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Preparation of phenylethylene-dialkene special copolymer

A technology of diene and styrene, applied in the field of preparation of styrene-diene special copolymer, can solve the problems that the product quality is not stable, the production cycle is long, and the operation cost is high, and the production cost is low, the reaction time is short, and the operation cost is low. low cost effect

Inactive Publication Date: 2011-04-06
ZHEJIANG SANPO POLYMER
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

This process is flexible in operation, easy to adapt to different operating conditions and product varieties, and is suitable for the production of products with small batches, multiple varieties, and long reaction time. However, the batch-type production process requires auxiliary operations such as loading and unloading. It is not easy to be stable, the equipment investment is large, the production cycle is long, and the overall operating cost is high

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0014] The working temperature of the forward conveying twin-screw extruder with an aspect ratio of 10 is controlled at -20° C., and the rotational speed is controlled at 200 r / min. The liquid monomer styrene is pumped into the forward conveying twin-screw extruder for one-stage polymerization; when the conversion rate of the first-stage monomer reaches more than 95%, 1,3-butadiene is added for two-stage polymerization, and the polymerization is completed After adding 1,3-butadiene and styrene mixed monomer polymerization; when the second-stage monomer conversion rate is greater than 95%, add styrene to carry out the last stage polymerization, the weight percentage of 1,3-butadiene in the final polymer 0.1%, adding alkyllithium as a catalyst during the polymerization, the total polymerization time is 0.5min. The polymerization reaction temperature was -20°C. At the end of the polymerization, terminator water was added. The monomer exists in liquid state throughout the polyme...

Embodiment 2

[0016] The operating temperature of the reverse conveying twin-screw extruder with an aspect ratio of 40 is controlled at 200° C., and the rotational speed is controlled at 50 r / min. The monomer styrene in the liquid state is pumped into the reverse conveying twin-screw extruder for one-stage polymerization; when the conversion rate of the first-stage monomer reaches more than 95%, 2-methyl-1,3-butadiene is added for two-stage polymerization. After the polymerization is completed, 2-methyl-1,3-butadiene and styrene are added to the monomer polymerization; when the conversion rate of the second-stage monomer is greater than 95%, styrene is added for the last stage of polymerization, and the final polymer The weight percent of 2-methyl-1,3-butadiene is 19.9%, and alkyllithium is added as a catalyst during the polymerization process, and the total polymerization time is 120 minutes. A certain amount of solvent toluene is added to the monomer in any of the above processes for pre-...

Embodiment 3

[0018] The working temperature of the forward conveying four-screw extruder with an aspect ratio of 200 was controlled at 100° C., and the rotational speed was controlled at 50 r / min. The monomer styrene in the liquid state is pumped into the reverse conveying twin-screw extruder for one-stage polymerization; when the conversion rate of the first-stage monomer reaches more than 95%, 2-methyl-1,3-butadiene is added for two-stage polymerization. After the polymerization is completed, 2-methyl-1,3-butadiene and styrene are added to the monomer polymerization; when the conversion rate of the second-stage monomer is greater than 95%, styrene is added for the last stage of polymerization, and the final polymer The weight percent of 2-methyl-1,3-butadiene is 9.8%, and alkyllithium is added as a catalyst during the polymerization process, and the total polymerization time is 100 min. A certain amount of solvent toluene is added to the monomer in any of the above processes for premixin...

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PUM

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Abstract

The invention discloses a preparation method for a styrene-diolefin special copolymer. The preparation method comprises the following steps: taking a styrene-diolefin block random copolymer as PS-PB-PB / PS-PS; wherein PS representing a styrene copolymer block, PB representing a diolefin copolymer block, and PB / PS representing a styrene-diolefin random copolymer block; and adopting an anionic continuous polymerization method. The preparation method avoids the defects of a batch still and is characterized by low production cost, short production cycle, low operating cost, short reaction time andhigh yield.

Description

technical field [0001] The invention relates to a preparation method of a styrene-diene special copolymer. Background technique [0002] Styrene resin is one of the five general-purpose synthetic resins, and generally ranks fourth in terms of output after PE, PVC and PP. Polystyrene (PS), in 1925, the German I.G.Farben Industrial Company began to engage in the industrial production and development of styrene, and realized industrial production in 1930. In 1958, China began to prepare for production equipment, creating the industrial production of polystyrene resin in China. In the early stage of the development of styrene-based resins, only general-purpose polystyrene was produced. It is hard and brittle, has low mechanical strength, poor heat resistance, and is flammable. For this reason, people have done a lot of improvement work, forming high-impact polystyrene (HIPS), expandable polystyrene (EPS), styrene-butadiene copolymer (K-Resin) and so on. Bulk styrenic resin s...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C08F297/04
Inventor 周赞斌高书峰程国丽冯震高碧波
Owner ZHEJIANG SANPO POLYMER
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