KR100751020B1 - Continuous Polymerization Process of High Impact Polystyrene Resin with High Heat Resistance and High Gloss and High Falling Dart Impact - Google Patents

Abstract

Continuous production method of high impact polystyrene resin of the present invention (1) 20-50% by weight of raw sheath polybutadiene rubber and 50-80% by weight based on the total amount of styrene-based monomers and total rubber introduced into ethylbenzene in the first reactor The rubber mixture solution consisting of a combination of two synthetic polybutadiene rubbers in which styrene butadiene copolymers were dissolved and a viscosity modifier of 200 to 400 ppm were continuously added to the rubber mixture solution to react before the phase transition. To produce a first polymer of 15-25%; (2) continuously introducing the first polymer into the second reactor and polymerizing to produce a second polymer having a solid content of 35 to 45%; (3) continuously introducing the second polymer into the third reactor and reacting to produce a third polymer having a solid content of 60 to 75%; And (4) continuously adding the third polymer to the fourth reactor and reacting to produce a fourth polymer having a solid content of 78 to 90%.

Full charged continuous stirring reactor, surface gloss, practical impact strength, heat resistance

Description

Continuous Polymerization Process of High Impact Polystyrene Resin with High Heat Resistance and High Gloss and High Falling Dart Impact}

1 is a process diagram schematically showing a continuous polymerization apparatus for producing a high impact polystyrene resin according to the present invention.

Field of invention

The present invention relates to a continuous production method of high impact polystyrene (HIPS) resin having excellent heat resistance, surface gloss and practical impact strength. More specifically, the present invention employs an appropriate amount of viscosity modifier in ethylbenzene, styrene monomer and two synthetic butadiene polymers having different characteristics, and introduces an appropriate reactor before and after phase transition, thereby providing heat resistance. It relates to a continuous production method for producing a high impact polystyrene resin excellent in properties, surface glossiness and practical impact strength.

Background of the Invention

Styrene-based resins have been produced commercially a lot of excellent transparency, thermal stability, processability. In particular, high impact polystyrene (HIPS) resins having enhanced impact resistance have been developed by introducing rubber particles into styrene resins. These HIPS resins disperse rubber having a low glass transition temperature (Tg) in monovinylidene aromatic compounds such as styrene, alpha-methyl styrene, and ring-substituted styrene, in particular polybutadiene particles, in a matrix of styrene polymers for impact resistance. It is reinforced.

In particular, in recent years, as consumer preferences for large products have increased, home appliance companies have increased the output of large products, and at the same time, measures to reduce the thickness of products have been attempted to reduce the weight and manufacturing cost of large products. In addition, the demand for products with excellent surface gloss for the beautiful appearance of the injection molded products is increasing. However, if the rubber particle size of the high impact polystyrene resin is reduced in order to reduce the thickness of the product and improve the surface glossiness, there is a problem that the practical impact strength is reduced and cracks appear in the appearance of the molded product even with a small impact. There is a disadvantage in that the stability to the heat of the molded article is reduced by the reduction. Therefore, the resin manufacturer is focusing on researching and developing a product having a high enough rubber stability and practical impact strength in the manufacture of high impact polystyrene resin to sufficiently compensate for these disadvantages.

Japanese Patent Laid-Open No. 60-217254 discloses a method of improving the practical impact strength by adding polydimethylsiloxane to a styrene resin to increase the flexibility of the resin, but still has a problem.

Another conventional technique to increase the practical impact strength is to disperse the particle size of the rubber phase, which is a dispersed phase of the high impact polystyrene (HIPS) resin, in the form of bimodal or trimodal form, and thus have different rubber particle sizes. There is a method of pre-polymerizing the impact polystyrene (HIPS) resin and mixing in the reactor after the phase transition. However, in order to make different particle diameters, not only reactors with different polymerization raw material costs are required in the previous phase transition, but also have disadvantages of complicated control for polymerization and insufficient practical impact strength, and satisfactory surface glossiness. There is a drawback that is difficult to obtain a product having.

Another conventional technique for increasing the practical impact strength is a method of increasing the binding force of the rubber phase in the dispersed phase and the polystyrene phase in the continuous phase by improving the graft ratio. However, the method of increasing the graft ratio of the rubber phase and the polystyrene phase by using the initiator has a problem that the continuous bulk polymerization is difficult due to the increased reactivity with the use of the initiator, and the appearance of the product is deteriorated.

Meanwhile, in order to obtain high impact polystyrene resin having excellent surface glossiness, low viscosity special rubber has been used. The low viscosity special rubber is a low sheath polybutadiene rubber, characterized in that the viscosity of the rubber solution prepared in 5% by weight dissolved in styrene monomer is 30 to 45 centipoise.

However, when the low viscosity special rubber is used, the graft efficiency is low, and thus the practical impact strength is low. In addition, the use of an initiator to improve the graft efficiency had a disadvantage that the appearance characteristics of the final product is lowered.

On the other hand, the conventional method of improving the heat resistance of the high-impact polystyrene resin is a method of reducing the amount of rubber to be added or reducing the amount of flow improver, such as mineral oil to be injected for the control of fluidity and the third method that can improve the heat resistance There is a method of adding a monomer. However, if the rubber content is reduced, the practical impact strength is lowered, and if the flow improver is reduced, the practical impact strength is lowered, the resin flowability is lowered, and the appearance characteristics are lowered. When the third monomer is added, manufacturing cost increases.

In order to overcome the above problems, the present inventors improved the graft ratio of the final product by using two kinds of synthetic polybutadiene polymers having different characteristics to improve surface glossiness and practical impact strength characteristics, and do not add a flow enhancer. The heat resistance is improved by the method. In addition, by adding a viscosity control agent for controlling the viscosity of the polymer in the first reactor to reduce the viscosity of the polymer in the phase inversion step was able to improve the disadvantages that occur when the flow improver is not added. In addition, by introducing the appropriate reactor in the phase before and after the phase transition, by giving the optimum reaction conditions to develop a high impact polystyrene resin excellent in both heat resistance and surface gloss and practical impact strength.

SUMMARY OF THE INVENTION An object of the present invention is to provide a continuous production method of a high impact polystyrene resin having excellent heat resistance, surface glossiness and practical impact strength by using two kinds of synthetic butadiene rubbers having different characteristics within an appropriate range.

Another object of the present invention is to provide a continuous production method of a high impact polystyrene resin excellent in heat resistance, surface glossiness and practical impact strength by adding an appropriate amount of viscosity regulator in the polymerization step before the phase transition.

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

Summary of the Invention

The present invention relates to (1) 20 to 50% by weight of raw sheath polybutadiene rubber and 50 to 80% by weight of styrene butadiene copolymer based on the amount of styrene monomer and total amount of rubber introduced into ethylbenzene in the first reactor. A rubber mixed solution composed of a synthetic polybutadiene rubber species and a viscosity modifier of 200 to 400 ppm were continuously added to the rubber mixed solution, and the first polymer having a solid content of 15 to 25% was reacted until the phase transition point. Create; (2) continuously introducing the first polymer into the second reactor and polymerizing to produce a second polymer having a solid content of 35 to 45%; (3) continuously introducing the second polymer into the third reactor and reacting to produce a third polymer having a solid content of 60 to 75%; And (4) continuously adding the third polymer to the fourth reactor and reacting to produce a fourth polymer having a solid content of 78 to 90%. will be.

Hereinafter, specific contents of the present invention will be described in detail below.

Detailed Description of the Invention

Preparation of First Polymer

In the method of manufacturing a high impact polystyrene resin according to the present invention, first, a rubber mixed solution is prepared by dissolving rubber in ethylbenzene and a styrene monomer in a dissolution tank, and then the rubber mixed solution is transferred to a full charge reactor, which is a first reactor. do. During continuous transfer of the rubber mixture solution to the first reactor, 200 to 400 ppm of a viscosity modifier (tertiary dodecyl mercaptan) is continuously supplied to the rubber mixture solution.

The rubber mixture solution is composed of 3 to 7 parts by weight of ethylbenzene, 83 to 91 parts by weight of styrene monomer, and 6 to 10 parts by weight of rubber component.

The styrene monomers include styrene, α-methyl styrene, α-ethyl styrene, p-methyl styrene, and the like.

The rubber component used in the preparation of the rubber solution is composed of a combination of two kinds of synthetic polybutadiene rubbers, and the composition ratio of each rubber is 20 to 50% by weight of the raw sheath polybutadiene rubber and the styrene butadiene copolymer It is the range of 50-80 weight%.

Low cis polybutadiene rubber, one of two synthetic polybutadiene rubbers having different characteristics of the present invention, has a viscosity of 150 to 200 centimeters of a rubber solution prepared by dissolving in a styrene monomer at 5% by weight. Styrene-Butadiene Copolymer, a poise and the other type, has a viscosity of 25-50 centipoise and a styrene content of 35-45 weight in a copolymer prepared by dissolving 5% by weight in a styrene monomer. It is characterized by the denial.

As a solvent according to the present invention, aromatic compounds such as ethyl benzene, benzene, toluene, methyl ethyl ketone, and the like may be used.

In addition, a viscosity modifier continuously supplied to the first polymerization reactor may be used α-methyl styrene dimer, mercaptan, halides, terpenes and the like. In particular, in the present invention, 200 to 400 ppm of a tertiary dodecyl mercaptan was used as a viscosity modifier for the rubber mixture solution.

The first reactor of the present invention is a full charge type in which the polymerization mixture is fed to the bottom of the reactor in a continuous flow stirred reactor (CSTR) and the reactant is discharged upwards to the reactor. The polymerization temperature is 115-135 ° C. and the polymerization proceeds for 1-2 hours. At this time, the solid content is 15 to 25% after the reaction until the phase transition phase transfer to the second polymerization reactor.

The product of the first polymerization reactor is a polystyrene polymerized in a continuous rubber phase in the dispersed phase.

Preparation of Second Polymer

The first polymer is continuously introduced into a second reactor, which is a phase transfer reactor, to prepare a second polymer having a solid content of 35 to 45%. The second reactor is a continuous flow stirred reactor (CSTR) as a phase transfer reactor.

In the second reactor, the polymerization proceeds at a polymerization temperature of 125 to 145 ° C for 1.2 to 2.2 hours, and the solid content is 35 to 45%.

An important role of the second polymerization reactor of the present invention is to disperse the rubber particles on the continuous polystyrene. The reactants of the first polymerization reactor are dispersed in a polystyrene phase on the continuous rubber, but the volume volume of the polystyrene produced by the polymerization in the second polymerization reactor is equal to the volume volume of the initially charged rubber (including polystyrene grafted to rubber). At this point, the phase transition begins and a rubber dispersed phase is formed on the polystyrene continuous phase.

The particle diameter and distribution of the rubber particles produced through the phase transition process and the occlusion of the polystyrene in the rubber particles are important factors for determining the physical properties of the high impact polystyrene resin.

Preparation of Third Polymer

The second polymer is continuously introduced into the third reactor to prepare a third polymer having a solid content of 60 to 75%.

The third reactor is a horizontal flow (Horizental Reactor) to make a flow of the flow of the reactant reacts for 0.5 to 1.5 hours at a reaction temperature of 150 to 170 ℃, the solid content is 60 to 75%.

Then, 0.1-0.3 parts by weight of silicone oil having a viscosity of 500,000 to 1,000,000 centistokes at room temperature is continuously supplied to the third reactor into the third reactor.

Preparation of the fourth polymer

The third polymer is continuously added to the fourth reactor to prepare a fourth polymer having a solid content of 78 to 90%.

The fourth reactor of the present invention is divided into four regions from the inlet to the outlet, and is a full-charged flow flow reactor capable of temperature control and easy control of reaction heat generated by polymerization.

The fourth reactor is a final reactor in the polymerization stage and reacted at a temperature of 140 to 160 ° C. for 0.5 to 1.0 hours to polymerize to a solid content of 78 to 90%.

The polymer having 78% to 90% solids content through the fourth reactor is transferred to a devolatilizer to remove unreacted monomers and solvents, thereby preparing a final high impact polystyrene resin.

The invention can be better understood by the following examples, which are intended for the purpose of illustration of the invention and are not intended to limit the scope of protection defined by the appended claims.

Example

Example 1

87.0 parts by weight of styrene monomer, 6.4 parts by weight of styrene butadiene copolymer having a viscosity of 34 centipoise, 1.6 parts by weight of low sheath polybutadiene rubber having a viscosity of 170 centipoise, and 5.0 parts by weight of ethylbenzene in a complete mixing bath Was prepared and supplied to the first reactor, where a viscosity modifier (tertiary dodecyl mercaptan) was added to the raw material solution introduced into the first reactor during continuous transfer of the mixed solution to the first reactor. Continuous feeding at ppm. The first reactor was reacted at 125 ° C. for 1.45 hours.

The reactant passed through the first reactor was reacted for 1.7 hours in a second reactor at 135 ° C. and 36 RPM, and then introduced into a third reactor.

In the third reactor, 0.2 parts by weight of silicon oil was continuously fed into the third reactor, and reacted at 160 ° C. and 15 RPM for 0.94 hours, and then the reactants were transferred to the fourth reactor. The fourth reactor was reacted by raising the temperature step by step, and the reaction temperature was reacted at 142, 143, 145, and 147 ° C for 0.78 hours. The polymers passed through the four reactors were removed by pelletization and unreacted monomers through a volatilizer to prepare a final polymer. Resin characteristic analysis and physical property analysis of the injection molded product were carried out for the final polymerized product.

The reaction conditions and the results at each step are shown in Table 1, and the physical property evaluation method is as follows.

(1) Izod impact strength was measured by ASTM D-256.

(2) Flowability: measured by ASTM D-1238.

(3) Glossiness: Measured by ASTM D-523.

(4) Heat resistance property: measured by ASTM D1525.

(5) Rubber particle size: measured by Malvern's Mastersizer S Ver 2.14.

(6) Practical impact strength: measured by CEAST DAS4WIN Extended Version.

(7) Graft rate (%): It calculated | required by the following formula.

Graft Rate (%) = 100 × {[MEK Solvent Insoluble (%)-Polybutadiene Input (%)]} / {Polybutadiene Input (%)}

Example 2

In the same manner as in Example 1, except that the rubber composition used to prepare the rubber solution was changed to 5.6 parts by weight of styrene butadiene copolymer having a viscosity of 34 centipoise and 2.4 parts by weight of low sheath polybutadiene rubber having a viscosity of 170 centipoise. Was performed.

Example 3

The rubber composition used to prepare the rubber solution is 4.0 parts by weight of styrene butadiene copolymer of viscosity 34 centipoise and 4.0 parts by weight of low sheath polybutadiene rubber of viscosity 170 centipoise. The same procedure as in Example 1 was conducted except for the change.

Comparative Example 1

Same as Example 1, except that the rubber composition ratio used to prepare the rubber solution was changed to 7.2 parts by weight of styrene butadiene copolymer having a viscosity of 34 centipoise and 0.8 parts by weight of low sheath polybutadiene rubber having a viscosity of 170 centipoise. Was performed.

Comparative Example 2

     The rubber composition used in the preparation of the rubber solution was changed to 3.2 parts by weight of styrene butadiene copolymer having a viscosity of 34 centipoise and 4.8 parts by weight of low sheath polybutadiene rubber having a viscosity of 170 centipoise, and mineral oil 1.0 as a flow improver in the third reactor. The same procedure as in Example 1 was carried out except that parts by weight were added.

Comparative Example 3

The rubber composition ratio used to prepare the rubber solution is changed to 5.6 parts by weight of styrene butadiene copolymer having a viscosity of 34 centipoise and 2.4 parts by weight of low sheath polybutadiene rubber having a viscosity of 170 centipoise, and the raw material solution introduced into the first reactor A viscosity modifier (tertiary dodecyl mercaptan) was carried out in the same manner as in Example 1 except that the rubber mixture solution was continuously supplied at 100 ppm per hour.

Comparative Example 4

The rubber composition ratio used to prepare the rubber solution is changed to 5.6 parts by weight of styrene butadiene copolymer having a viscosity of 34 centipoise and 2.4 parts by weight of low sheath polybutadiene rubber having a viscosity of 170 centipoise, A viscosity modifier (tertiary dodecyl mercaptan) was carried out in the same manner as in Example 1 except that the rubber mixture solution was continuously supplied at 500 ppm per hour.

division Example Comparative Example One 2 3 One 2 3 4 Input Styrene Monomer Content 87.0 parts by weight Input polybutadiene rubber content 8.0 parts by weight Input ethylbenzene content 5.0 parts by weight Rubber type and composition ratio Styrene Butadiene Copolymer Rubber 80 wt% 70 wt% 50 wt% 90 wt% 40 wt% 70 wt% 70 wt% Low Sheath Poly Butadiene Rubber 20 wt% 30 wt% 50 wt% 10 wt% 60 wt% 30 wt% 30 wt% First reactor Viscosity Regulator (ppm) 250 250 250 250 250 100 500 Solid content (%) 20 19.6 20.5 19.5 20.0 20.1 19.8 Reaction temperature (℃) 124 Stirring Speed (RPM) 120 Retention time (hr) 1.45 Second reactor Fluid Enhancer (MO) 0 0 0 0 1.0 wt% 0 0 Solid content (%) 40 39.6 40.1 40 39.7 40.3 39.8 Reaction temperature (℃) 135 Stirring Speed (RPM) 36 Retention time (hr) 1.7 Third reactor Solid content (%) 67.0 66.8 66.9 67.0 67.5 67.2 69.5 Reaction temperature (℃) 160 Stirring Speed (RPM) 15 Retention time (hr) 0.94 Fourth reactor Solid content (%) 82.0 81.6 82.2 82.0 81.5 81.9 81.7 Reaction temperature (℃) 1 zone / 2 zone / 3 zone / 4 zone = 142/143/145/147 Retention time (hr) 0.78 Property results Impact Strength (kgfcm / cm) 11.2 12.0 12.5 9.5 13.0 9.4 9.6 Fluidity (g / 10min, 5kg, 200 ℃) 2.9 3.0 3.0 2.9 5.5 0.9 8.0 Heat resistance (VST) (5kg, 50 ℃ / hr, ℃) 96.3 96.5 96.6 96.3 93.0 96.2 95.0 Rubber Particle Size (㎛) 0.33 0.36 0.38 0.27 0.50 0.28 0.70 Glossiness (%, 60 °) 94.0 92.0 90.0 100 70.0 83 60.0 Graft Rate (%) 205 200 203 195 180 204 160 Practical Impact Strength (J) 20.0 23.0 25.0 14.0 23.0 15.0 12.0

As shown in Examples 1 to 3 of Table 1, a low sheath polybutadiene rubber and styrene butadiene copolymer rubber having different characteristics may be mixed in an appropriate range, and a viscosity modifier may be used in an appropriate range for the first reactor. In this case, it was possible to obtain high-impact polystyrene excellent in heat resistance, surface glossiness and practical impact strength and excellent in appearance of the injection molded product. In the case of Comparative Example 1, the ratio of the input amount of styrene butadiene copolymer and the input amount of low sheath polybutadiene rubber is 90% by weight and 10% by weight, and the rubber particle size formed in the final product is too small, so that the impact strength and practical impact The strength of the final product was not satisfactory, and in Comparative Example 2, the ratio of the input amount of styrene butadiene copolymer and the input amount of low-cis polybutadiene rubber was 40% by weight and 60% by weight. The particle size was so large that the surface glossiness was not satisfactory. In addition, when 1.0 parts by weight of mineral oil was added to the third reactor as a flow improver, the heat resistance was sharply lowered. In the case of Comparative Example 3, the ratio of the input amount of styrene butadiene copolymer and the input amount of low cis polybutadiene rubber is 70% by weight and 30% by weight, and a viscosity modifier (tertiary dodecyl mercaptan) is added to the first reactor. In case of continuous injection at 100 ppm per hour, the rubber particles of the final product were so small that the impact strength and practical impact strength were lowered, and the unstable rubber particles were formed. The property dropped sharply. In the case of Comparative Example 4, the ratio of the input amount of the styrene butadiene copolymer and the input amount of the low cis polybutadiene rubber was 70% by weight and 30% by weight, and a viscosity modifier (tertiary dodecyl mercaptan) was added to the first reactor. When 500 ppm was added continuously, the molecular weight and the graft ratio of the final product were low, the impact strength and the impact strength were lowered, and the rubber particle size was increased, thereby decreasing the surface glossiness.

The present invention provides a high impact polystyrene resin having excellent heat resistance, surface gloss and practical impact strength by mixing two kinds of synthetic butadiene rubbers having different characteristics within an appropriate range and adding an appropriate amount of viscosity modifier to the polymerization step before the phase transition. The invention has the effect of providing a continuous production method.

Simple modifications and variations of the present invention can be readily used by those skilled in the art, and all such variations or modifications can be considered to be included within the scope of the present invention.

Claims (8)

(1) Synthesis of two kinds of styrene-based monomers and 20 to 50% by weight of raw sheath polybutadiene rubber and 50 to 80% by weight of styrene butadiene copolymer based on the total amount of styrene-based monomers and the total amount of rubber introduced into ethylbenzene in the first reactor. 200 to 400 ppm of a viscosity modifier is continuously added to the rubber mixture solution composed of a combination of polybutadiene rubber and the rubber mixture solution and reacted to a point before the phase change to produce a first polymer having a solid content of 15 to 25%; (2) continuously introducing the first polymer into the second reactor and polymerizing to produce a second polymer having a solid content of 35 to 45%; (3) continuously introducing the second polymer into the third reactor and reacting to produce a third polymer having a solid content of 60 to 75%; And (4) continuously adding the third polymer to the fourth reactor and reacting to produce a fourth polymer having a solid content of 78 to 90%; Continuous production method of high impact polystyrene resin, characterized in that consisting of steps. According to claim 1, wherein the low cis polybutadiene rubber (Low Cis Polybutadiene Rubber) is a rubber solution prepared by dissolving in a styrene monomer of 5% by weight has a viscosity of 150 to 200 centipoise, and the styrene-butadiene copolymer (Styrene -Butadiene Copolymer) is a continuous process for producing a high impact polystyrene resin, characterized in that the viscosity of the rubber solution prepared in 5% by weight dissolved in styrene monomer is 25 to 50 centipoise and the styrene content is 35 to 45 parts by weight in the copolymer. . The method of claim 1, wherein the viscosity modifier is a tertiary dodecyl mercaptan, characterized in that the continuous production method of high impact polystyrene resin. According to claim 1, wherein the ethyl benzene is 3 to 7 parts by weight, the styrene monomer is 83 to 91 parts by weight and the rubber component is 6 to 10 parts by weight, 500,000 to 1,000,000 centistokes of the third reactor at room temperature A continuous production method of a high impact polystyrene resin, characterized by continuously supplying 0.1 to 0.3 parts by weight of a silicone oil having a viscosity. The method of claim 1, wherein (1) in the first reactor, the reaction is carried out at 115 to 135 ° C. for 1 to 2 hours; (2) in the second reactor for 1.2 to 2.2 hours at 125 to 145 ° C; (3) reacting in the third reactor at 150 to 170 ° C. for 0.5 to 1.5 hours; And (4) reacting in the fourth reactor at 140 to 160 ° C. for 0.5 to 1.0 hour; Continuous production method of a high impact polystyrene resin, characterized in that. The reactor of claim 1, wherein the first reactor is a full charge continuous stirred tank type reactor; The second reactor is a continuous stirred tank type reactor as a phase transfer reactor; The third reactor is a horizontal reactor for producing a flow of flux flow of reactants; In addition, the fourth reactor is divided into four regions from the inlet to the outlet, and each of the high-impact polystyrene resins is a flow-flow full-charged reactor capable of temperature control and easy control of reaction heat generated by polymerization. Continuous method of preparation. The method of claim 1, further comprising removing the unreacted monomer and the solvent by adding the fourth polymer to a volatile remover. A high impact polystyrene resin prepared by the continuous production method of a high impact polystyrene resin according to claim 1 and having a surface gloss property of 88 to 100% as measured by ASTM D-523.

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