplastic copolymer (B-8) was produced at a rate of 3.6 kg / h. The average residence time of the cyclizer at this time was 60 minutes.
- MMA Methyl methacrylate
- MAA Methacrylic acid
- GAH Glutaric anhydride
- Table 5 shows the thermoplastic copolymers (B) obtained in the above Examples;! To 21 and Comparative Examples 1 and 3 to 7, and the rubbery polymer (D) obtained in Reference Example 5.
- kneading at a cylinder temperature of 280 ° C and a screw rotation speed of lOOrpm
- the obtained pellet-shaped thermoplastic resin composition was subjected to an injection molding machine (SG75H MIV manufactured by Sumitomo Heavy Industries, Ltd.) to mold each test piece.
- thermoplastic polymer (B) + 150) ° C glass transition temperature of thermoplastic polymer (B) + 150) ° C, mold temperature: 80 ° C, injection time: 5 seconds, cooling time: 10 seconds, molding pressure: pressure that fills the mold with all the resin (Molding lower limit pressure) + IMPa.
- Table 5 shows the evaluation results of the obtained thermoplastic resin composition.
- thermoplastic resin composition of the present invention contains the thermoplastic copolymer (B) obtained in Examples 1 to 21. From this, it can be seen that the weight loss during the heat retention can be suppressed, and the thermal stability is excellent. That is, it can be seen that the thermoplastic resin composition of the present invention is excellent in high transparency, heat resistance, and toughness, and particularly excellent in thermal stability and color tone. On the other hand, it can be seen that the thermoplastic resin composition outside the scope of the present invention is inferior in terms of color tone and heat loss.
- the present invention is a method for industrially producing a copolymer containing dartaric anhydride units having excellent transparency and thermal stability, and the copolymer obtained by this method is an optical lens or prism. It can be used for optical materials such as mirrors, optical disks, optical fibers, liquid crystal display sheets, films, and light guide plates.
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Description
Claims
Priority Applications (3)
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US12/442,343 US7888456B2 (en) | 2006-09-20 | 2007-09-13 | Process for production of thermoplastic copolymer |
CN2007800429829A CN101616940B (zh) | 2006-09-20 | 2007-09-13 | 热塑性共聚物的制造方法 |
EP07807192A EP2065410A4 (en) | 2006-09-20 | 2007-09-13 | PROCESS FOR PREPARING THERMOPLASTIC COPOLYMER |
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US (1) | US7888456B2 (ja) |
EP (1) | EP2065410A4 (ja) |
KR (1) | KR20090068215A (ja) |
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US20150085362A1 (en) * | 2008-10-02 | 2015-03-26 | Lg Chem, Ltd | Optical film and method of preparing same |
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US11311196B2 (en) | 2018-02-23 | 2022-04-26 | Boston Scientific Scimed, Inc. | Methods for assessing a vessel with sequential physiological measurements |
WO2019183432A1 (en) | 2018-03-23 | 2019-09-26 | Boston Scientific Scimed, Inc. | Medical device with pressure sensor |
WO2019195721A1 (en) | 2018-04-06 | 2019-10-10 | Boston Scientific Scimed, Inc. | Medical device with pressure sensor |
US11666232B2 (en) | 2018-04-18 | 2023-06-06 | Boston Scientific Scimed, Inc. | Methods for assessing a vessel with sequential physiological measurements |
WO2022122806A1 (en) | 2020-12-09 | 2022-06-16 | Röhm Gmbh | Optical grade moulding compositions having increased heat resistance |
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US9690027B2 (en) * | 2008-10-02 | 2017-06-27 | Lg Chem, Ltd. | Optical film and method of preparing same |
Also Published As
Publication number | Publication date |
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CN101616940B (zh) | 2012-06-20 |
US20100087605A1 (en) | 2010-04-08 |
US7888456B2 (en) | 2011-02-15 |
EP2065410A1 (en) | 2009-06-03 |
KR20090068215A (ko) | 2009-06-25 |
MY145624A (en) | 2012-03-15 |
CN101616940A (zh) | 2009-12-30 |
EP2065410A4 (en) | 2012-08-08 |
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