CN104592544A - Process for refining solvent in synthetic rubber production process - Google Patents
Process for refining solvent in synthetic rubber production process Download PDFInfo
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- CN104592544A CN104592544A CN201510040290.7A CN201510040290A CN104592544A CN 104592544 A CN104592544 A CN 104592544A CN 201510040290 A CN201510040290 A CN 201510040290A CN 104592544 A CN104592544 A CN 104592544A
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- weight
- removing column
- solvent
- reboiler
- synthetic rubber
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to a process for refining a solvent in a synthetic rubber production process. The conventional double-effect series rectification process is replaced by adopting an MVR (mechanical vapor recompression type heat pump) process, the gas phase on the tower top of a heavy removal tower is conveyed to a compressor by virtue of a pipeline, and the compressed and boosted outlet gas phase is conveyed to a heavy removal tower reboiler to serve as a heat energy of the heavy removal tower reboiler. According to the process disclosed by the invention, in addition to startup, vapor is not consumed in normal production process of the heavy removal tower. Compared with the double-effect series rectification process, the process disclosed by the invention has the advantages that the heating energy consumption can be saved by about 37 percent, and the cooling energy consumption can be saved by about 81 percent. According to the process disclosed by the invention, the heat utilization efficiency is improved, the energy consumption is reduced, and the production cost of products is reduced.
Description
Technical field
The invention belongs to chemical technology field, relate to solvent refining processes in a kind of synthetic rubber production process, be specifically related to one and utilize MVR(mechanical steam recompression formula heat pump) technique removes heavy component impurity in synthetic rubber production process in solvent.
Background technology
In synthetic rubber production process, owing to adopting solution polymerization, polyreaction needs a large amount of solvents, solvent cohesion working section steam stripping out after refine to solvent treatment workshop section, utilize Light ends and water in dehydration tower desolvation, the heavy component then in weight-removing column desolvation.What in current production process, solvent treatment adopted is that single tower or double tower two imitate rectification process flow process, and product per ton consumes steam generally at 2-3 ton, and observable index is higher.
MVR(mechanical steam recompression formula heat pump) principle of work is the steam of low-pressure low-temperature rectifying tower tower top low-temp low-pressure gas phase or vaporizer steamed by mechanically operated compressor, be compressed to elevated pressures and high-temperature, become the thermal source of high-temperature position, as rectifying tower reboiler, well heater and vaporizer thermal source, to make full use of the latent heat of secondary steam or vapor condensation, with alternative external steam thermal source, except start up, without the need to steam in whole treating process, it is a high-efficiency energy-saving technology.Be generally used for the unit operation such as rectifying, evaporation.
Summary of the invention
The object of the invention is to provide solvent refining processes in a kind of synthetic rubber production process, removes the heavy component impurity in synthetic rubber production process in solvent, can improve efficiency of utilization, reduces energy expenditure, reduces products production cost.
This technical process is made up of weight-removing column, weight-removing column reboiler, compressor, weight-removing column return tank and pump.
Technical scheme of the present invention is: solvent refining processes in a kind of synthetic rubber production process, it is characterized in that: synthetic rubber production process solvent removes through dehydration tower and enters weight-removing column after Light ends and water and carry out rectifying, working pressure 0.12-0.14MPa.A is absolute pressure value, weight-removing column still temperature is 85-95 DEG C, weight-removing column top gaseous phase enters weight-removing column tower reactor reboiler and is condensed as its thermal source after compressor pressurization heats up, and compressor outlet gaseous pressure is 0.3-0.4MPa.A, temperature is 115-125 DEG C, solvent refining processes adopts MVR mechanical steam recompression formula heat pump using the thermal source as weight-removing column reboiler after weight-removing column top gaseous phase compression supercharging intensification, the technique of employing MVR mechanical steam recompression formula heat pump is: remove the solvent after Light ends and water through dehydration tower, enter in the middle part of weight-removing column, weight-removing column adopts pressure-fired rectifying, working pressure is 0.12-0.14MPa.A, weight-removing column still temperature is 85-95 DEG C, adopt low-pressure steam as weight-removing column driving reboiler thermal source when device is driven, in normal course of operation, weight-removing column top gaseous phase enters weight-removing column tower reactor reboiler shell side after compressor pressurization heats up, be condensed as its thermal source, phlegma enters weight-removing column return tank, then weight-removing column is returned as reflux through weight-removing column reflux pump small part, rest part is sent to product tank field through water cooler cooling.Weight-removing column bottom product is pumped to residual liquid tank through weight-removing column tower reactor.
Described gas phase after compression enters solvent weight-removing column return tank in reboiler after heat exchange condensation; Then be back in weight-removing column by a reflux pump part, another part is as product extraction after water cooler cooling.
Described solvent removes after Light ends and water through dehydration tower and enters in the middle part of weight-removing column.
Adopt low-pressure steam as weight-removing column reboiler thermal source when described solvent refining unit is driven, in normal course of operation, weight-removing column top gaseous phase enters weight-removing column tower reactor reboiler shell side, as its thermal source after compressor pressurization heats up.
Feature of the present invention and effect
The present invention is by MVR technology for the synthesis of solvent treatment in rubber production process, and the single tower distillation, two towers two that replace use now imitate rectifying desolvation heavy constituent technique.Technique of the present invention is imitated rectification flow technique relative to double tower two and is reduced about 37% and heat energy consumption and about 81% and cool energy consumption.
Technique of the present invention, except start up, does not consume steam in weight-removing column normal productive process, only consumes a small amount of electricity.
Accompanying drawing explanation
Fig. 1 is apparatus of the present invention and process flow diagram.
In figure: 1-weight-removing column, 2-weight-removing column reboiler, 3-compressor, 4-weight-removing column return tank, 5-weight-removing column reflux pump, 6-weight-removing column tower reactor pump, 7-solvent cooler, 8-weight-removing column driving reboiler;
LS-low-pressure steam CW-recirculated water.
Embodiment
Further illustrate the present invention below in conjunction with accompanying drawing, but do not form limitation of the invention.
Embodiment 1:
Produce 20000 tons of SEBS devices per year, adopt MVR(mechanical steam recompression formula heat pump) technical process, as shown in Figure 1.
Cohesion process recovered solvent enters solvent treatment operation and removes after Light ends and water through dehydration tower, enter weight-removing column (1) middle part, weight-removing column (1) adopts pressure-fired rectifying, working pressure is 0.12-0.14MPa.A, weight-removing column still temperature is 85-95 DEG C, low-pressure steam is adopted to drive reboiler (8) thermal source as weight-removing column when device is driven, in normal course of operation, weight-removing column (1) top gaseous phase enters weight-removing column tower reactor reboiler (2) shell side after compressor (3) pressurization heats up, be condensed as its thermal source, phlegma enters weight-removing column return tank (4), then weight-removing column (1) is returned as reflux through weight-removing column reflux pump (5) small part, rest part is sent to product tank field through water cooler (7) cooling.Weight-removing column bottom product delivers to residual liquid tank through weight-removing column tower reactor pump (6).
This MVR(mechanical steam recompression formula heat pump) technique is except start up, and do not consume steam in weight-removing column normal productive process, only consumption is a small amount of electric.
Solvent treatment weight-removing column adopts two effect rectification process, and heating energy consumption is 3.645MW; Cooling energy consumption is 3.42 MW.
Solvent treatment weight-removing column adopts MVR(mechanical steam recompression formula heat pump) technique, total power consumption is 0.7MW, and according to the level of the current thermal power generation of China, electric heating gain factor gets 3.29, and total heating energy consumption that total power consumption 0.7MW converts is 2.303MW; Cooling energy consumption is 0.65 MW.
Solvent treatment weight-removing column adopts MVR(mechanical steam recompression formula heat pump) technique imitates rectification flow technique relative to double tower two and reduces about 37% and heat energy consumption and about 81% and cool energy consumption.
Claims (4)
1. solvent refining processes in a synthetic rubber production process, it is characterized in that: synthetic rubber production process solvent removes through dehydration tower and enters weight-removing column after Light ends and water and carry out rectifying, working pressure 0.12-0.14MPa.A is absolute pressure value, weight-removing column still temperature is 85-95 DEG C, weight-removing column top gaseous phase enters weight-removing column tower reactor reboiler and is condensed as its thermal source after compressor pressurization heats up, and compressor outlet gaseous pressure is 0.3-0.4MPa.A, temperature is 115-125 DEG C, solvent refining processes adopts MVR mechanical steam recompression formula heat pump using the thermal source as weight-removing column reboiler after weight-removing column top gaseous phase compression supercharging intensification, the technique of employing MVR mechanical steam recompression formula heat pump is: remove the solvent after Light ends and water through dehydration tower, enter in the middle part of weight-removing column, weight-removing column adopts pressure-fired rectifying, working pressure is 0.12-0.14MPa.A, weight-removing column still temperature is 85-95 DEG C, adopt low-pressure steam as weight-removing column driving reboiler thermal source when device is driven, in normal course of operation, weight-removing column top gaseous phase enters weight-removing column tower reactor reboiler shell side after compressor pressurization heats up, be condensed as its thermal source, phlegma enters weight-removing column return tank, then weight-removing column is returned as reflux through weight-removing column reflux pump small part, rest part is sent to product tank field through water cooler cooling, weight-removing column bottom product is pumped to residual liquid tank through weight-removing column tower reactor.
2. solvent refining processes in synthetic rubber production process according to claim 1, is characterized in that: gas phase enters solvent weight-removing column return tank in reboiler after heat exchange condensation after compression; Then be back in weight-removing column by a reflux pump part, another part is as product extraction after water cooler cooling.
3. solvent refining processes in synthetic rubber production process according to claim 1, is characterized in that: solvent removes after Light ends and water through dehydration tower and enters in the middle part of weight-removing column.
4. solvent refining processes in synthetic rubber production process according to claim 1, it is characterized in that: when solvent refining unit is driven, adopt low-pressure steam as weight-removing column reboiler thermal source, in normal course of operation, weight-removing column top gaseous phase enters weight-removing column tower reactor reboiler shell side, as its thermal source after compressor pressurization heats up.
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| CN201510040290.7A CN104592544B (en) | 2015-01-27 | 2015-01-27 | Solvent refining processes in a kind of synthetic rubber production process |
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| CN201510040290.7A CN104592544B (en) | 2015-01-27 | 2015-01-27 | Solvent refining processes in a kind of synthetic rubber production process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105949500A (en) * | 2016-06-07 | 2016-09-21 | 中国石油集团东北炼化工程有限公司吉林设计院 | Waste solvent treatment method for rubber production |
| CN108939590A (en) * | 2018-08-10 | 2018-12-07 | 深圳市瑞升华科技股份有限公司 | Energy-saving ethylene glycol rectification and purification equipment and technique |
| CN111793154A (en) * | 2020-06-30 | 2020-10-20 | 北京诺维新材科技有限公司 | Preparation method and preparation device of rubber |
| CN114432721A (en) * | 2020-11-03 | 2022-05-06 | 北京诺维新材科技有限公司 | Method for concentrating polymer solution and application thereof |
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2015
- 2015-01-27 CN CN201510040290.7A patent/CN104592544B/en active Active
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105949500A (en) * | 2016-06-07 | 2016-09-21 | 中国石油集团东北炼化工程有限公司吉林设计院 | Waste solvent treatment method for rubber production |
| CN105949500B (en) * | 2016-06-07 | 2019-10-25 | 中国石油集团东北炼化工程有限公司吉林设计院 | For the solvent slop processing method in rubber production |
| CN108939590A (en) * | 2018-08-10 | 2018-12-07 | 深圳市瑞升华科技股份有限公司 | Energy-saving ethylene glycol rectification and purification equipment and technique |
| CN111793154A (en) * | 2020-06-30 | 2020-10-20 | 北京诺维新材科技有限公司 | Preparation method and preparation device of rubber |
| CN114432721A (en) * | 2020-11-03 | 2022-05-06 | 北京诺维新材科技有限公司 | Method for concentrating polymer solution and application thereof |
| CN114432721B (en) * | 2020-11-03 | 2023-09-15 | 北京诺维新材科技有限公司 | Polymer solution concentration method and application thereof |
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| CN104592544B (en) | 2017-07-21 |
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