KR101637063B1 - Resin powders and method for preparing them - Google Patents

Abstract

The present invention relates to a resin powder and a method for producing the same, and it is possible to manufacture a resin powder having excellent heat stability and solving various problems in the prior art without significantly changing the conventional manner of use.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to resin powders,

More particularly, the present invention relates to a resin powder excellent in thermal stability without requiring a step of removing residual metal ions after salt aggregation of a polymer latex and a method for producing the resin powder.

Emulsion Polymerization Polymer latex agglomeration is a chemical method in which each latex particle stabilized by an emulsifier is chemically or strongly broken by mechanical force by breaking the stability of the latex by mechanical force. It is chemically The stability is broken by the phosphorus method, or the repulsive force between the emulsifier is overcome by the strong shearing force, and the latex particles and the particles are aggregated, and the stability is broken by the mechanical force.

And a rapid coagulation method. The above method is to inject an aqueous solution of a flocculant such as an inorganic salt and an acid in an excessive amount to break the stability of the emulsifier and rapidly coagulate the polymer in the latex.

In this case, since the slurry in which the polymer particles are aggregated is physically weakly bonded, it can be easily broken by an external shear force such as an agitator. Therefore, the agglomerated slurry is aged in order to increase the binding force by mutual penetration between chains. It is then obtained in the form of a powder by dewatering and drying.

Another example is a gas-phase spray method in which a resin of a polymer latex having a high solid content is sprayed on a surface of an excess coagulant using an atomizer, and recovered as a spherical powder. Since rapid rapid aggregation occurs at the moment of contact with the flocculant, high apparent specific gravity and recovery of the spherical powder required in the slow flocculation process are possible.

However, since an excessive amount of coagulant is used to prevent unreacted reaction, excessive generation of wastewater can not be prevented, clogging of the atomizer frequently occurs, and the process stability may be deteriorated.

Another example is a shear coagulation method in which a shear force is applied with a strong mechanical force to form a slurry in which latex particles and latex particles are aggregated. That is, a polymer latex slurry can be prepared by applying a shear stress by high-speed rotation of 4,000 rpm or more under the condition that the coagulant is not used.

However, the emulsion polymerized latex has disadvantages in that it causes thermal stability and adverse effect on the color due to the residual emulsifier in the powder recovered from the polymer latex.

There are other methods in which the particle size of the powder is controlled and the apparent specific gravity is improved in the presence of an organic solvent. In this case, however, an excessive amount of organic solvent must be used.

On the other hand, in the conventional agglomeration and aging separation type agglomeration process, the pH control step is performed in the aging step or the slurry storing step because the agglomeration ability due to the reaction of the agglomerating agent and the neutralizing agent is considered when the agglomerating agent is added to the agglomeration step.

Accordingly, it is an object of the present invention to provide an efficient method of manufacturing a resin powder and an integrated reactor to be used therein, which can solve various problems of the prior art without significantly changing the conventional method of use.

The present invention also provides a resin powder obtained by using an acid flocculant even under the condition of use of a salt flocculant, which has been improved in thermal stability.

According to the present invention,

Characterized in that the polymer latex is neutralized during salt agglomeration and agglomeration using an integrated reactor for agglomeration and aging in the production of a resin powder by agglomeration, aging, dehydration and drying process from polymer latex. ≪ / RTI >

According to the present invention, there is provided an integrated type reactor for agglomeration and aging used in the above-described method, comprising: a hollow reaction tube through which a latex passes; at least one barrel pin protruding inward from the inner wall of the reaction tube; At least one stirrer protruding toward the inner wall of the reaction tube from an outer surface of the rotating shaft, the rotating shaft extending along the central axis of the reaction tube,

A polymer latex injection line, a coagulant injection line and a steam injection line are provided on the reactor inlet side, and a neutralizing agent injection line is provided at the inlet side of the reactor, thereby providing an integrated reactor for agglomeration and aging.

Further, according to the present invention,

A resin powder obtained by the above-described method, wherein the yellowing index (b value) is 10.0 or less and the thermal stability is improved.

Hereinafter, the present invention will be described in detail.

In the present invention, since the viscosity of the slurry is high and the agglomeration time is very short, it is possible to control the viscosity of the slurry without decreasing the coagulation property when the neutralizing agent is added after the completion of the agglomeration. In addition, the slurry clustering in the form of agglomerates is crushed and the neutralization agent can be injected into the slurry particles, thereby improving the thermal stability.

Therefore, it is possible to provide a technical feature to exhibit the advantage of reacting with the residual metal ion without decreasing the cohesive strength to improve the thermal stability.

The salt flocculant of the present invention can be, for example, sulfate or chloride salt such as magnesium sulfate, calcium sulfate, aluminum sulfate, magnesium chloride, calcium chloride, aluminum chloride and the like, and salt flocculant combined with metal ion.

The amount of the salt flocculant may be an amount not less than a theoretical value required for flocculation, and may be, for example, 0.5 to 5 parts by weight, or 0.5 to 3 parts by weight based on 100 parts by weight of the polymer latex. The polymer latex can be effectively agglomerated within the above-mentioned range. Since the total amount of the produced material is determined by the encounter of the emulsifier and the flocculant, the effect is not exerted to a large extent.

The neutralizing agent is not particularly limited as long as it is a hydroxy group-containing basic substance, and specific examples thereof include KOH and NaOH.

The amount of the neutralizing agent may be such that the pH of the slurry produced in the aggregation reaction is maintained at 9 or more. This is because the emulsifier used in the production of the latex reacts with the flocculant to form a reaction product. When the product is left in the product, the thermal stability of the product is lowered and it is one of the main causes of changing the color. The product is reacted with the added neutralizing agent and reduced to the original emulsifier form, which can be easily removed in the washing process, thereby improving the quality of the final product. The neutralizing agent may be continuously introduced or placed in a batch.

The polymer latex is, for example, an emulsion polymer latex having a solid content of 10 to 90% by weight or 25 to 60% by weight, and includes a graft copolymer comprising a vinyl cyan compound-conjugated dienic compound-aromatic vinyl compound .

The graft copolymer is prepared by polymerizing a monomer mixture of an aromatic vinyl compound and a vinyl cyan compound with a conjugated diene compound.

The conjugated diene compound may be at least one selected from the group consisting of butadiene rubber (BR), ethylene-propylene-diene monomer rubber (EPDM), ethylene propylene rubber (EPR), halobutyl rubber, butyl rubber, styrene- Rubber (SBR).

In addition, the vinyl cyan compound is selected from the group consisting of acrylonitrile, methacrylonitrile, ethacrylonitrile, and derivatives thereof.

The aromatic vinyl compound is selected from the group consisting of styrene, alphamethylstyrene, alphaethylstyrene, para-methylstyrene, vinyltoluene, and derivatives thereof.

The graft copolymer may include 40 to 85% by weight of butadiene, 5 to 50% by weight of acrylonitrile, and 10 to 55% by weight of styrene .

The polymer latex is not limited to the graft copolymer composed of the vinyl cyan compound-conjugated dienic compound-aromatic vinyl compound described above, and other polymer latex including an emulsifier and maintaining its stability may be used.

Examples of the other polymer latex include a styrene polymer, a butadiene polymer, a styrene-butadiene copolymer, an alkyl acrylate polymer, an alkyl methacrylate polymer, an alkyl acrylate-acrylonitrile copolymer, an acrylonitrile-butadiene copolymer, Styrene copolymers, acrylonitrile-alkyl acrylate-styrene copolymers, alkyl methacrylate-butadiene-styrene copolymers, and alkyl acrylate-alkyl methacrylate copolymers.

When the solid content of the polymer latex used is higher than the solid content of the polymer slurry to be produced, the polymer latex slurry may be selectively added to the polymer latex in order to control the solid content. Liquid water may be added. At this time, the amount of water added may be selected so as to have an appropriate solid content within a range of 5 to 500 parts by weight based on 100 parts by weight of the polymer latex.

The above-mentioned polymer latex, coagulant, direct steam, and, if necessary, liquid water can be added to the agglomerating and aging integrated reactor to perform agglomeration and aging.

The aggregation and aging conditions may be, for example, from 60 to 100 ° C. or from 60 to 80 ° C. When the integral reactor having the structure of FIG. 1 is used within the above range, the polymer latex, the flocculant, The agglomeration reaction occurs in the second half of the reactor, and agglomeration and aging can proceed simultaneously in substantially the same reactor.

In addition, in the present invention, a polymer slurry having a high solid content can be produced through agglomeration and aging in a short residence time without aging at a high temperature. Due to such agglomeration characteristics, the powder obtained through dehydration and drying has a high apparent specific gravity, and the content of fine particles is very small.

The residence time may be 0.5 to 30 minutes, 0.5 to 10 minutes, or 0.5 to 5 minutes. This means that conventional agglomeration and aging processes are separately carried out to produce a slurry having excellent powder characteristics even with a very short residence time, unlike the need for a long residence time of about 30 minutes to 1 hour. During the residence time, the agglomeration period is completed within a few seconds to one minute, and aging proceeds as soon as the agglomeration is finished for the time, and the polymer slurry continues to be discharged until the polymer slurry is discharged to the outside.

The solid content of the resulting polymer latex slurry of the present invention varies depending on the solid content of the polymer latex, but may be 25 to 60 wt%, or 35 to 50 wt%. If the amount is less than 25% by weight, the flowability of the slurry may be too high to secure the retention time of the slurry. When the amount exceeds 60% by weight, the feeding power of the slurry may be lowered.

If necessary, a slurry having a high viscosity can be prepared by including water in a liquid state. The mechanical strength of the agitator can be used to adjust the water content, and the powder having a low water content, for example, may be prepared. The final polymer latex slurry powder may have an apparent specific gravity within a water content of 30% by weight.

The agglomerated and aged integrated reactors used in the above method may be, for example, those having the structure shown in Fig.

That is, a hollow reaction tube 100 through which the latex passes and at least one barrel fin 140a and 140b protruding from the inner wall of the reaction tube toward the inner side of the reaction tube, And at least one stirrer 150 protruding from the outer surface of the rotating shaft toward the inner wall of the reaction tube. The polymer latex injection line 110, the flocculant injection line 120, And a steam input line 130. The reactor may be provided with a neutralizing agent input line 160 spaced apart from the reactor inlet.

In the integrated reactor 100, the ratio of the length (D) to the length (L) is preferably 5 to 20 times in view of simultaneous agglomeration and aging, and is preferable in terms of grain size control through pulverization. In addition, water consumption is minimized and direct steam is used to induce condensation of steam to efficiently supply heat.

The material of the reactor 100 may be, for example, SUS, Inconel, Hastelloy or the like.

Here, the polymer latex injection line 110, the flocculant injection line 120, the steam injection line 130, and the neutralizer injection line 160 may be in the form of a single pipe or a double pipe.

For reference, the barrel pins 140a and 140b in the present invention refer to a barrel equipped with a pin.

Specifically, the outer portion of the reactor is provided with a fixed barrel, and the barrel is fixedly attached to the barrel with a predetermined distance ranging from 1 to 10 along the radial direction.

The length of the barrel may be in the range of 5 to 20 times the diameter. If the barrel is less than 5 times, the barrel may be too short to include the aging process due to the mechanical force. If the barrel is more than 20 times, The efficiency becomes excessively large, and the slurry discharge may be difficult.

The inside of the barrel is constituted by a shaft fixed to the motor and paddles fixed to the shaft. The paddles are positioned one by one between the pins and the paddles are fixed to two by 180 degrees. Up to six blades Can be attached.

The neutralizer injection line 160 may be disposed at a distance of 30-90% from the inlet side to the outlet side of the reactor. If the neutralizing agent input line 160 is located at a position 30% before the longitudinal direction of the reactor, it may react with the flocculant before flocculation to lower the flocculating ability, thereby causing deterioration of physical properties due to non-flocculation. However, if the neutralization agent input line 160 is located at a position 90% in the longitudinal direction of the reactor, there is no problem in terms of physical properties as a whole. However, if the neutralization agent is broken by the pin and pedal, There may be some time difference in penetration, so it is desirable to put it at 30-50% separation point.

Since the polymer slurry is continuously rotated by the polymer, the stirrer 150 can induce the polymer slurry to be well pulverized without coming into contact with the stirrer 150 and the barrel fins 140a and 140b. That is, the apparatus of the present invention can control the viscosity of the polymer slurry by the action of the barrel pin and the stirrer as well as the structure of the integrated reactor, and can make the slurry having a high viscosity and control the water content by using the mechanical force.

The barrels 140a and 140b may be selected from various types such as circular, triangular, oblique, elliptical, rhombic, and square. The agitator 150 may also be selected from a variety of types such as paddles, screws, biaxial screws and pins.

The polymer slurry in which the coagulation and aging proceeds simultaneously in the reactor 100 is transferred to the slurry storage tank. The agglomerated and aged slurry can be recovered as powder by conventional dewatering and drying processes.

According to the above-described method, the yellowing index (b value) is also 10.0 or less, and the thermal stability improves to the thermal stability superior to that of the acid flocculant.

According to the method of the present invention, there is no need for a post-treatment step for removing residual metal ions resulting from the use of a conventional salt flocculant, and corrosion of a mold due to low pH during a post- In addition, it is possible to provide a resin powder which is superior in heat stability and acid flocculant when used in addition to preventing yellowing.

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic cross-sectional view of an agglomerated, agglomerated, integrated reactor used in the process of the present invention.

EXAMPLES Hereinafter, the present invention will be described in more detail with reference to the following examples. However, the scope of the present invention is not limited to the following examples.

Example  One

<Production of polymer latex>

20 parts by weight of a rubber latex having an average particle size of 0.095 占 퐉 and a gel content of 83% by weight, 35 parts by weight of a rubber latex having an average particle diameter of 0.31 占 퐉 and a gel content of 75% by weight, 120 parts by weight of ion- 3.0 parts by weight of acrylonitrile, 12 parts by weight of styrene, 0.5 part by weight of potassium rosinate, and 0.1 part by weight of tertiary dodecyl mercaptan were charged, and the reaction temperature was raised to 45 캜. When the temperature inside the reactor reached 45 ° C, 0.1 part by weight of tertiary butyl hydroperoxide, 0.25 parts by weight of an activator composed of dextrose, sodium pyrophosphate and ferrous sulfate was added to the reactor to initiate the polymerization reaction , And the reaction temperature was raised to 70 DEG C for 60 minutes. The polymerization conversion rate at this time was 73%.

In a separate mixing apparatus, 6 parts by weight of acrylonitrile, 24 parts by weight of styrene, 25 parts by weight of ion-exchanged water and 1.2 parts by weight of potassium rosinate were mixed to prepare a monomer emulsion, which was then continuously introduced into the reactor for about 2 hours Respectively. At the same time, 0.15 part by weight of tertiary butyl hydroperoxide was added continuously into the reactor for about 2 hours. At this time, the reaction temperature was maintained at 70 占 폚.

After the addition of the monomer emulsion, 0.12 parts by weight of an activator composed of dextrose, sodium pyrophosphate, and ferrous sulfate and 0.05 part by weight of tertiary butyl hydroperoxide were fed into the reactor, After the temperature was raised to 80 ° C over 1 hour, the reaction was terminated to prepare an ABS polymer latex. At this time, the polymerization conversion was 99%.

<Agglomeration and Aging>

The polymer latex (solid content 44%) was charged into the integral reactor of FIG. 1 at a flow rate of 12 kg / hr.

As shown in FIG. 1, the integral reactor (SUS material) includes a hollow reaction tube 100 through which the latex passes and at least one barrel fin 140a and 140b protruding inward from the inner wall of the reaction tube. , At least one stirrer (150) protruding from the outer surface of the rotating shaft toward the inner wall of the reaction tube, the rotating shaft extending along the central axis of the reaction tube (indicated by a dotted line) And has a structure in which a latex introduction line 110, a coagulant injection line 120 and a steam injection line 130 are provided and the neutralizing agent injection line 160 is integrally provided at a distance of 40% from the reactor inlet side.

MgSO4 was added to the flocculant input line 120 in the range of parts by weight shown in Table 1 with respect to the total polymer content of 100 parts by weight and KOH (2% aqueous solution) was added to the neutralizer input line 110 at a solid content of 100 weight parts And 0.2 part by weight were continuously added.

The solid content of the polymer latex slurry was adjusted to 30% by addition of direct steam while additionally admixing the liquid water with the flocculant in accordance with the solid content of the slurry.

The residence time of the integral reactor was 1.5 minutes on average and the agglomeration temperature was 75 ° C. The mechanical force averaged 40 N.m (measured using a torque meter) continued until the slurry was discharged outside.

The agglomerated slurry exits through the agitator 150 in the reactor and is transferred to the slurry storage tank. The agglomerated slurry was recovered as a polymer resin powder after centrifugal dehydration and fluidized bed drying process.

<Melting Kneading >

The resulting ABS polymer powder and SAN resin were mixed at a ratio of 25:75, and 1.6 parts by weight of the processing aid was mixed and pelletized at 200 ° C using a twin-screw extruder and then injected again to prepare a physical specimen.

Example  2

In Example 1, a polymer resin powder was prepared in the same manner as in Example 1, except that KOH (2% aqueous solution) was added in an amount of 0.5 part by weight based on 100 parts by weight of the solid content.

Comparative Example  One

A polymer resin powder was prepared in the same manner as in Example 1 except that KOH (2% aqueous solution) was not added in Example 1 above.

Comparative Example  2

The polymer resin powder was prepared in the same manner as in Example 1, except that KOH was not added in Example 1 and 0.8 parts by weight of sulfuric acid instead of MgSO 4 was added to 100 parts by weight of the solid content.

Comparative Example  3

Except that 0.8 parts by weight of KOH was added to 100 parts by weight of the solid content in Example 1 and 0.8 parts by weight of sulfuric acid instead of MgSO4 was added to 100 parts by weight of the solid content of the composition. .

The polymeric resin powders obtained in Examples 1-2 and 1-3 were measured for oxygen induction time (OIT) as a thermal stability, a scorch measurement value at 200 ° C in an oven, and b And the results are summarized together in Table 1 below.

[Test Example]

The properties of the ABS polymer powder (before processing) and ABS resin (after processing) prepared in Examples 1 to 2 and Comparative Examples 1 to 3 were measured by the following methods, and the results are shown in the following Table 1 Respectively.

Color (whiteness): L, a, and b values were measured using a color difference meter (Color Quest II, Hunter Lab Co.). Each of L, a, and b represents a coordinate value indicating a unique color, and L may have a value ranging from 0 to 100. The closer to 0, the blacker, and the closer to 100, the whiteer. a can have positive and negative numbers based on 0, a larger value of 0 means a red color, and a value smaller than 0 means a green color. b can have positive and negative numbers based on 0. When it is larger than 0, it means that it has a yellow color. When it is smaller than 0, it means that it has a blue color.

* Thermal stability:

1) Oxidative Induction Time (O.I.T): Measured while introducing 50 ml / min of oxygen at 190 ° C. using a differential scanning calorimeter (DSC). The oxidation induction time refers to the time taken for oxidation to take place under oxygen isothermal conditions. The larger the OIT, the better the thermal stability.

2) Scorch test: The sample was placed in an oven at 200 ° C., and the time until the vaporized gas was generated when the sample ran and the vaporized carbide was detected in the sensor was measured.

division Coagulant Type Coagulant input (phr) Slurry pH corrector Thermal stability color singularity
matters Input location
(%) Input content
(Parts by weight) O.I.T Scorch
Time
(min) b value
(+ yellow,
-blue) Example 1 MgSO4 1.0 9.2 40% 0.2 17.52 70 5.8 Example 2 1.0 10.5 40% 0.5 17.93 70 5.8 Comparative Example 1 1.0 7.7 - 0 12.83 50 7.1 Comparative Example 2 H2SO4 0.8 3.1 - 0 15.83 65 8.4 Comparative Example 3 0.8 9.1 40% 0.8 10.82 40 7.9

As shown in Table 1, in Examples 1 and 2 according to the present invention, improved results were obtained in terms of both thermal stability and yellowing index. This is because when the reactant formed by the reaction of the emulsifier contained in the latex with the coagulant reacts with the neutralizer, the potassium ion in the neutralizer changes the reactant into the emulsifier, thereby helping to wash the reactant weak in heat during the dehydration process. And reacts with the metal ions (magnesium) that have come out and is re-reacted with a substance resistant to heat, so that a resin stable to heat is produced.

On the other hand, in the case of Comparative Example 1 in which the same steps as those of Examples 1 and 2 were repeated but the pH of the slurry was not kept at 9.0 or higher, the thermal stability was poor and the content of the reactant formed by reacting with the flocculant increased, It was confirmed that discoloration of the resin was severe.

In addition, when using the acid flocculating agent, it was confirmed that the bonding between the emulsifier and the hydrogen ion is stronger than the bonding force between the emulsifier and the metal ion, and therefore, it is difficult to effectively remove the emulsifier and the metal ion is not added. In Comparative Example 2, in which an acid flocculant (sulfuric acid) was used instead of an actual salt flocculant (MgSO 4), the thermal stability was improved as compared with the use of a salt flocculant, but the yellowing of the resin became worse and the product characteristics after the treatment were poor. This is because the reactant generated by the reaction of the emulsifier and the acid in the latex is vulnerable to heat and decomposes under high processing, attacking the linkage of the polymer, and the polymer is decomposed and easily discolored and yellowed.

Furthermore, in Comparative Example 3 where an acid flocculant (sulfuric acid) was applied instead of a salt flocculant (MgSO4) and the titration pH was adjusted with a neutralizing agent, the yellowing index was lower than that of Comparative Example 2. However, But it did not improve as compared with the embodiment because it completely escaped to the outside and remained without reacting with the neutralizing agent. In addition, the thermal stability was lowered because the acidic substance was reduced by the neutralizing agent and remained in the water phase but could not be completely removed and remained so that the polymer attacked the polymer chain during the carbonization and the polymer was easily carbonized.

<Add Experimental Example  1-8>

In Experimental Examples 1 to 8, the position of the neutralizing agent input line 160 of 40% in Example 1 was changed from 0%, 10%, 20%, 30%, 50%, 70%, 85% Polymer resin powder was prepared in the same manner as in Example 1 except that the reactor was changed to a 100% point, and the properties were measured in the same manner as in Example 1. The results are summarized in Table 2 below.

division Coagulant Type Coagulant input (phr) Slurry pH corrector Thermal stability color singularity
matters Input location
(%) Input content
(Parts by weight) O.I.T Scorch
Time
(min) b value
(+ yellow,
-blue) Additional Experimental Example 1 MgSO4 1.0
- 0% 0.2 - - - Coagulation Further Experimental Example 2 1.0 - 10% 0.2 - - - Coagulation Add
Experimental Example 3 1.0 - 20% 0.2 - - - Coagulation Further Experimental Example 4 1.0 9.2 30% 0.2 17.12 65 5.9 Example 1 1.0 9.2 40% 0.2 17.52 70 5.8 Further Experimental Example 5 1.0 9.2 50% 0.2 17.83 70 5.8 Further Experimental Example 6 1.0 9.3 70% 0.2 17.30 70 5.9 Further Experimental Example 7 1.0 9.4 85% 0.2 16.84 70 5.9 Further Experimental Example 8 1.0 9.5 100%
(exit
eve) 0.2 16.92 65 6.0

As shown in Table 2, when the neutralizer injection line 160 is located at 40 to 50% from the inlet side of the integrated reactor of FIG. 1 (corresponding to Example 1, Additional Experiment 5), the yellowing of the obtained polymer resin We can identify the desirable ones when considering the index values.

100: Integrated reactor for agglomeration and aging (hollow reaction tube type)
110: Polymer latex injection line
120: Coagulant input line
130: Steam injection line
140a, b: Barrel pin (fixed barrel type)
150: stirrer (internal mounting type)
160: Neutralizer input line
D: Diameter
L: Length

Claims (12)

In preparing a resin powder by agglomeration, aging, dehydration, and drying process from an emulsion-containing polymer latex, the polymer latex is neutralized during salt agglomeration and aging by using an integrated reactor for agglomeration and aging.
The salt flocculation is carried out by adding 0.5 to 5 parts by weight of at least one flocculant selected from magnesium sulfate, calcium sulfate, aluminum sulfate, magnesium chloride, calcium chloride and aluminum chloride based on 100 parts by weight of the polymer latex, Is continuously carried out in such an amount as to maintain the pH of the slurry produced in the reactor at a pH of 9 or higher.
delete delete delete The method according to claim 1,
The polymer latex may be selected from the group consisting of styrene polymer latex, butadiene polymer latex, styrene-butadiene copolymer latex, alkyl acrylate polymer latex, alkyl methacrylate polymer latex, alkyl acrylate-acrylonitrile copolymer latex, acrylonitrile-butadiene copolymer Latex, acrylonitrile-butadiene-
Styrene copolymer latex, an alkyl acrylate-styrene copolymer latex, an acrylonitrile-alkyl acrylate-styrene copolymer latex, an alkyl methacrylate-butadiene-styrene copolymer latex, and an alkyl acrylate-alkyl methacrylate copolymer latex Characterized by
A method for producing a resin powder.
The method according to claim 1,
Wherein the solid content of the polymer latex is 10 to 90% by weight
A method for producing a resin powder.
The method according to claim 1,
Characterized in that the agglomeration and aging step is carried out at a temperature of 60 to 100 DEG C for a residence time of 0.5 to 30 minutes
A method for producing a resin powder.
The method according to claim 1,
Characterized in that the solid content of the slurry produced by said flocculation and aging step is 25 to 60% by weight
A method for producing a resin powder.
delete delete delete A resin powder obtained by the method of claim 1, wherein the yellowing index (b value) is 10.0 or less.

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