KR20070035778A - Method and apparatus for preparing of high macromolecule latex resin powder - Google Patents

Abstract

The present invention relates to a method for producing a polymer latex resin powder and apparatus thereof, and more particularly, in a method for producing a polymer latex resin powder comprising the step of agglomerating and aging a polymer latex, a part of the powder produced is recycled The present invention relates to a method for producing a polymer latex resin powder, and a device, characterized in that the step comprises the step of introducing into a flocculation tank.

In the present invention, it is possible to remove fine particles, fine particles in the powder, without increasing the amount of emulsifier or water, and also to reduce the amount of coarse particles, which have a large particle size. The present invention provides a method for producing a polymer latex resin powder and an apparatus having an effect of reducing logistics costs, such as packaging costs and transportation costs.

Polymer latex, powder, slow flocculation process, fine recycle, fine emulsification tank

Description

Method for manufacturing polymer latex resin powder and apparatus therefor {METHOD AND APPARATUS FOR PREPARING OF HIGH MACROMOLECULE LATEX RESIN POWDER}

1 is a schematic diagram of a slow flocculation process apparatus comprising a fine emulsification tank of the present invention.

2 is a schematic diagram of a conventional slow flocculation process apparatus.

* Description of Major Symbols in Drawings *

1: Latex storage tank 2: Primary coagulation tank

3: secondary flocculation tank 4: aging tank

5: Dehydrator 6: Dryer

7, 8: cyclone 9: fine emulsification tank

11: Emulsifier input line 12: Latex input line

13: Water supply line 14: 1st flocculant input line

15: Secondary flocculant input line 16: Dehydration liquid discharge line

17: Product recovery line 18: Fine recovery line

19: waste gas discharge line 20: emulsified fine input line

21: water input line for emulsion

The present invention relates to a method for producing a polymer latex resin powder, and more particularly, it is possible to remove fine particles, fine particles in the powder, without increasing the amount of emulsifier or water, etc. The present invention relates to a method for producing a polymer latex resin powder having excellent particle size distribution and improved apparent specific gravity and flowability, and a device thereof.

In a general emulsion polymerization process, a rapid coagulation process for preparing a polymer resin in latex as a powder is as follows. First, an excessive amount of an aqueous solution of a coagulant such as an inorganic salt or an acid is added to the polymer latex, thereby breaking up the electrostatic stabilization by the emulsifier to aggregate the polymer particles in the latex. The agglomeration of the polymer particles of latex is called coagulation, and the agglomeration of the polymer particles is called a slurry, and since they are physically weakly bound, they are easily crushed by an external shear force by an agitator. Break-up phenomenon.

Therefore, the first aggregated slurry is subjected to an aging process, which is a process of increasing the binding force by mutual penetration between chains by raising the temperature. The slurry having physically relatively strong bonds thus produced is finally obtained in powder form through dehydration and drying.

However, such a process breaks the stability of the latex in an instant using an excess of flocculant, so that the process of entanglement of the polymer particles occurs very quickly and disorderly. As a result, the final particles obtained by the rapid agglomeration process have a very irregular shape, which results in poor flowability and reduced apparent specific gravity. This is not only a problem due to the scattering of the powder but also a logistics cost such as packaging and transportation. There is a problem that increases.

In addition, the disordered coagulation process of the rapid coagulation process causes the particle size distribution to be very wide, which causes a lot of problems in the process. First, fine particles, which are fine particles having a particle diameter of about 75 μm or less, degrade the performance of the dehydrator and the dryer, and are easily scattered into the air, causing many problems in the transport and packaging of the powder in the process. In addition, a coarse having a particle size of about 400 μm or more has a problem of transport and storage, and has a disadvantage of incompatibility with other polymer resins.

The slow coagulation process proposed to solve this problem is a method of improving the powder characteristics of the final particles produced by controlling the aggregation rate through the divided input of the flocculant.

A conventional slow flocculation process apparatus generally used in FIG. 2 is shown. The method for producing a latex polymer resin powder through a slow flocculation process is as follows.

First, a stabilized emulsifier is introduced into the latex storage tank 1 by an emulsifier input line 11 to secure stability of the polymer latex. This is necessary to induce slow coagulation by making the coagulation process reversible. If this process is omitted, even if a small amount of coagulant is added to the primary coagulation, the coagulation occurs only partially, resulting in wider particle size distribution and lower apparent specific gravity. Next, the latex into which the emulsifier is added is introduced into the primary coagulant tank 2 together with an appropriate amount of the primary coagulant and water into the primary coagulant inlet line 14 and the water supply line 13, and stays for 1 to 5 minutes. Tea agglomerates. Here, water is added for the purpose of adjusting the solid content concentration of the primary flocculation tank. The slurry thus obtained is transferred to the secondary flocculation tank 3, the secondary flocculant is introduced into the secondary flocculant input line 15, and secondary flocculation is carried out. Stay for 90 minutes to mature. The finally obtained slurry is dehydrated in the dehydrator (5), dried in the dryer (6), and then recovered from the two cyclones (7, 8) genuine and fine.

The slow coagulation process as described above has an advantage that powder characteristics such as particle size distribution, apparent specific gravity, sphericity and flowability thereof are improved as compared with a general rapid coagulation process.

However, even in the slow flocculation process, since the particles of the slurry obtained in the primary flocculation tank are physically very weakly bound, the phenomenon of being crushed by the stirrer of the secondary flocculation tank occurs, thereby generating fine particles. In addition, if the stirring speed of the secondary flocculation tank is lowered in order to reduce this phenomenon, the slurry is agglomerated by the excess secondary flocculant introduced into the secondary flocculation tank and a course occurs. Therefore, in the existing slow flocculation process, the secondary flocculation tank must be stirred at an appropriate speed to minimize the amount of fine. However, this is not a solution that can fundamentally prevent the generation of fines.

In order to solve the problems of the prior art as described above, the present invention can not only remove fine particles, fine particles in powder without increasing the amount of emulsifier or water, but also reduce the amount of coarse particles. It is an object of the present invention to provide a method for producing a polymer latex resin powder having an excellent particle size distribution and an apparent specific gravity and flowability.

Moreover, an object of this invention is to provide the manufacturing apparatus of a polymer latex resin powder.

The above and other objects of the present invention can be achieved by the present invention described below.

In order to achieve the above object, the present invention provides a method for producing a polymer latex resin powder comprising the step of agglomerating and aging polymer latex,

It provides a method for producing a polymer latex resin powder, characterized in that the continuously made including a step of recycling the generated powder to the flocculation tank.

It is another object of the present invention to provide an apparatus for producing a polymer latex resin powder comprising a fine emulsification tank for recycling a part of powder.

Hereinafter, the present invention will be described in detail.

The manufacturing method of the polymer latex resin powder of the present invention improves the problem of the conventional slow flocculation process, and in the flocculation process of the polymer latex resin powder, primary coagulation after emulsifying the fine particles of a part of the powder produced It is a method for producing a polymer latex resin powder having a uniform particle size distribution and an improved apparent specific gravity by recirculating into a bath to serve as a seed of the aggregation process.

The manufacturing apparatus of the polymer latex resin powder of the present invention is a slow flocculation process apparatus shown in Figure 1, the latex storage tank (1) to secure the stability of the polymer latex by introducing a stabilized emulsifier into the emulsifier input line (11), In the first flocculation tank (2), in which a suitable amount of primary coagulant and water are added to the first coagulant inlet line (14) and the water supply line (13), and coagulated by primary coagulation. Secondary flocculating tank (3) for introducing and flocculating secondary flocculant into secondary flocculant inlet line (15), Aging tank (4) for aging the secondary flocculated slurry, Dehydrator for dewatering and drying the finally obtained slurry (5) and a dryer (6), water for emulsifying the separated fines in a conventional slow flocculation process apparatus consisting of two cyclones (7, 8) separating the dried powder into genuine and fine particles A fine emulsification tank 9 to which the inlet line 21 and the emulsifier input line 11 are connected, and an emulsified fine input line 20 connected to the latex input line 12 in order to input the emulsified pine into the latex are additionally installed. The device is a continuous process.

The polymer latex resin is 80 to 99 parts by weight of a monomer mixture used alone or in combination of two or more acrylic or methacrylic ester monomers having 1 or 2 carbon atoms, and 0.5 to 1.0 parts by weight of a crosslinking agent capable of crosslinking polymerization with the monomer mixture. 0 to 50 parts by weight of acrylonitrile monomer, 0 to 100 parts by weight of methacryl or acrylic ester monomer, 0 to 90 parts by weight of vinyl aromatic monomer and the monomer in the presence of 20 to 80 parts by weight of acrylic rubber latex prepared by emulsion polymerization It is possible to use a polymer latex obtained by graft polymerization by continuously adding a monomer mixture of 0 to 10 parts by weight of a crosslinking agent or a graft agent copolymerizable with the acrylic rubber latex to 20 to 80 parts by weight based on the total reactants.

In addition, the polymer latex is vinyl aromatic in the presence of 20 to 60 parts by weight of butadiene-based rubbery latex prepared by emulsion polymerization of 30 to 50 parts by weight of styrene, 50 to 70 parts by weight of butadiene and 0 to 3 parts by weight of a crosslinking agent capable of crosslinking polymerization. Alone or two of 20 to 60 parts by weight of a monomer mixture, 5 to 20 parts by weight of a vinyl cyanide monomer and an alkyl acrylate and a glycidyl acrylate having an alkyl group having 1 to 12 carbon atoms, used alone or in combination of two or more thereof. The polymer latex which graft-polymerized by continuously adding the monomer mixture which consists of 0-5 weight part of monomer mixture used by mixing to the said butadiene type rubbery latex can be used.

In order to improve the stability of the polymer latex resin, the emulsifier is introduced into the latex storage tank 1 by the emulsifier input line 11.

The emulsifier alone or sodium lauryl sulfate, sodium dioctylsulfosuccinate, sodium dodecyl benzene sulfonate or dow-fax It can mix and use 2 or more types.

The emulsifier is preferably used in 0.1 to 0.5 parts by weight based on 100 parts by weight of the polymer latex resin.

The polymer latex resin stabilized with the emulsifier is aggregated in the primary flocculation tank 2 and the secondary flocculation tank 3 by introducing the flocculant into the flocculant input lines 14 and 15.

The coagulant may be used in the same manner as the primary coagulant and the secondary coagulant, and may use water-soluble inorganic acids such as sulfuric acid, phosphoric acid and hydrochloric acid, or inorganic salts such as sulfate and calcium salts.

The input amount of the primary coagulant is different depending on the input amount of the stabilizing emulsifier, which can be adjusted according to the particle size and sphericity of the slurry that overflows in the primary coagulation tank.

The secondary flocculant is generally added in excess, and it is preferable to use 0.5 to 2.0 parts by weight based on 100 parts by weight of the polymer latex resin.

The agglomerated polymer latex resin is aged in a aging tank (4), dehydrated in a dehydration tank (5), dried in a dryer (6), and then separated into genuine and fine in two cyclones (7, 8) do.

The fine recovered in the second cyclone 8 is emulsified with water and emulsifier into a fine emulsification tank 9 to which the water input line 21 and the emulsifier input line 11 are connected, and are stirred together.

The fine powder collected and put into the emulsification tank is preferably a powder having a particle size of 75 μm or less.

The emulsifier concentration in the emulsification tank for fully emulsifying the fine in water is preferably 1 to 10%. When the concentration is less than 1%, the fine particles are not emulsified properly, so that the fine particles are agglomerated, and when the concentration exceeds 10%, there is a problem such as storage and transportation due to foam generation.

The fine is preferably added within 15% of the polymer latex resin input amount, in order to control the operating conditions of the primary coagulation tank should be appropriately adjusted. If the content is more than 15% there is a problem that the course is increased because the fine emulsification is not made completely.

The water containing the fines circulated in the fine emulsification tank is introduced into the primary coagulation tank through the emulsified fine input line 21 connected to the latex input line 12. This is to ensure the stability of the latex before the polymer latex resin is introduced into the primary flocculation tank and meets the flocculant. If the fine emulsion emulsified in water is directly introduced into the primary flocculation tank, fine and coarse occurs during the initial mixing process. There is this.

The fine particles introduced into the primary coagulation bath act as a seed during the coagulation process to produce a slurry having a denser structure, and as a result, powder having a high apparent specific gravity can be obtained.

In the flocculation tank and the aging tank, the slurry is transferred to the next step by the overflow method, and all the steps of the present invention are operated continuously.

Hereinafter, preferred examples are provided to help understanding of the present invention, but the following examples are merely to illustrate the present invention, and the scope of the present invention is not limited to the following examples.

EXAMPLE

Example 1

Preparation of Rubber Latex Resins

1) One Step Reaction-Seed Preparation

In the step of polymerizing the seed, 339.8 g of ion-exchanged water was introduced into the reactor, and the temperature was raised to 70 ° C. When the temperature of the ion-exchanged water reaches 70 ° C., 49.85 g of butyl acrylate, 0.05 g of allyl methacrylate, 0.10 g of 1,3-butanediol dimethacrylate, 16.59 g of sodium lauryl sulfate (SLS) (3 wt% solution) ) Was added at the same time. The seed was polymerized by adding 26.77 g (1 wt% solution) of potassium persulfate while maintaining the temperature in the reactor at 70 ° C.

2) Two stage reaction-core manufacture

Polymerizing the core rubber layer, 208.4 g of ion-exchanged water, 448.66 g of butyl acrylate, 0.450 g of allyl methacrylate, 0.90 g of 1,3-butanediol dimethacrylate, 74.68 g (3 wt% solution) of SLS Was mixed to prepare a preemulsion. After the stabilized pre-emulsion was prepared, the seed latex prepared in the one-step reaction was continuously added for 1 hour 30 minutes at a constant flow rate. At the same time, 149.34 g (1 wt% solution) of potassium persulfate was continuously added for 1 hour and 30 minutes to proceed with the polymerization. And the core portion was completed by aging for 1 hour at 70 ℃ reaction temperature.

3) 3-step reaction-shell preparation

In the step of polymerizing the shell portion to the core portion prepared up to step 2, first, a preemulsion of 197.5 g of ion-exchanged water, 117.75 g of methyl methacrylate, 9.2 5 g of ethyl acrylate, and 13.8 g (3 wt% solution) of SLS was prepared. It was. The pre-emulsion and 69.2 g (1 wt% solution) of potassium persulfate were continuously added to the core latex in two stages at the same time for 1 hour to allow reaction of the shell portion. Likewise, the polymerization was completed by aging for 1 hour while maintaining a constant temperature in the reactor at 70 ℃. Water was added so that the solid content concentration of the polymerized latex was 40% to complete the latex production.

Preparation of Polymer Latex Resin Powder

The prepared latex was introduced into the primary coagulation tank at a flow rate of 15000 g / hr, and as the primary coagulant, 1.5 parts by weight of 900 g of calcium chloride (CaCl ₂ ) diluted to 10% based on 100 parts by weight of the total polymer latex content was used. / hr was added and water was added to adjust the concentration of the solids in the primary coagulation tank to 16%. The residence time of the primary coagulation bath was 2 minutes, and the process temperature was kept at 42 degreeC. The first flocculated slurry was transferred to a secondary flocculation tank, and 1.0 part by weight of calcium chloride diluted to 10% was introduced at a flow rate of 600 g / hr as the secondary flocculation agent, and the residence time of the secondary flocculation tank was changed. 7 minutes and process temperature hold | maintained at 42 degreeC, and it secondary-aggregated. The aggregated slurry was aged at a residence time of 60 minutes and a process temperature of 90 ° C. in a aging tank. The aged slurry was dehydrated and dried to prepare a powder, which was separated into cyclones and product. The separated fines were fed into an emulsification tank stirred at RPM 200 with 480 g / hr of water at a flow rate of 120 g / hr, 0.2 parts by weight of sodium lauryl sulfate diluted to 10%. At this time, the emulsifier concentration in the emulsion tank was 2%. The powder properties such as apparent specific gravity and particle size distribution of the polymer latex resin powder obtained through the continuous process as described above are shown in Table 1 below.

Example 2

In the manufacturing step of the polymer latex resin powder of Example 1 was carried out in the same manner as in Example 1 except that the amount of water introduced into the emulsion tank was adjusted so that the concentration of the emulsifier in the emulsion tank is 1%.

Example 3

Except that the emulsifier was added to 0.3 parts by weight based on 100 parts by weight of the polymer latex resin in the manufacturing step of the polymer latex resin powder of Example 1 was carried out in the same manner as in Example 1.

Example 4

In the manufacturing step of the polymer latex resin powder of Example 3 was carried out in the same manner as in Example 3 except that the amount of water introduced into the emulsion tank was adjusted so that the concentration of the emulsifier in the emulsion tank is 1%.

Comparative Example 1

In the manufacturing step of the polymer latex resin powder of Example 1 was carried out in the same manner as in Example 1 except for stabilizing by directly adding the emulsifier to the latex without using an emulsification tank to recycle the fine.

Comparative Example 2

In the manufacturing step of the polymer latex resin powder of Example 3 was carried out in the same manner as in Example 3 except for stabilizing by directly adding the emulsifier to the latex without using an emulsification tank that can recycle the fine.

Example 5

Preparation of Rubber Latex Resins

In a 120 L high-pressure polymerization vessel equipped with a stirrer, 180 parts by weight of ion-exchanged water, 0.5 parts by weight of buffer solution, 0.8 parts by weight of potassium oleate as emulsifier, 0.065 parts by weight of sodium pyrophosphate, 0.0047 parts by weight of ethylenediamine tetrasodium acetate, polymerization As an initiator, 0.003 parts by weight of ferrous sulfate, 0.02 parts by weight of sodium formaldehyde sulfoxylate and 0.11 parts by weight of diisopropylbenzene hydroperoxide were added. Then, 12 parts by weight of butadiene, 36 parts by weight of styrene, and 2 parts by weight of divinylbenzene with a graft crosslinking agent were added and reacted at a reaction temperature of 35 ° C., thereby preparing a core latex.

50 parts by weight of butadiene as a monomer, 0.2 parts by weight of potassium oleate as an emulsifier, 0.02 parts by weight of sodium formaldehyde sulfoxylate as a polymerization initiator and 0.11 parts by weight of diisopropylbenzene hydroperoxide were added to the core latex, and polymerized for 10 hours. A shell having an average particle diameter of 950 mm 3 was prepared.

100 parts by weight of water, 88 parts by weight of ethylenediaminetetrasodium acetate, 0.003 parts by weight of ferrous sulfate, 0.02 parts by weight of sodium formaldehyde sulfoxylate, and 0.13 parts by weight of potassium peroxide. After the addition, 12 parts by weight of methyl methacrylate was added thereto. The mixture was heated at a temperature of 80 ° C. for 30 minutes and polymerized for 60 minutes to complete the polymerization. Water was added to the polymerized latex so that the solid content concentration was 40% to complete the latex production.

Preparation of Rubber Latex Resin Powders

The prepared latex was introduced into the primary flocculation tank at a flow rate of 15000 g / hr, and 0.4 parts by weight of 240 g of sulfuric acid (H ₂ SO ₄ ) diluted to 10% as the primary flocculant was added to 100 parts by weight of the total polymer content. / hr was added, and water was added to adjust the concentration of solids in the primary coagulation bath to 16%. The residence time of the primary coagulation tank was maintained for 2 minutes and the process temperature was 35 degreeC. The first flocculated slurry was transferred to a secondary flocculation tank, and 1.0 part by weight of sulfuric acid diluted to 10% was introduced at a flow rate of 600 g / hr as the secondary flocculant, and the residence time of the secondary flocculation tank was 7 minutes, the process temperature was maintained at 35 ℃. The aggregated slurry was aged at a residence time of 60 minutes and a process temperature of 60 ° C in a aging tank. The aged slurry was dehydrated and dried to prepare a powder, which was separated into cyclones and product. The separated fines were fed into an emulsification tank stirred at RPM 200 with 480 g / hr of water at a flow rate of 120 g / hr of 0.2 parts of Dow-fax diluted to 10%. At this time, the emulsifier concentration in the emulsion tank was 2%. Powder properties such as apparent specific gravity and particle size distribution of the polymer latex resin powder obtained through the continuous process as described above are shown in Table 2 below.

Example 6

In the manufacturing step of the polymer latex resin powder of Example 5 was carried out in the same manner as in Example 5 except that the amount of water introduced into the emulsion tank was adjusted so that the concentration of the emulsifier in the emulsion tank is 1%.

Example 7

Except that the emulsifier was added to 0.3 parts by weight based on 100 parts by weight of the polymer latex resin in the manufacturing step of the polymer latex resin powder of Example 5 was carried out in the same manner as in Example 5.

Example 8

In the manufacturing step of the polymer latex resin powder of Example 7 was carried out in the same manner as in Example 7, except that the amount of water introduced into the emulsion tank was adjusted so that the concentration of the emulsifier in the emulsion tank is 1%.

Comparative Example 3

In the manufacturing step of the polymer latex resin powder of Example 5 was carried out in the same manner as in Example 5, except that the emulsion was added directly to the latex to stabilize without using an emulsification tank that can recycle fine.

Comparative Example 4

In the manufacturing step of the polymer latex resin powder of Example 7 was carried out in the same manner as in Example 7 except that the emulsion was added directly to the latex to stabilize without using an emulsification tank that can recycle fine.

The apparent specific gravity and particle size distribution of the high molecular weight latex resin powder in Examples and Comparative Examples were measured by the following method, and the results are shown in Tables 1 and 2 below.

A) apparent specific gravity-measured according to ASTM D1985.

B) Particle size distribution—The particle size was measured using a standard network, and the content of fine fine particles having a particle diameter of 75 μm or less and large particle coarse particles of 400 μm or more was measured.

Example 1 Example 2 Comparative Example 1 Example 3 Example 4 Comparative Example 2 Emulsifier input amount (part by weight) 0.2 0.2 0.2 0.3 0.3 0.3 Emulsifier Concentration in Emulsification Tank (%) 2 One - 2 One - Apparent specific gravity (g / ml) 0.52 0.50 0.49 0.52 0.51 0.50 Fine (less than 75 μm) Content (% by weight) 0.0 0.0 6.7 0.0 0.0 4.8 Course (400㎛ or more) Content (wt%) 3.7 3.9 4.7 2.9 3.2 3.4

Example 5 Example 6 Comparative Example 3 Example 7 Example 8 Comparative Example 4 Emulsifier input amount (part by weight) 0.2 0.2 0.2 0.3 0.3 0.3 Emulsifier Concentration in Emulsification Tank (%) 2 One - 2 One - Apparent specific gravity (g / ml) 0.50 0.50 0.46 0.51 0.51 0.47 Fine (less than 75 μm) Content (% by weight) 0.0 0.0 7.4 0.0 0.0 6.9 Course (400㎛ or more) Content (wt%) 4.5 5.0 5.2 3.2 3.7 4.7

Through Tables 1 and 2, Examples 1 to 4 prepared by a continuous process of emulsifying the fine part of the powder to recycle to the primary flocculation tank using a slow flocculation process apparatus including a fine emulsification tank of the present invention And the polymer latex resin powder of Examples 5 to 8 it can be confirmed that because the recycled pine acts as a seed, the production of fine pine is completely suppressed and the production of the course is also reduced. Accordingly, the post-treatment process such as the transfer of the polymer latex resin powder and the packaging of the product is facilitated, and the scattering of fine particles is eliminated, thereby providing an advantage of improving the working environment. In addition, the apparent specific gravity of the powder was also improved because the recycled pine acts as a seed to cause the slurry to have a more dense structure, and the apparent specific gravity of the powder was also improved. It was confirmed that the characteristics of the powder were improved as the temperature increased.

In contrast, the polymer latex resin powders of Comparative Examples 1 to 2 and Comparative Examples 3 to 4 prepared using a stabilized emulsifier but not directly using a fine emulsification tank of the present invention were stabilized in the same amount as in Examples. Despite the use of the emulsifier, it was confirmed that the slurry was pulverized in the secondary agglomeration tank so that the fine powder was formed in the powder produced and the apparent specific gravity of the powder was reduced.

As described above, using a slow flocculation process apparatus including a fine emulsification tank of the present invention, a method for producing a polymer latex resin comprising a continuous process of emulsifying the fine part of the powder and recycling it to the primary flocculation tank is Fully inhibits production and reduces the formation of coarse, resulting in a particle size distribution of more than 75 μm and less than 400 μm of 95% by weight or more, and particles of 400 μm or more of less than 5% by weight of very good particle size distribution At the same time, the apparent specific gravity is very good at 0.5 g / ml or more, thereby providing a polymer latex resin powder having an effect of reducing logistics costs such as packaging costs and transportation costs.

Although described in detail above with reference to the specific embodiments of the present invention, it will be apparent to those skilled in the art that various changes and modifications can be made within the scope and spirit of the present invention, and such variations and modifications belong to the appended claims. It is also natural.

Claims (7)

In the method for producing a polymer latex resin powder comprising the step of coagulating and aging the polymer latex, A method for producing a polymer latex resin powder, comprising the steps of recycling the resulting powder to a flocculation tank. The method of claim 1, The method for producing the polymer latex resin powder Latex storage tank step to ensure the stability of the polymer latex by adding an emulsifier; A first flocculation tank and a second flocculation tank step of agglomerating the stabilized latex into a slurry; Aging tank step of the aggregated slurry; Dehydrating the aged slurry; Drying step of drying the dehydrated slurry to prepare a powder; A cyclone step of separating the prepared powder; A fine emulsification tank step for emulsifying a part of the separated powder; And Recycling a portion of the emulsified powder into a primary flocculation tank; Method for producing a polymer latex resin powder, characterized in that made continuously including. In a slow flocculation process apparatus comprising a latex storage tank, a coagulation tank, a aging tank, a dehydrator, a dryer and a cyclone, An apparatus for producing polymer latex resin powder for carrying out the method for producing a polymer latex resin according to claim 1, further comprising a fine emulsification tank for emulsifying a part of the powder to be recycled. The method of claim 3, wherein The fine emulsification tank includes a water input line 21 and an emulsifier input line 11 for supplying water and an emulsifier required for emulsification of the recycled powder, and a latex input line 12 for introducing the emulsified powder into the polymer latex. Apparatus for producing a polymer latex resin powder comprising an emulsified fine input line 20 connected to the. The method according to claim 1 or 2, Part of the recycled powder is a fine particle fine method of producing a polymer latex resin powder, characterized in that the particle size of 75 ㎛ or less. The method according to claim 1 or 2, The recycled powder is a method for producing a polymer latex resin powder, characterized in that the content of less than 15% of the input amount of the polymer latex resin. The method of claim 2, The fine emulsification tank step is a method for producing a polymer latex resin powder, characterized in that the concentration of the emulsifier in the tank 1 to 10%.

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