JP2005248109A - Method for producing rubbery polymer particle and method for producing resin composition containing the same - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method wherein impurities are removed from a water-based latex of rubbery polymer particles to get successively an aggregate having a stable particle size, and the dried powder of the aggregate and the rubbery polymer particles are dispersed in an organic solvent to efficiently produce a dispersion; and a method for producing efficiently a resin composition to contain a well-dispersed rubbery polymer particles. <P>SOLUTION: The water-based latex of rubbery polymer particles is mixed with an organic solvent partly dissolving in water to get a mixture, which is then successively fed with water to bring into contact with water in a stirring vessel equipped with many stairs of scraping-up slant paddles, thereby to get successively and stably the aggregate of the rubbery polymer particles. The aggregate is separated and dried to obtain an aggregate or a dried powder containing little impurities. Alternatively, an organic solvent is added to the aggregate to get a dispersion, which is then mixed with a polymerizable organic compound having a reactive group and distilled to evaporate volatile components, thereby to obtain a resin composition in which the rubbery polymer particles are well dispersed and little impurities are contained. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

  The present invention relates to a method for continuously producing purified rubber-like polymer particles from an aqueous latex of rubber-like polymer particles, and by using a stirring tank having a plurality of lifted inclined paddle blades, Provided is a method for producing a stable and stable product. Furthermore, the present invention relates to a method for producing a dispersion in which purified rubber-like polymer particles are re-dispersed in an organic solvent, and a resin composition in which rubber-like polymer particles are uniformly dispersed in a thermosetting resin such as an epoxy resin. With regard to a method for producing a product, it is possible to provide a resin composition in which impurities are significantly reduced as compared with conventional methods.

  Conventionally, when a rubber-like polymer is produced from an aqueous latex of rubber-like polymer particles, an aggregate is first obtained by various methods, and then the aggregate is dehydrated or desolvated and then dried to obtain a rubber-like polymer. The method of obtaining is implemented.

  Examples of the method for obtaining the aggregate include (1) a method of adding an inorganic electrolyte or acid as a coagulant, (2) a method of adding a polymer flocculant, and (3) a method of directly contacting an organic solvent with latex. (4) A method of heating or freezing latex, (5) a method of applying a mechanical shear force, or a method of appropriately combining these has been proposed.

  At this time, as a measure for removing impurities such as an emulsifier and electrolyte derived from the polymer, and an inorganic electrolyte used as a coagulant from the obtained aggregate, a method of bringing the aggregate into contact with water is widely performed. Yes. However, the present situation is that not only a large amount of water is required to remove these impurities, but also the impurities cannot be removed sufficiently. Moreover, although the method of washing | cleaning with an organic solvent is also performed, a process becomes complicated and it becomes an industrially disadvantageous process.

  On the other hand, a cured product of a polymerizable organic compound having a reactive group, such as a cured product of an epoxy resin, has many points such as dimensional stability, mechanical strength, electrical insulation properties, heat resistance, water resistance, chemical resistance, and the like. Is excellent. However, cured products of epoxy resins have low fracture toughness and may exhibit very brittle properties, and such properties are often a problem in a wide range of applications.

  As one of the methods for solving these problems, an attempt has been made to blend a rubber component in an epoxy resin. Among them, a method of blending a rubbery polymer prepared in advance into particles using a polymerization method in an aqueous medium represented by emulsion polymerization, dispersion polymerization, suspension polymerization, etc. In principle, compared to a method in which a dispersed phase of rubber component is generated in the continuous phase of epoxy resin by causing phase separation in the curing process after dissolving and mixing the crosslinked amorphous rubber component Difficult to cause variation in dispersion state due to curing conditions, and by pre-crosslinking the rubber component, there is no mixing of the rubber component into the epoxy resin cured product continuous phase and there is little decrease in heat resistance and rigidity, etc. Various manufacturing methods have been proposed because of the advantages. For example, after (6) partially crosslinked rubbery random copolymer particles prepared by emulsion polymerization using a nonionic emulsifier or the like are heated to a temperature higher than the cloud point of the emulsifier, the solidified body is washed with water as necessary. , A method of mixing with an epoxy resin (see, for example, Patent Documents 1 to 3), (7) a method of mixing a rubbery polymer latex and an epoxy resin, and then distilling off water to obtain a mixture (for example, Patent Document 4) And (8) a method in which a rubber-like polymer latex is mixed with an epoxy resin in the presence of an organic solvent to obtain a mixture (see, for example, Patent Document 5).

  In the above method (6), since an aggregate is obtained by using a coagulant mainly composed of an inorganic electrolyte, impurities such as an emulsifier are attached to the polymer during aggregation or inside the aggregated polymer. The current situation is that impurities cannot be removed sufficiently even if a large amount of water is used due to being confined. Furthermore, since the rubber-like polymer particles are firmly fixed by coagulation, including coagulation by heating, when mixed with an epoxy resin, pulverization and dispersion operations with a considerable mechanical shear force are required, and a large amount In spite of the use of this energy, it is often difficult to uniformly disperse the rubber-like polymer particles in the epoxy resin.

  In the method (7), impurities such as an emulsifier derived from a polymer and an electrolyte remain as they are, and the epoxy resin is hardly soluble in water. In some cases, aggregates of aggregates may be generated in this unmixed portion.

  In the above method (8), since there is no coagulation operation, it is easy to obtain an epoxy resin composition in which the rubber-like polymer is uniformly dispersed. However, in mixing the rubber-like polymer latex and the epoxy resin, It is necessary to separate or distill off a large amount of water (in the mixture) that exceeds the amount of water that the organic solvent can dissolve, but for the separation of the organic solvent layer and the aqueous layer, for example, day and night, It may take a lot of time, or the organic solvent layer and the aqueous layer may form a stable emulsified suspension state, and separation may be substantially difficult. In addition, when water is distilled off, a large amount of energy is required, and water-soluble impurities such as emulsifiers and auxiliary materials usually used in the production of rubber-like polymer latex remain in the composition. It is also inferior. For this reason, in any method of separation and distillation, removal of water is complicated and it cannot be said that it is industrially preferable.

On the other hand, Japanese Patent Application No. 2003-326711 discloses a method of obtaining an aggregate by adding water to a mixture of an aqueous latex of rubber-like polymer particles and an organic solvent having partial solubility in water. It is shown.
Japanese Patent No. 1708498 Japanese Patent No. 2751071 JP-A-5-295237 JP-A-6-107910 US Pat. No. 4,778,851

  The object of the present invention is obtained in the state of aqueous latex as a method shown in Japanese Patent Application No. 2003-326711, that is, a method for producing purified rubber-like polymer particles from an aqueous latex of rubber-like polymer particles. In a production method in which loose agglomerates are obtained without using a coagulant in the presence of an organic solvent in the presence of an organic solvent and impurities are discharged to the aqueous phase side, a slow agglomerate with a stable particle size is continuously used for a long time. It is to provide a manufacturing method. Further, after the loose aggregates are dispersed again in the organic solvent and then mixed with the reactive polymerizable organic compound, the rubber-like polymer particles are uniformly mixed in the reactive polymerizable organic compound. It is an object of the present invention to provide a method for easily and efficiently producing a resin composition that can be dispersed and greatly reduces impurities such as an emulsifier derived from polymer particles and an electrolyte.

  In the first aspect of the present invention, a mixture (C) obtained by mixing an aqueous latex of rubber-like polymer particles (A) with an organic solvent (B) having partial solubility in water and water (D) are scraped. Aggregates (F) of the rubber-like polymer particles (A) containing the organic solvent (B) are continuously supplied to a stirring tank provided with multi-stage inclined paddle blades and mixed and contacted with each other. E) It is related with the continuous manufacturing method of the refined rubber-like polymer particle | grains characterized by isolate | separating an aggregate (F) continuously after producing | generating in.

  A preferred embodiment is characterized in that the mixture (C) and water (D) are supplied from the bottom of the stirring tank, and the mixture of the aggregate (F) and the aqueous phase (E) is recovered from the top of the stirring tank. It relates to the manufacturing method.

  In a preferred embodiment, the purified rubber-like polymer is characterized in that the aggregate (F) of purified rubber-like polymer particles obtained by any of the production methods described above is dehydrated and / or desolvated and then dried. The present invention relates to a method for producing particles.

  In the second aspect of the present invention, an organic solvent having an affinity for the rubber-like polymer particles (A) is added to the aggregate (F) of the purified rubber-like polymer particles obtained by any one of the above production methods, The present invention relates to a method for producing a dispersion (G), characterized in that a dispersion (G) in which the rubbery polymer particles (A) are dispersed in the organic solvent is obtained.

  3rd of this invention is a manufacturing method of the resin composition which disperse | distributed rubber-like polymer particle (A) in the polymeric organic compound (H) which has a reactive group, Comprising: The dispersion | distribution obtained by the said manufacturing method It is related with the manufacturing method of the resin composition characterized by distilling a volatile component after mixing with a body (G) and the said polymeric organic compound (H).

  4th of this invention is a manufacturing method of the resin composition which disperse | distributed rubber-like polymer particle (A) in the polymeric organic compound (H) which has a reactive group, Comprising: By the manufacturing method in any one of the said It is related with the manufacturing method of the resin composition characterized by distilling a volatile component after mixing with the obtained aggregate (F) and the said polymeric organic compound (H).

  A preferred embodiment relates to the method for producing a resin composition according to any one of the above, wherein the polymerizable organic compound (H) having a reactive group is an epoxy resin.

  A preferred embodiment relates to any one of the production methods described above, wherein the solubility of the organic solvent (B) in water at 20 ° C. is 5 wt% or more and 40 wt% or less.

  In a preferred embodiment, water (D) is brought into contact with a mixture (C) obtained by mixing an aqueous latex of rubber-like polymer particles (A) and an organic solvent (B) having partial solubility in water. The amount is 40 to 350 parts by weight with respect to 100 parts by weight of the organic solvent (B).

  A preferred embodiment is characterized in that the rubber-like polymer particle (A) is a polymer having a multilayer structure of two or more layers, and includes at least one or more crosslinked rubber-like polymer layers. It relates to the manufacturing method according to the above.

  In a preferred embodiment, the rubber-like polymer particles (A) are 50 to 100% by weight of at least one monomer selected from diene monomers and (meth) acrylate monomers, and other In the presence of 40 to 95% by weight of a rubber particle core (A-1) comprising a rubber elastic body composed of 0 to 50% by weight of a copolymerizable vinyl monomer, a polysiloxane rubber-based elastic body, or a mixture thereof. And a shell layer (A-) comprising at least one vinyl polymerizable monomer selected from (meth) acrylic acid ester, aromatic vinyl, vinyl cyanide, unsaturated acid derivative, (meth) acrylamide derivative, and maleimide derivative. 2) The method according to any one of the above, which is a graft copolymer obtained by polymerizing 5 to 60% by weight.

  In a preferred embodiment, the shell layer (A-2) of the rubber-like polymer particle (A) has at least one reactive functional group selected from the group consisting of an epoxy group, a carboxyl group, a hydroxyl group, and a carbon-carbon double bond. It has a group, and relates to the above production method.

  According to the production method of the present invention, an aggregate having a stable particle diameter can be continuously obtained for a long time from an aqueous latex of rubber-like polymer particles without using a coagulant in the presence of an organic solvent. In addition, impurities can be efficiently discharged to the water phase side. Therefore, the rubber-like polymer particles purified by a simple method can be produced efficiently and stably. Furthermore, according to this method, since the aggregate particle size becomes stable and aggregates staying in the agitation tank are reduced, it is possible to reduce the trouble of the apparatus in which the inside of the tank is blocked by the coalesced and grown aggregates. . In addition, since the obtained agglomerates have reversibility, rubber particles are uniformly dispersed in the polymerizable organic compound by redispersing in an organic solvent and mixing with the polymerizable organic compound. Can be mixed and dispersed. That is, a resin composition in which impurities such as an emulsifier derived from polymer particles and an electrolyte are significantly reduced can be produced.

  In the production method of the present invention, first, an aqueous latex of rubber-like polymer particles (A) is mixed with an organic solvent (B) that shows partial solubility in water. The rubber-like polymer particle (A) is not particularly limited, but it has two or more layers because it is easy to achieve both the design as a rubber and the ease of production of the resin composition in the production method of the present invention. A polymer having a structure is preferable, and a polymer called a core-shell type polymer is particularly preferable. The core-shell type polymer is a rubber particle core (A-1) formed from a polymer mainly composed of an elastomer or a rubber-like polymer, and a shell layer (A-) formed from a polymer component graft-polymerized thereto. 2), the shell layer (A-2) is a part or the whole of the surface of the rubber particle core (A-1) by graft polymerization of the monomer constituting the graft component onto the core. It is characterized by covering.

  The polymer constituting the rubber particle core (A-1) is cross-linked, and the polymer constituting the rubber particle core (A-1) can swell in an appropriate solvent, but does not substantially dissolve. Is preferred. Further, when the rubber particle core (A-1) is intended to be dispersed in an epoxy resin, the rubber particle core (A-1) is preferably insoluble in the epoxy resin. In the core (A-1), it is 60% by weight or more, more preferably 80% by weight or more, particularly preferably 90% by weight or more, and most preferably 95% by weight or more. On the other hand, the polymer constituting the rubber particle core (A-1) has a glass transition temperature (Tg) because it can be easily produced by a known polymerization method such as emulsion polymerization and has good properties as a rubber. 0 ° C. or lower, preferably −10 ° C. or lower.

  The polymer constituting the rubber particle core (A-1) can be obtained at a low cost, and the diene monomer (conjugated diene monomer) from the viewpoint that the resulting polymer has excellent rubber properties. And a rubber composed of 50 to 100% by weight of at least one monomer selected from (meth) acrylate monomers and 0 to 50% by weight of other copolymerizable vinyl monomers It is preferable to use an elastic body, a polysiloxane rubber-based elastic body, or a combination thereof. In the present invention, (meth) acryl means acryl and / or methacryl.

  The conjugated diene monomer constituting the rubber elastic body is not particularly limited, and examples thereof include butadiene, isoprene and chloroprene. Of these, butadiene is particularly preferred because the resulting polymer has excellent rubber properties. Further, the (meth) acrylic acid ester monomer is not particularly limited, and examples thereof include butyl acrylate, 2-ethylhexyl acrylate, lauryl methacrylate, etc., but the properties of the resulting polymer as rubber are excellent. In view of the above, butyl acrylate or 2-ethylhexyl acrylate is particularly preferable. These can be used alone or in combination of two or more.

  Further, the rubber elastic body may be a copolymer of a conjugated diene monomer or a (meth) acrylic acid ester monomer and a vinyl monomer copolymerizable therewith. Examples of the monomer copolymerizable with the conjugated diene monomer or the (meth) acrylic acid ester monomer include aromatic vinyl monomers and vinyl cyanide monomers. As the aromatic vinyl monomer, for example, styrene, α-methylstyrene, vinyl naphthalene and the like can be used. As the vinyl cyanide monomer, for example, (meth) acrylonitrile, substituted acrylonitrile and the like can be used. It can be used. These can be used alone or in combination of two or more.

  The amount of the conjugated diene monomer or (meth) acrylic acid ester monomer used is preferably 50% by weight or more, more preferably 60% by weight or more based on the total weight of the rubber elastic body. . When the amount of the conjugated diene monomer or (meth) acrylic acid ester monomer used for the entire rubber elastic body is less than 50% by weight, a cured product of the polymerizable organic compound (H) having a reactive group For example, the ability to impart toughness to the epoxy resin may be reduced. On the other hand, the amount of the monomer copolymerizable with these is preferably 50% by weight or less, more preferably 40% by weight or less, based on the weight of the entire rubber elastic body.

  Further, as a component constituting the rubber elastic body, a polyfunctional monomer may be included in order to adjust the degree of crosslinking. Examples of the polyfunctional monomer include divinylbenzene, butanediol di (meth) acrylate, triallyl (iso) cyanurate, allyl (meth) acrylate, diallyl itaconate, diallyl phthalate, and the like. These are used in an amount of not more than 10% by weight, preferably not more than 5% by weight, more preferably not more than 3% by weight, based on the total weight of the rubber elastic body. When the amount used exceeds 10% by weight, the rubber particle core (A-1) has a tendency to lower the ability to impart toughness to the cured product of the polymerizable organic compound (H) having a reactive group.

  Moreover, in order to adjust the molecular weight and the degree of crosslinking of the polymer constituting the rubber elastic body, a chain transfer agent may be used as necessary. As a chain transfer agent, a C5-C20 alkyl mercaptan etc. can be illustrated, for example. The amount of these used is 5% by weight or less, more preferably 3% by weight or less, based on the total weight of the rubber elastic body. When the amount used exceeds 5% by weight, the amount of the uncrosslinked component of the rubber particle core (A-1) increases. For example, when an epoxy resin composition is prepared, the heat resistance and rigidity of the composition are adversely affected. Tend to give.

  Furthermore, it is also possible to use a polysiloxane rubber-based elastic body as the rubber particle core (A-1) in place of or in combination with the rubber elastic body. When polysiloxane rubber is used as the rubber particle core (A-1), for example, polysiloxane rubber composed of alkyl or aryl disubstituted silyloxy units such as dimethylsilyloxy, methylphenylsilyloxy, diphenylsilyloxy, etc. Can be used. When using such a polysiloxane rubber, if necessary, partially use a polyfunctional alkoxysilane compound during polymerization, or radically react a silane compound having a vinyl reactive group. It is more preferable to introduce a crosslinked structure in advance, for example.

  The shell layer (A-2) is a polymer having a reactive group for the rubber-like polymer particles (A) to be stably dispersed in the state of primary particles in the polymerizable organic compound (H) having a reactive group. Affinity for the organic compound (H) can be imparted.

  The polymer constituting the shell layer (A-2) is graft-polymerized to the polymer constituting the rubber particle core (A-1), and is substantially bonded to the polymer constituting the core part (A-1). It is preferable. The polymer constituting the shell layer (A-2) is 70% by weight or more, more preferably 80% by weight or more, and still more preferably 90% by weight from the viewpoint of facilitating the production of the resin composition in the production method of the present invention. It is desirable that the above is coupled to the core part (A-1).

  The shell layer (A-2) is a polymer having an organic solvent (B) and a reactive group, which will be described later, from the viewpoint of easily mixing and dispersing the rubber-like polymer particles in the polymerizable organic compound having a reactive group. Those having swellability, compatibility or affinity for the water-soluble organic compound (H) are preferred. Moreover, the shell layer (A-2) has reactivity with the polymerizable organic compound (H) having a reactive group or a curing agent blended at the time of use, depending on the necessity at the time of use, and is reactive. It is preferable that the polymerizable organic compound (H) having a group has a function capable of chemically reacting with these to form a bond under a condition in which the polymerizable organic compound (H) is cured by reacting with a curing agent.

  The polymer constituting the shell layer (A-2) is at least one selected from (meth) acrylic acid esters, aromatic vinyl compounds, vinyl cyanide compounds, unsaturated acid derivatives, (meth) acrylamide derivatives, and maleimide derivatives. A polymer or copolymer obtained by polymerizing or copolymerizing the components is preferred. In addition, when the chemical reactivity at the time of curing the epoxy resin is particularly required for the shell layer (A-2), in addition to the (meth) acrylic acid alkyl ester, the aromatic vinyl compound or the vinyl cyanide compound, an epoxy group, A polymerizable organic compound (H) having at least one functional group selected from a carboxyl group, a hydroxyl group, a carbon-carbon double bond, an amino group, an amide group, and the like, having a reactive group described later, or a curing agent thereof; It is preferable to use a copolymer obtained by copolymerizing at least one monomer containing a functional group having reactivity with a curing catalyst or the like. Further, the functional group is more preferably at least one reactive functional group selected from the group consisting of an epoxy group, a carboxyl group, a hydroxyl group, and a carbon-carbon double bond.

  Examples of the (meth) acrylic acid ester include (meth) acrylic acid alkyl esters such as methyl (meth) acrylate, ethyl (meth) acrylate, butyl (meth) acrylate, and 2-ethylhexyl (meth) acrylate. Can be given. Examples of the aromatic vinyl compound include styrene, α-methylstyrene, alkyl-substituted styrene, and halogen-substituted styrenes such as bromostyrene and chlorostyrene. Examples of the vinyl cyanide compound include (meth) acrylonitrile and substituted acrylonitrile. Moreover, as a monomer containing the functional group which has the said reactivity, (meth) acrylic acid ester which has a reactive side chain, for example, (meth) acrylic acid 2-hydroxyethyl, (meth) acrylic acid 2 -Aminoethyl, glycidyl (meth) acrylate, etc. are mentioned. Examples of the vinyl ether containing a reactive group include glycidyl vinyl ether and allyl vinyl ether. Examples of the unsaturated carboxylic acid derivative include (meth) acrylic acid, itaconic acid, crotonic acid, maleic anhydride and the like. Examples of the (meth) acrylamide derivative include (meth) acrylamide (including N-substituted product). Examples of maleimide derivatives include maleic imide (including N-substituents).

  The preferred rubber particle core (A-1) / shell layer (A-2) ratio (weight ratio) of the rubber-like polymer particles (A) is in the range of 40/60 to 95/5, more preferably 60 / 40-85 / 15. When the ratio (A-1) / (A-2) deviates from 40/60 and the ratio of the rubber particle core (A-1) decreases, the toughness improving effect on the polymerizable organic compound (H) having a reactive group Tends to decrease. If the ratio of the shell layer (A-2) falls outside 95/5, it tends to cause aggregation during handling in the present production method, causing problems in operability and possibly preventing the expected physical properties from being obtained.

  The rubber-like polymer particles (A) can be produced by a known method such as emulsion polymerization, suspension polymerization, microsuspension polymerization and the like. Among these, emulsion polymerization is particularly easy because the composition design of rubber-like polymer particles is easy, industrial production is easy, and latex of rubber-like polymer particles suitable for this production method can be easily obtained. The production method is preferred. As the emulsifying or dispersing agent in the aqueous medium, it is preferable to use an emulsifying or dispersing agent that does not impair the emulsifying or dispersing stability even when the pH of the aqueous latex is neutral. Specifically, alkyl or aryl sulfonic acid such as dioctyl sulfosuccinic acid and dodecyl benzene sulfonic acid, alkyl or aryl ether sulfonic acid, alkyl or aryl sulfuric acid such as dodecyl sulfuric acid, alkyl or aryl ether Sulfuric acid, alkyl or aryl substituted phosphoric acid, alkyl or aryl ether substituted phosphoric acid, N-alkyl or aryl sarcosine acid represented by dodecyl sarcosine acid, alkyl or aryl carboxylic acid represented by oleic acid, stearic acid, etc. Nonionic emulsifiers or dispersants such as alkali metal salts or ammonium salts of various acids such as acids, alkyl or aryl ether carboxylic acids, alkyl or aryl substituted polyethylene glycols, etc. Alcohol, alkyl substituted cellulose, polyvinyl pyrrolidone, dispersants such as polyacrylic acid derivatives. These can be used alone or in combination of two or more.

  From the viewpoint of the present invention, the above emulsifying or dispersing agent may be used as little as possible as long as it does not hinder the emulsification / dispersion stability in the latex preparation process of the rubber-like polymer particles (A). Preferably, it is more preferable that the aqueous phase (E) has a property of being extracted and washed to a residual amount that does not affect the physical properties of the resin composition produced in the present production method.

  The particle size of the rubber-like polymer particles (A) that can be used in the production method of the present invention is not particularly limited, and any particles can be used as long as (A) can be stably obtained in an aqueous latex state. However, in terms of industrial productivity, those having a volume average particle size of 0.03 to 2 μm are more preferable in terms of easy production.

  The organic solvent (B) having partial solubility in water used in the present invention is obtained when the aqueous latex of rubber-like polymer particles (A) is mixed with the organic solvent (B). Can be used without limitation as long as at least one or two or more organic solvents or organic solvent mixtures can be mixed without substantially solidifying and precipitating, but the solubility in water at 20 ° C. is 5% by weight or more, 40 The organic solvent is preferably not more than wt%, more preferably not less than 5 wt% and not more than 30 wt%. If the solubility of the organic solvent (B) in water at 20 ° C. exceeds 40% by weight, the aqueous latex of the polymer particles (A) may partially coagulate and hinder smooth mixing operation. When the solubility in water is less than 5% by weight, the mixing property of the polymer particles (A) with the aqueous latex becomes insufficient, and smooth mixing tends to be difficult.

  Specific examples of the organic solvent (B) include esters such as methyl acetate, ethyl acetate, propyl acetate and butyl acetate, ketones such as acetone, methyl ethyl ketone, diethyl ketone and methyl isobutyl ketone, ethanol, (iso) propanol, One kind selected from alcohols such as butanol, ethers such as tetrahydrofuran, tetrahydropyran, dioxane and diethyl ether, aromatic hydrocarbons such as benzene, toluene and xylene, halogenated hydrocarbons such as methylene chloride and chloroform, etc. Examples of the organic solvent or mixture thereof are those having a solubility in water at 20 ° C. satisfying the above range. Of these, those containing 50% by weight or more of methyl ethyl ketone are more preferred, and those containing 75% by weight or more are particularly preferred from the viewpoints of affinity with a polymerizable organic compound having reactivity and availability.

  The amount of the organic solvent (B) used may vary depending on the type of the rubber-like polymer particles (A) or the solid content concentration of the rubber-like polymer particles (A) in the aqueous latex. The organic solvent (B) is preferably used in an amount of 50 to 400 parts by weight, more preferably 70 to 300 parts by weight, based on 100 parts by weight of the latex of the particles (A). If the amount of the organic solvent (B) is less than 50 parts by weight, the rubber-like polymer particles (A) may not be stably dispersed, and the viscosity tends to increase and handling becomes difficult. On the other hand, when the amount exceeds 400 parts by weight, the amount of the organic solvent (B) increases, which is uneconomical in consideration of subsequent removal.

  No special apparatus or method is required for the mixing operation of the rubber-like polymer particles (A) with the aqueous latex and the organic solvent (B) having partial solubility in water, and an apparatus capable of obtaining a good mixed state. Alternatively, any known method can be used. A typical apparatus includes an agitation tank with an agitating blade, but continuous processing using a static mixer (static mixer) or a line mixer (a system in which an agitator is incorporated in a part of piping) is also possible.

  In the present invention, the mixture (C) obtained as described above is brought into contact with water (D). By this operation, a part of the organic solvent (B) contained in the mixture (C) is dissolved in water (D) to form an aqueous phase (E). At the same time, water derived from the aqueous latex contained in the mixture (C) is also removed to the aqueous phase (E). For this reason, the mixture (C) becomes the form which concentrated the rubber-like polymer particle (A) in the organic solvent (B) containing water, and produces | generates an aggregate (F) as a result.

  From the viewpoint of preventing partial generation of non-aggregates, it is desirable that the aggregate generation operation be performed under stirring or under flow conditions that can impart fluidity equivalent to that of stirring. For example, it can be carried out by batch operation or continuous operation in a stirring tank equipped with a stirrer. In the present invention, in order to perform this agglomerate production operation more efficiently and stably, the mixture (C) and water (D) are continuously supplied to a stirring tank in which the inclined type paddle blades are installed in multiple stages, By mixing and contacting, the aggregate (F) and the aqueous phase (E) are obtained continuously. The stirring blade diameter and the tank shape are not particularly limited, and known ones can be used, but the ratio of the stirring blade diameter and the tank diameter is about 0.5 to 0.8 in terms of reducing aggregates staying in the tank. Is preferred. When the ratio between the stirring blade diameter and the tank diameter exceeds 0.8, the clearance between the stirring blade and the tank becomes narrow, which may hinder the rise of the aggregates. In some cases, the agitation effect is reduced, and aggregates may remain.

  The above-described lift-up type inclined paddle blade is not particularly limited and a known one can be used, but the inclination angle of the paddle blade is preferably about 30 to 60 °. When the inclination angle of the lift-up type inclined paddle blade exceeds 60 °, conversely, if it is less than 30 °, the aggregate may not rise and may stay. The number of steps of the lift-up type inclined paddle blade is not particularly limited, but the distance between the blade and the blade is preferably about 0.45 to 0.75 times the tank diameter. More preferably, it is about 0.6 times. When the distance between the wings exceeds 0.75 times, the aggregate may not rise and may stay, whereas if the distance is less than 0.45 times, the contact between the particles increases and the particles are united. However, the particle size may become unstable.

  The particle size of the agglomerate thus obtained can be obtained continuously by controlling the fluctuation within a range of ± 20% of the 50% diameter on the sieve based on the wet sieve measurement. In addition, as a wet sieve measurement method used for the measurement of the particle size, 20 to 100 g of the aggregate (F) and the aqueous phase (E) are weighed and placed on a standard sieve having an opening according to the particle size. The agglomerate (F) was removed with a piget or the like, and the aqueous phase (E) was evenly poured, and the mixture of the passed aqueous phase (E) and agglomerate (F) was dried and weighed. Thereafter, the agglomerate (F) remaining on the net was transferred onto a sieve having a larger opening, and the same operation was repeated. From the relationship between the particle size and the weight obtained here, the particle size based on weight can be calculated.

  In addition, since the aggregate (F) is generally floatable with respect to the aqueous phase (E), the mixture (C) and water (D) are supplied from the bottom of the stirring tank, and the aggregate (F) and the aqueous phase (E ) Is preferably extracted from the upper part of the stirring tank. Here, the bottom of the device means that the height from the bottom of the device to the liquid level is 1/3 or less from the bottom, and the top of the device means from the bottom of the device to the liquid level. It means that the height is 1/3 or more from the top. Thus, by making the production | generation operation | movement of an aggregate (F) continuous, the suppression of the installation cost by the size reduction of an apparatus and the improvement of productivity can be aimed at.

  The amount of water (D) to be mixed and contacted with the mixture (C) depends on the kind of the rubber-like polymer particles (A), the solid content concentration of the rubber-like polymer particles (A) in the aqueous latex, and the organic solvent (B). The amount of water (D) is 40 parts by weight or more and 350 parts by weight or less with respect to 100 parts by weight of the organic solvent (B) used for mixing with the aqueous latex. Preferably, it is 60 parts by weight or more and 250 parts by weight or less. If the amount of the water (D) is less than 40 parts by weight, the aggregate (F) of the rubber-like polymer particles (A) tends to be difficult to be formed. Since the concentration of the organic solvent (B) in F) becomes low, the dispersibility tends to decrease, for example, the time required to redisperse the aggregate (F) in the organic solvent in a later step is prolonged.

  The aggregation operation and the produced aggregate (F) in the present invention have the following characteristics. (A) In general, in an agglomeration operation by adding a coagulant such as an electrolyte or an acid or a heating operation, most of the emulsifier and electrolyte derived from the latex of the rubber-like polymer particles (A) are adsorbed on the aggregate surface, or coagulation is performed. In many cases, it is contained within the aggregate, and even if it is washed with water after aggregation, it is not easy to remove it. On the other hand, in the present invention, rubbery polymer particles (A) are obtained through operations from mixing of latex of rubbery polymer particles (A) and organic solvent (B) to aggregation of rubbery polymer particles (A). Since the emulsifier and electrolyte derived from) move from the aggregate (F) to the aqueous phase (E), they can be easily removed. (B) In general, an aggregate formed by adding a coagulant such as an electrolyte or an acid or a heating operation can be re-dispersed from the aggregate to the state of primary particles of the rubber-like polymer particles (A) by mechanical shearing. It is a strong agglomerate that is difficult. On the other hand, in the aggregate (F) obtained in the present invention, after that, for example, by mixing with an organic solvent having an affinity with the rubber-like polymer particles (A) under stirring, most of the aggregate (F) is rubber. It can be dispersed again as primary particles of the polymer (A). That is, the aggregate (F) obtained by the present invention has reversibility in the organic solvent with respect to the coalescence dispersion of the particles. In the present invention, this is called a slow aggregate.

  Here, although the reason regarding the above (b) has not been fully elucidated, in the production method of the present invention, the rubber-like polymer particles (A) are dispersed from the organic solvent (B). As a result of the addition of water (D), the polymer was concentrated through the elution of the organic solvent (B) component into the aqueous phase (E), resulting in a reversible change to a mild aggregate state containing the organic solvent. It is considered that aggregates (F) are formed, and therefore, it is considered that the dispersion of the rubber-like polymer particles (A) can be easily reproduced by re-addition of the organic solvent.

  Therefore, by separating the produced aggregate (F) and the aqueous phase (E) containing the organic solvent (B), the moisture contained in the organic solvent (B) accompanying the aggregate (F) is removed, Purified rubber-like polymer particles obtained by separating and removing most of the emulsifier and electrolyte derived from the rubber-like polymer particles (A) from the rubber-like polymer particles (A) together with the aqueous phase (E) can be obtained.

  Separation from the agglomerates (F) and aqueous phase (E) is good, and is carried out using a general filtration device such as filtration using filter paper, filter cloth, or a relatively coarse metal screen. be able to.

  When it is desired to obtain the purified rubber-like polymer particles as a dry powder, the aggregate (F) can be obtained by dehydration and / or desolvation followed by drying. At this time, it is preferable that the aggregate (F) is finally washed with water not containing the organic solvent (B). This is because if the organic solvent (B) is contained in a large amount, the particles are easily united during drying. As described above, a dry powder of rubber-like polymer particles with very few impurities can be obtained.

  On the other hand, a dispersion (G) or a resin composition in which rubber-like polymer particles (A) are dispersed in an organic solvent having an affinity for rubber-like polymer particles (A) or a polymerizable organic compound (H) having a reactive group When the product is produced, the amount of the organic solvent (B) contained in the aggregate (F) obtained through the above aggregation and separation operations is 30% by weight or more with respect to the total weight of the aggregate (F). It is preferable that the content is 35% by weight or more. By containing the organic solvent (B), it is possible to satisfactorily disperse in the organic solvent or the polymerizable organic compound having a reactive group having an affinity with the rubber-like polymer particles (A) to be subsequently carried out. When the content of the organic solvent (B) is less than 30% by weight with respect to the total weight of the aggregate (F), an organic solvent or reactive group having an affinity with the rubber-like polymer particles (A) as the next step is added. In some cases, the time required for dispersing in the polymerizable organic compound (H) may be prolonged, or irreversible aggregates may easily remain, resulting in polymerization of the rubber-like polymer particles (A). The dispersibility in the volatile organic compound (H) tends to be remarkably lowered.

  The amount of the rubber-like polymer particles (A) contained in the water phase (E) separated and removed by the above series of operations is 10% by weight or less, preferably 5% by weight, based on the total amount of the water phase (E). Hereinafter, it is more preferably 2% by weight or less, and most preferably the rubber-like polymer particles (A) are not substantially contained.

  Next, the dispersion of the obtained aggregate (F) in an organic solvent having an affinity for the rubber-like polymer particles (A) will be described. By this operation, it is possible to obtain a dispersion (G) in which the purified rubber-like polymer particles (A) in the aggregate (F) are substantially dispersed in the state of primary particles in the organic solvent.

  The amount of the organic solvent added at this time can vary depending on the type of the rubber-like polymer particles (A) and the type and amount of the organic solvent. The amount of the organic solvent to be added is preferably 40 to 1400 parts by weight, more preferably 200 to 1000 parts by weight with respect to 100 parts by weight of the rubber-like polymer particles (A). When the amount of the organic solvent to be added is less than 40 parts by weight, the rubber-like polymer particles (A) are difficult to uniformly disperse in the organic solvent, and the aggregates (F) of the rubber-like polymer particles (A) are formed. It tends to remain or become difficult to handle due to an increase in viscosity. If it exceeds 1400 parts by weight, a large amount of energy and a large-scale apparatus are required for the final evaporation of volatile components, which is uneconomical. The organic solvent having an affinity for the rubber-like polymer particles (A) used here is not particularly limited as long as the rubber-like polymer particles (A) can be redispersed. Examples thereof include those exemplified for the organic solvent (B) used in 1), aliphatic hydrocarbons such as hexane, heptane, octane, cyclohexane and ethylcyclohexane, and mixtures thereof. Further, from the viewpoint of ensuring the redispersibility of the loose agglomerates, it is preferable to use the same type of organic solvent as the organic solvent (B) used in the previous step.

  In the present invention, the mixing operation of the organic solvent having an affinity for the aggregate (F) and the rubber-like polymer particles (A) is not particularly limited, and is carried out with an apparatus having a general stirring and mixing function. be able to.

  Next, after mixing the polymerizable organic compound (H) having a reactive group with the dispersion (G) in which the rubber-like polymer particles (A) thus obtained are dispersed, the volatile components are removed. Explain what to leave. By this operation, a rubber-like polymer particle (A) is dispersed in the polymerizable organic compound (H) having a reactive group, and a resin composition containing almost no emulsifier or electrolyte derived from the polymer particle is obtained. Can do.

  Examples of the polymerizable organic compound (H) having a reactive group used in the present invention include thermosetting resins such as epoxy resins, phenol resins, polyurethane resins, and vinyl ester resins, aromatic vinyl compounds, and (meth) acrylic acid. Examples thereof include radical polymerizable monomers such as derivatives, vinyl cyanide compounds and maleimide compounds, and aromatic polyester raw materials such as dimethyl terephthalate and alkylene glycol. Especially, the method of this invention can be used especially suitably with respect to the thermosetting resin represented by the epoxy resin in which it is comparatively difficult to mix | blend the above rubber-like polymer particle | grains normally.

  The epoxy resin that can be used in the present invention is not particularly limited as long as it is a compound having an epoxy group, but the epoxy resin that can be used in the present invention is preferably an epoxy resin also called a polyepoxide. Examples of the epoxy resin include polyglycidyl ethers such as addition reaction products of polyphenols such as bisphenol A, bisphenol F, biphenol, and phenol novolac and epichlorohydrin, aniline, diaminobenzene, aminophenol, phenylenediamine, and diaminophenyl ether. Polyamines derived from monoamines such as polyamines and polyamines, alicyclic epoxy resins having an alicyclic epoxy structure such as cyclohexyl epoxy, addition reaction products of polyhydric alcohols and epichlorohydrin, Examples include halogenated epoxy resins in which part of the hydrogen is substituted with a halogen element such as bromine, and homopolymers or copolymers obtained by polymerizing monomers containing unsaturated monoepoxides such as allyl glycidyl ether. It is. These may be one kind or a mixture of two or more kinds. Many polyepoxides synthesized from polyhydric phenols are disclosed, for example, in US Pat. No. 4,431,782. Examples of polyepoxides are further described in U.S. Pat. Nos. 3,804,735, 3,892,819, 3,948,698, 4,014,771, and an epoxy resin handbook ( Nikkan Kogyo Shimbun, 1987).

  The epoxy resin that can be used in the present invention is as described above, and generally includes an epoxy resin having an epoxy equivalent weight of 80 to 2000. These polyepoxides can be obtained by a well-known method. As a commonly used method, for example, an excess amount of epihalohydrin is reacted with a polyhydric alcohol or polyhydric phenol in the presence of a base.

  The epoxy resin that can be used in the present invention may contain a monoepoxide, for example, an aliphatic glycidyl ether such as butyl glycidyl ether, phenyl glycidyl ether, or cresyl glycidyl ether as a reactive diluent. As is generally known, the monoepoxide affects the stoichiometry of the polyepoxide formulation, but this can be adjusted by the amount of hardener or other well-known methods.

  The epoxy resin component used in the present invention may contain a curing agent and / or a curing accelerator of the above epoxy group-containing compound, but is not substantially intended as an epoxy resin under the conditions of this production method. A curing agent and / or a curing accelerator that does not cause a curing reaction is preferable. As such curing agents and / or curing accelerators, for example, those satisfying the above requirements can be selected from those described in the aforementioned epoxy resin handbook.

  In addition, a well-known method is applicable as a distillation method of volatile matters, such as an organic solvent (B). For example, a method of charging the mixture into a tank and distilling it under reduced pressure, a method of countercurrently contacting the mixture with a dry gas in the tank, a continuous method using a thin film evaporator, and a devolatilization mechanism Examples thereof include a method using an extruder or a continuous stirring tank. Conditions such as temperature and required time for distilling off the volatile components can be appropriately selected within a range that does not impair the quality of the resin composition. Further, the amount of volatile components remaining in the composition can be appropriately selected within a range where there is no problem depending on the purpose of use of the composition.

  According to the production method of the present invention, an epoxy resin composition in which the rubber-like polymer particles (A) are uniformly dispersed in the polymerizable organic compound (H), for example, an epoxy resin component, and further contains few impurities, is simple and efficient. Can be manufactured. The resin composition obtained by the present invention, for example, an epoxy resin composition is a fiber or filler reinforced composite material useful for industrial materials and sports equipment, adhesives, paints, coating materials, binders, semiconductor encapsulants and circuit boards. Rubber-like polymer particles (A) in cured products that can be widely used for various applications in which epoxy resins are usually used, such as laminates for plastics, and electrical / electronic component materials such as resin-coated metal foil It is possible to obtain a cured molded product having a very stable dispersion state and having few impurities.

  As described above, according to the present invention, it is possible to continuously obtain an aggregate (F) from which impurities are largely removed. Thereby, the operation of dehydrating and / or desolvating the mixture of the aggregate (F) and the aqueous phase (E), the operation of dispersing the aggregate (F) after the dehydration and / or desolving again in the organic solvent, the aggregate The operation of mixing the dispersion (G) in which the dispersion (F) is dispersed with the polymerizable organic compound (H) and the operation of distilling off the volatile components from the mixture of the dispersion (G) and the polymerizable organic compound (H) are continuously performed. Therefore, it is possible to achieve a continuous production method suitable for producing a large quantity and a small variety.

  EXAMPLES Hereinafter, although an Example demonstrates this invention concretely, this invention is not limited to these Examples.

  In the following, the residual amount of impurities was analyzed using the amount of emulsifier (anionic surfactant) and total ions as indicators. In addition, the dispersion state of the rubber-like polymer particles in the epoxy resin component, that is, the presence or absence of aggregation, was determined with a transmission electron microscope (TEM) after making an ultrathin section from the cured product of the obtained epoxy resin composition. Judgment was made by observation.

  Prior to the examples, the analytical measurement method used in the present invention will be described below.

[1] Amount of residual emulsifier The amount of residual emulsifier is determined by measuring the amount of emulsifier remaining in the dispersion (G) before mixing with the epoxy resin (H) by the following analytical method. The amount of emulsifier used in the polymerization was expressed as a ratio (% by weight) based on 100% by weight and used as an index.

[1-1] Sample Pretreatment In the following Examples, 5 ml of the dispersion (G) in which the rubber-like polymer particles (A) before mixing with the epoxy resin (H) are dispersed is taken, dried, and then beakered. The solution was put together with 50 ml of ethanol. After stirring the sample for 10 minutes, the supernatant was used as an analysis sample by the methylene blue method described later.

[1-2] Methylene blue method 30 ml of water, 10 ml of an alkaline sodium borate solution, and 5 ml of a methylene blue solution (0.025 wt% aqueous solution) were charged into a separating funnel. To this, 20 ml of chloroform was added and shaken for 3 to 5 minutes to separate and remove the chloroform layer. The operation of adding / removing chloroform was repeated until the chloroform layer was no longer colored. Next, 3 ml of dilute sulfuric acid (2.9 wt% aqueous solution), 20 ml of chloroform and 2 ml of the sample prepared in [1-1] were added and shaken for 3 to 5 minutes, and then the chloroform layer was subjected to a spectrophotometer (Corporation). Using a spectrophotometer UV-2200 manufactured by Shimadzu Corporation, the amount of residual emulsifier in the dispersion (G) before mixing the epoxy resin (A) was measured in absorption at a wavelength of 650 nm. The alkaline sodium borate solution was prepared by mixing 500 ml of a 0.4 wt% sodium hydroxide solution with 500 ml of a 1.9 wt% aqueous solution of sodium tetraborate decahydrate.

[2] Residual electrolyte (total ions)
The supernatant obtained in the same manner as the sample pretreatment was used as a sample for measuring electrical conductivity, and measured using an electrical conductivity meter (GM-117, manufactured by Kyoto Electronics Industry Co., Ltd.). The ratio of the amount of ions removed by a series of operations to the total amount of ions derived from the latex of the rubber-like polymer particles (A) (measured value obtained by drying the rubber-like polymer particles (A)) The total ion removal rate was calculated.

[3] Volatile component in epoxy resin composition In Examples and Comparative Examples, in order to obtain an epoxy resin composition, vacuum distillation was continued until the volatile component defined below reached 5000 ppm. About 3 g of the epoxy resin composition is precisely weighed and then heated in a hot air dryer at a set temperature of 170 ° C. for 20 minutes. By measuring the weight before and after heating, the reduced weight is used as a volatile component (ppm) before heating. The weight fraction with respect to the weight of was calculated.

[4] Dispersion state of rubbery polymer particles [4-1] Preparation of cured epoxy resin In a 100 ml beaker, 51.9 g of epoxy resin compositions obtained in Examples and Comparative Examples and diaminodiphenyl sulfone (Tokyo Kasei Co., Ltd.) (Made) 13.1 g was added and mixed under stirring. The mixture was allowed to stand in a vacuum dryer, and first heated to 130 ° C. under a nitrogen atmosphere, and then the volatile components were defoamed and removed for 10 minutes under reduced pressure. This mixture was poured into a 100 mm × 150 mm × 3 mm size mold, heated at 180 ° C. for 2 hours, and further cured at 220 ° C. for 2 hours to obtain a cured molded product.

[4-2] Observation of dispersion state of rubber-like polymer particles by transmission electron microscope A part of the obtained molding was cut out, and after the rubber-like polymer particles were dyed with osmium oxide, a thin piece was cut out. Using an electron microscope (manufactured by JEOL Ltd., JEM1200EX type), the dispersion state of the rubber-like polymer particles in the cured epoxy resin was determined by observation at a magnification of 10,000 times.

(Production Example 1) Production of rubber-like polymer particles (A) Latex In a 100 L pressure-resistant polymerization machine, water 200 parts by weight, tripotassium phosphate 0.03 parts by weight, potassium dihydrogen phosphate 0.25 parts by weight, ethylenediamine After adding 0.002 parts by weight of 4 acetic acid, 0.001 part by weight of ferrous sulfate and 1.5 parts by weight of sodium dodecylbenzenesulfonate, nitrogen was sufficiently substituted while stirring to remove oxygen, and then butadiene 75 Part by weight and 25 parts by weight of styrene were charged into the system, and the temperature was raised to 45 ° C. Polymerization was initiated by adding 0.015 parts by weight of paramentane hydroperoxide, followed by 0.04 parts by weight of sodium formaldehyde sulfoxylate. Four hours after the start of polymerization, 0.01 part by weight of paramentane hydroperoxide, 0.0015 part by weight of ethylenediaminetetraacetic acid and 0.001 part by weight of ferrous sulfate were added. At 10 hours after the polymerization, the residual monomer was removed by devolatilization under reduced pressure to complete the polymerization. The polymerization conversion was 98%, and the volume average particle diameter of the obtained styrene-butadiene rubber latex was 0.1 μm.

  Subsequently, 1300 g of the rubber latex (including 420 g of styrene / butadiene rubber particles and 1.5 wt% sodium dodecylbenzenesulfonate based on the solid content of the rubber) and 440 g of pure water are added to a 3 L glass container. The mixture was charged and stirred at 70 ° C. while replacing with nitrogen. After adding 1.2 g of azobisisobutyronitrile (AIBN), a mixture of 54 g of styrene, 72 g of methyl methacrylate, 36 g of acrylonitrile, and 18 g of glycidyl methacrylate was continuously added over 3 hours for graft polymerization. After completion of the addition, the reaction was terminated by further stirring for 2 hours to obtain a latex of rubber-like polymer particles (A). The polymerization conversion rate was 99.5%. The obtained latex was used as it was.

(Example 1)
In a vertical 1 L stirring tank having a tank diameter of 70 mm and a height of 350 mm, four stages of a raised 45 ° inclined paddle blade having a blade diameter of 50 mm were installed and stirred at 450 rpm. Subsequently, an aqueous latex of rubber-like polymer particles (A) of Production Example 1 and methyl ethyl ketone (B) mixed at an equal weight (C) were supplied at a rate of 128 ml / min from a position 50 mm from the bottom of the stirring tank. Feeded at speed. At the same time, water (D) was supplied at a supply rate of 92 ml / min from another supply port installed at the same height at the bottom of the stirring tank. The mixing ratio of the aqueous latex of the rubber-like polymer particles (A), methyl ethyl ketone (B), and water (D) is 100 parts by weight, 100 parts by weight, and 160 parts by weight, and the residence time in the stirring tank is 4.5. Minutes. The height from the bottom of the stirring tank to the liquid level was 300 mm. The slurry liquid which consists of an aggregate (F) and an aqueous phase (E) was collect | recovered by the overflow from the liquid level position of a stirring tank upper part. The operation was carried out for 3 hours to agglomerate 10.4 kg of the aqueous latex of rubber-like polymer particles (A). As a result of measuring the particle diameter of the aggregate collected every 15 minutes from the liquid surface position in the upper part of the stirring tank with a wet sieve, the 50% diameter on the basis of the weight on the sieve is 1500 μm, and the 95% diameter is 750 μm, 5 The% diameter was 3000 μm and there was no change. In addition, no agglomerated particles were observed due to staying in the tank, and stable continuous operation was possible. Furthermore, the obtained slurry was dehydrated, methyl ethyl ketone was added to the aggregate (F) to prepare a dispersion (G), and the remaining emulsifier and electrolyte were measured. The removal rates of emulsifier and electrolyte were 95% and 90%, respectively.

(Example 2)
136 g of methyl ethyl ketone was added to 94 g of the aggregate obtained in Example 1, and mixed for 30 minutes under a stirring condition of 500 rpm per minute to obtain a dispersion in which rubbery polymer particles were uniformly dispersed. This dispersion was transferred to a 1 L tank with a jacket and a stirrer (a stirrer equipped with an anchor blade having an inner diameter of 100 mm and an airfoil of 90 mm), and 92 g of epoxy resin (Epicoat 828, manufactured by Japan Epoxy Resin Co., Ltd.) was added and mixed uniformly. The jacket temperature (warm water) is set to 60 ° C., and the vacuum pump (oil rotary vacuum pump, TSW-150 manufactured by Sato Vacuum Co., Ltd.) is used until the volatile components reach a predetermined concentration (5000 ppm) under reduced pressure. The process was continued and a transparent epoxy resin composition containing rubber-like polymer particles was obtained. The time required for volatilization was 5 hours and 20 minutes. As a result of observing the dispersion state of the rubber-like polymer particles in the cured product obtained from this epoxy resin composition, the rubber-like polymer particles were uniformly dispersed without agglomeration.

(Example 3)
10 g of the aggregate obtained in Example 1 was dried for 2 hours at a temperature of 70 ° C. using a dryer. As a result of measuring the dried particles with a wet sieve, spherical particles having a 50% diameter of 1400 μm based on the weight on the sieve were obtained.

Example 4
The same operation as in Example 1 was performed except that the supply amount of water (D) was 106 ml / min and 184 parts by weight. The residence time in the apparatus was 4.3 minutes. As a result of measuring the particle diameter of the aggregate collected every 15 minutes from the liquid surface position in the upper part of the stirring tank with a wet sieve, the 50% diameter on the basis of the weight on the sieve is 700 μm, and the 95% diameter is 180 μm and 5%. There was no change at a diameter of 1300 μm. In addition, no agglomerated particles were observed due to staying in the tank, and stable continuous operation was possible. Further, a dispersion dope was prepared by adding methyl ethyl ketone to a part of the aggregate (F) recovered by overflow from the liquid level at the top of the stirring tank, and the remaining emulsifier and electrolyte were measured. The removal rates of emulsifier and electrolyte were 90% and 80%, respectively.

(Example 5)
173 g of methyl ethyl ketone was added to the aggregate obtained in Example 4 and mixed for 30 minutes under a stirring condition of 400 rpm per minute to obtain a dispersion in which rubber-like polymer particles were uniformly dispersed. This dispersion was transferred to a 1 L tank with a jacket and a stirrer (stirrer equipped with an anchor blade having an inner diameter of 100 mm and an airfoil of 90 mm), and 116 g of epoxy resin (Epicoat 828, manufactured by Japan Epoxy Resin Co., Ltd.) was added and mixed uniformly. The jacket temperature (warm water) is set to 60 ° C., and a volatile component is continuously distilled off to a predetermined concentration (5000 ppm) under reduced pressure using a vacuum pump, and a transparent epoxy resin composition containing rubbery polymer particles I got a thing. The time required for volatilization was 5 hours and 20 minutes. As a result of observing the dispersion state of the rubber-like polymer particles in the cured product obtained from this epoxy resin composition, the rubber-like polymer particles were uniformly dispersed without agglomeration.

(Example 6)
10 g of the aggregate obtained in Example 4 was dried at a temperature of 70 ° C. for 2 hours using a dryer. As a result of measuring the dried particles with a wet sieve, spherical particles having a 50% diameter of 600 μm based on the weight on the sieve were obtained.

(Comparative Example 1)
Four stages of flat turbine blades having a blade diameter of 50 mm were installed in a vertical 1 L stirring tank having a tank diameter of 70 mm and a height of 350 mm, and stirred at 450 rpm. Subsequently, an aqueous latex of rubber-like polymer particles (A) of Production Example 1 and methyl ethyl ketone (B) mixed at an equal weight (C) were supplied at a rate of 128 ml / min from a position 50 mm from the bottom of the stirring tank. Feeded at speed. At the same time, water (D) was supplied at 92 ml / min from another supply port installed at the same height at the bottom of the stirring tank. The mixing ratio of the aqueous latex of the rubber-like polymer particles (A), methyl ethyl ketone (B), and water (D) is 100 parts by weight, 100 parts by weight, and 160 parts by weight, and the residence time in the stirring tank is 4.5. Minutes. The height from the bottom of the stirring tank to the liquid level was 300 mm. The slurry liquid which consists of an aggregate (F) and an aqueous phase (E) was collect | recovered by the overflow from the liquid level position of a stirring tank upper part. The operation was performed for 60 minutes to aggregate 10.4 kg of the aqueous latex of rubber-like polymer particles (A). As a result of measuring the particle diameter of the aggregate collected every 15 minutes from the liquid surface position in the upper part of the stirring tank with a wet sieve, the 50% diameter on the basis of the sieve weight after 15 minutes is 1500 μm, the 95% diameter is 750 μm, 5 The% diameter was 3000 μm. After 50 minutes, the 50% diameter on the basis of the weight on the sieve was 3000 μm, the 95% diameter was 750 μm, and the 5% diameter was 4000 μm. Grain growth was observed over time, and a stable particle diameter was not obtained. In addition, massive particles of about 30 mm in which the rubber-like polymer particles (A) were laminated due to particle retention in the tank were observed, and stable continuous operation was not possible.

(Comparative Example 2)
The same operation as in Comparative Example 1 was performed except that the supply amount of water (D) was 106 ml / min and 184 parts by weight. The residence time in the apparatus was 4.3 minutes. As a result of measuring the particle size of the aggregates collected every 15 minutes from the liquid level at the top of the stirrer with a wet sieve, the 50% diameter on the sieve after 15 minutes is 680 μm, the 95% diameter is 180 μm, and 5%. The diameter was 1300 μm. After 50 minutes, the 50% diameter on the basis of the weight on the sieve was 1400 μm, the 95% diameter was 750 μm, and the 5% diameter was 3000 μm. Grain growth was observed over time, and stable continuous operation was not possible.

Claims (12)

  A mixture of an aqueous latex of rubber-like polymer particles (A) and an organic solvent (B) that is partially soluble in water is mixed with a mixture (C) and water (D). The mixture was continuously supplied to the stirring tank installed in the vessel and mixed and contacted to produce an aggregate (F) of rubber-like polymer particles (A) containing the organic solvent (B) in the aqueous phase (E). Then, the continuous manufacturing method of the refined rubber-like polymer particle | grains characterized by isolating an aggregate (F) continuously.   The mixture (C) and water (D) are supplied from the bottom of the stirring tank, and the mixture of the aggregate (F) and the aqueous phase (E) is recovered from the top of the stirring tank. Production method.   3. Production of purified rubber-like polymer particles, wherein the aggregate (F) of purified rubber-like polymer particles obtained by the production method according to claim 1 or 2 is dehydrated and / or desolvated and then dried. Method.   An organic solvent having an affinity for the rubber-like polymer particles (A) is added to the aggregate (F) of the purified rubber-like polymer particles obtained by the production method according to claim 1 or 2, and the rubber-like polymer A method for producing a dispersion (G), wherein a dispersion (G) in which polymer particles (A) are dispersed in the organic solvent is obtained.   It is a manufacturing method of the resin composition which disperse | distributed rubber-like polymer particle (A) in the polymeric organic compound (H) which has a reactive group, Comprising: The dispersion | distribution (G which was obtained by the manufacturing method of Claim 4 (G) ) And the polymerizable organic compound (H), and then the volatile component is distilled off.   It is a manufacturing method of the resin composition which disperse | distributed the rubber-like polymer particle (A) in the polymeric organic compound (H) which has a reactive group, Comprising: The aggregate obtained by the manufacturing method of Claim 1 or 2 After mixing with (F) and the said polymerizable organic compound (H), a volatile component is distilled off, The manufacturing method of the resin composition characterized by the above-mentioned.   The method for producing a resin composition according to claim 5 or 6, wherein the polymerizable organic compound (H) having a reactive group is an epoxy resin.   8. The method according to claim 1, wherein the solubility of the organic solvent (B) in water at 20 ° C. is 5 wt% or more and 40 wt% or less.   The amount of water (D) to be brought into contact with the mixture (C) obtained by mixing the aqueous latex of the rubber-like polymer particles (A) and the organic solvent (B) that is partially soluble in water is the organic solvent. (B) The manufacturing method according to any one of claims 1 to 8, wherein the amount is 40 to 350 parts by weight with respect to 100 parts by weight.   The rubber-like polymer particle (A) is a polymer having a multilayer structure of two or more layers, and includes at least one or more crosslinked rubber-like polymer layers. The manufacturing method of crab.   The rubber-like polymer particles (A) are at least one monomer selected from diene monomers and (meth) acrylic acid ester monomers, 50 to 100% by weight, and other copolymerizable vinyls In the presence of 40 to 95% by weight of a rubber particle core (A-1) composed of a rubber elastic body composed of 0 to 50% by weight of monomer, a polysiloxane rubber-based elastic body, or a mixture thereof, (meth) Shell layer (A-2) 5-60 comprising at least one vinyl polymerizable monomer selected from acrylic ester, aromatic vinyl, vinyl cyanide, unsaturated acid derivative, (meth) acrylamide derivative, maleimide derivative The production method according to any one of claims 1 to 10, which is a graft copolymer obtained by polymerizing a weight percent.   The shell layer (A-2) of the rubber-like polymer particle (A) has at least one reactive functional group selected from the group consisting of an epoxy group, a carboxyl group, a hydroxyl group, and a carbon-carbon double bond. The manufacturing method according to claim 11, wherein