JP2746275B2 - Method for producing polymer particles - Google Patents

Description

Description: TECHNICAL FIELD The present invention relates to a method capable of producing polymer particles having a uniform particle size with good reproducibility.

TECHNICAL BACKGROUND OF THE INVENTION Polymer particles having a particle diameter in the range of 1.0 to 10 μm, a narrow particle distribution and a uniform particle diameter (spherical monodisperse polymer particles) are used for toner, toner additives, paints, adhesives, It is widely used as a fiber treatment agent, cosmetic additive, or medical diagnostic additive.

Such spherical monodisperse polymer particles, dispersion polymerization method,
It can be produced by a method such as a suspension polymerization method, an emulsion polymerization method, and a soap-free emulsion polymerization method. Among such production methods, the dispersion polymerization method has the advantage that the polymerization operation is very simple because the raw materials are charged at once and the polymerization is carried out in a homogeneous system, so that monodisperse polymer particles are produced. It is suitable as a method for

However, in the case of monodisperse polymer particles produced using the dispersion polymerization method, the particle size of the obtained polymer particles varies significantly depending on the polymerization conditions, and the polymerization conditions are set when obtaining polymer particles having a narrow particle size distribution. Very difficult. In particular, at the laboratory level, even when polymer particles having a very narrow particle size distribution can be produced, when scaled up to an industrial scale, the reaction set at the laboratory level as described above. Even if you apply the conditions as they are,
In general, it was not possible to obtain polymer particles having the same particle size distribution. And it is not clear which reaction condition among various reaction conditions is acting as a factor for determining the particle size distribution, and therefore, when the production scale is changed, preliminary polymerization is performed every time. And it is necessary to set suitable polymerization conditions again, and there is a problem that the operation is very complicated. In addition, the particle size distribution of the polymer particles polymerized under the polymerization conditions set in this manner is easy to fluctuate, and polymer particles having a different particle size distribution are often obtained at each production, which is very poor in reproducibility. There was a problem.

An object of the present invention is to solve the problems of the prior art as described above, and an object of the present invention is to provide a method capable of producing monodisperse polymer particles having a narrow particle size distribution with good reproducibility. And

SUMMARY OF THE INVENTION The method for producing polymer particles according to the present invention comprises, in the presence of a dispersant comprising a copolymer having a hydrophilic segment, a perfluoroalkyl group and a hydrophilic group, a polymerizable monomer having a Pv value of 0.005 to 0.30. Dispersion polymerization is performed under the stirring condition of Kw / m ³ .

In the present invention, the dispersion polymerization refers to polymerization in which polymer particles are synthesized using a polymerizable monomer, a solvent that dissolves the polymerizable monomer but does not dissolve the formed polymer, a dispersant, and a polymerization initiator that is soluble in the solvent. Say the way. In such dispersion polymerization, the polymerization of the polymerizable monomer proceeds due to the decomposition of the polymerization initiator, and as the polymerization proceeds and the molecular weight of the produced polymer increases, the polymer cannot be dissolved in the solvent and precipitates to form a particle nucleus. The polymerization proceeds further, and the particle nuclei grow to become polymer particles.

According to the method for producing polymer particles according to the present invention, the dispersant comprising a specific graft polymer is used, and the polymerization reaction is performed under specific stirring conditions. Polymer particles having a small particle size distribution and a narrow particle size distribution can be produced with good reproducibility.

Next, the method for producing the polymer particles of the present invention will be specifically described.

In the method for producing polymer particles of the present invention, a polymerizable monomer is subjected to dispersion polymerization under specific stirring conditions in the presence of a specific dispersant.

Dispersant used in the present invention, a hydrophilic segment,
It is a copolymer having a perfluoroalkyl group and a hydrophilic group.

Such copolymers include a monomer having a hydrophilic segment and a reactive double bond, a monomer having a perfluoroalkyl group and a reactive double bond, and a monomer having a hydrophilic group and a reactive double bond. It can be obtained by copolymerizing with a monomer having a bond.

A monomer having a hydrophilic segment and a reactive double bond used for producing such a copolymer (in the present invention, this compound is referred to as a "macromonomer") is usually 1,000 to 1,000. 100000, preferably 3000-50000
It is. Therefore, this hydrophilic segment usually contains
It contains 10-1000, preferably 30-500, hydrophilic groups.

Examples of the hydrophilic group contained in the hydrophilic segment include a hydroxyl group, a carboxyl group, an alkali metal salt thereof, an amine salt thereof, an ammonium salt thereof, a sulfone group, an amine salt thereof, an ammonium salt thereof, and a dialkylaminoalkyl (meth) group. ) Groups derived from a basic nitrogen-containing vinyl monomer represented by the following formula such as acrylate.

In the above formula, R ¹¹ represents a hydrogen atom or an alkyl group having 1 to 5 carbon atoms; R ¹² and R ¹³ each independently represent a hydrogen atom or an alkyl group having 1 to 6 carbon atoms; 6 to an integer.

As such a macromonomer, a compound containing the above-described hydrophilic group in a predetermined amount and having a reactive double bond can be used. In particular, in the present invention, it is preferable to use a compound represented by the following formula [I] as a macromonomer.

However, in the above formula [I], R ¹ each independently represents a hydrogen atom or a methyl group. It is particularly preferred that R ¹ is a methyl group. R ² and R ³ are usually each independently preferably 1 to 5 carbon atoms, in particular, R ² is preferably an alkyl group of 1 to 2, and further R ³ is an alkyl group of 1 to 2 Is preferred. In the above formula [I], m represents 5-1000 and n represents 5-1000. The ratio between m and n (m: n) is usually 1: 200 to
It is in the range of 200: 1, preferably 1:10 to 10: 1.

The above-mentioned macromonomer is prepared, for example, by first polymerizing an ethylenically unsaturated monomer in the presence of a reaction initiator to prepare an addition-type polymer having a terminal functional group capable of a condensation reaction. Can be produced by, for example, reacting an epoxy compound having a vinyl group at the terminal to introduce a vinyl group into the terminal.

Examples of the ethylenically unsaturated monomer used for producing the above-mentioned macromonomer include (meth) acrylamide and its derivatives; N-methylol (meth) acrylamide and its derivatives; diacetone (meth) acrylamide and its derivatives Hydroxyalkyl (meth) acrylates such as hydroxyethyl (meth) acrylate, hydroxypropyl (meth) acrylate, hydroxybutyl (meth) acrylate and derivatives thereof; polyhydric alcohols such as methyltriglycol (meth) acrylate ( (Meth) acrylate and derivatives thereof; vinylpyrrolidone and derivatives thereof; ethyl carbitol (meth) acrylate and derivatives thereof; 2-hydroxyethylacryloyl phosphate and derivatives thereof 2-methoxyethyl (meth) acrylate and alkoxyalkyl (meth) acrylates such as butoxyethyl (meth) acrylate.

Further, as the epoxy compound used to introduce a vinyl group at the terminal, it can be appropriately selected from compounds having an epoxy group and a vinyl group, and examples thereof are as follows. Glycidyl (meth) acrylate, 2-methylglycidyl (meth) acrylate, aryl glycidyl ether, aryl-2
-Methyl glycidyl ether.

The macromonomers as described above can be used alone or in combination.

Further, as the reaction initiator used in the above reaction, 4,4′-azobis-4-cyanovaleric acid, 2,2 ′
Customary initiators such as amidinopropanoate, potassium peroxide, ammonium peroxide, azobisisobutyronitrile, benzoyl peroxide can be used.

The content of the macromonomer in the copolymer as a dispersant is usually 1 to 30% by weight, preferably 5 to 20% by weight.

Examples of the monomer having a fluoroalkyl group and a reactive double bond used in the preparation of the copolymer used as the dispersant in the present invention (described as “fluorine-containing monomer” in the present invention) include: Trifluoroethyl (meth) acrylate, 3-[(p-octadecylfluoro) -2-oxybenzoyloxy] -2-hydroxypropyl (meth) acrylate, 3-methyl-4- [perfluoro (7-methyl-1) −
Octyl)] butyl (meth) acrylate, 2- (N, N-propylperfluorooctylsulfonamido) ethyl (meth) acrylate, 2- (perfluorooctylethyl (meth) acrylate, 3,3,3-trifluoropropylene Examples thereof include (meth) acrylate, hexafluoropropylene (meth) acrylate, and difluorohexafluorobutene-2- (meth) acrylate.

Further, as such a fluorine-containing monomer, a compound represented by the following formula can also be used.

However, in the above formula, R ¹ is a hydrogen atom, -C
Represents H ₃ , —CHF ₂ , —CH ₂ F or —CF ₃ , R ² represents a hydrogen atom or —OCOCH ₃ , and R ₃ represents a hydrogen atom or —CH ₃ .

In the present invention, as the above-mentioned fluorine-containing monomer, a monomer having a perfluoroalkyl group is preferable, and among such monomers, a compound represented by the following formula [II] is particularly preferable.

_{^{CH 2 = CR 1 COOR 2 C}} q F 2q + 1 ... [II] However, in the above formula [II], R ¹ represents a hydrogen atom or a methyl group, particularly preferably a methyl group. R ² generally represents an alkylene group having 1 to 5 carbon atoms, preferably an alkylene group having 1 to 2 carbon atoms.
Then, q in the above formula [II] is usually an integer of 1 to 8, preferably an integer of 3 to 8.

The above-mentioned fluorine-containing monomers can be used alone or in combination.

The content of the fluorine-containing monomer in the copolymer as a dispersant is usually 1 to 40% by weight, preferably 10 to 40% by weight.
30% by weight.

Further, a monomer having a hydrophilic group and a reactive double bond used for producing the copolymer which is the dispersant of the present invention includes a carboxyl group, a sulfone group and an alkali metal salt or an amine salt thereof. And compounds having a hydrophilic group such as ammonium salt. Examples of such compounds include unsaturated monocarboxylic acids such as (meth) acrylic acid, crotonic acid, isocrotonic acid, vinyl acetic acid, angelic acid, tiglic acid, allyl acid; maleic acid, fumaric acid, citraconic acid, methyl fumaric acid Unsaturated dicarboxylic acids such as acid, glutaconic acid, itaconic acid and allylmalonic acid; or monoalkyl esters of dicarboxylic acids; 2-acrylamido-2-methylpropanesulfonic acid, vinylsulfonic acid, allylsulfonic acid, 2-methylallylsulfonic acid , Styrenesulfonic acid, (meth) acrylic acid-2-sulfoethyl, (meth) acrylic acid-2-
Sulfopropyl and the like and acceptable salts of the above compounds can be mentioned.

Particularly, in the present invention, it is preferable to use methacrylic acid.

These compounds having a hydrophilic group and a reactive double bond can be used alone or in combination.

The content of the monomer having a hydrophilic group in the copolymer as a dispersant is usually 1 to 30% by weight, preferably 5 to 20% by weight.

In the present invention, the copolymer used as the dispersant may be a copolymer of the above-mentioned monomer components, and more usually a monomer having no hydrophilicity such as alkyl (meth) acrylate. It is obtained by copolymerization.

Examples of such a monomer having no hydrophilicity include aromatic vinyl monomers such as styrene, vinyltoluene, α-methylstyrene, and chlorostyrene; conjugated diene monomers such as butadiene, isoprene, and chloroprene; ) (Meth) acrylates such as methyl acrylate, ethyl (meth) acrylate, propyl (meth) acrylate, and butyl (meth) acrylate; vinyl chloride and vinylidene such as vinyl chloride, vinyl bromide, and vinylidene chloride And vinyl esters such as vinyl acetate and vinyl propionate.

These monomers can be used alone,
They can be used in combination.

The content of the monomer having no hydrophilic group in the copolymer as a dispersant is usually 10 to 80% by weight, preferably 30 to 60% by weight.

The graft copolymer used as a dispersant in the present invention, the above-described macromonomer, a fluorine-containing monomer, a monomer having a hydrophilic group, and further optionally a monomer having no hydrophilic group, using a known method It can be produced by graft polymerization. Examples of a polymerization method that can be used for the graft polymerization include an emulsion polymerization method, a suspension polymerization method, and a dispersion polymerization method.

The molecular weight of the graft copolymer produced by using such a polymerization method is usually 5,000 to 300,000, preferably 10
It is in the range of 0000 to 100,000.

Since the copolymer as described above has a hydrophilic segment and a hydrophilic group in a side chain, it is obtained by dissolving in an alcohol / cellosolve-based mixed solvent preferably used in the method for producing polymer particles of the present invention. It is a good dispersant for polymer particles.

In the method for producing polymer particles of the present invention using the above dispersant, various monomers can be used as the polymerizable monomer used for producing the polymer particles.

Examples of such polymerizable monomers include styrene,
Aromatic vinyl monomers such as vinyltoluene, α-methylstyrene, chlorostyrene; conjugated diene monomers such as butadiene, isoprene, chloroprene; methyl (meth) acrylate, ethyl (meth) acrylate, (meth) acryl (Meth) acrylic acid alkyl esters such as propyl acrylate and butyl (meth) acrylate; vinyl halides or vinylidene halides such as vinyl chloride, vinyl bromide, vinylidene chloride and vinylidene bromide; vinyl acetate and vinyl propionate Vinyl esters can be mentioned.

In particular, in the present invention, the polymerizable monomer is preferably one containing styrene as a main component. In this case, the content of styrene in the polymerizable monomer is 50 mol% or more, preferably 60 mol% or more. It is desirable.

Such a dispersion polymerization reaction is usually performed in an organic solvent. As a solvent used in this reaction, it is preferable to use a mixed solvent of an alcohol and a cellosolve-based solvent. As the alcohol that can be used in this case, it is preferable to use an alcohol having 1 to 5 carbon atoms such as methanol, ethanol, and isopropanol.As the cellosolve-based solvent, methyl cellosolve, ethyl cellosolve, isopropyl cellosolve, and It is preferable to use a cellosolve-based solvent having an alkyl group having 1 to 4 carbon atoms, such as butyl cellosolve.

Among such mixed solvents of alcohols and cellosolve solvents, a mixed solvent of methanol and methyl cellosolve, a mixed solvent of ethanol and methyl cellosolve, or a mixed solvent of isopropanol and methyl cellosolve is used. It is preferred to use.

Such a mixed solvent is generally used in an amount of 200 to 2000 parts by weight, preferably 250 to 1000 parts by weight, based on 100 parts by weight of the polymerizable monomer.

In the production method of the present invention, the average particle size of the obtained polymer particles can be controlled by changing the mixing ratio of the alcohol and the cellosolve-based solvent.

For example, FIG. 1 shows an example of the effect of the solvent composition on the particle size when styrene is used as the polymerizable monomer, methyl cellosolve is used as the cellosolve solvent, and methanol, ethanol or isopropanol is used as the alcohol. .

That is, in the example shown in FIG. 1, the ratio of the total weight of alcohol and cellosolve solvent and the weight of styrene is fixed to 335: 100, and the mixing ratio to the total weight of alcohol, cellosolve solvent and styrene is changed. As a result, the average particle diameter of the obtained polymer particles changes. The average particle size of the polymer particles is more easily controlled when ethanol is used than when isopropanol is used as the alcohol, and the average particle size is more easily controlled by using methanol. That is, as the alcohol having a smaller number of carbon atoms is used, the average particle size of the obtained polymer particles tends to be more easily controlled.

In the present invention, when the polymerizable monomer is subjected to dispersion polymerization using the above dispersant, it is necessary to perform stirring under specific conditions. That is, in the dispersion polymerization system as described above, the particle size of the obtained polymer particles varies significantly depending on the stirring conditions. Further, the stirring conditions are a main factor in determining the average particle size of the obtained polymer particles. Therefore, by specifying the stirring conditions, the particle size of the obtained polymer particles is specified, and the particle size of the obtained polymer particles is less likely to fluctuate with scale-up.

In the present invention, it is necessary to set the Pv value when stirring in the above dispersion polymerization system in the range of 0.005~0.30Kw / m ^3, further this Pv value of 0.01~0.15Kw / m ³ It is preferable to set within the range.

 Here, the Pv value is represented by the following equation.

In the above formula, ω: stirring speed T: stirring torque V: reaction capacity

FIG. 2 shows an example of the relationship between the Pv value, the average particle diameter of the obtained polymer particles, and the Cv value of the polymer particles.

By the Pv value in the range of 0.005~0.30Kw / m ³ in the production scale of 10l, it is possible to obtain polystyrene particles having an average particle size of about 1 to 10 [mu] m, yet produced in such conditions Polystyrene particles have a Cv value of 1-3
%, And the particle diameters are very uniform.

Further, it can be seen that even when the production scale is scaled up to 400 l, the average particle diameter and the Cv value of the polymer particles produced at the production scale of 10 l are equivalent.

Further, by setting the Pv value in the range of 0.01 to 0.15 Kw / m ³ , it becomes particularly easy to produce polymer particles having a uniform particle diameter.

Such a Pv value can be controlled by changing the stirring torque and the stirring speed in a predetermined reaction vessel as described above. That is, the Pv value can be controlled by changing the power for stirring, the size or shape of the blade for stirring, and further changing the stirring torque and the stirring speed.

In the dispersion polymerization performed under such stirring conditions, the temperature condition is usually set to a temperature in the range of 50 to 80 ° C.
Further, it is preferable to set the temperature within the range of 60 to 75 ° C. It is preferable that the fluctuation range of the temperature is small. Usually, the fluctuation range of the temperature is controlled within the range of 0.1 to 2 ° C, preferably 0.1 to 0.5 ° C.

Further, in the present invention, this reaction can be carried out in two stages. However, it is preferable that the temperature fluctuation width in each stage is small, and it is particularly preferable that the temperature fluctuation width is set to the above-mentioned temperature fluctuation width.

The reaction time in the present invention, the amount of the monomer used,
It can be appropriately set in consideration of reaction conditions and the like,
Usually 5 to 30 hours, preferably 7 to 24 hours.

FIG. 3 shows an example of the relationship between reaction time and temperature when the reaction is performed in two stages. In FIG. 3, “BP
"O" indicates the time when benzoyl peroxide as a reaction initiator was added, and the reaction substantially started from this time.

In FIG. 3, the reaction is carried out at 70 ° C. for 2 hours and then at 75 ° C. for 6.5 hours. An electron micrograph of the polymer particles obtained by the reaction is shown in FIG. As is clear from FIG. 4, polymer particles of the present invention can be produced by dividing the reaction into two stages and producing the polymer particles of the present invention as described above.

The polymer particles thus obtained can be obtained, for example, by removing the dispersant using a method such as filtration or centrifugation, and then drying.

Effect of the Invention According to the method for producing polymer particles according to the present invention, a dispersant composed of a specific graft polymer is used, and the polymerization reaction is performed under specific stirring conditions. The particle size distribution of the polymer particles is less likely to fluctuate, and polymer particles having a narrow particle size distribution can be produced with good reproducibility.

Next, the present invention will be described with reference to examples.
These examples should not be construed as limiting.

In the following examples and comparative examples,
The expression "parts" means "parts by weight" unless otherwise specified.

Dispersant Production Example 1 300 parts of methyl ethyl ketone and 300 parts of a monomer mixture according to the composition shown in Table 1 were placed in a four-necked flask equipped with a reflux condenser, a thermometer, a nitrogen blowing tube, and a stirring device of a mixing system. And 1.5 parts of azobisisobutyronitrile were added, and kept at 70 ± 2 ° C. for 8 hours under a nitrogen stream to complete the graft polymerization.

Next, the obtained polymer was thrown into methanol to precipitate, and dried to obtain a dispersant (A) as a powder.

Dispersant Production Examples 2 to 4 Dispersants (B), (C) and (D) were obtained in the same manner as in Dispersant Production Example 1 except that a monomer mixture having the composition shown in Table 1 was used.

Dispersant Production Comparative Example 1 300 parts of methyl ethyl ketone and 60 parts of N-methylolacrylamide macromer described in Table 1 were placed in a 14-necked flask equipped with a reflux condenser, a thermometer, a nitrogen blowing tube, and a stirring device of a mixing system. Was mixed with 60 parts of N-methylolacrylamide, and the other conditions were the same as in Production Example 1, and the dispersant (A) was produced in the same manner as in Dispersant Production Example 1.
I got

Dispersant Production Comparative Example 2 300 parts of methyl ethyl ketone, 2- (perfluorooctyl) -ethyl shown in Table 1 were placed in a 14-necked flask equipped with a reflux condenser, a thermometer, a nitrogen blowing tube and a stirring device of a mixing system. Instead of 90 parts of methacrylate, 90 parts of decyl methacrylate was blended.
And a dispersant (b) was obtained in the same manner as in Production Example 1.

Example 1 183 parts of ethanol, 152 parts of methylcellosolve, 100 parts of styrene (st) were placed in one reaction vessel equipped with a reflux condenser, a thermometer, a nitrogen inlet tube, and a stirrer equipped with a torque meter. 10 parts of the synthesized dispersant (A) was added, and the mixture was stirred under a nitrogen stream under stirring conditions of a PV value of 0.017 KW / m ² .

Next, the temperature of the reaction solution was raised to 70 ° C., and when the temperature reached 70 ° C., 3 parts of benzoyl peroxide (BPO) was added as a polymerization initiator to initiate polymerization.

After performing the reaction for 2 hours while maintaining the temperature of the reaction solution at 70 ° C., the temperature of the reaction solution was raised to 75 ° C., and the polymerization was further performed for 6 hours.

The obtained polymer dispersion was filtered through a 200-mesh wire net, but hardly any aggregate was observed.

When the obtained polymer particles were observed with a scanning electron microscope, monodispersed polystyrene particles having a CV value of 4.6% and a CV value of 2.3% were obtained.

Examples 2 to 4 In the same manner as in Example 1, except that the dispersants (B), (C) and (D) prepared in Dispersant Preparation Examples 2 to 4 were used instead of the dispersant (A). Styrene dispersion polymerization was performed.

 Table 2 shows the characteristics of the obtained polymer particles.

 All of the polymer particles were monodisperse particles.

Examples 5 to 7 Dispersion polymerization of styrene was carried out in the same manner as in Example 1 except that the stirring conditions were changed to PV values of 0.005 KW / m ² , 0.05 KW / m ² and 0.15 KW / m ² .

 Table 3 shows the properties of the obtained polymer particles.

Examples 8 to 10 In Example 1, the type and amount of the alcohol as the polymerization solvent were changed to 183 parts of ethanol and 152 parts of methylcellosolve (Example 8) 183 parts of methanol and 152 parts of methylcellosolve (Example 9) and isopropyl Dispersion polymerization of styrene was carried out in the same manner except that 248 parts of alcohol and 87 parts of methylcellosolve (Example 10) were used.

 Table 4 shows the properties of the obtained polymer particles.

Comparative Example 1 The procedure of Example 1 was repeated, except that 10 parts of the dispersant (a) synthesized in Dispersant Preparation Comparative Example 1 was used instead of the dispersant (A) synthesized in Dispersant Preparation Example 1. Styrene dispersion polymerization was performed.

The average particle size of the obtained polymer particles is 5.5 microns and CV
A value of 6% with a wide particle size distribution was obtained.

Comparative Example 2 Styrene was prepared in the same manner as in Example 1 except that the dispersant (A) synthesized in Dispersant Preparation Example 1 was replaced by 10 parts of the dispersant (B) synthesized in Dispersant Preparation Example 2. Was subjected to dispersion polymerization.

The average particle size of the obtained polymer particles was 4.6 microns, and a CV value of 7% and a wide particle size distribution were obtained.

Comparative Example 3 In Example 1, the PV value of 0.018 KW / m ² , which was the stirring condition, was used.
Was subjected to dispersion polymerization of styrene under the same stirring conditions except that the PV value was changed to 0.7 KW / m ² .

The average particle size of the obtained polymer particles was 9 μm, and a CV value of 11% and a particle having a considerably wide particle size distribution were obtained.

Comparative Example 6 In Example 1, the PV value of 0.018 KW / m ² which was the stirring condition was used.
Was subjected to dispersion polymerization of styrene under the same stirring conditions except that the PV value was changed to 0.002 KW / m ² .

The average particle size of the obtained polymer particles is 3.7 μm and the CV value is 3.5%
And a slightly wider particle size distribution was obtained.

[Brief description of the drawings]

FIG. 1 is a graph showing an example of the effect of the composition of the solvent on the particle size. FIG. 2 is a graph showing an example of the relationship between the Pv value and the average particle size and Cv value of the obtained polymer particles. FIG. 3 is a graph showing an example of the relationship between the reaction time and the temperature. FIG. 4 is an example of an electron micrograph showing the particle structure of the polymer particles obtained by the method of the present invention.

Claims (5)

(57) [Claims] 1. A polymerizable monomer is dispersed under stirring conditions having a Pv value of 0.005 to 0.30 Kw / m ³ in the presence of a dispersant comprising a copolymer having a hydrophilic segment, a perfluoroalkyl group and a hydrophilic group. A method for producing polymer particles, comprising polymerizing. 2. The method for producing polymer particles according to claim 1, wherein the main component of the polymerizable monomer is styrene. 3. A dispersant comprising (meth) acrylic acid alkyl ester, (meth) acrylic acid, a macromonomer represented by the following formula [I], and a fluorine-containing monomer represented by the following formula [II]: 2. The method for producing polymer particles according to claim 1, wherein the method is a graft copolymer; (However, in the above formula [I], R ¹ independently represents a hydrogen atom or a methyl group, R ² and R ³ each independently represent an alkylene group having 1 to 5 carbon atoms, and m represents 5 to 5 carbon atoms. 1000, n is ^{_{5~1000), CH 2 = CR 1}} COOR 2 C q F 2q + 1 ... [II] ( where in the formula [II], R ¹ represents a hydrogen atom or a methyl radical, R ² represents an alkylene group having 1 to 5 carbon atoms, and q represents an integer of 1 to 8). 4. The method according to claim 1, wherein the dispersion polymerization is carried out in a mixed solvent of an alcohol and a cellosolve solvent.
The method for producing polymer particles according to the above item. 5. The method according to claim 4, wherein the dispersion polymerization is carried out at a temperature in the range of 50 to 80 ° C.