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Technique of refining solvent in process of producing synthetic rubber

A production process and solvent refining technology, applied in the field of solvent refining technology in synthetic rubber production process, can solve the problem of high energy consumption

Active Publication Date: 2007-02-07
HUNAN BAILI ENGINEERING SCIENCE AND TECHNOLOGY CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0002] In the production process of synthetic rubber, such as: solution styrene-butadiene rubber (SSBR), solution polymerization ethylene propylene rubber, butadiene rubber and styrene block copolymer SBC (SBS, SIS, SEBS) production equipment, in the polymerization or coagulation stage There are a lot of solvents, and a lot of solvents are recycled in the device. The devices are equipped with solvent recovery and refining units or related equipment. At present, almost all solvent refining is to remove water and light components in the dehydration tower first, and then remove the water and light components in the rectification tower. The single-effect rectification process for removing heavy components in the middle, generally consumes 2-3 tons of steam per ton of product, and the energy consumption is high

Method used

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  • Technique of refining solvent in process of producing synthetic rubber
  • Technique of refining solvent in process of producing synthetic rubber
  • Technique of refining solvent in process of producing synthetic rubber

Examples

Experimental program
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Effect test

Embodiment 1

[0026] A two-effect series rectification process for recovering cyclohexane solvent, such as figure 1 As shown, the cyclohexane recovered by the condensation unit enters the dehydration tower of the solvent refining unit to remove water and light components, and is sent to the first-effect rectification tower 1 and the second-effect rectification tower in equal proportions from the dehydration tower tank through the pump. Middle of Tower 3. The operating pressure of the first-effect rectification tower 1 is 0.25MPa (table), the temperature at the top of the tower is 121°C, and the temperature at the bottom of the tower is 128°C. The siphon reboiler 2 is heated by low-pressure steam, and part of the solvent is vaporized in the column tube. Mass transfer separation occurs in the tower, and the solvent with the required purity reaches the shell side of the siphon reboiler 4 of the second-effect rectification tower 3 in gas phase from the top of the first-effect rectification towe...

Embodiment 2

[0031] A two-effect series rectification process for recovering cyclohexane solvent, such as figure 2shown. The cyclohexane recovered by the condensation unit enters the dehydration tower of the solvent refining unit to remove water and light components, and then is pumped to the middle of the first-effect rectification tower 1. The operating pressure of the first-effect rectification tower 1 is 0.25Mpa (table), the temperature at the top of the tower is 121°C, and the temperature at the bottom of the tower is 126°C. The siphon type reboiler 2 is heated by low-pressure steam, and part of the solvent is vaporized in the column tube. Mass transfer separation occurs in the tower, and the solvent with the required purity is discharged from the top of the first-effect tower to the shell side of the siphon reboiler 4 of the second-effect rectification tower 3 in gas phase. The impurity-containing solvent is pressed into the middle part of the second-effect rectification tower 3 fr...

Embodiment 3

[0036] A three-effect cascade rectification process for recovering cyclohexane solvent, such as image 3 shown.

[0037] After the cyclohexane recovered by the condensation unit enters the dehydration tower of the solvent refining unit for dehydration, it is pumped from the bottom of the dehydration tower to the middle of the first-effect rectification tower 1 . The operating pressure of the first-effect rectification tower 1 is 0.5MPa (table), the temperature at the top of the tower is 140°C, and the temperature at the bottom of the tower is 144°C. The siphon type reboiler 2 is heated by low-pressure steam, and part of the solvent is vaporized in the column tube. Mass transfer separation occurs in the tower, and the solvent with the required purity reaches the shell side of the siphon reboiler 4 of the second-effect rectification tower 3 from the top of the first-effect rectification tower 1 in gas phase. The impurity-containing solvent is pressed into the middle part of the...

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Abstract

the invention discloses a solvent refining technology of rubber synthetic manufacturing course, which is characterized by the following: adopting multiple rectifying towers to replace present single rectifying tower to reduce steam by about 60-50%; adopting cooled heat of last rectifying top gas as heat source of next tower through improving operational pressure of one tower to utilize pressure difference and temperature difference of each tower; adopting two-effective paralleling combination, two-effective cascading combination or three-effective cascading combination in the course.

Description

1. Technical field: [0001] The invention relates to a process for refining solvent recovery in the production process of synthetic rubber. 2. Background technology: [0002] In the production process of synthetic rubber, such as: solution styrene-butadiene rubber (SSBR), solution polymerization ethylene propylene rubber, butadiene rubber and styrene block copolymer SBC (SBS, SIS, SEBS) production equipment, in the polymerization or coagulation stage There are a lot of solvents, and a lot of solvents are recycled in the device. The devices are equipped with solvent recovery and refining units or related equipment. At present, almost all solvent refining is to remove water and light components in the dehydration tower first, and then remove the water and light components in the rectification tower. The single-effect rectification process for removing heavy components in the middle, generally consumes 2-3 tons of steam per ton of product, and the energy consumption is high. 3...

Claims

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Application Information

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IPC IPC(8): C08J11/02
Inventor 李文辉蔡日新
Owner HUNAN BAILI ENGINEERING SCIENCE AND TECHNOLOGY CO LTD
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