WO2015119233A1 - (メタ)アクリル樹脂組成物の製造方法 - Google Patents
(メタ)アクリル樹脂組成物の製造方法 Download PDFInfo
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- WO2015119233A1 WO2015119233A1 PCT/JP2015/053341 JP2015053341W WO2015119233A1 WO 2015119233 A1 WO2015119233 A1 WO 2015119233A1 JP 2015053341 W JP2015053341 W JP 2015053341W WO 2015119233 A1 WO2015119233 A1 WO 2015119233A1
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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
- C08F20/00—Homopolymers and 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
- C08F20/62—Monocarboxylic acids having ten or more carbon atoms; Derivatives thereof
- C08F20/68—Esters
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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
- C08F120/00—Homopolymers 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
- C08F120/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
- C08F120/10—Esters
- C08F120/12—Esters of monohydric alcohols or phenols
- C08F120/14—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
- C08F2/02—Polymerisation in bulk
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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
- C08F2/38—Polymerisation using regulators, e.g. chain terminating agents, e.g. telomerisation
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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
- C08F20/00—Homopolymers and 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
- C08F20/02—Monocarboxylic acids having less than ten carbon atoms, Derivatives thereof
- C08F20/10—Esters
- C08F20/12—Esters of monohydric alcohols or phenols
- C08F20/14—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
- 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
- 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
- C08F220/16—Esters of monohydric alcohols or phenols of phenols or of alcohols containing two or more carbon atoms
- C08F220/18—Esters of monohydric alcohols or phenols of phenols or of alcohols containing two or more carbon atoms with acrylic or methacrylic acids
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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
- C08F6/00—Post-polymerisation treatments
- C08F6/06—Treatment of polymer solutions
- C08F6/10—Removal of volatile materials, e.g. solvents
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L33/00—Compositions of homopolymers or 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 of salts, anhydrides, esters, amides, imides or nitriles thereof; Compositions of derivatives of such polymers
- C08L33/04—Homopolymers or copolymers of esters
- C08L33/06—Homopolymers or copolymers of esters of esters containing only carbon, hydrogen and oxygen, which oxygen atoms are present only as part of the carboxyl radical
Definitions
- the present invention relates to a method for producing a (meth) acrylic resin composition. More specifically, in the present invention, in the continuous bulk polymerization method, even when the operation is temporarily stopped, the polymerization conversion rate of the reaction liquid in the reaction tank is hardly changed, and the deterioration of the raw material liquid staying in the pipe does not proceed.
- the present invention relates to a method for producing a (meth) acrylic resin composition.
- a molded product made of a (meth) acrylic resin composition has excellent transparency and little optical distortion, it is used for optical lenses, disk substrates, automobile parts, signboards, nameplates, lighting covers, light guide plates, and the like.
- a raw material liquid containing a polymerizable monomer, a polymerization initiator, etc. is continuously supplied to a tank reactor to perform bulk polymerization and continuously produce a reaction product.
- This continuous bulk polymerization method is suitable for producing a large amount of a (meth) acrylic resin composition having excellent optical properties.
- the operation may be stopped for cleaning or replacement of parts.
- the temperature of the reaction solution in the polymerization tank is lowered in order to prevent oxidation and deterioration of the resin, or all of the reaction solution is withdrawn from the polymerization tank as necessary. For this reason, it takes time and effort to resume operation, and the loss of raw materials and heat is one of the causes of increased manufacturing costs.
- One countermeasure is to maintain the amount, temperature, and polymerization conversion rate of the reaction liquid in the tank reactor while the supply of the polymerizable monomer and polymerization initiator is stopped using a chain transfer agent.
- Japanese Patent Application Laid-Open No. H10-228561 proposes a method for performing this.
- the object of the present invention is to prevent the polymerization conversion rate of the reaction liquid in the reaction vessel from changing substantially even when the operation is temporarily stopped in the continuous bulk polymerization method, and also to prevent deterioration of the raw material liquid staying in the pipe or the like. It is possible to provide a method for producing a (meth) acrylic resin composition.
- a raw material solution containing methyl methacrylate, alkyl acrylate and chain transfer agent in a mass ratio of alkyl acrylate / methyl methacrylate of 0/100 to 20/80 and having a dissolved oxygen concentration of 50 ppm or less ( A) Prepare Containing a radical polymerization initiator, a polymerization inhibitor and methyl methacrylate, and preparing a raw material liquid (B) maintained at a liquid temperature of 10 ° C.
- the raw material liquid (A) and the raw material liquid (B) are continuously supplied to the tank reactor, Bulk reaction at a polymerization conversion rate of 40 to 70% by mass in a tank reactor to obtain a reaction product,
- a method for producing a (meth) acrylic resin composition comprising a step of continuously extracting a reaction product from a tank reactor.
- a raw material liquid containing a polymerization initiator and a tank reactor The reaction liquid inside can be maintained in a stable state, and the operation can be stabilized immediately even when the operation is resumed.
- the method for producing a (meth) acrylic resin composition includes preparing a raw material liquid (A), preparing a raw material liquid (B), and preparing a raw material liquid (A) and a raw material liquid (B). Is continuously supplied to the tank reactor, bulk polymerization is performed in the tank reactor to obtain a reaction product, and the reaction product is continuously extracted from the tank reactor.
- the raw material liquid (A) contains methyl methacrylate, alkyl acrylate and a chain transfer agent.
- the methyl methacrylate and alkyl acrylate contained in the raw material liquid (A) are preferably in a mass ratio of alkyl acrylate / methyl methacrylate, preferably 0/100 to 20/80, more preferably 0/100 to 10 / 90.
- the total supply amount of methyl methacrylate and alkyl acrylate contained in the raw material liquid (A) may be contained in the raw material liquid (A) from 100 parts by mass of all polymerizable monomers used for polymerization. It is the amount obtained by subtracting the supply amount of methyl methacrylate contained in the other polymerizable monomer and the raw material liquid (B) described later.
- alkyl acrylate examples include methyl acrylate, ethyl acrylate, propyl acrylate, butyl acrylate, and 2-ethylhexyl acrylate. These alkyl acrylates can be used alone or in combination of two or more. Of these, methyl acrylate is preferred.
- the raw material liquid (A) can contain other polymerizable monomers.
- the polymerizable monomer include methacrylic acid alkyl esters other than methyl methacrylate such as ethyl methacrylate, propyl methacrylate, butyl methacrylate and 2-ethylhexyl methacrylate; aryl methacrylates such as phenyl methacrylate; methacrylic acid Methacrylic acid cycloalkyl esters such as cyclohexyl and norbornenyl methacrylate; Acrylic acid aryl esters such as phenyl acrylate; Acrylic acid cycloalkyl esters such as cyclohexyl acrylate and norbornenyl acrylate; Styrene, ⁇ -methylstyrene, etc.
- Examples include vinyl monomers having only one polymerizable alkenyl group in one molecule such as aromatic vinyl monomer; acrylamide; methacrylamide; acrylonitrile; methacrylonitrile; It is.
- the amount of the other polymerizable monomer is preferably 10 parts by mass or less, more preferably 5 parts by mass or less, with respect to 100 parts by mass of all the polymerizable monomers subjected to polymerization.
- the methyl methacrylate, acrylic acid alkyl ester and other polymerizable monomers used in the present invention preferably contain a polymerization inhibitor.
- the polymerization inhibitor is not particularly limited as long as it exhibits a polymerization inhibition effect in the presence of oxygen, but is preferably one that does not inhibit the polymerization reaction under an inert gas atmosphere.
- Typical examples of such a polymerization inhibitor include phenol-based polymerization inhibitors such as butylxylenol, methoquinone and hydroquinone; phenothiazine and the like.
- the content of such a polymerization inhibitor is preferably from 0.1 ppm to 50 ppm, more preferably from 0.5 ppm to 30 ppm, based on the total amount of polymerizable monomers contained in the raw material liquid (A).
- Examples of the chain transfer agent contained in the raw material liquid (A) include n-octyl mercaptan, n-dodecyl mercaptan, t-dodecyl mercaptan, 1,4-butanedithiol, 1,6-hexanedithiol, ethylene glycol bisthiol.
- chain transfer agents can be used alone or in combination of two or more.
- the amount of the chain transfer agent is preferably 0.1 to 1 part by weight, more preferably 0.2 to 0.8 part by weight, based on 100 parts by weight of all polymerizable monomers subjected to polymerization.
- the amount is preferably 0.3 to 0.6 parts by mass.
- the dissolved oxygen concentration of the raw material liquid (A) is 50 ppm or less, preferably 1 ppm or less. When the dissolved oxygen concentration of the raw material liquid (A) is large, stable polymerization may be hindered.
- b * is preferably ⁇ 1 to 2, and more preferably ⁇ 0.5 to 1.5.
- CIE International Commission on Illumination
- the raw material liquid (A) is not particularly limited by its preparation method.
- it can be obtained by mixing methyl methacrylate, alkyl acrylate and chain transfer agent at a predetermined ratio, and then contacting with an inert gas such as nitrogen gas to drive out dissolved oxygen.
- the methyl methacrylate, acrylic acid alkyl ester and chain transfer agent used in the raw material liquid (A) are polymerized as described below, with virgin ones that have been transferred from the raw material tank (not yet subjected to the polymerization reaction). It may include those that have been subjected to the reaction but recovered as unreacted substances.
- the recovered unreacted material may contain a dimer or trimer in addition to methyl methacrylate, alkyl acrylate and chain transfer agent.
- b * may be high in the unreacted material due to heat applied during recovery. In such a case, it is purified by a known method to remove the dimer or trimer, and b * is preferably ⁇ 1 to 2, more preferably ⁇ 0.5 to 1.5. can do. When the b * is in this range, when the resulting (meth) acrylic resin composition is molded, it is advantageous for obtaining a molded product with little coloration with high production efficiency.
- the supply amount (kg / h) of the raw material liquid (A) relative to the supply amount of inert gas (Nm 3 / h) may be less than 0.30. preferable. With such a supply amount ratio, the dissolved oxygen concentration of the raw material liquid (A) can be efficiently reduced.
- the inert gas can be bubbled in the raw material liquid (A).
- the raw material liquid (B) contains a radical polymerization initiator, a polymerization inhibitor and methyl methacrylate.
- the radical polymerization initiator contained in the raw material liquid (B) is not particularly limited as long as it generates reactive radicals. However, the half-life at a temperature in the tank reactor described later is 0.5 to 120 seconds. Preferably 2 to 60 seconds.
- the polymerization initiator preferably has a hydrogen abstraction ability of 40% or less, and more preferably 30% or less. These polymerization initiators can be used alone or in combination of two or more.
- radical polymerization initiator examples include t-hexyl peroxyisopropyl monocarbonate, t-hexyl peroxy 2-ethylhexanoate, 1,1,3,3-tetramethylbutylperoxy 2-ethylhexanoate, t-butylperoxypivalate, t-hexylperoxypivalate, t-butylperoxyneodecanoate, t-hexylperoxyneodecanoate, 1,1,3,3-tetramethylbutylperper Oxyneodecanoate, 1,1-bis (t-hexylperoxy) cyclohexane, benzoyl peroxide, 3,5,5-trimethylhexanoyl peroxide, lauroyl peroxide, 2,2'-azobis (2-methyl) Propionitrile), 2,2′-azobis (2-methylbutyronitrile), di And methyl 2,2'-azobis (2-methylpropionate
- 2,2′-azobis (2-methylpropionitrile), t-hexylperoxy 2-ethylhexanoate, 1,1-bis (t-hexylperoxy) cyclohexane, dimethyl 2,2 ′ -Azobis (2-methylpropionate) is preferred.
- the hydrogen abstraction ability can be known from technical data (for example, Non-Patent Document 1) of the polymerization initiator manufacturer. Further, it can be measured by a radical trapping method using ⁇ -methylstyrene dimer, that is, ⁇ -methylstyrene dimer trapping method. The measurement is generally performed as follows. First, the polymerization initiator is cleaved in the presence of ⁇ -methylstyrene dimer as a radical trapping agent to generate radical fragments. Among the generated radical fragments, radical fragments having a low hydrogen abstraction ability are added to and trapped by the double bond of ⁇ -methylstyrene dimer.
- a radical fragment having a high hydrogen abstraction capacity abstracts hydrogen from cyclohexane to generate a cyclohexyl radical, and the cyclohexyl radical is added to and trapped by a double bond of ⁇ -methylstyrene dimer to generate a cyclohexane trapping product. Therefore, the ratio (mole fraction) of radical fragments having a high hydrogen abstraction capacity with respect to the theoretical radical fragment generation amount, which is obtained by quantifying cyclohexane or cyclohexane supplement product, is defined as the hydrogen abstraction capacity.
- the supply amount of the radical polymerization initiator is smaller than the supply amount of the raw material liquid (A), it is diluted by dissolving the radical polymerization initiator in methyl methacrylate to facilitate the supply of the radical polymerization initiator.
- the concentration of the radical polymerization initiator in the raw material liquid (B) is preferably 0.01% by mass to less than 4% by mass, more preferably 0.1% by mass to less than 2% by mass. Since the raw material liquid (B) having a radical polymerization initiator concentration that is too low needs to be supplied in a large amount to the reaction vessel, the polymerization tends to become unstable.
- the raw material liquid (B) having a radical polymerization initiator concentration that is too high has low storage stability, if the operation is stopped for a long period of time, there is a tendency that inconvenience is likely to occur when the operation is resumed.
- the polymerization inhibitor contained in the raw material liquid (B) is not particularly limited as long as it exhibits a polymerization inhibition effect in the presence of oxygen, but is preferably one that does not inhibit the polymerization in an inert gas atmosphere.
- Typical examples of such a polymerization inhibitor include phenol-based polymerization inhibitors such as butylxylenol, methoquinone and hydroquinone; phenothiazine and the like.
- the content of such a polymerization inhibitor is preferably 0.1 ppm to 50 ppm, more preferably 0.5 ppm to 30 ppm with respect to methyl methacrylate contained in the raw material liquid (B).
- the raw material liquid (B) is maintained at a liquid temperature of 10 ° C. or lower, preferably 5 ° C. or lower, more preferably 2 ° C. or lower, and further preferably 0 ° C. or lower.
- Oxygen can be present, for example, by blowing air into the raw material liquid (B) preparation tank.
- the temperature of the raw material liquid (B) is maintained at 10 ° C. or lower, alteration of the raw material liquid (B) is suppressed.
- the temperature is higher than 10 ° C., radicals are generated by decomposition of the radical polymerization initiator, and the polymerization reaction of methyl methacrylate as a solvent may proceed.
- a solvent is not used in principle, but when it is necessary to adjust the viscosity, the solvent can be contained in the raw material liquid (A) or the raw material liquid (B).
- the solvent aromatic hydrocarbons such as benzene, toluene and ethylbenzene are preferable. These solvents can be used alone or in combination of two or more.
- the amount of the solvent used is preferably 30 parts by mass or less, more preferably 10 parts by mass or less, with respect to 100 parts by mass of all polymerizable monomers to be subjected to polymerization.
- the tank reactor used in the method of the present invention is usually a reaction tank, a stirring means for stirring the liquid in the reaction tank, a supply port for supplying the raw material liquid to the reaction tank, and a reaction generated from the reaction tank. It has an outlet for extracting objects.
- the supply port for supplying the raw material liquid to the reaction tank may be installed on the top surface of the reaction tank, or may be installed on the side surface of the reaction tank. However, it may be installed on the bottom of the reaction vessel.
- the height of the supply port may be higher than the liquid level in the reaction tank, or may be lower than the liquid level in the reaction tank.
- the shape of the supply port may be the shape of the cut end of the circular tube itself, or may be a shape in which the raw material liquid is widely dispersed on the liquid surface in the reaction tank.
- the method for supplying the raw material liquid (A) and the raw material liquid (B) to the tank reactor is not particularly limited.
- the raw material liquid (A) and the raw material liquid (B) may be supplied through the respective supply ports, or a tank type having at least one supply port.
- the flow of the raw material liquid (A) and the flow of the raw material liquid (B) may be merged in a pipe or mixing tank immediately before the supply port, and then supplied through the supply port.
- the junction may be equipped with a dynamic stirrer or a static stirrer.
- the supply amount of the raw material liquid (A) and the raw material liquid (B) to the tank reactor is preferably 10/1 to 1000/1 as the mass ratio of the raw material liquid (A) to the raw material liquid (B).
- the ratio of the supply amount of the raw material liquid (A) is too large, the radical polymerization initiator concentration of the raw material liquid (B) must be increased in order to start the polymerization reaction. As a result, the storage stability of the raw material liquid (B) tends to decrease.
- the ratio of the supply amount of the raw material liquid (A) is too small, the dissolved oxygen concentration in the polymerization reaction tank becomes high and the polymerization tends to become unstable.
- the total amount of the raw material liquid supplied to the reaction tank and the total amount of the reaction product withdrawn from the reaction tank are balanced so that the liquid volume in the reaction tank becomes substantially constant.
- the amount of liquid in the reaction tank is preferably 1 ⁇ 4 or more, more preferably 1/4 to 3/4, and still more preferably 1/3 to 2/3 with respect to the volume of the reaction tank.
- the bulk polymerization reaction is preferably carried out in an inert gas atmosphere by introducing an inert gas into the gas phase portion of the reaction vessel.
- the stirring means include a Max blend type stirring device, a lattice blade type stirring device, a propeller type stirring device, a screw type stirring device, a helical ribbon type stirring device, and a paddle type stirring device.
- the Max blend type stirring device is preferable from the viewpoint of uniform mixing.
- the temperature in the tank reactor that is, the temperature of the liquid in the reaction tank is preferably 100 to 170 ° C, more preferably 110 to 160 ° C, and still more preferably 115 to 150 ° C.
- the liquid temperature can be controlled by an external heat exchange type adjustment method such as a jacket or a heat transfer tube, a self heat exchange type adjustment method in which a raw material liquid or a tube through which a reaction product flows is arranged in the reaction tank.
- bulk polymerization is preferably carried out until the polymerization conversion becomes 40 to 70% by mass, preferably 42 to 65% by mass.
- the water content in the reaction liquid in the tank reactor is preferably 1000 ppm or less, more preferably 700 ppm or less, and 280 ppm or less. Is more preferable.
- the moisture is preferably 1000 ppm or less, it is possible to suppress the generation of resin foreign matter having a size of several ⁇ m to several tens of ⁇ m during the polymerization reaction, and the obtained (meth) acrylic resin composition is formed into a film or sheet by melt molding. Occasionally, the occurrence of a defect with an outer diameter of several tens of ⁇ m with the resin foreign substance as a core can be greatly reduced.
- the high molecular weight (meth) acrylic resin produced in the gas phase part of the reaction vessel is mixed in as a resin foreign matter, which becomes an unmelted product at the core of the defect during melt molding. Estimated to be.
- an inert gas is introduced into the gas phase portion of the tank reactor or a method of treating the raw material liquid with an adsorption dehydration tower or the like before supplying it to the tank reactor, Examples include a method in which a part of the vapor is accompanied by an inert gas, condensed by a brine-cooled condenser, and extracted out of the system.
- Another reactor may be connected to the subsequent stage of the tank reactor.
- the reactor that can be connected to the subsequent stage may be a tank reactor or a tube reactor.
- the bulk polymerization can be further advanced to further increase the polymerization conversion rate.
- the reaction product obtained by the bulk polymerization as described above is withdrawn from a tank reactor (or a downstream reactor when another reactor is connected to the downstream). It is preferable to balance the extraction amount of the reaction product with the supply amount of the raw material liquid so that the liquid amount in the reaction tank is constant.
- the reaction product contains a (meth) acrylic resin, an unreacted polymerizable monomer (such as methyl methacrylate or an alkyl acrylate ester), and an unreacted chain transfer agent.
- the content of (meth) acrylic resin in the reaction product is preferably 40 to 70% by mass, more preferably 42 to 65% by mass.
- a large stirring power tends to be required for increasing the viscosity.
- the content of the (meth) acrylic resin is too low, the removal of the unreacted product in the step of removing the unreacted product in the reaction product becomes insufficient, and the resulting (meth) acrylic resin composition is molded. , There is a tendency to cause appearance defects such as silver in the molded product.
- the weight average molecular weight (hereinafter sometimes abbreviated as Mw) of the (meth) acrylic resin is preferably 35,000 to 200,000, more preferably 40,000 to 150,000, and even more preferably 45,000 to 130,000.
- Mw weight average molecular weight
- Mw is too small, the impact resistance and toughness of the molded product obtained from the (meth) acrylic resin composition tend to decrease.
- Mw is too large, the fluidity of the (meth) acrylic resin composition is lowered and the moldability tends to be lowered.
- the (meth) acrylic resin has a weight average molecular weight / number average molecular weight ratio (hereinafter, this ratio may be referred to as a molecular weight distribution), preferably 1.5 to 2.6, more preferably 1.6. To 2.3, particularly preferably 1.7 to 2.0.
- a weight average molecular weight and a number average molecular weight are molecular weights of standard polystyrene conversion measured by GPC (gel permeation chromatography).
- the weight average molecular weight and molecular weight distribution of the (meth) acrylic resin can be controlled by adjusting the types and amounts of the polymerization initiator and the chain transfer agent.
- Unreacted substances contained in the reaction product can be recovered by known chemical engineering means.
- a recovery method for example, a method by heat devolatilization is preferable.
- the heat devolatilization method include an equilibrium flash evaporation method and an adiabatic flash evaporation method, but an adiabatic flash evaporation method is preferable.
- the temperature at which the adiabatic flash evaporation method is performed is preferably 200 to 300 ° C., more preferably 220 to 270 ° C. If the temperature at which the adiabatic flash evaporation method is performed is less than 200 ° C., it takes time for devolatilization, resulting in insufficient devolatilization, which may cause appearance defects such as silver in the molded product.
- the (meth) acrylic resin composition tends to be colored due to oxidation, burning, or the like.
- the adiabatic flash evaporation method may be performed in multiple stages.
- the reaction product flowing through the heat transfer tube can be heated with the unreacted vapor that has been flash evaporated, and the heated reaction product can be fed into a low pressure flash tank for flash evaporation.
- the reaction product can be pressurized by a pump or the like.
- the unreacted material just recovered by the pressure devolatilization method includes a dimer or a trimer in addition to methyl methacrylate, an alkyl acrylate ester, and a chain transfer agent. Since the dimer or trimer may affect the properties of the (meth) acrylic resin, it is preferably removed from the unreacted material. In removing the dimer or trimer, a part of the chain transfer agent and the solvent may be removed. Removal of the dimer or trimer can be carried out by known chemical engineering means. For example, a distillation method is preferable.
- the distillation column used in the present invention is not particularly limited, but is preferably a multistage distillation column having about 6 to 20 stages and a reflux ratio of about 0.4 to 2.0.
- the (meth) acrylic resin composition according to the present invention is obtained by recovering the unreacted product from the reaction product.
- the obtained (meth) acrylic resin composition can be made into pellets or particles according to a known method in order to facilitate handling as a molding material.
- the amount of the polymerizable monomer remaining in the (meth) acrylic resin composition obtained in the present invention is preferably 1% by mass or less, and more preferably 0.5% by mass or less.
- additives can be blended in the (meth) acrylic resin composition obtained by the production method of the present invention, if necessary.
- the amount of the additive is preferably 0.5% by mass or less, more preferably 0.2% by mass or less, based on the (meth) acrylic resin composition. If the amount of the additive is too large, appearance defects such as silver may occur in the molded product.
- Additives include antioxidants, thermal degradation inhibitors, UV absorbers, light stabilizers, lubricants, mold release agents, polymer processing aids, antistatic agents, flame retardants, dyes and pigments, light diffusing agents, organic dyes , Matting agents, impact resistance modifiers, phosphors and the like.
- An antioxidant exhibits the effect of preventing oxidative degradation of the resin alone in the presence of oxygen.
- examples thereof include phosphorus antioxidants, hindered phenol antioxidants, and thioether antioxidants. These antioxidants can be used alone or in combination of two or more.
- a phosphorus-based antioxidant or a hindered phenol-based antioxidant is preferable, and a combination of a phosphorus-based antioxidant and a hindered phenol-based antioxidant is more preferable. preferable.
- the ratio is not particularly limited, but is preferably a mass ratio of phosphorus antioxidant / hindered phenol antioxidant, preferably 1/5. ⁇ 2 / 1, more preferably 1 ⁇ 2 to 1/1.
- Examples of phosphorus antioxidants include 2,2-methylenebis (4,6-di-t-butylphenyl) octyl phosphite (Asahi Denka Co., Ltd .; trade name: ADK STAB HP-10), Tris (2,4-dit -Butylphenyl) phosphite (manufactured by Ciba Specialty Chemicals; trade name: IRUGAFOS168), 3,9-bis (2,6-di-t-butyl-4-methylphenoxy) -2,4,8,10 -Tetraoxa-3,9-diphosphaspiro [5.5] undecane (manufactured by ADEKA; trade name: ADK STAB PEP-36) is preferred.
- pentaerythrityl-tetrakis [3- (3,5-di-t-butyl-4-hydroxyphenyl) propionate] (manufactured by Ciba Specialty Chemicals; trade name IRGANOX 1010)
- Octadecyl-3- (3,5-di-t-butyl-4-hydroxyphenyl) propionate (manufactured by Ciba Specialty Chemicals; trade name IRGANOX 1076) is preferred.
- the thermal degradation inhibitor can prevent thermal degradation of the resin by scavenging polymer radicals generated when exposed to high heat in a substantially oxygen-free state.
- the thermal degradation inhibitor include 2-t-butyl-6- (3′-t-butyl-5′-methyl-hydroxybenzyl) -4-methylphenyl acrylate (manufactured by Sumitomo Chemical Co., Ltd .; trade name Sumilizer GM), 2,4-di-t-amyl-6- (3 ′, 5′-di-t-amyl-2′-hydroxy- ⁇ -methylbenzyl) phenyl acrylate (manufactured by Sumitomo Chemical Co., Ltd .; trade name Sumitizer GS) preferable.
- the ultraviolet absorber is a compound having an ability to absorb ultraviolet rays.
- the ultraviolet absorber is a compound that is said to have a function of mainly converting light energy into heat energy.
- Examples of the ultraviolet absorber include benzophenones, benzotriazoles, triazines, benzoates, salicylates, cyanoacrylates, succinic anilides, malonic esters, formamidines, and the like. These can be used alone or in combination of two or more.
- benzotriazoles or ultraviolet absorbers having a maximum molar extinction coefficient ⁇ max at a wavelength of 380 to 450 nm of 1200 dm 3 ⁇ mol ⁇ 1 cm ⁇ 1 or less are preferable.
- an ultraviolet absorber used when a (meth) acrylic resin composition is applied to applications requiring the above properties is applied to applications requiring the above properties. As preferred.
- benzotriazoles examples include 2- (2H-benzotriazol-2-yl) -4- (1,1,3,3-tetramethylbutyl) phenol (manufactured by Ciba Specialty Chemicals; trade name TINUVIN329), 2 -(2H-benzotriazol-2-yl) -4,6-bis (1-methyl-1-phenylethyl) phenol (manufactured by Ciba Specialty Chemicals; trade name TINUVIN234), 2,2'-methylenebis [4 -T-octyl-6- (2H-benzotriazol-2-yl) phenol] (manufactured by ADEKA; LA-31), 2- (5-octylthio-2H-benzotriazol-2-yl) -6-tert- Butyl-4-methylphenol and the like are preferable.
- the ultraviolet absorber having the maximum molar extinction coefficient ⁇ max at wavelengths of 380 to 450 nm of 1200 dm 3 ⁇ mol ⁇ 1 cm ⁇ 1 or less can suppress the yellowness of the obtained molded product.
- an ultraviolet absorber having a maximum molar extinction coefficient ⁇ max at a wavelength of 380 to 450 nm of 1200 dm 3 ⁇ mol ⁇ 1 cm ⁇ 1 or less, 2-ethyl-2′-ethoxy-oxalanilide (manufactured by Clariant Japan, Inc .; Trade name Sundeyuboa VSU).
- benzotriazoles are preferably used from the viewpoint of suppressing resin degradation due to ultraviolet irradiation.
- the light stabilizer is a compound that is said to have a function of capturing radicals generated mainly by oxidation by light.
- Suitable light stabilizers include hindered amines such as compounds having a 2,2,6,6-tetraalkylpiperidine skeleton.
- the mold release agent is a compound having a function of facilitating release of the molded product from the mold.
- the release agent include higher alcohols such as cetyl alcohol and stearyl alcohol; glycerin higher fatty acid esters such as stearic acid monoglyceride and stearic acid diglyceride.
- the ratio is not particularly limited, but the mass ratio of higher alcohols / glycerin fatty acid monoester is preferably 2.5 / 1 to 3.5 / 1. The preferred range is 2.8 / 1 to 3.2 / 1.
- the polymer processing aid is a compound that exhibits an effect on thickness accuracy and thinning when a (meth) acrylic resin composition is molded.
- the polymer processing aid is polymer particles having a particle diameter of 0.05 to 0.5 ⁇ m, which can be usually produced by an emulsion polymerization method.
- the polymer particles may be single layer particles composed of polymers having a single composition ratio and single intrinsic viscosity, or multilayer particles composed of two or more kinds of polymers having different composition ratios or intrinsic viscosities. May be.
- particles having a two-layer structure having a polymer layer having a low intrinsic viscosity in the inner layer and a polymer layer having a high intrinsic viscosity of 5 dl / g or more in the outer layer are preferable.
- the polymer processing aid preferably has an intrinsic viscosity of 3 to 6 dl / g. If the intrinsic viscosity is too small, the effect of improving moldability is low. If the intrinsic viscosity is too large, the melt fluidity of the (meth) acrylic resin composition tends to be lowered.
- An impact modifier may be added to the (meth) acrylic resin composition.
- the impact modifier include a core-shell type modifier containing acrylic rubber or diene rubber as a core layer component; a modifier containing a plurality of rubber particles, and the like.
- the organic dye a compound having a function of converting ultraviolet rays that are harmful to the resin into visible light is preferably used.
- the light diffusing agent and matting agent include glass fine particles, polysiloxane crosslinked fine particles, crosslinked polymer fine particles, talc, calcium carbonate, and barium sulfate.
- the phosphor include a fluorescent pigment, a fluorescent dye, a fluorescent white dye, a fluorescent brightener, and a fluorescent bleach.
- additives may be added at the reaction raw material stage, may be added at the reaction product stage, or may be added at the stage of the (meth) acrylic resin composition obtained after devolatilization. Good.
- molded products can be obtained by molding (melt heat molding) the (meth) acrylic resin composition obtained by the production method of the present invention by a conventionally known molding method such as injection molding, compression molding, extrusion molding, or vacuum molding.
- molded products made of the (meth) acrylic resin composition include billboard parts such as advertising towers, stand signs, sleeve signs, column signs, and rooftop signs; display parts such as showcases, partition plates, and store displays; Lighting parts such as light covers, mood lighting covers, lamp shades, light ceilings, light walls, and chandeliers; interior parts such as pendants and mirrors; doors, domes, safety window glass, partitions, staircases, balcony waistboards, leisure buildings Building parts such as roofs; aircraft windshields, pilot visors, motorcycles, motorboat windshields, bus shading plates, automotive side visors, rear visors, head wings, headlight covers, and other transportation equipment related parts; Electronics such as stereo covers, TV protective masks, and vending machines Instrument parts; Medical equipment parts such as incubators and
- the present invention will be described more specifically with reference to examples and comparative examples.
- this invention is not restrict
- the present invention includes all aspects that are obtained by arbitrarily combining the above-described items representing technical characteristics such as characteristic values, forms, manufacturing methods, and uses.
- the polymerization conversion was measured during continuous operation. The supply of the raw material liquid to the tank reactor and the extraction of the reaction product from the tank reactor were stopped. Next, the polymerization conversion was measured when 5 hours had passed since the shutdown. A case where the change in the polymerization conversion rate during continuous operation and 5 hours after the stop of the operation was 5% or more was regarded as defective (x). A case where the change in the polymerization conversion rate during continuous operation and after 5 hours from the stop of the operation was less than 5% was evaluated as good ( ⁇ ).
- Example 1 In an autoclave equipped with a stirrer and a sampling tube, 98.9 parts by mass of purified methyl methacrylate (MMA), 1.1 parts by mass of methyl acrylate (MA), and 0.257 mass of n-octyl mercaptan (OM) as a chain transfer agent
- the raw material liquid (A) was obtained by mixing and mixing the parts. Nitrogen gas was blown into the raw material liquid (A) so that the ratio of the supply amount (kg / h) of the raw material liquid (A) to the supply amount of nitrogen gas (Nm 3 / h) was 0.2.
- the dissolved oxygen concentration of the raw material liquid (A) was adjusted to 0.3 ppm.
- MMA methyl methacrylate
- AIBN 2,2′-azobis (2-methylpropionitrile)
- butylxylenol polymerization inhibitor
- the raw material liquid (B) was obtained by adjusting the liquid temperature to 0 ° C. in an atmosphere substituted with industrial air.
- the inside of a continuous flow tank reactor (capacity 0.1 m 3 , tank diameter 500 mm, Max blend blade, blade diameter 260 mm, rotation speed 200 rpm) equipped with a brine cooled condenser was replaced with nitrogen gas.
- the raw material liquid (A) and the raw material liquid (B) are mixed so that the polymerization initiator concentration is 74 ppm to obtain a reaction liquid, and the above tank-type reaction is performed at a constant flow rate so that the average residence time is 120 minutes.
- the reaction solution was continuously supplied to the reactor, and the reaction solution temperature was adjusted to 140 ° C. and the pressure in the tank reactor was adjusted to 0.3 MPa, and bulk polymerization was performed. At the same time, the reaction product was continuously extracted from the tank reactor.
- the pressure in the tank reactor was adjusted by a pressure regulating valve connected to the brine cooling condenser.
- the polymerization stability and the storage stability of the raw material liquid (B) were evaluated. The results are shown in Table 1.
- Examples 2 to 3 and Comparative Examples 1 to 3 A continuous bulk polymerization reaction was performed in the same manner as in Example 1 except that the recipe shown in Table 1 was changed.
- Table 1 shows the evaluation results of the polymerization stability and the storage stability of the raw material liquid (B).
- the polymerization conversion rate of the reaction liquid in the reaction vessel does not change so much even when the operation is temporarily stopped in the continuous bulk polymerization method. Moreover, since the raw material liquid (B) can also be maintained in a stable state, the state before the stop can be restored immediately after restarting the operation.
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Abstract
Description
〔1〕 メタクリル酸メチル、アクリル酸アルキルエステルおよび連鎖移動剤を、アクリル酸アルキルエステル/メタクリル酸メチルの質量比0/100~20/80で含有し、且つ溶存酸素濃度が50ppm以下の原料液(A)を調製し、
ラジカル重合開始剤、重合禁止剤およびメタクリル酸メチルを含有し、酸素存在下、液温10℃以下に維持された原料液(B)を調製し、
原料液(A)および原料液(B)を槽型反応器に連続的に供給し、
槽型反応器内で重合転化率40~70質量%で塊状重合して反応生成物を得、
反応生成物を槽型反応器から連続的に抜き出す工程を有する、(メタ)アクリル樹脂組成物の製造方法。
〔3〕 原料液(B)のラジカル重合開始剤濃度が0.01質量%以上4質量%未満である、〔1〕または〔2〕に記載の(メタ)アクリル樹脂組成物の製造方法。
〔4〕 原料液(A)の溶存酸素濃度の調節は、不活性ガスの供給量[Nm3/h]に対する原料液(A)の供給量[kg/h]の割合が0.30未満になる条件にて原料液(A)と不活性ガスとを混合することを有する方法によって行われる、〔1〕~〔3〕のいずれかひとつに記載の製造方法。
〔5〕 反応生成物から未反応物を除去する工程をさらに有する、〔1〕~〔4〕のいずれかひとつに記載の(メタ)アクリル樹脂組成物の製造方法。
原料液(A)に含有されるメタクリル酸メチルとアクリル酸アルキルエステルは、アクリル酸アルキルエステル/メタクリル酸メチルの質量比で、好ましくは0/100~20/80、より好ましくは0/100~10/90である。原料液(A)に含有されるメタクリル酸メチルとアクリル酸アルキルエステルの合計供給量は、重合に供される全ての重合性単量体100質量部から、原料液(A)に含有させることができる他の重合性単量体および後述する原料液(B)に含有されるメタクリル酸メチルの供給量を差し引いた量である。
原料液(B)に含有されるラジカル重合開始剤は、反応性ラジカルを発生するものであれば特に限定されないが、後述する槽型反応器内の温度における半減期が、0.5~120秒のものが好ましく、2~60秒のものがより好ましい。また、該重合開始剤は、水素引抜き能が40%以下のものが好ましく、30%以下のものがより好ましい。これら重合開始剤は1種単独でまたは2種以上を組み合わせて用いることができる。
原料液(B)のラジカル重合開始剤濃度は、好ましくは0.01質量%以上4質量%未満、より好ましくは0.1質量%以上2質量%未満である。低すぎるラジカル重合開始剤濃度の原料液(B)は反応槽に多量に供給する必要があるので、重合が不安定になる傾向がある。一方、高すぎるラジカル重合開始剤濃度の原料液(B)は、貯蔵安定性が低いので、運転の停止が長期間になると、運転再開時に不都合が生じやすい傾向がある。
反応生成物中の(メタ)アクリル樹脂の含有率は、好ましくは40~70質量%、より好ましくは42~65質量%である。(メタ)アクリル樹脂の含有率が高すぎると粘度上昇のために大きな攪拌動力が必要となる傾向がある。(メタ)アクリル樹脂の含有率が低すぎると、反応生成物中の未反応物を除去する工程における未反応物の除去が不十分となり、得られる(メタ)アクリル樹脂組成物を成形した場合に、成形品にシルバーなどの外観不良を起こす傾向がある。
なお、重量平均分子量および数平均分子量は、GPC(ゲルパーミエーションクロマトグラフィ)で測定した標準ポリスチレン換算の分子量である。(メタ)アクリル樹脂の重量平均分子量や分子量分布は、重合開始剤および連鎖移動剤の種類や量などを調整することによって制御できる。
フラッシュ蒸発させられた未反応物の蒸気で伝熱管を流れる反応生成物を加熱し、加熱された反応生成物を低圧のフラッシュタンク内に供給してフラッシュ蒸発させることができる。また、反応生成物はポンプなどによって加圧することができる。
二量体または三量体の除去は、公知の化学工学的手段によって行うことができる。例えば、蒸留による方法が好ましいものとして挙げられる。本発明において用いられる蒸留塔は、特に制限されないが、段数が6~20段程度、還流比が0.4~2.0程度の多段式蒸留塔であることが好ましい。
添加剤としては、酸化防止剤、熱劣化防止剤、紫外線吸収剤、光安定剤、滑剤、離型剤、高分子加工助剤、帯電防止剤、難燃剤、染顔料、光拡散剤、有機色素、艶消し剤、耐衝撃性改質剤、蛍光体などが挙げられる。
リン系酸化防止剤とヒンダードフェノール系酸化防止剤とを併用する場合、その割合は特に制限されないが、リン系酸化防止剤/ヒンダードフェノール系酸化防止剤の質量比で、好ましくは1/5~2/1、より好ましくは1/2~1/1である。
該熱劣化防止剤としては、2-t-ブチル-6-(3’-t-ブチル-5’-メチル-ヒドロキシベンジル)-4-メチルフェニルアクリレート(住友化学社製;商品名スミライザーGM)、2,4-ジ-t-アミル-6-(3’,5’-ジ-t-アミル-2’-ヒドロキシ-α-メチルベンジル)フェニルアクリレート(住友化学社製;商品名スミライザーGS)などが好ましい。
紫外線吸収剤としては、ベンゾフェノン類、ベンゾトリアゾール類、トリアジン類、ベンゾエート類、サリシレート類、シアノアクリレート類、蓚酸アニリド類、マロン酸エステル類、ホルムアミジン類などが挙げられる。これらは1種単独でまたは2種以上を組み合わせて用いることができる。
これらの中でも、ベンゾトリアゾール類、または波長380~450nmにおけるモル吸光係数の最大値εmaxが1200dm3・mol-1cm-1以下である紫外線吸収剤が好ましい。
εmax=[Amax/(10×10-3)]×Mw
これら紫外線吸収剤の中、紫外線被照による樹脂劣化が抑えられるという観点からベンゾトリアゾール類が好ましく用いられる。
該重合体粒子は、単一組成比および単一極限粘度の重合体からなる単層粒子であってもよいし、また組成比または極限粘度の異なる2種以上の重合体からなる多層粒子であってもよい。この中でも、内層に低い極限粘度を有する重合体層を有し、外層に5dl/g以上の高い極限粘度を有する重合体層を有する2層構造の粒子が好ましいものとして挙げられる。
極限粘度が小さすぎると成形性の改善効果が低い。極限粘度が大きすぎると(メタ)アクリル樹脂組成物の溶融流動性の低下を招きやすい。
光拡散剤や艶消し剤としては、ガラス微粒子、ポリシロキサン架橋微粒子、架橋ポリマー微粒子、タルク、炭酸カルシウム、硫酸バリウムなどが挙げられる。
蛍光体として、蛍光顔料、蛍光染料、蛍光白色染料、蛍光増白剤、蛍光漂白剤などが挙げられる。
ガスクロマトグラフ((株)島津製作所製、GC-14A)に、カラム(GLC-G-230 Sciences Inc.製、INERT CAP 1(df=0.4μm、I.D.0.25mm、長さ60m))を繋ぎ、injection温度180℃、detector温度180℃、カラム温度を昇温速度10℃/分で60℃から200℃に昇温する条件にて分析した。
連続運転時に重合転化率を測定した。槽型反応器への原料液の供給および槽型反応器からの反応生成物の抜き出しを停止させた。次いで、運転停止から5時間経過した時に重合転化率を測定した。
連続運転時と運転停止から5時間経過時の重合転化率の変化が5%以上であった場合を不良(×)とした。連続運転時と運転停止から5時間経過時の重合転化率の変化が5%未満であった場合を良(○)とした。
調製された原料液(B)を調合槽内で1日保管した。その後、原料液(B)をサンプリングし、メタノールに添加し、液の状態を観察した。
目視にて白濁が見られる場合は重合反応が進んでいるので不良(×)とした。目視にて白濁が見られない場合は重合反応が実質的に進んでいないので良(○)とした。
攪拌機および採取管付オートクレーブに、精製されたメタクリル酸メチル(MMA)98.9質量部、アクリル酸メチル(MA)1.1質量部、連鎖移動剤としてn-オクチルメルカプタン(OM)0.257質量部を入れて混ぜ合わせて原料液(A)を得た。窒素ガスの供給量(Nm3/h)に対する原料液(A)の供給量(kg/h)の割合が0.2となるように窒素ガスを原料液(A)に吹き込んだ。原料液(A)の溶存酸素濃度が0.3ppmに調整された。
2,2’-アゾビス(2-メチルプロピオニトリル)(重合開始剤:AIBN)1.0質量%およびブチルキシレノール(重合禁止剤)1ppmを含有するようにそれらをメタクリル酸メチル(MMA)に溶解させ、産業空気で置換された雰囲気下、液温を0℃に調節して原料液(B)を得た。
ブライン冷却凝縮器を備えた連続流通式槽型反応器(容量0.1m3、槽径500mm、マックスブレンド翼、翼径260mm、回転数200rpm)内を窒素ガスで置換した。
原料液(A)と原料液(B)とを重合開始剤濃度が74ppmになるように混ぜ合わせて反応液を得、これを平均滞留時間120分となるように一定流量で前記の槽型反応器に連続的に供給し、反応液温度140℃、槽型反応器内の圧力0.3MPaに調整して塊状重合させ、同時に槽型反応器から反応生成物を連続的に抜き出した。なお、槽型反応器内の圧力は、ブライン冷却凝縮器に接続された圧力調整弁によって調整した。重合安定性および原料液(B)の貯蔵安定性の評価を行った。その結果を表1に示す。
表1に示すレシピに変更した以外は実施例1と同じ方法で連続塊状重合反応を行った。重合安定性および原料液(B)の貯蔵安定性の評価結果を表1に示す。
Claims (5)
- メタクリル酸メチル、アクリル酸アルキルエステルおよび連鎖移動剤を、アクリル酸アルキルエステル/メタクリル酸メチルの質量比0/100~20/80で含有し、且つ溶存酸素濃度が50ppm以下の原料液(A)を調製し、
ラジカル重合開始剤、重合禁止剤およびメタクリル酸メチルを含有し、酸素存在下、液温10℃以下に維持された原料液(B)を調製し、
原料液(A)および原料液(B)を槽型反応器に連続的に供給し、
槽型反応器内で重合転化率40~70質量%で塊状重合して反応生成物を得、
反応生成物を槽型反応器から連続的に抜き出す工程を有する、(メタ)アクリル樹脂組成物の製造方法。 - 原料液(A)の溶存酸素濃度が1ppm以下である、請求項1に記載の(メタ)アクリル樹脂組成物の製造方法。
- 原料液(B)のラジカル重合開始剤濃度が0.01質量%以上4質量%未満である、請求項1または2に記載の(メタ)アクリル樹脂組成物の製造方法。
- 原料液(A)の溶存酸素濃度の調節は、不活性ガスの供給量[Nm3/h]に対する原料液(A)の供給量[kg/h]の割合が0.30未満になる条件にて原料液(A)と不活性ガスとを混合することを有する方法によって行われる、請求項1~3のいずれかひとつに記載の製造方法。
- 反応生成物から未反応物を除去する工程をさらに有する、請求項1~4のいずれかひとつに記載の(メタ)アクリル樹脂組成物の製造方法。
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SG11201606349SA SG11201606349SA (en) | 2014-02-06 | 2015-02-06 | Production method of (meth)acrylic resin composition |
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JP2015561046A JP6645834B2 (ja) | 2014-02-06 | 2015-02-06 | (メタ)アクリル樹脂組成物の製造方法 |
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EP15745810.0A EP3103819B1 (en) | 2014-02-06 | 2015-02-06 | Production method of (meth)acrylic resin composition |
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EP (1) | EP3103819B1 (ja) |
JP (1) | JP6645834B2 (ja) |
KR (1) | KR102164738B1 (ja) |
CN (1) | CN105980414A (ja) |
MY (1) | MY182425A (ja) |
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WO2022230913A1 (ja) * | 2021-04-28 | 2022-11-03 | 三菱ケミカル株式会社 | メタクリル酸メチル含有組成物及びメタクリル酸メチル重合体の製造方法 |
WO2024090576A1 (ja) * | 2022-10-28 | 2024-05-02 | 三菱ケミカル株式会社 | 単量体組成物、メタクリル系樹脂組成物及びその製造方法、並びに樹脂成形体 |
WO2024095957A1 (ja) * | 2022-10-31 | 2024-05-10 | 三菱ケミカル株式会社 | エステル化合物含有組成物及びその製造方法、重合性組成物、(メタ)アクリル系重合体及びその製造方法 |
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WO2018151030A1 (ja) * | 2017-02-16 | 2018-08-23 | 株式会社クラレ | アクリル系ブロック共重合体と光拡散剤を含む樹脂組成物 |
JP7135670B2 (ja) * | 2018-09-27 | 2022-09-13 | 住友電気工業株式会社 | 光ファイバ及び紫外線硬化型樹脂組成物 |
JP7402633B2 (ja) * | 2019-07-30 | 2023-12-21 | 住友化学株式会社 | 重合性液晶組成液含有容器および重合性液晶組成液の保管方法 |
KR20210106092A (ko) | 2020-02-20 | 2021-08-30 | 에스케이이노베이션 주식회사 | 에틸렌-카르복실산 공중합체의 제조 방법 |
EP4237222A1 (en) | 2020-11-02 | 2023-09-06 | Röhm GmbH | Device for degassing of a two-component multiphase polymer-monomer material and use thereof in a degassing extruder |
DE102023115797A1 (de) | 2022-06-29 | 2024-01-04 | Röhm Gmbh | Verbessertes Verfahren zur Herstellung eines Polymers |
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- 2015-02-06 JP JP2015561046A patent/JP6645834B2/ja active Active
- 2015-02-06 WO PCT/JP2015/053341 patent/WO2015119233A1/ja active Application Filing
- 2015-02-06 SG SG11201606349SA patent/SG11201606349SA/en unknown
- 2015-02-06 US US15/116,676 patent/US9920142B2/en active Active
- 2015-02-06 CN CN201580007698.2A patent/CN105980414A/zh active Pending
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Also Published As
Publication number | Publication date |
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CN105980414A (zh) | 2016-09-28 |
EP3103819B1 (en) | 2019-10-09 |
MY182425A (en) | 2021-01-25 |
JP6645834B2 (ja) | 2020-02-14 |
US20160347879A1 (en) | 2016-12-01 |
JPWO2015119233A1 (ja) | 2017-03-30 |
TWI641623B (zh) | 2018-11-21 |
US9920142B2 (en) | 2018-03-20 |
KR20160118206A (ko) | 2016-10-11 |
TW201538535A (zh) | 2015-10-16 |
EP3103819A4 (en) | 2017-10-04 |
EP3103819A1 (en) | 2016-12-14 |
KR102164738B1 (ko) | 2020-10-13 |
SG11201606349SA (en) | 2016-09-29 |
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