METHOD OF PRODUCING EMULSION POLYMER

Abstract: A method of producing an emulsion polymer which comprises adding a polymerizable monomer to an emulsion polymer containing a high-molecular-weight compound having a weight average molecular weight of 20,000 to 2,000,000 as a seed polymer, the amount of the unsatu­ rated monomer being 1.5 to 9.5 times the total volume of the solids in the emulsion polymer, and thereafter, polymerizing the monomer in the presence of a film-­ forming aid.

Description: This invention relates to a novel process for producing an emulsion polymer. More specifically, this invention relates to a novel and useful process for producing an emulsion polymer, which comprises causing an emulsion polymerization dispersion containing a specific high-molecular-weight compound as a seed polymer to absorb a specific amount of a polymerizable unsaturated monomer, and thereafter polymerizing the unsaturated monomer in the presence of a film-forming aid. With an expansion of the utility of emulsion polymers in recent years, they have been required to have various properties. One important property among them is the monodispersity of the polymer particles, but no method has yet been established which can strictly control the particle diameter and particle size distribution of polymer particle. Desirably, to improve flowability or for use as a matt agent, the emulsion polymers should have a larger particle diameter and a narrower particle size distribution than ordinary emulsion polymer particles. One method now in practice of producing an emulsion polymer of a large particle diameter is to polymerize a polymerizable unsaturated monomer in the presence of an electrolyte. Since, however, the amount of the electrolyte that can be added is naturally limited, the particle diameters can be controlled only to a limited extent. Furthermore, the remaining electrolyte may exert deleterious effects, for example the degradation of properties such as water resistance of the emulsion film, on the resulting polymer. Methods of obtaining mono-disperse emulsion polymers of a large particle diameter are proposed, for example, in Japanese Laid-Open Patent Publications Nos. 97582/1979, 126288/1979 and 206803/1980. The method described in Japanese Laid-Open Patent Publication No. 97582/1979 comprises synthesizing a polymer (seed polymer) of a much lower molecular weight than ordinary polymer latices by adding a chain transfer agent during polymerization, causing the seed polymer to absorb a slightly water-soluble polymerizable unsaturated monomer, and then polymerizing the unsaturated monomer. If this polymerization is carried out by using such an oil-soluble or water-soluble polymerization initiator as is used normally, a coagulum or new particles may result, and it is difficult to obtain a monodisperse emulsion polymer of a large particle diameter stably in good yields. The method described in Japanese Laid-Open Patent Publication No. 126288/1979 involves a first step wherein a seed polymer is caused to absorb a difficultly water-soluble organic compound having a water solubility lower than 10⁻² g/liter of H₂O and a second step wherein the seed polymer is caused to absorb a slightly water-soluble monomer in an amount of as large as 100-fold to form swollen particles and then the absorbed monomer is polymerized in the presence of a water-soluble or oil-soluble polymerization initiator while maintaining the monomer in the particulate form. If, however, when the polymerization is carried out using the oil-soluble initiator, the monomer phase which does not participate in the swelling of the seed polymer is also polymerized so that a large amount of a coagulum forms and the yield of the polymer is decreased. In addition, when a low-molecular-weight substance is used as the seed particles, the resulting emulsion polymer is likely to have lowered durability. The method described in Japanese Laid-Open Patent Publication No. 206803/1980 comprises a first step wherein a seed polymer is caused to absorb a difficultly water-soluble organic compound having a water solubility lower than 10⁻² g/liter of H₂O and a second step wherein the seed polymer is caused to absorb a monomer in an amount of as large as 10- to 400-fold to form swollen particles and then the absorbed monomer is polymerized in the presence of a redox-system radical polymerization initiator in an emulsifier concentration below the critical micelle concentration while maintaining the monomer in the particulate form. Since a large amount of the monomer is added to a small amount of the seed particles in this method, that portion of the monomer which is not absorbed by the seed polymer exists in a large amount and is polymerized by the redox-system radical polymerization initiator. As a result, as in the aforesaid method, a large amount of a coagulum results and the yield of the polymer is decreased. Another method of producing a highly monodisperse emulsion polymer having a large particle diameter is to expand seed particles gradually to a larger size and then perform polymerization. According to this method, an emulsifier and a monomer must be added stepwise. The process steps therefore become complex, and the particle size distribution of the resulting particles is liable to become broad. Makromol. Chem. 180 , 737-744 (1979) discloses a further method for producing a monodisperse latex with large particle size. The method comprises a two-step swelling process comprising a first step of allowing polymer particles to absorb a water insoluble relatively low molecular weight compound, and a second step of allowing the particles to absorb a slightly water soluble compound. The slightly water soluble compound may be a vinyl monomer, which may subsequently be polymerised. It is an object of this invention to remedy the various defects of the prior art described above and to provide a method by which a highly monodisperse emulsion polymer having a large particle diameter can be produced while the occurrence of a coagulum or new particles during the polymerization is inhibited to a low level. In accordance with this invention, there is provided a method of producing an emulsion polymer which comprises adding a polymerizable unsaturated monomer to an emulsion polymer comprising a high-molecular-weight compound not containing a polyfunctional cross-linkable monomer or a chain transfer agent and having a weight average molecular weight of 20,000 to 2,000,000 as a seed polymer, the amount of the unsaturated monomer being 1.5 to 9.5 times the total volume of the solids in the emulsion polymer, and thereafter, polymerizing the monomer in the presence of a film-forming aid which is at least one compound selected from ethylene glycol; ether, ester or etherester derivatives of ethylene glycol; glycols having 3 to 8 carbon atoms; alkyl-substituted C₃-C₈ glycols; ether, ester or etherester derivatives of said glycols; diethylene glycol; ether, ester or etherester derivatives of diethylene glycol; glycerol; glycerol derivatives; aromatic alcohols; substituted aromatic alcohols; aromatic polycarboxylic acid esters; and alkyl-substituted aromatic polycarboxylic acid esters. It is critical that the seed polymer should be easy to plasticize by the film-forming aid to assume a structure permitting easy absorption of a polymerizable unsaturated monomer. A specific method of imparting this structure, for example, is to use the lowest necessary amount of the emulsifier so as to inhibit formation of an aggregate or a coagulum and perform the polymerization under the aforesaid conditions by an ordinary emulsion-polymerization method. The high-molecular-weight compound may be, for example, homopolymers or copolymers of alpha,beta-ethylenically unsaturated monomers, polyesters and polyurethanes. The (co)polymers of alpha,beta-ethylenically unsaturated monomers may be prepared from at least one monomer selected from monomers to be described hereinbelow. Carboxyl-free monomers are preferred. The polyesters may be, for example, ionomer-type aqueous aromatic polyesters, typically FINTEX ES* series produced by Dainippon Ink and Chemicals, Inc. The polyurethanes may be, for example, ionomer-type or water-dispersible polyether polyurethanes or polyester polyurethanes. Typical examples ore HYDRAN HW SERIES AND VONDIC series produced by Dainippon Ink and Chemicals, Inc. The weight average molecular weight of the high-molecular-weight compound is 20,000 to 2,000,000, preferably 200,000 to 1,500,000. If this molecular weight is lower than 20,000, the final emulsion polymer particles have lowered durability characteristics, for example lowered water resistance, when used as a pigment or a filler. If it exceeds 2,000,000, the seed polymer is extremely difficult to plasticize by the film-forming aid and to swell by absorption of the polymerizable unsaturated monomer. Hence, molecular weights outside the specified range are undesirable. The term "film-forming aid", as used herein, generically denotes film-forming aids, plasticizers and specific solvents which have been used heretofore in preparing water-base paints. Typical examples of the film-forming aids include ethylene glycol or its ether-type, ester-type or etherester-type derivatives such as ethylene glycol, methyl Cellosolve , ethyl Cellosolve , butyl Cellosolve , methyl Cellosolve acetate, ethyl Cellosolve acetate, butyl Cellosolve acetate, ethylene glycol monoacetate and ethylene glycol diacetate; diethylene glycol or its ether-type, ester-type or etherester-type derivatives such as diethylene glycol, methylcarbitol, ethylcarbitol, butylcarbitol, methylcarbitol acetate, ethylcarbitol acetate and butylcarbitol acetate; unsubstituted or alkyl-substituted glycols having 3 to 8 carbon atoms or their ether-type, ester-type or etherester-type derivatives such as 2-methyl-2,4-pentanediol, 2,2,4-trimethyl-1,3-pentanediol monoisobutyrate and 2,2,4-trimethyl-1,3-pentanediol isobutyrate; glycerol or its derivatives such as glycerol acetate (also called acetin); unsubstituted or alkyl-substituted aromatic alcohols such as benzyl alcohol and isopropyl benzyl alcohol; and esters of aromatic polycarboxylic acids such as dibutyl phthalate and dioctyl phthalate. At least one of these is used as the film-forming aid. The suitable molecular weight of the film-forming aid is in the range of 62 to 1,000, preferably 100 to 800. In the present invention, the use of unsubstituted or alkyl-substituted monoalcohols such as 2-ethylhexanol or n-octanol and ketones such as methyl ethyl ketone, methyl isobutyl ketone or methyl amyl ketone is not desirable because it induces occurrence of flocs, but the combined use of these with the aforesaid film-forming aids is not prohibited. The suitable amount of the film-forming aid is 0.1 to 10.0 % by weight, preferably 0.2 to 8 % by weight, based on the solids of the emulsion polymer finally obtained. The film-forming aid may be added at any desired time, for example as shown below. (1) It is fed into the aqueous phase prior to emulsion polymerization for obtaining the emulsion polymerization dispersion (seed emulsion). (2) It is fed, either alone or together with the polymerizble unsaturated monomer, in a step of polymerization performed after adding the polymerizable unsaturated monomer to the above seed emulsion. (3) It is fed in both of the above steps (1) and (2). The emulsion polymerization finally obtained by the method of this invention is desirably a multilayered polymer having three or more layers. In order to obtain such a polymer, it is possible to perform polymerization in the presence of the film-forming aid in the aqueous phase and/or the polymerizable unsaturated monomer in the stage of obtaining each layer. Preferably, an inner layer is formed in the presence of the film-forming aid to obtain a swollen inside layer, and then an outside layer is provided by polymerization. Examples of the polymerizable unsaturated monomer used to obtain the emulsion polymer particles in the method of this invention include carboxyl-containing vinyl monomers and unsaturated dicarboxylic acids typified by unsaturated group-containing hydroxyalkyl esters of monocarboxylic acids such as adducts of (meth)acrylic acid, crotonic acid, maleic acid, fumaric acid, itaconic acid, citraconic acid or an acid anhydride group-containing monomer (such as maleic anhydride or itaconic anhydride) with glycols; and alpha,beta-ethylenically unsaturated carboxylic acids such as the aforesaid acid anhydride group-containing monomers mentioned above. These monomers may be used singly or in combination. Other examples of the polymerizable unsaturated monomer are alkyl esters of (meth)acrylic acid having a linear, branched or cyclic alkyl group with 1 to 8 carbon atoms such as methyl(meth)acrylate, ethyl(meth)acrylate, butyl(meth)acrylate, 2-ethylhexyl(meth)acrylate or cyclohexyl(meth)acrylate; and aromatic vinyl monomers such as styrene, alpha-methylstyrene, p-tert-butylstyrene, p-methylstyrene and vinyltoluene. They may be used either singly or in combination. Still other examples of the polymerizable unsaturated monomer include hydroxyalkyl esters of (meth)acrylic acid such as 2-hydroxyethyl (meth)acrylate, 2-hydroxypropyl (meth)acrylate, 3-hydroxypropyl (meth)acrylate, 2-hydroxybutyl (meth)acrylate, 3-hydroxybutyl (meth)acrylate, 4-hydroxybutyl (meth)acrylate, 3-chloro-2-hydroxypropyl (meth)acrylate and polyethylene glycol mono(meth)acrylate; unsaturated group-containing polyhydroxyalkyl esters typified by di-hydroxyalkyl esters of the aforesaid unsaturated dicarboxylic acids; and hydroxyl-containing vinyl monomers such as hydroxyvinyl ether and hydroxyalkyl vinyl ethers. Further examples of the polymerizable unsaturated polymerizable unsaturated monomer include substituted or unsubstituted aromatic ring-containing (meth)acrylic acid esters such as benzyl (meth)acrylate; esters formed between the aforesaid unsaturated dicarboxyic acids and monohydric alcohols; vinyl esters such as vinyl acetate, vinyl benzoate and Veoba (vinyl ester produced by Shell Chemical Co. of Netherlands); (per-fluoroalkyl group-containing vinyl esters such as octafluorobutyl (meth)acrylate, trifluoromethyl (meth)acrylate, perfluorocyclohexyl (meth)acrylate, diperfluorocyclohexyl fumarate and N-isopropyl perfluorooctanesulfonamidoethyl (meth)acrylate); olefins such as vinyl chloride, vinylidene chloride, vinyl fluoride, vinylidene fluoride, chlorotrifluoroethylene, ethylene and propylene; monomers containing carboxylic acid amide groups such as (meth)acrylamide, N,N-dimethyl (meth)acrylamide, N-alkoxymethylated (meth)acrylamide, diacetone acrylamide and N-methylol (meth)acrylamide; monomers containing a sulfonamide group such as p-styrenesulfonamide, N-methyl-p-styrenesufonamide and N,N-dimethyl-p-styrenesulfonamide; monomers having a tertiary amino group, for example N,N-dialkylaminoalkyl (meth)acrylates such as N,N-diethylaminoethyl (meth)acrylate, and adducts formed between the aforesaid acid anhydride group-containing monomers and compounds having both an active hydrogen atom and a tertiary amino group capable of reacting with the acid anhydride group; cyano group-containng monomers such as (meth)acrylonitrile; phosphoric ester group-containing monomers obtained by condensation reaction of the aforeasid hydroxyalkyl esters of (meth)acrylic acid with phosphoric acid or its derivative; and sulfonic acid group-containing monomers such as 2-acrylamide-2-methyl-propanesulfonic acid or organic amine salts thereof. In order to improve the durability and solvent resistance of the final emulsion polymer particles, a crosslinkable monomer may be used in providing the outermost layer by emulsion polymerization. Typical examples of the crosslinkable monomer include monomers having at least two polymerizable unsaturated groups in the molecule, such as ethylene glycol di(meth)acrylate, propylene glycol di(meth)acrylate, trimethylolpropane tri(meth)acrylate, divinylbenzene, trivinylbenzene and diallyl phthalate; and monomers having a hydrolyzable silyl group, such as vinyltriethoxysilane, gamma-(meth)acryloyloxypropyltrimethoxysilane, gamma-(meth)acryloyloxypropylmethyldimethoxysilane, gamma-(meth)acryloyloxypropyltriethoxysilane and gamma-(meth)acryloyloxypropylmethyldiethoxysilane. Additives to be described below may be used in performing the emulsion polymerization by the method of this invention. Anionic emulsifiers, nonionic emulsifiers, cationic emulsifiers, other reactive emulsfiers, and substances having surface activating ability such as acrylic oligomers may be used as emulsifiers in the method of this invention. The use of nonionic emulsifiers and anionic emulsifiers is desirable because it permits preparation of a stable emulsion with little formation of an aggregate or a coagulum during the polymerization. Typical examples of the nonionic emulsifiers are polyoxyethylene alkyl phenyl ethers, polyoxyethylene alkyl ethers, polyoxyethylene higher fatty acid esters and an ethylene oxide/propylene oxide block copolymer. Typical examples of the anionic emulsifiers include alkali metal salts of alkylbenzenesulfonic acids, alkali metal salts of alkyl sulfates and alkali metal salts of polyoxyethylene alkyl phenyl sulfates. Water-soluble oligomers composed of polycarboxylic acid salts or polysulfonic acid salts may be used instead of, or in combination of, the aforesaid anionic emulsifiers. Water-soluble polymeric substances such as polyvinyl alcohol or hydroxyethyl cellulose may be used as protective colloids. The use of such a protective colloid easily leads to emulsion particles having a large particle diameter, but results in a degradation in the water resistance of a film or the like containing the resulting emulsion polymer particles. Accordingly, the amount of the protective colloid should be limited to not more than 5 % by weight, preferably not more than 2 % by weight, based on the total amount of the polymerizaable unsaturated monomer. The suitable amount of the emulsifier is about 0.1 to 10 % by weight based on the total amount of the monomers. Any polymerization initiators which are generally used in emulsion polymerization may be used in this invention without any particular limitation. Typical examples are water-soluble inorganic peroxides such as hydrogen peroxide, persulfates such as potassium persulfate and ammonium persulfate, organic peroxides such as cumene hydroperoxide and benzoyl peroxide, and azo initiators such as azobisisobutyronitrile and azobiscyanovaleric acid. They may be used singly or in combination. Use of two or more water-soluble polymerization initiators having different half-lives is especially effective for synthesis of an emulsion having a large particle diameter. The suitable amount of the polymerization initiator is 0.1 to 2 % by weight based on the total amount of the polymerizable monomer. Of course, it is possible to use a so-called redox polymerization technique involving use of a combination of the polymerization initiator and a metallic ion or a reducing agent in the method of this invention. In performing the method of this invention, at least one of the polymerizable monomers is added to a reactor at a time, portionwise, or continuously in the presence of water preferably in the copresence of deionized water and the emulsifier. Furthermore, the polymerization initiator is added, and the mixture is heated at a temperature of 0 to 100 °c, preferably 30 to 90 °C to give an emulsion polymer containing emulsion particles (seed polymer) as an inside layer capable of being easily swollen with the film-forming aid and the monomer. Then, the above polymerizable monomer in an amount 1.5 to 9.5 times the total volume of the solids of the seed polymer is added to the emulsion polymer (seed emulsion) containing preferably 10 to 100 % by weight of the seed polymer so as to cause it to be absorbed by the seed polymer. The absorbed polymerizable monomer is then polymerized in the presence of the film-forming aid. The polymerizable monomer may be added to the seed emulsion and polymerized, either together with the film-forming aid or in the emulsified state. Preferably, the film-forming aid is first added to the seed emulsion, and the polymerizable monomer is added and polymerized. Desirably, the polymerizable monomer is added after the lapse of at least 30 minutes from the addition of the film-forming aid. The monomer is desirably polymerized after it is aged for at least 30 minutes from the addition. The foregoing procedure may be repeated a number of times required for obtaining the desired particle diameter. As stated above, the aforesaid crosslinkable monomer is preferably used in order to form the outermost layer. This improves the water resistance and durability of the finally obtained large-diameter particles. Preferably, the (co)polymer constituting the outermost layer has a glass transition temperature of at least 40 °C, preferably 50 to 250 °C. According to this invention, the use of the film-forming aid facilitates absorption of the polymerizable unsaturated monomer in the seed particles and swelling of the seed particles, and makes it easy to form particles of a large particle diameter. Consequently, particles of a highly monodisperse emulsion polymer having a large diameter can be obtained in less process steps. Furthermore, according to the present invention, new particles which are particles other than the desired emulsion polymer particles do not appreciably form. Hence, the seed particles themselves grow efficiently to give highly monodisperse particles having a narrow particle size distribution. The suitable final solids concentration is 5 to 65 % by weight, especially 10 to 65 % by weight, and the suitable particle diameter of the finally obtained emulsion particles is usually within the range of 1.0 to 20.0 µm. The polymer emulsion of a large particle diameter obtained by the method of this invention can be powderized by a conventional drying method, for example by spray drying at 100 to 250 °C, tray drying or vat drying at 50 to 70 °C, or fluidized bed drying. The resin powder obtained by spray-drying generally consists of agglomerates (secondary particles) of primary particles (particles in emulsion state), and are completely spherical. The emulsion polymer obtained by the method of this invention may be used, for example, in the field of water-base paints as a pigment or filler, or in the field of coating agents such as coating agents or surface-finishing agents for paper or fibers in combination with suitable binders. A powder of the emulsion polymer may be used, for example, as a matt agent for solvent-base paints, a rheology controlling agent, a filler for molding resins, light-weight fillers, a lubricant for cosmetics or a carrier for latex diagnostic agent. The following examples illustrate the present invention more specifically. All parts and percentages in these examples are by weight unless otherwise specified. All reactions described below were carried out in a nitrogen gas atmosphere. EXAMPLE 1 Deionized water (350 parts), 0.230 part of sodium polyoxyethylene alkyl phenyl ether sulfate and 100 parts of styrene were introduced into a reactor equipped with a stirrer, a reflux condenser, a dropping funnel and a thermometer, and well stirred. The reactor was then heated to maintain its inside at 70 °C. A mixture of 0.5 part of ammonium persulfate and 25 parts of deionized water was added dropwise over 5 hours and the mixture was maintained at this temperature for 1 hour. The reaction mixture was then cooled to give a seed emulsion (M-1) of a high-molecular-weight compound having a weight average molecular weight, measured by gel permeation chromatography using tetrahydrofuran as a solvent, of 380,000 (hereinafter, the weight average molecular weights were mesured by the same method). The seed emulsion (M-1) had a solids concentration of 21.2 %, a pH of 2.5 and an average particle diameter (measured by Coulter Model N4 of Coulter Co. (same hereinafter)), of 0.28 µm. Sodium polyoxyethylene alkyl phenyl ether sulfate (0.115 part) was added to 47.2 parts of the seed emulsion (M-1). Further, 2.0 parts of 2,2,4-trimethyl-1,3-pentanediol monoisobutyrate (to be referred to as Texanol hereinafter) and 370 parts of deionized water were added. The mixture was well stirred at 30 to 40 °C for 1 hour to permit Texanol to be absorbed by the seed polymer. Thereafer, the mixture was heated to 50 °C, and 85 parts of styrene and 5 parts of divinylbenzene were added. The mixture was stirred for 2 hours. The reactor was further heated to maintain its inside at 70 °C, and a mixture of 0.5 part of ammonium persulfate and 25 parts of deionized water was added dropwise over 5 hours. The mixture was further maintained at this temperature for 1 hour, and then cooled to give an emulsion (A-1). The emulsion (A-1) was a dispersion of monodisperse gelled particles having a solids concentration of 18.5 %, a pH of 2.6, and an average particle diameter of 1.05 µm. EXAMPLE 2 Deionized water (250.3 parts), 0.352 part of sodium laurylsulfate and 100 parts of styrene were introduced into a reactor equipped with a stirrer, a reflux condenser, a thermometer, and a dropping funnel, and well stirred. The reactor was then heated to maintain its inside at 80 °C. A mixture of 0.25 part of ammonium persulfate and 25 parts of deionized water was added dropwise over 2.5 hours and further maintained at this temperature for 1 hour. The reaction mixture was then cooled to give a seed emulstion (M-2) of a high-molecular-weight compound having a weight average molecular weight of 410,000. The seed emulsion had a solids concentration of 25.1 %, a pH of 2.3 and an average particle diameter of 0.26 µm. Sodium laurylsulfate (0.152 part), 3.0 parts of butylcarbitol acetate and 450.8 parts of deionized water were added to 59.8 parts of the seed emulsion (M-2). The mixture was well stirred at 30 to 40 °C for 1 hour to permit absorption of butylcarbitol acetate in the seed polymer. The mixture was heated to 50 °C, and 85 parts of styrene was added. The mixture was stirred for 2 hours. The reactor was further heated to maintain its inside at 70 °C, and a mixture of 0.25 part of ammonium persulfate and 25 parts of deionized water was added drowpise over 2.5 hours. The reactor was further heated to maintain its inside at 80 °C. A mixture of 0.25 part of potassium persulfate and 25 parts of deionized water was added dropwise. The mixture was further maintained at this temperature for 1 hour, and then cooled to give a seed emulsion (M-3) of a high-molecular-weight compound having a molecular weight of 650,000. The seed emulsion (M-3) had a solids concentration of 17.8 %, a pH of 2.3, and an average particle diameter of 0.86 µm. Sodium laurylsulfate (0.136 part), 1.0 part of butylcarbitol acetate and 485 parts of deionized water were added to 56.2 parts of the seed emulsion (M-3). The mixture was well stirred at 30 to 40 °C for 1 hour, and then heated to 50 °C. A mixture of 85 parts of styrene and 5 parts of divinylbenzene was added, and the mixture was stirred for 2 hours. While maintaining the inside of the reactor at 70 °C, a mixture of 0.25 part of ammonium persulfate and 25 parts of deionized water was added dropwise over 2.5 hours. The reactor was then further heated to maintain its inside at 80 °C. A mixture of 0.25 part of potassium persulfate and 25 parts of deionized water was added dropwise over 2.5 hours. The mixture was maintained at this temperature for 1 hour, and then cooled to give an emulsion (A-2) which was a dispersion of monodisperse gel particles having a solids concentration of 14.7 %, a pH of 2.5 and an average particle diameter of 3.28 µm. EXAMPLE 3 Deionized water (302.5 parts), 0.238 part of sodium laurylbenzenesulfate and 100 parts of styrene were introduced into a reactor equipped with a stirrer, a reflux condenser, a dropping funnel and a thermometer, and well stirred. Then, the reactor was heated to maintain its inside at 70 °C. A mixture of 0.5 part of potassium persulfate and 50 parts of deionized water was added dropwise over 5 hours. The reactor was then further heated and maintained at 80 °C for 1 hour. It was then cooled to give a seed emulsion (M-4) of a high-molecular-weight compound having a molecular weight of 320,000. This seed emulsion had a solids concentration of 22.2 %, a pH of 2.5 and an average particle diameter of 0.27 µm. Sodium laurylbenzenesulfate 0.108 part), 4.0 parts of butyl Cellosolve and 358 parts of deionized water were added to 90.1 parts of the seed emulsion (M-4). The mixture was well stirred at 30 to 40 °C for 1 hour and heated to 50 °C. Styrene (80 parts) was added, and the mixture was stirred for 2 hours. The reactor was further heated to maintain its inside at 70 °C, and a mixture of 0.5 part of potassium persulfate and 50 parts of deionized water was added dropwise over 5 hours. The reactor was further heated and maintained at 80 °C for 1 hour. It was then cooled to give a seed emulsion (M-5) of a high-molecular-weight compound having a molecular weight of 580,000. The seed emulsion (M-5) had a solids concentration of 17.3 %, a pH of 2.4 and an average particle diameter of 0.75 µm. Sodium laurylbenzenesulfate (0.108 part), 3.0 parts of butyl Cellosolve and 363 parts of deionized water were added to 86.7 parts of the seed emulsion (M-5), and the mixture was well stirred. The mixture was stirred at 30 to 40 °C for 1 hour, and heated to 50 °C. Styrene (85 parts) was added and the mixture was stirred for 2 hours to permit absorption of the styrene monomer efficiently in the seed particles. The reactor was further heated to maintain its inside at 70 °C. A mixture of 0.5 part of potassium persulfate and 50 parts of deionized water was added dropwise over 5 hours. The reactor was further heated and its inside was maintained at 80 °C for 1 hour. The reactor was then cooled to give a seed emulsion (M-6) of a high-molecular-weight compound having a molecular weight of 950,000. The seed emulsion (M-6) had a solids concentration of 17.1 %, a pH of 2.5 and an average particle diameter of 2.35 µm. Sodium laurylbenzenesulfonate (0.108 part), 1.0 part of butyl Cellosolve and 420 parts of deionized water were added to 58.5 parts of the seed emulsion (M-6). The mixture was well stirred at 30 to 40 °C for 1 hour, and then heated to 50 °C. Styrene (85 parts) and 5 parts of divinylbenzene were added to the mixture, and the mixture was maintained at 50 °C for 2 hours. While maintaining the inside of the reactor at 70 °C, a mixture of 0.5 part of potassium persulfate and 50 parts of deionized water was added over 5 hours. The inside of the reactor was then heated to 80 °C, and maintained at this temperature for 1 hour. The reactor was then cooled to give an emulsion (A-3). The emulsion (A-3) is a dispersion of monodisperse gel particles having a solids concentration of 16.2 %, a pH of 2.8 and an average particle diameter of 6.80 µm. EXAMPLE 4 Sodium laurylbenzenesulfonate (0.108 part), 1.0 part of Texanol and 420 parts of deionized water were added to 58.5 parts of the seed emulsion (M-6) obtained in Example 3. The mixture was well stirred, maintained at 30 to 40 °C for 1 hour, and heated to 50 °C. A mixture of 60 parts of styrene, 25 parts of n-butyl acrylate and 5 parts of divinylbenzene was added, and the resulting mixture was maintained at 50 °C for 2 hours. The reactor was then further heated to maintain its inside at 70 °C. A mixture of 0.5 part of potassium persulfate and 50 parts of deionized water was added over 5 hours. The reactor was further heated and maintained at 80 °C for 1 hour. It was then cooled to give an emulsion (A-4). The emulsion (A-4) was a dispersion of monodisperse gel particles having a solids concentration of 16.2 %, a pH of 2.5 and an average particle diameter of 6.52 µm. COMPARATIVE EXAMPLE 1 For comparison, an emulsion (B-1) was prepared in the same way as in Example 1 except that Texanol was not used. The emulsion (B-1) had a solids concentration of 18.9 %, a pH of 2.5 and an average particle diameter of 0.58 µm. COMPARATIVE EXAMPLE 2 For comparison, an emulsion (B-2) was prepared in the same way as in Example 1 except that 10 parts, as solids of a polystyrene emulsion having a particle diameter of 0.25 µm, and a molecular weight of 3,000 was used as the seed emulsion; Texanol was not used; and that styrene was used as the monomer. The emulsion (B-2) had a solids concentration of 18.6 %, a pH of 2.4 and an average particle diameter of 0.75 µm. COMPARATIVE EXAMPLE 3 For comparison, an emulsion (B-3) was prepared in the same way as in Example 1 except that 10 parts, as solids, of polystyrene gel particles having a particle diameter of 0.25 µm was used as the seed emulsion, and Texanol was not used. The emulsion (B-3) had a solids concentration of 18.7 %, a pH of 2.6 and an average particle diameter of 0.48 µm. COMPARATIVE EXAMPLE 4 For comparison, an emulsion (B-4) was prepared in the same way as in Example 1 except that in the second step, Texanol was not used, but a mixture of 85 parts of styrene and 5 parts of divinylbenzene was added dropwise over 5 hours simultaneously with the addition of the initiator solution. The emulsion (B-4) had a solids concentration of 18.6 %, a pH of 2.4 and an average particle diameter of 0.58 µm. APPLICATION EXAMPLES 1-3 AND COMPARATIVE APPLICATION EXAMPLES 1-4 Each of the emulsions (A-1) to (A-3) and (B-1) to (B-4) obtained in the foregoing Examples and Comparative Examples was mixed with a binder and a thickener (hydroxyethyl cellulose) in the amounts indicated in Table 1. The mixture was stirred to a constant viscosity to form a paint. The paint was coated on a glass plate by a 6-mil applicator, and dried at room temperature for 1 day. The 60° and 75° glosses and water resistance of the coated film were evaluated in the initial stage and after drying and rubbing. The binder used was an emulsion having a non-volatile content of 50 % obtained by emulsion polymerization of a monomeric mixture composed mainly of methyl methacrylate and 2-ethylhexyl acrylate in a customary manner.

Claims: A method of producing an emulsion polymer which comprises adding a polymerizable unsaturated monomer to an emulsion polymer comprising a high-molecular-weight compound not containing a polyfunctional cross-linkable monomer or a chain transfer agent and having a weight average molecular weight of 20,000 to 2,000,000 as a seed polymer, the amount of the unsaturated monomer being 1.5 to 9.5 times the total volume of the solids in the emulsion polymer, and thereafter, polymerizing the monomer in the presence of a film-forming aid which is at least one compound selected from ethylene glycol; ether, ester or etherester derivatives of ethylene glycol; glycols having 3 to 8 carbon atoms; alkyl-substituted C₃-C₈ glycols; ether, ester or etherester derivatives of said glycols; diethylene glycol; ether, ester or etherester derivatives of diethylene glycol; glycerol; glycerol derivatives; aromatic alcohols; substituted aromatic alcohols; aromatic polycarboxylic acid esters; and alkyl-substituted aromatic polycarboxylic acid esters. A method according to claim 1 wherein the seed polymer is a homopolymer or copolymer of an alpha,beta-ethylenically unsaturated monomer. A method according to claim 2 wherein the ethylenically unsaturated monomer does not contain a carboxyl group. A method according to claim 1 wherein the seed polymer is a polyester. A method according to claim 1 wherein the seed polymer is a polyurethane. A method according to any one of the preceding claims wherein the emulsion polymer produced has an average particle diameter of 1.0 to 20.0 µm.

Inventors: KUWAMURA, SHINICHI, TAKARABE, KUNIHIDE
Applicants: DAINIPPON INK AND CHEMICALS, INC.
Application year: 1988
Main classification: C08F291
IPC codes: C08F2, C08F291, C08F283