Polymer particle manufacturing device

Abstract

The present invention provides a polymer particle manufacturing apparatus that can stably prepare emulsifiers and reproducibly produce polymer particles of a desired particle size. [Solution] The polymer particle manufacturing apparatus comprises a first channel for supplying a first aqueous phase, a second channel for supplying an emulsifier, a first mixer for mixing the first aqueous phase and the emulsifier to form a second aqueous phase, a third channel for supplying the second aqueous phase mixed in the first mixer, a fourth channel for supplying a monomer phase containing monomers, and a second mixer for mixing the second aqueous phase and the monomer phase to form a third aqueous phase in which the monomer phase on which the emulsifier has been adsorbed is dispersed. The length of the third channel is set to have a residence time shorter than the time during which the emulsifier becomes unstable in the second aqueous phase in the third channel.

Description

[Technical Field]

[0001] This disclosure relates to a polymer particle manufacturing apparatus for producing polymer particles by emulsion polymerization. [Background technology]

[0002] Polymer particles are widely used in industries such as automotive and electronics. In particular, when considering applications as paints, there is a need to efficiently synthesize polymer particles with a small average particle size and a uniform particle size distribution.

[0003] Emulsion polymerization is a known method for synthesizing polymer particles (see, for example, Patent Document 1). In this method, a monomer, which is the oil phase, is mixed with an emulsifier and dispersed in an aqueous phase, and a polymerization reaction of the monomer is carried out to obtain fine polymer particles. [Prior art documents] [Patent Documents]

[0004] [Patent Document 1] Patent No. 6122698 [Overview of the project] [Problems that the invention aims to solve]

[0005] However, in emulsion polymerization, emulsifiers are prepared in advance with water or other substances to the desired concentration. If the emulsifier is hydrophobic, the dispersion of the emulsifier may become uneven after concentration adjustment, making it difficult to obtain polymer particles of the desired size.

[0006] This disclosure has been made in consideration of these challenges, and aims to provide a polymer particle manufacturing apparatus that can stably prepare emulsifiers and reproducibly produce polymer particles of a desired particle size. [Means for solving the problem]

[0007] The polymer particle manufacturing apparatus according to this disclosure comprises a first channel for supplying a first aqueous phase, a second channel for supplying an emulsifier, a first mixer for mixing the first aqueous phase and the emulsifier to form a second aqueous phase, a third channel for supplying the second aqueous phase mixed in the first mixer, a fourth channel for supplying a monomer phase containing monomers, and a second mixer for mixing the second aqueous phase and the monomer phase to form a third aqueous phase in which the emulsifier is adsorbed and dispersed on the monomers, wherein the channel length of the third channel is set to have a residence time shorter than the time during which the emulsifier becomes unstable in dispersion in the second aqueous phase in the third channel. [Effects of the Invention]

[0008] According to the polymer particle manufacturing apparatus described herein, polymer particles having a desired average particle size can be manufactured with high reproducibility. [Brief explanation of the drawing]

[0009] [Figure 1] This is a schematic diagram showing the configuration of the polymer particle manufacturing apparatus according to Embodiment 1. [Figure 2] This is a schematic diagram showing the configuration of the polymer particle manufacturing apparatus related to Experimental Example 1. [Figure 3] Table 1 shows the hydrophilic / hydrophobic values ​​of the emulsifier, the channel length of the third channel, the residence time, and the evaluation of the resulting polymer particles in Experimental Examples 1 to 14. [Modes for carrying out the invention]

[0010] The polymer particle manufacturing apparatus according to the first embodiment comprises a first channel for supplying a first aqueous phase, a second channel for supplying an emulsifier, a first mixer for mixing the first aqueous phase and the emulsifier to form a second aqueous phase, a third channel for supplying the second aqueous phase mixed in the first mixer, a fourth channel for supplying a monomer phase containing monomers, and a second mixer for mixing the second aqueous phase and the monomer phase to form a third aqueous phase in which the emulsifier is adsorbed and dispersed on the monomers, wherein the length of the third channel is set such that the residence time in the third channel is shorter than the time during which the emulsifier becomes unstable in dispersion in the second aqueous phase.

[0011] In the polymer particle manufacturing apparatus according to the second aspect, in the above first aspect, the channel length of the third channel may be in the range of 100 mm to 15,000 mm.

[0012] In the polymer particle manufacturing apparatus according to the third aspect, in the above first aspect, the residence time of the second aqueous phase in the third channel may be 0.1 seconds or more and 25 seconds or less.

[0013] In the polymer particle manufacturing apparatus according to the fourth aspect, in any of the above first to third aspects, the polymer particle manufacturing apparatus may further include a reaction tank that holds the third aqueous phase and polymerizes the monomer in the monomer phase adsorbed with the emulsifier to produce polymer particles.

[0014] In the polymer particle manufacturing apparatus according to the fifth aspect, in the above fourth aspect, the polymer particle manufacturing apparatus may further include a fifth channel that feeds the third aqueous phase mixed by the second mixer to the reaction tank, and a sixth channel that feeds a polymerization initiator that starts the polymerization of the monomer to the reaction tank.

[0015] In the polymer particle manufacturing apparatus according to the sixth aspect, in any of the above first to fifth aspects, the channel diameter of the third channel between the first mixer and the second mixer may be 0.1 mm to 10 mm.

[0016] In the polymer particle manufacturing apparatus according to the seventh aspect, in any of the above first to sixth aspects, when the emulsifier is a nonionic surfactant, the HLB (Hydrophile Lipophile Balance) may be 13 or more.

[0017] In the polymer particle manufacturing apparatus according to the eighth aspect, in any of the above first to sixth aspects, when the emulsifier is an ionic surfactant, the solubility parameter (hereinafter referred to as the SP value) may be 7 (cal / cm 3 ) 0.5 or more.

[0018] In the polymer particle manufacturing apparatus according to the ninth embodiment, if the emulsifier is a nonionic surfactant, the HLB (Hydrophile Lipophile Balance) may be 15 or higher.

[0019] The polymer particle manufacturing apparatus according to the tenth embodiment, in any of the first to sixth embodiments described above, when the emulsifier is an ionic surfactant, has an SP value of 9 (cal / cm²). 3 ) 0.5 That's fine too.

[0020] The polymer particle manufacturing apparatus according to the embodiments of this disclosure will be described below with reference to the attached drawings.

[0021] (Embodiment 1) Figure 1 is a schematic diagram showing the configuration of the polymer particle manufacturing apparatus 100 according to Embodiment 1. As shown in Figure 1, the polymer particle manufacturing apparatus 100 according to Embodiment 1 includes a first channel 10 for supplying a first aqueous phase, a second channel 20 for supplying an emulsifier, a first mixer 30 for mixing the first aqueous phase and the emulsifier to form a second aqueous phase, a third channel 40 for supplying the second aqueous phase mixed in the first mixer 30, a fourth channel 50 for supplying a monomer phase containing monomers, and a second mixer 60 for mixing the second aqueous phase and the monomer phase to form a third aqueous phase in which the emulsifier is adsorbed and dispersed on the monomers. In this polymer particle manufacturing apparatus 100, the channel length of the third channel 40 is configured such that the residence time in the third channel 40 is shorter than the time during which the emulsifier becomes unstable in the second aqueous phase. As shown in Figure 1, the polymer particle manufacturing apparatus 100 may further include a reaction tank 90. ​​In the reaction tank 90, a third aqueous phase is maintained, and polymer particles are produced by polymerizing monomers in a monomer phase in which an emulsifier is adsorbed and dispersed.

[0022] <First Water Phase> The first aqueous phase is, for example, water. The water may be, for example, distilled water, deionized water, or other pure water, or ultrapure water. As shown in Experimental Example 1 of Figure 2, the first aqueous phase may be held, for example, in a syringe, or in a water tank.

[0023] <First channel> The first channel 10 for delivering the first aqueous phase has an inner diameter in the range of, for example, 0.01 mm to 5.00 mm. It may also be in the range of 0.05 mm to 4.00 mm. As shown in Experimental Example 1 in Figure 2, the first aqueous phase may be supplied by, for example, a plunger pump.

[0024] <Emulsifier> The emulsifier may be an ionic surfactant, a nonionic surfactant, or a polymerizable emulsifier. If the emulsifier is an ionic surfactant, for example, the solubility parameter (SP value) should be 7 (cal / cm³). 3 ) 0.5 The value is ) or higher. If the emulsifier is a nonionic surfactant, for example, the HLB (Hydrophile Lipophile Balance) is 13 or higher. The SP value was calculated using Fedors' estimation formula. As for ionic surfactants, anionic emulsifiers such as sodium dodecylbenzenesulfonate, sodium lauryl sulfate, sodium alkyldiphenyl ether disulfonate, and sodium polyoxyethylene alkyl ether sulfate can be used. As for cationic emulsifiers, stearylbenzyldimethylammonium chloride and distearylbenzyldimethylammonium chloride can be used. Examples of nonionic surfactants that can be used include polyoxyethylene alkyl ethers, polyoxyethylene alkylphenyl ethers, polyoxyalkylene polyols, and polypropylene glycol ethylene oxide adducts. Examples of polymerizable emulsifiers that can be used include sodium alkylallyl sulfosuccinate and sodium (meth)acryloyl polyoxyalkylene sulfate. These may be used individually or in combination of two or more types. As shown in Experimental Example 1 in Figure 2, the emulsifier may be held, for example, in a syringe, or in a water tank.

[0025] <Second flow path> The second channel 20 for delivering the emulsifier has an inner diameter in the range of, for example, 0.01 mm to 5.00 mm. Furthermore, it may be in the range of 0.05 mm to 4.00 mm. As shown in Experimental Example 1 of Figure 2, the emulsifier may also be delivered by a plunger pump, for example.

[0026] <First mixer> The first mixer 30 is installed at the confluence of the first flow path 10 and the second flow path 20, and mixes the first aqueous phase with the emulsifier to form the second aqueous phase. The first mixer 30 is not particularly limited, but examples include a T-shaped mixer, a Y-shaped mixer, a V-shaped mixer, a plate mixer processed into any shape, and a double-tube mixer. The inner diameter of the first mixer is, for example, in the range of 0.01 mm to 3.00 mm. Furthermore, it may be in the range of 0.05 mm to 2.50 mm.

[0027] <Third flow path> The third channel 40, which delivers the second aqueous phase mixed in the first mixer 30, has an inner diameter in the range of, for example, 0.01 mm to 5.00 mm. Furthermore, it may be in the range of 0.05 mm to 4.00 mm. The length of the third channel 40 is set so that its residence time is shorter than the time during which the emulsifier becomes unstable in the second aqueous phase. Specifically, the length of the third channel 40 is, for example, in the range of 100 mm to 15000 mm. The residence time of the second aqueous phase in the third channel is, for example, between 0.1 seconds and 25 seconds. By setting the above-mentioned channel length and residence time for the third channel, the emulsifier can be mixed with the monomer phase in a stable state in the second aqueous phase in the second mixer 60. In the second aqueous phase, which is a mixture of the first aqueous phase and the emulsifier, the emulsifier is initially dispersed in the aqueous phase. However, the state of the emulsifier alone is a high-energy, unstable state, and over time, the dispersed emulsifier aggregates and coalesces, eventually separating from the aqueous phase. In the intermediate stages, for example, after 25 seconds, the mixture becomes in an unstable dispersion state, such as heterogeneous dispersion.

[0028] <Monomer> The monomers included in the monomer phase are not limited to those listed below, but since this is an O / W emulsion type emulsion polymerization, the monomers are insoluble or sparingly soluble in water. For example, they may be styrene-based monomers including derivatives of styrene and methylstyrene, acrylic acid derivatives, acrylamide derivatives, methacrylic acid derivatives, methacrylic acid esters, or methacrylamide derivatives. In addition, other monomers suitable for emulsion polymerization, such as phenylene, thiophene, fluorene, alkyl, sulfone, ether, and fluoride, can also be used. These monomers may be used individually or in combination of two or more. As shown in Experimental Example 1 of Figure 2, the monomer phase may be held, for example, in a syringe, or in a water tank.

[0029] <Fourth channel> The fourth channel 50, which delivers the monomer phase containing the monomer, has an inner diameter in the range of, for example, 0.01 mm to 5.00 mm. Furthermore, it may be in the range of 0.05 mm to 4.00 mm. As shown in Experimental Example 1 in Figure 2, the monomer phase may also be delivered by a plunger pump, for example.

[0030] <Second mixer> The second mixer 60 is located at the confluence of the third channel 40 and the fourth channel 50, and mixes the second aqueous phase with the monomer phase to form a third aqueous phase in which the emulsifier is adsorbed and dispersed on the monomer.

[0031] <Fifth channel> The fifth channel 70, which delivers the third aqueous phase mixed in the second mixer 60 to the reaction vessel 90, has an inner diameter in the range of, for example, 0.01 mm to 5.00 mm. Furthermore, it may be in the range of 0.05 mm to 4.00 mm.

[0032] <Polymerization initiator> The polymerization initiator is not limited to the following, but since this is an O / W emulsion type emulsion polymerization, it must be water-soluble. For example, when using styrene-based monomers, peroxides such as ammonium persulfate, potassium persulfate, and sodium persulfate can be used. Water-soluble organic peroxides, water-soluble azo compounds, redox initiators, and persulfates can also be used. These may be used individually or in combination of two or more. The polymerization initiator may also be supplied, for example, as an aqueous solution. As shown in Experimental Example 1 of Figure 2, the polymerization initiator may be held, for example, in a syringe, or in a water tank.

[0033] <Sixth channel> The sixth channel 80, which delivers the polymerization initiator to the polymerization tank to start the polymerization of monomers, has an inner diameter in the range of, for example, 0.01 mm to 5.00 mm. Furthermore, it may be in the range of 0.05 mm to 4.00 mm. As shown in Experimental Example 1 in Figure 2, the polymerization initiator may also be delivered by a plunger pump, for example.

[0034] <Reaction vessel> A reaction vessel 90 for holding a third aqueous phase may be provided. In the reaction vessel 90, the third aqueous phase is held, and polymer is produced by polymerizing the monomer phase on which the emulsifier is adsorbed and dispersed. The reaction vessel 90 only needs to be capable of holding a predetermined amount of the third aqueous phase and producing polymer particles by emulsion polymerization. The reaction vessel 90 may be stirred and mixed as appropriate. Temperature control may also be performed.

[0035] By using a reaction vessel 90 with a predetermined capacity instead of a flow channel, the problem of needing a flow channel with a long length for long-duration polymerization reactions can be solved. In other words, the reaction vessel 90 can accommodate long-duration polymerization reactions. For example, if the flow channel length is 10,000 mm (10 m) and the residence time is 16 seconds, and the polymerization reaction time is 30 minutes, then a flow channel with a length of 1,125,000 mm (1,125 m), exceeding 1 km, would be required to carry out the polymerization reaction in the flow channel. Furthermore, if the polymerization reaction time is 2 hours, then a flow channel with a length of 4,500,000 mm (4,500 m: 4.5 km) would be required to carry out the polymerization reaction in the flow channel. In contrast, with a reaction vessel 90, it is sufficient to prepare a reaction vessel 90 with a capacity that can hold the third aqueous phase. Note that the reaction vessel 90 can be provided at will.

[0036] According to the polymer particle manufacturing apparatus of Embodiment 1, polymer particles having a desired average particle size can be manufactured with high reproducibility.

[0037] (Regarding Experimental Examples 1-14) The following describes experimental examples 1-14 of the production of polymer particles (polystyrene).

[0038] (Experimental Example 1) Figure 2 is a schematic diagram showing the configuration of the polymer particle manufacturing apparatus 100a related to Experimental Example 1. In this experimental example 1, the raw material solution for synthesizing the polymer consisted of ultrapure water as the first raw material and sodium sulfosuccinate (Sulfurity Parameter, hereafter SP value, SP value = 9 (cal / cm)) as the second raw material, which is an ionic surfactant. 3 ) 0.5 A 40% by weight aqueous solution of emulsifier, a monomer phase containing the third raw material monomer (styrene monomer), and a polymerization initiator aqueous solution prepared by adjusting the fourth raw material ammonium persulfate to 5.1% by weight with ultrapure water were prepared separately.

[0039] Two plunger pumps, 12 and 22, were used to deliver the first and second raw materials, respectively. The flow rates of each plunger pump 12 and 22 were adjusted so that the flow rate of the mixed solution was 15 mL / min (flow rate of first raw material: flow rate of second raw material = 5.3:1). At this flow rate, the emulsifier concentration after mixing the two liquids was 6.4% by weight.

[0040] A T-shaped mixer (made of SUS316 stainless steel, with an inner diameter of 0.25 mm) was used as the mixer 30 for the first and second raw materials (hereinafter referred to as the first mixer).

[0041] A plunger pump 52 was also used for the delivery of the third raw material. The set flow rate of the plunger pump 52 was adjusted so that the flow rate of the mixed solution was 30 mL / min (flow rate of the mixture of the first and second raw materials : flow rate of the third raw material = 1:1).

[0042] A T-shaped mixer (made of SUS316 stainless steel, with an inner diameter of 0.25 mm) was also used in the mixer 60 (hereinafter referred to as the second mixer) that combined the mixture of the first and second raw materials with the third raw material. The length of the third channel 40 from the first mixer 30 to the second mixer 60 was set to 100 mm. In this case, the residence time in the third channel was 0.2 seconds.

[0043] The third aqueous phase, which was the mixture from the second mixer, was collected in reaction vessel 90 (a screw tube with a capacity of 50 mL), and stirred using a hot stirrer with the stirring bar set to 400 rpm.

[0044] A plunger pump 82 was also used for the delivery of the fourth raw material. The fourth raw material was delivered to the reaction vessel 90 at a flow rate of 1 mL / min so that the ratio of the weight of the fourth raw material to the weight of the third aqueous phase, which was the mixture recovered in the second mixer in the reaction vessel 90, was 0.023:1. After adding the polymerization initiator aqueous solution of the fourth raw material, a hot stirrer was set to raise the liquid temperature in the reaction vessel 90 to 70°C and the mixture was stirred for 2 hours to produce polymer particles made of polystyrene.

[0045] (Experimental Example 2) As an emulsifier, except for using sodium sulfosuccinate (SP value = 7 (cal / cm 3 )) 0.5 ), polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0046] (Experimental Example 3) As an emulsifier, except for using polyoxyalkylene alkyl ether (HLB 15), which is a nonionic surfactant, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0047] (Experimental Example 4) As an emulsifier, except for using polyoxyalkylene alkyl ether (HLB 13), which is a nonionic surfactant, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0048] (Experimental Example 5) Except for setting the channel length of the third channel from the first mixer to the second mixer to 1000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0049] (Experimental Example 6) Except for setting the channel length of the third channel from the first mixer to the second mixer to 10000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0050] (Experimental Example 7) Except for setting the channel length of the third channel from the first mixer to the second mixer to 15000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0051] (Experimental Example 8) As an emulsifier, except for using sodium sulfate (SP value = 8 (cal / cm 3 )) 0.5 ), polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0052] (Experimental Example 9) Except for setting the channel length of the third channel from the first mixer to the second mixer to 20,000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0053] (Experimental Example 10) Except for setting the channel length of the third channel from the first mixer to the second mixer to 20,000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 2.

[0054] (Experimental Example 11) Except for setting the channel length of the third channel from the first mixer to the second mixer to 20,000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 3.

[0055] (Experimental Example 12) Except for setting the channel length of the third channel from the first mixer to the second mixer to 20,000 mm, polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 4.

[0056] (Experimental Example 13) As an emulsifier, sodium sulfosuccinate (SP value = 5 (cal / cm³)) is an ionic surfactant. 3 ) 0.5 Except for using ), polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1.

[0057] (Experimental Example 14) Polymer particles made of polystyrene were synthesized in the same manner as in Experimental Example 1, except that polyoxyalkylene alkyl ether (HLB11), a nonionic surfactant, was used as an emulsifier.

[0058] (evaluation) The obtained polymer particles made of polystyrene were subjected to particle size distribution measurements, and the standard deviation of particle diameter and the average particle diameter were calculated to determine the coefficient of variation (CV) value (standard deviation ÷ average particle diameter). A smaller CV value indicates that the particle size distribution is concentrated in the range close to the average particle diameter. Conversely, a larger CV value indicates that the particle size distribution is spread out in a range far from the average particle diameter. A CV value of less than 20% was classified as A, 20% to less than 25% as B, 25% to less than 30% as C, and 30% or more as D.

[0059] Figure 3 is shown in Table 1, which contains the hydrophilic / hydrophobic values ​​of the emulsifier, the channel length of the third channel, the residence time, and the evaluation of the resulting polymer particles in Experimental Examples 1 to 14. As shown in Figure 3, when the length of the third channel is in the range of 100 mm to 15000 mm, and the residence time of the second aqueous phase in the third channel is 0.1 seconds or more and 25 seconds or less, and the emulsifier is a nonionic surfactant, or when the HLB (Hydrophile Lipophile Balance) is 13 or more, and the emulsifier is an ionic surfactant, the solubility parameter (hereinafter SP value) is 7 (cal / cm³). 3 ) 0.5 In the above cases, experimental examples 1 to 8, the CV value was 25% or less.

[0060] Comparing Experimental Examples 1, 5-7, and 9, the same emulsifier was used, and the length of the third channel was varied to 100 mm, 1000 mm, 10000 mm, 15000 mm, and 20000 mm, while the residence time also varied correspondingly to 0.2 seconds, 1.6 seconds, 16 seconds, 24 seconds, and 31 seconds. In this case, the CV values ​​for Experimental Example 1 (channel length 100 mm, residence time 0.2 seconds) and Experimental Example 5 (channel length 1000 mm, residence time 1.6 seconds) were approximately the same, at 16% and 17%, respectively. However, as the flow path length and residence time increase in Experimental Example 6 (flow path length 10,000 mm, residence time 16 seconds), Experimental Example 7 (flow path length 15,000 mm, residence time 24 seconds), and Experimental Example 9 (flow path length 20,000 mm, residence time 31 seconds), the CV value increases to 20%, 23%, and 27%, respectively.

[0061] Comparing Experimental Example 2 and Experimental Example 10, the same emulsifier was used, and the length of the third channel was changed to 100 mm and 20,000 mm, while the residence time also changed correspondingly to 0.2 seconds and 31 seconds. In this case, the CV value increased to 21% and 32% as the channel length and residence time increased.

[0062] Comparing Experimental Examples 1, 2, and 13, the channel length and residence time of the third channel are the same, and the solubility parameter SP value of the emulsifier is 9 (cal / cm²). 3 ) 0.5 , 7 (cal / cm 3 ) 0.5 , 5 (cal / cm 3 ) 0.5 This is how it is being changed. In this case, as the solubility parameter SP value decreases, the CV value increases to 16%, 21%, and 32%.

[0063] Comparing Experimental Examples 3, 4, and 14, the channel length and residence time of the third channel are the same, while the HLB of the emulsifier is varied to 15, 13, and 11. In this case, the CV value increases to 19%, 20%, and 35% as the HLB decreases, and increases particularly sharply around HLB 13. [Industrial applicability]

[0064] According to the polymer particle manufacturing apparatus described herein, the emulsifier can be mixed with the monomer phase in a stable state, making it possible to reproducibly manufacture polymer particles having a desired average particle size. [Explanation of symbols]

[0065] 10 First channel 12 Plunger pump 20 Second flow path 22 Plunger pump 30 First mixer 40 Third flow path 50 Fourth channel 52 Plunger pump 60 Second mixer 70 Fifth flow path 80 Sixth channel 82 Plunger pump 90 reaction vessels 100 Polymer particle manufacturing equipment

Claims

1. A first channel for supplying the first aqueous phase, A second channel for delivering the emulsifier, A first mixer mixes the first aqueous phase and the emulsifier to form a second aqueous phase, A third channel for supplying the second aqueous phase mixed in the first mixer, A fourth channel for delivering the monomer phase containing monomers, A second mixer mixes the second aqueous phase and the monomer phase to form a third aqueous phase in which the monomer phase, on which the emulsifier is adsorbed, is dispersed. Equipped with, A polymer particle manufacturing apparatus comprising a configuration in which the length of the third channel is set such that the residence time in the third channel is shorter than the time during which the emulsifier becomes in an unstable dispersion state in the second aqueous phase.

2. The polymer particle manufacturing apparatus according to claim 1, wherein the length of the third channel is in the range of 100 mm to 15,000 mm.

3. The polymer particle manufacturing apparatus according to claim 1, wherein the residence time of the second aqueous phase in the third channel is 0.1 seconds or more and 25 seconds or less.

4. The polymer particle manufacturing apparatus according to any one of claims 1 to 3, further comprising a reaction vessel for maintaining the third aqueous phase and polymerizing the monomer in a monomer phase in which the emulsifier is adsorbed to the monomer to produce polymer particles.

5. A fifth channel for supplying the third aqueous phase mixed in the second mixer to the reaction tank, A sixth channel for supplying a polymerization initiator to the reaction vessel to initiate polymerization of the monomer, It further possesses, The apparatus for producing polymer particles according to claim 4.

6. The polymer particle manufacturing apparatus according to any one of claims 1 to 3, wherein the diameter of the third channel between the first mixer and the second mixer is 0.1 mm to 10 mm.

7. The polymer particle manufacturing apparatus according to any one of claims 1 to 3, wherein the emulsifier is a nonionic surfactant, and the HLB (Hydrophile Lipophile Balance) is 13 or more.

8. If the emulsifier is an ionic surfactant, the solubility parameter (SP value) is 7 (cal / cm³). ３ ) ０．５ The polymer particle manufacturing apparatus according to any one of claims 1 to 3.

9. The polymer particle manufacturing apparatus according to any one of claims 1 to 3, wherein the emulsifier is a nonionic surfactant, and the HLB (Hydrophile Lipophile Balance) is 15 or more.

10. If the emulsifier is an ionic surfactant, the SP value is 9 (cal / cm²). ３ ) ０．５ The polymer particle manufacturing apparatus according to any one of claims 1 to 3.

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