CN111944098A

CN111944098A - Processing technology of transparent ABS resin

Info

Publication number: CN111944098A
Application number: CN202010795783.2A
Authority: CN
Inventors: 陶春风
Original assignee: Guangxi Changke New Material Co ltd
Current assignee: Guangxi Changke New Material Co ltd
Priority date: 2020-08-10
Filing date: 2020-08-10
Publication date: 2020-11-17

Abstract

The invention relates to a processing technology of transparent ABS resin, which comprises the following steps: s1, after being crushed, SBR rubber and styrene are added into a rubber dissolving tank, stirred and subjected to backflow grinding through a grinding pump to prepare a rubber styrene solution with the content of 5-15%; s2, continuously adding a rubber styrene solution, methyl methacrylate, an initiator and a molecular weight regulator into a first reactor according to a certain proportion, controlling the temperature to be 70-90 ℃ and the stirring speed to be 30-40rpm, and carrying out grafting reaction; s3, conveying the polymerization liquid from the first reactor to the second reactor through a gear pump to continue reacting, controlling the reaction temperature to be 90-110 ℃, the stirring speed to be 30-40rpm, and realizing phase inversion of the polymerization liquid in the second reactor to form grafted rubber particles with the particle size of 150-200 nm. Compared with the traditional emulsion grafting-mixing method technology, the bulk method technology has the advantages of short flow, less three wastes, less product odor, stable quality and the like.

Description

Processing technology of transparent ABS resin

Technical Field

The invention relates to the field of chemical industry, in particular to a processing technology of transparent ABS resin.

Background

The ABS resin is an Acrylonitrile-Butadiene-Styrene copolymer, and the ABS is an acronym of Acrylonitrile Butadiene Styrene, and is a thermoplastic high polymer material which has high strength, good toughness and easy processing and molding. The method is used for preparing various parts such as instruments, electrics, electrical appliances and machinery. ABS resins can be compounded with a variety of resins to blends, such as PC/ABS, ABS/PVC, PA/ABS, PBT/ABS, etc., resulting in new properties and new fields of application.

The transparent ABS resin has the advantages of transparency, processability, mechanical property and the like, and is popular in the market, but the transparent ABS is produced by adopting an emulsion grafting-blending method at present, the process is long, the process is complex, the quantity of three wastes is large, the product quality stability is poor, and the content of residual monomers is higher.

Disclosure of Invention

The invention aims to solve the defects in the prior art and provides a processing technology of transparent ABS resin.

In order to achieve the purpose, the technical scheme adopted by the invention is as follows:

a processing technology of transparent ABS resin comprises the following steps:

s1, after being crushed, SBR rubber and styrene are added into a rubber dissolving tank, stirred and subjected to backflow grinding through a grinding pump to prepare a rubber styrene solution with the content of 5-15%;

s2, continuously adding a rubber styrene solution, methyl methacrylate, an initiator (di-tert-butyl peroxide-cyclohexane) and a molecular weight regulator (n-dodecyl mercaptan) into a first reactor according to a certain proportion, controlling the temperature to be 70-90 ℃ and the stirring speed to be 30-40rpm, and carrying out grafting reaction;

s3, conveying the polymerization liquid from the first reactor to a second reactor through a gear pump to continue reacting, controlling the reaction temperature to be 90-110 ℃, the stirring speed to be 30-40rpm, and realizing phase inversion of the polymerization liquid in the second reactor to form grafted rubber particles with the particle size of 150-200 nm;

s4, adding polymerization liquid with the conversion rate of about 30 percent from the second reactor into a third reactor, simultaneously adding quantitative acrylonitrile, a solvent (toluene) and a recovered monomer (unreacted styrene, acrylonitrile and methyl methacrylate), controlling the reaction temperature to continue the polymerization reaction at 140-150 ℃, controlling the liquid level of the third reactor to be about 60-70 percent, removing the polymerization heat through evaporation and condensation of the polymerization liquid, and supplementing a certain amount of initiator into the third reactor to ensure that the conversion rate meets the requirement;

s5, conveying the polymerization solution from the third reactor to a fourth reactor, wherein the form and the size of the fourth reactor are the same as those of the third reactor, the temperature is controlled at 155 ℃, and the fourth reactor is used for crosslinking rubber and ensuring the conversion rate;

s6, conveying the polymerization solution from the fourth reactor to a first devolatilization device through a kettle bottom gear pump for first-step devolatilization, and removing unreacted acrylonitrile and the rest monomers and solvents under the conditions of temperature 160-180 ℃ and vacuum degree 50 KPa;

s7, conveying the polymerization liquid from the first devolatilization device to the second devolatilization device through a gear pump, completely removing unreacted monomers and solvents under the conditions of the temperature of 220-.

Further, the removed monomer and solvent are condensed and added into a third reactor for reuse.

Further, in step S2, the weight portion of the rubber styrene solution is 80-90, the weight portion of the methyl methacrylate is 10-20, the weight portion of the initiator is 1000-3000ppm, and the weight portion of the molecular weight regulator is 1000-3000 ppm.

Further, the first reactor and the second reactor are plug flow polymerizers, and the third reactor and the fourth reactor are kettle polymerizers.

The invention has the beneficial effects that: compared with the traditional emulsion grafting-mixing method technology, the bulk method technology has the advantages of short flow, less three wastes, less product odor, stable quality and the like.

Drawings

FIG. 1 is a schematic process flow diagram of the present invention;

fig. 2 is a schematic diagram of the apparatus according to the present invention.

Detailed Description

As shown in fig. 1 and fig. 2, a processing technology of a transparent ABS resin includes the following steps:

s1, after the SBR rubber is crushed, adding the crushed SBR rubber and styrene in a styrene tank body 1 into a rubber dissolving tank 2, stirring and carrying out backflow grinding through a grinding pump to prepare a rubber styrene solution with the content of 5-15%;

s2, continuously adding a rubber styrene solution, methyl methacrylate, an initiator (di-tert-butyl peroxide-cyclohexane) and a molecular weight regulator (n-dodecyl mercaptan) into a first reactor 8 according to a certain proportion, controlling the temperature to be 70-90 ℃ and the stirring speed to be 30-40rpm, and carrying out grafting reaction;

wherein, the rubber styrene solution is obtained by mixing SBR rubber particles in a rubber dissolving tank 2 and styrene for reaction, methyl methacrylate is supplied by a methyl methacrylate tank 3, an initiator is supplied by an initiator tank 6, a molecular weight regulator is supplied by a regulator tank 7, and the rubber styrene solution is supplied by a feeding tank 4 connected with the rubber dissolving tank 2;

s3, conveying the polymerization liquid from the first reactor 8 to the second reactor 9 through a gear pump to continue reacting, controlling the reaction temperature to be 90-110 ℃, the stirring speed to be 30-40rpm, and realizing phase inversion of the polymerization liquid in the second reactor 9 to form grafted rubber particles with the particle size of 150-200 nm;

s4, adding a polymerization solution with the conversion rate of about 30 percent from the second reactor 9 into a third reactor 10, simultaneously adding a certain amount of acrylonitrile, a solvent (toluene) and a recovered monomer (unreacted styrene, acrylonitrile and methyl methacrylate), wherein the recovered monomer is supplied through a recovered monomer tank 11, the acrylonitrile is supplied through an acrylonitrile tank 5, the solvent (toluene) is supplied through a toluene tank 15, the reaction temperature is controlled to be 150 ℃ for continuing the polymerization reaction, the liquid level of the third reactor 10 is controlled to be about 60-70 percent, the polymerization heat is removed through evaporation and condensation of the polymerization solution, and in order to ensure that the conversion rate meets the requirement, a certain amount of an initiator can be added into the third reactor 10;

s5, conveying the polymerization liquid from the third reactor 10 to a fourth reactor 12, wherein the form and the size of the fourth reactor 12 are the same as those of the third reactor 10, the temperature is controlled at 155 ℃, and the fourth reactor 12 is used for crosslinking rubber and ensuring the conversion rate;

s6, conveying the polymerization solution from the fourth reactor 12 to the first devolatilization device 13 through a kettle bottom gear pump for first-step devolatilization, and removing unreacted acrylonitrile and the rest monomers and solvents under the conditions of the temperature of 160-;

s7, conveying the polymerization liquid from the first devolatilization device 13 to the second devolatilization device 14 through a gear pump, completely removing unreacted monomers and solvents under the conditions of the temperature of 220-.

Further, the removed monomer and solvent are condensed and then added to the third reactor 10 for reuse.

Wherein the first reactor 8 and the second reactor 9 are plug flow polymerizers, and the third reactor 10 and the fourth reactor 12 are tank polymerizers. The first reactor 8 carries out graft polymerization, the second reactor 9 controls phase transition, the third reactor 10 adds a certain amount of acrylonitrile and recycled monomers to improve the conversion rate, and the fourth reactor 12 carries out moderate crosslinking on rubber.

Compared with the traditional emulsion grafting-mixing method technology, the bulk method technology has the advantages of short flow, less three wastes, less product odor, stable quality and the like.

The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are merely illustrative of the principles of the invention, but that various changes and modifications may be made without departing from the spirit and scope of the invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.

Claims

1. The processing technology of the transparent ABS resin is characterized by comprising the following steps:

s2, continuously adding a rubber styrene solution, methyl methacrylate, an initiator and a molecular weight regulator into a first reactor according to a certain proportion, controlling the temperature to be 70-90 ℃ and the stirring speed to be 30-40rpm, and carrying out grafting reaction;

s4, adding polymerization liquid with the conversion rate of about 30 percent from the second reactor into a third reactor, simultaneously adding quantitative acrylonitrile, a solvent and a recovered monomer, controlling the reaction temperature to be 140-150 ℃ to continue the polymerization reaction, controlling the liquid level of the third reactor to be about 60-70 percent, removing the polymerization heat through evaporation and condensation of the polymerization liquid, and supplementing a certain amount of initiator into the third reactor to ensure that the conversion rate meets the requirement;

2. The process according to claim 1, wherein the removed monomer and solvent are condensed and then added to the third reactor for reuse.

3. The process of claim 1, wherein in step S2, the weight portion of the styrene rubber solution is 80-90, the weight portion of the methyl methacrylate is 10-20, the weight portion of the initiator is 1000-3000ppm, and the weight portion of the molecular weight regulator is 1000-3000 ppm.

4. The process according to claim 1, wherein the first reactor and the second reactor are plug flow polymerizers, and the third reactor and the fourth reactor are tank polymerizers.

5. The process according to claim 1, wherein the initiator is t-butyl-cyclohexane diperoxide, the molecular weight regulator is n-dodecylmercaptan, the solvent is toluene, and the recovered monomers are unreacted styrene, acrylonitrile and methyl methacrylate.