KR100479750B1 - method of preparing thermoplastic resin having excellent release property and antiabrasive property - Google Patents

Abstract

In the thermoplastic resin manufacturing method of the present invention, in the production of polystyrene from a styrene monomer (raw material solution) by a continuous bulk polymerization reaction in the first reactor and the second reactor, the ratio of the total input flow rate of the styrene monomer is controlled Separating into the reactor and the second reactor, it is characterized in that a predetermined amount of continuous addition of dimethylsiloxane and white oil to the second reactor. In the first reactor, a core reaction occurs in which a styrene monomer is polymerized into a polystyrene having a high molecular weight, which is a condition of a high rigid resin, and a low molecular weight polystyrene is applied to the reactants from the first reactor that is continuously moved in the second reactor. At the same time, the addition of dimethyl polysiloxane for obtaining excellent abrasion resistance of the resin molded product and petroleum-extracted hydrocarbon compound for obtaining good releasability during resin molding are continuously added while inhibiting formation and giving an additional polymerization reaction to increase the final solid content. .

Description

Method of preparing thermoplastic resin having excellent release property and wear resistance {method of preparing thermoplastic resin having excellent release property and antiabrasive property}

Field of invention

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for preparing a thermoplastic resin having excellent releasability and abrasion resistance useful for manufacturing an audio tape case, a food and beverage container, and an experimental container. More specifically, specific reaction conditions are used in the continuous bulk polymerization method. By preparing a thermoplastic resin having a solid content (polystyrene) content and a molecular weight within a certain range, the present invention relates to a manufacturing method capable of providing a thermoplastic resin having excellent wear resistance and releasability as well as greatly improved rigidity.

Background of the Invention

In general, high stiffness polystyrene is used in the manufacture of audio tapes, food and beverage containers, laboratory containers, and the like. As a conventional technique for producing such high rigid polystyrene, a number of methods for polymerizing by using a plurality of reactors, by a solution polymerization method, and putting all the raw material solutions into the first reactor are known by US and Japanese patent documents and the like.

However, the above methods can obtain high rigidity polystyrene having a high molecular weight, but there are disadvantages in that a large number of reactors not only decreases productivity but also increases the amount of defects when changing varieties. In addition, the above methods have a problem in that they are not sufficient in the anti-wear function and the releasability function because the anti-wear agent is not formulated and the strength is improved by polymerization.

As a result of the study to solve the problems of the prior art as described above, the inventors of the present invention, by using the specific input and reaction conditions in the continuous bulk polymerization method proceeded in the first and second reactors, the yellowness is good and wear resistance It has been developed a method for producing a high molecular weight polystyrene resin having excellent release properties and excellent rigidity.

One object of the present invention is to provide a method for producing a high rigid polystyrene resin having excellent release properties and wear resistance and good yellowness.

Another object of the present invention is to provide a method for producing a thermoplastic resin having physical properties suitable for use in the manufacture of audio tape cases, food and beverage containers and laboratory containers.

The above and other objects of the present invention can be achieved by the present invention described below. Hereinafter, the content of the present invention will be described in detail.

In the thermoplastic resin manufacturing method of the present invention, in the production of polystyrene from a styrene monomer (raw material solution) by a continuous bulk polymerization reaction in the first reactor and the second reactor, the ratio of the total input flow rate of the styrene monomer is controlled Separating into the reactor and the second reactor, it is characterized in that a predetermined amount of continuous addition of dimethylsiloxane and white oil to the second reactor.

The first reactor undergoes a core reaction of polymerizing styrene monomer into polystyrene having a high molecular weight, which is a condition of high rigidity resin, as the main reactor, and in the second reactor, low molecular weight polystyrene is generated for reactants from the first reactor that is continuously moved. At the same time as suppression, additional polymerization reaction is given to increase the ratio of the final solid content, and dimethyl polysiloxane for obtaining excellent wear resistance of the resin molded product and petroleum-extracted hydrocarbon compound for obtaining good release property during resin molding are continuously added.

The thermoplastic resin production method of the present invention is characterized by satisfying the following conditions (i), (ii), (i) and (i) in the continuous bulk polymerization of styrene monomers.

(Iii) continuous mass polymerization was carried out by maintaining the styrene monomer input flow rate and reaction time in the first reactor under the conditions of the following formulas (A) and (B);

5.0 ≤ F ₁ / F ₂ ≤ 6.0 (F = F ₁ + F ₂ ) (A)

1.5 ≤ V ₁ / V ₁ '≤ 1.7 (B)

(F is the total flow rate styrene monomer is introduced into the reactor, F ₁ is the total flow rate styrene monomer is introduced into the first reactor, F ₂ is the total flow rate styrene monomer is introduced into the second reactor, V ₁ Is the reactor content in the first reactor, and V ₁ ′ is the content of the reaction liquid in the first reactor);

(Ii) continuous block polymerization was carried out in the second reactor with the flow rate and reaction conditions under the conditions of the following formulas (C) and (D);

F = F ₁ + F ₂ (C)

1.8 ≤ V ₂ / V ₂ '≤ 2.5 (D)

(Wherein F, F ₁ and F ₂ are as defined above, V ₂ is the content of the reactor in the second reactor and V ₂ ′ is the content of the reaction liquid of the second reactor);

(Iii) continuously feeding dimethylsiloxane and white oil to the second reactor so that the content of dimethylpolysiloxane is 0.5 to 1.5% by weight and the content of white oil is 0.3 to 1.2% by weight in the final pellet resin; And

(Iii) The unreacted monomer is separated from the polymer produced in the second reactor to prepare a final thermoplastic resin.

In addition, the continuous bulk polymerization in the first reactor is carried out at 118 to 130 ℃ and the continuous bulk polymerization in the second reactor is carried out at 140 to 160 ℃.

The content of polystyrene as the thermoplastic resin obtained by the method of the present invention is 55 to 70% by weight in the second reactor on a solids basis, and the average molecular weight of the final pellet resin is in the range of 280,000 to 380,000.

The method of the present invention is described in more detail as follows.

First, the styrene monomer is continuously supplied to the first reactor and the second reactor from the raw material tank in which the styrene monomer is stored. Styrene monomers that can be used in the present invention include styrene; branched alkyl substituted styrenes such as α-ethylstyrene and α-methylstyrene; Nuclear alkyl substituted styrenes such as vinyl xylene, o-t-butylstyrene, p-t-butylstyrene and p-methylstyrene; Halogenated styrenes such as monochlorostyrene, dichlorostyrene, tribromostyrene and tetrabromostyrene; p-hydroxystyrene; And o-methoxystyrene. Of these, styrene is most commonly used.

1) Polymerization in the first reactor:

The flow rate into which the raw material solution (styrene monomer) is introduced into the first reactor is F ₁ , the flow rate into the second reactor is F ₂ , the total flow rate of the raw material solution into the first reactor and the second reactor is F, and V ₁ less the content of the first reactor, the first reactor occupied by the reaction liquid when the information indicates the enemy _{V 1 ', 5.0 ≤ F 1} / F 2 ≤6.0 (F = F 1 + F 2) and 1.5 ≤ V ₁ / V Continuous mass polymerization is performed at a temperature of 118 to 130 ° C. by maintaining the condition of ₁ ′ ≦ 1.7 and adjusting the stirrer speed of the first reactor to 30 times / minute.

In the case of F ₁ / F ₂ > 6.0, it is difficult to form high molecular weight polystyrene, and when F ₁ / F ₂ <5.0, the viscosity of the reactants becomes too high, causing a problem of poor transfer to the second reactor, resulting in a second reactor. Not only is it difficult to control the temperature, but also a large amount of low molecular weight polystyrene is generated in the second reactor, so that the desired high stiffness resin cannot be obtained. In addition, the reason for maintaining the flow rate in the first reactor in the above conditions is to use the two reactors effectively to control the viscosity, to facilitate the transfer of the reactants, and to polymerize with a high molecular weight resin to have a high rigidity.

In the case of V ₁ / V ₁ '> 1.7, the viscosity becomes too high and the load of the stirrer increases, which makes the operation difficult, and it is difficult to cope quickly in the event of an emergency, resulting in process interruption and waste of raw materials. In _{contrast, V 1 / V 1 '<} 1.5 a case, it is not possible to obtain a desired solids content can not be high molecular weight is reduced to obtain a resin of molecular weight.

After all, the reason for maintaining the above conditions in the first reactor is to achieve a smooth transfer of the reactants in the continuous bulk polymerization without using a solvent and to obtain a high rigidity high molecular weight resin having an average molecular weight of 280,000 to 380,000.

The polymerized product in the first reactor is then continuously fed to the second reactor to further undergo continuous bulk polymerization.

2) polymerization in the second reactor:

The flow rate into which the raw material solution (styrene monomer) is introduced into the first reactor is F ₁ , the flow rate into which the second reactor is introduced into F ₂ , the total flow rate of the raw material solution into the first reactor and the second reactor into F, and When the contents of the reactor are represented by V ₂ , and the contents of the reaction solution in the second reactor are represented by V ₂ ', the conditions of F = F ₁ + F ₂ and 1.8 ≤ V ₂ / V ₂ ' ≤ 2.5 are maintained. Continuous block polymerization is carried out so that the polystyrene resin solids content is 55 to 70% by weight at a reaction temperature of 140 to 160 ° C by fixing the rotation speed at 20 times / min. In addition, 0.5 to 1.5% by weight of dimethylsiloxane and 0.3 to 1.2% by weight of hydrocarbon compound are continuously added to the second reactor based on the weight of the final pellet resin.

In the second reactor, when V ₂ / V ₂ '> 2.5, the solid content is reduced to lower the productivity. On the other hand, in the case of V ₂ / V ₂ '<1.8, a large amount of low molecular weight material is generated to obtain a high rigid resin, and it is difficult to control the polymerization temperature due to an increase in calorific value.

In the second reactor, when the reaction temperature is lower than 140 ° C., the productivity is lowered. When the reaction temperature is higher than 161 ° C., a high molecular weight substance generation rate is low, so that the desired high rigid resin cannot be obtained.

The dimethylpolysiloxane is added to exhibit excellent wear resistance when the thermoplastic resin prepared according to the present invention is manufactured and used as a molded article. In addition, the hydrocarbon compound is added in order to exhibit excellent releasability during molding of the thermoplastic resin, and a hydrocarbon compound extracted from petroleum is used.

Dimethyl polysiloxanes having a viscosity of about 100 cPS are commercially available from Shin-Etsu, Dow Corning Korea, and the like. Hydrocarbon compounds generally use what is known as white oil (WHITE OIL), and are marketed under the product names of LP-350, TOMI-350, etc. in the Far Eastern Oil and Unchanged Petroleum.

In conclusion, maintaining the input flow rate and the reaction conditions in the second reactor as described above is to obtain a high yield of high-strength high molecular weight polystyrene excellent in wear resistance and releasability.

Other additives such as molecular weight regulators, antistatic agents, antioxidants and the like may be appropriately added to the first reactor and the second reactor depending on the end use of the resin, which can be easily carried out by those skilled in the art.

After the polymerization reaction is completed in the second reactor, an unreacted monomer is separated while passing through a temperature increaser, a volatilization tank, and the like, and is then cut into pellets. The average molecular weight of the final resin in this pellet form is in the range of 280,000 to 380,000.

Example

Example 1

The flow rate into which the raw material solution (styrene monomer) is introduced into the first reactor is F ₁ , the flow rate into which the second reactor is introduced into F ₂ , the total flow rate of the raw material solution into the first reactor and the second reactor into F, and 1 information, the information less reaction solution in V _1, a first reactor of the reactor occupied "when referring _{to, F 1 / F 2 = 5.2} (F = F 1 + F 2) and V ₁ / V _1, less V ₁ = 1.55 The continuous bulk polymerization was performed on condition of the following. During the polymerization reaction, the stirrer speed of the first reactor was maintained at 30 times / minute, and the polymerization temperature was maintained at 122 ° C.

The polymer of the first reactor was fed to the second reactor continuously in the same manner as the feed flow rate of the first reactor.

The "when referring to, F = F ₁ + F ₂ and V ₂ / V ₂ '2 reactor contents less V _2, the second reaction vessel contents less V ₂ The reaction liquid occupied in the = continuous mass polymerization to maintain the condition of 2.0 The reaction was carried out. During the reaction, the stirrer speed of the second reactor was maintained at 20 times / minute, and the polymerization temperature was maintained at 149 ° C.

In the second reactor, 0.9% by weight of dimethylpolysiloxane and 0.6% by weight of white oil were continuously added from separate storage tanks based on the weight of the final pellet resin.

The polymer obtained from the second reactor was continuously sent to a devolatilization tank and heated up to 245 ° C., followed by a devolatilization step in which volatile components such as unreacted monomers were removed, and then prepared as a final resin pellet.

Molecular weight and tensile strength of the resin pellets obtained in this example were measured, and a test specimen for wear resistance was produced in the measuring mold of the injection molding machine.

Example 2

By adjusting the reactor flow rate of the raw material solution (styrene monomer), the ratio of the styrene monomer flow rate (F ₁ ) to the first reactor and the styrene monomer flow rate (F ₂ ) to the second reactor is F ₁ / F ₂ = 5.9 Except for maintaining as, continuous block polymerization was carried out in the same manner as in Example 1. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Example 3

By adjusting the residence time of the first reactor, the contents of the first reactor (V ₁ ) and the contents of the reaction solution of the first reactor (V ₁ ') are changed to V ₁ / V ₁ ' = 1.50. Then, continuous bulk polymerization was carried out in the same manner as in Example 1. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Example 4

By adjusting the residence time of the second reactor, the contents of the second reactor (V ₂ ) and the contents of the reaction liquid of the second reactor (V ₂ ') are changed to V ₂ / V ₂ ' = 2.40. Then, continuous bulk polymerization was carried out in the same manner as in Example 1. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Example 5

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that the temperature of the second reactor was changed to 165 ° C. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Example 6

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that the amount of the white oil continuously added to the second reactor was changed to 1.1 wt%. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Example 7

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that the amount of dimethylpolysiloxane continuously added to the second reactor was changed to 1.3% by weight. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 1

Continuous bulk polymerization in the same manner as in Example 1, except that the ratio of the styrene monomer flow rate (F ₂ ) to the second reactor was maintained at 0 by controlling the reactor input flow rate of the raw material solution (styrene monomer). Was carried out. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 2

By adjusting the residence time of the first reactor, the contents of the first reactor (V ₁ ) and the contents of the reaction solution of the first reactor (V ₁ ') are changed to V ₁ / V ₁ ' = 1.90. Then, continuous bulk polymerization was carried out in the same manner as in Example 1. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 3

By adjusting the residence time of the second reactor, the contents of the second reactor (V ₂ ) and the contents of the reaction solution of the second reactor (V ₂ ') are changed to V ₂ / V ₂ ' = 1.6. Then, continuous bulk polymerization was carried out in the same manner as in Example 1. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 4

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that the temperature of the second reactor was changed to 172 ° C. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 5

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that white oil was not added to the second reactor. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 6

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that the amount of the white oil continuously added to the second reactor was changed to 1.5% by weight. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 7

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that dimethylpolysiloxane was not added to the second reactor. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

Comparative Example 8

Continuous bulk polymerization was carried out in the same manner as in Example 1, except that the amount of dimethylpolysiloxane continuously added to the second reactor was changed to 1.7 wt%. The physical properties of the obtained resin pellets were evaluated in the same manner as in Example 1.

The working conditions used in Examples 1 to 7 and Comparative Examples 1 to 8 are shown in Tables 1 and 2, respectively, and the properties of the prepared resins were evaluated according to the following property evaluation methods. Shown in

〈Physical property evaluation method〉

(1) Tensile strength: measured according to ASTM D638 (speed: 20 mm / min).

(2) Molecular weight: Take 5 mg of sample from final resin pellet, mix 5 ml of THF, place in shaker and shake for 30 minutes to completely dissolve. The molecular weight was measured.

(3) Deformation failure rate: The specimen was injected into a 5.3 OZ injection machine manufactured by Venus Cable Co., Ltd., and the specimens were ejected using the grid mold for evaluation of releasability.

(4) Wear resistance: The amount of wear was measured using a wear tester manufactured by Daesung Engineering Co., Ltd. for specimens manufactured in an injection molding machine.

              Example No. Reaction Condition    One    2    3    4    5    6    7 Monomer flow rate introduced into the first reactor / Monomer flow rate introduced into the second reactor (F ₁ / F ₂ )   5.2   5.9   5.2   5.2   5.2   5.2   5.2 Inner volume of the first reactor / Inner volume of the reaction solution of the first reactor (V ₁ / V ₁ ')   1.55  1.55  1.50   1.55  1.55   1.55   1.55 Inner volume of the second reactor / Inner volume of the reaction solution of the second reactor (V ₂ / V ₂ ')   2.0   2.0   2.0   2.4  2.0   2.0   2.0 Dimethyl polysiloxane input to the second reactor (% by weight)   0.9   0.9   0.9   0.9  0.9   0.9   1.3 Hydrocarbon compound input to the second reactor (% by weight)   0.6   0.6   0.6   0.6  0.6   1.1   1.1 Temperature of the first reactor (℃)   122   122   122   122  122   122   122 Temperature of Second Reactor (℃)   149   149   149   149  165   149   149

         Comparative Example No. Reaction Condition    One    2    3    4    5    6    7   8 Monomer flow rate introduced into the first reactor / Monomer flow rate introduced into the second reactor (F ₁ / F ₂ ) F ₂ = 0   5.2   5.2   5.2  5.2   5.2  5.2   5.2 Inner volume of the first reactor / Inner volume of the reaction solution of the first reactor (V ₁ / V ₁ ')  1.55  1.90  1.55  1.55 1.55  1.55 1.55  1.55 Inner volume of the second reactor / Inner volume of the reaction solution of the second reactor (V ₂ / V ₂ ')   2.0   2.0   1.6   2.0  2.0   2.0  2.0   2.0 Dimethyl polysiloxane input to the second reactor (% by weight)   0.9   0.9   0.9   0.9  0.9   0.9   0   1.7 Hydrocarbon compound input to the second reactor (% by weight)   0.6   0.6   0.6   0.6   0   1.5  0.6   0.6 Temperature of the first reactor (℃)   122   122   122   122  122   122  122   122 Temperature of Second Reactor (℃)   149   149   149   172  149   149  149   149

Properties Average molecular weight (MW / 1,000) Tensile Strength (Kg / ㎠) Resin wear amount (mg) Deformation failure rate (%) Example 1 310 540 0.16 0.2 Example 2 330 550 0.15 0.1 Example 3 300 540 0.16 0.2 Example 4 350 560 0.16 0.2 Example 5 370 570 0.14 0.1 Example 6 310 535 0.15 0.1 Example 7 310 535 0.13 0.1 Comparative Example 1 230 500 2.6 10 Comparative Example 2 240 490 2.8 12 Comparative Example 3 250 510 2.7 11 Comparative Example 4 245 505 2.9 13 Comparative Example 5 310 540 2.4 6 Comparative Example 6 310 530 2.5 5 Comparative Example 7 310 535 2.8 10 Comparative Example 8 310 535 2.7 10

As can be seen from the results of the above table, according to the thermoplastic resin manufacturing method of the present invention, in the continuous bulk polymerization method proceeding in the first and second reactors, the yellowness is good and wear resistance and releasability are used by using specific input and reaction conditions. This excellent and high rigidity high-molecular weight polystyrene resin can be prepared, and the produced resin has the effect of the invention showing excellent physical properties when used in the manufacture of an audio tape case, a food and beverage container and a test container.

Simple modifications or changes of the present invention can be easily carried out by those skilled in the art, and all such modifications or changes can be seen to be included in the scope of the present invention.

1 is a schematic diagram schematically showing an apparatus for carrying out the continuous bulk polymerization method of the present invention.

<Description of the code | symbol about the principal part of drawing>

1: total flow rate (F) in which styrene monomer is introduced into the first and second reactors

2: flow rate of the styrene monomer to the first reactor (F ₁ )

3: flow rate of the styrene monomer to the second reactor (F ₂ )

4: Reactor volume of the first reactor (V ₁ )

5: Internal volume of the reaction solution in the first reactor (V ₁ ')

6: Reactor Content of Second Reactor (V ₂ )

7: Content of the reaction solution in the second reactor (V ₂ ')

Claims (5)

1. (iii) Continuous mass polymerization is carried out by maintaining the styrene monomer input flow rate and reaction time in the first reactor under the conditions of the following formulas (A) and (B). 5.0 ≤ F ₁ / F ₂ ≤ 6.0 (F = F ₁ + F ₂ ) (A) 1.5 ≤ V ₁ / V ₁ '≤ 1.7 (B) (F is the total flow rate styrene monomer is introduced into the reactor, F ₁ is the total flow rate styrene monomer is introduced into the first reactor, F ₂ is the total flow rate styrene monomer is introduced into the second reactor, V ₁ and the reactor contents from the first reactor and V ₂ is V ₁ 'is the internal volume occupied by the reaction liquid in the first reactor); (Ii) continuous block polymerization was carried out in the second reactor with the flow rate and reaction conditions under the conditions of the following formulas (C) and (D); F = F ₁ + F ₂ (C) 1.8 ≤ V ₂ / V ₂ '≤ 2.5 (D) (Wherein F, F ₁ and F ₂ are as defined above, V ₂ is the content of the reactor in the second reactor and V ₂ ′ is the content of the reaction liquid of the second reactor); (Iii) continuously feeding dimethylsiloxane and white oil to the second reactor so that the content of dimethylpolysiloxane is 0.5 to 1.5% by weight and the content of white oil is 0.3 to 1.2% by weight in the final pellet resin; And (Iii) separating the unreacted monomer from the polymer produced in the second reactor and then pelletizing to obtain the final thermoplastic resin: Method for producing a highly rigid thermoplastic resin, characterized in that. The method of claim 1, wherein the polymerization temperature of the first reactor is in the range of 118 to 130 ° C. The method for producing a highly rigid thermoplastic resin according to claim 1, wherein the polymerization temperature of the second reactor is in the range of 140 to 160 ° C. The method of claim 1, wherein the polystyrene solids content in the second reactor is in the range of 55 to 70% by weight. The method of claim 1, wherein the average molecular weight of the final pellet resin is in the range of 280,000 to 380,000.