CN103360620A - Method for recovering hexane from production of high-density polyethylene - Google Patents
Method for recovering hexane from production of high-density polyethylene Download PDFInfo
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- CN103360620A CN103360620A CN2012100849090A CN201210084909A CN103360620A CN 103360620 A CN103360620 A CN 103360620A CN 2012100849090 A CN2012100849090 A CN 2012100849090A CN 201210084909 A CN201210084909 A CN 201210084909A CN 103360620 A CN103360620 A CN 103360620A
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Abstract
The invention relates to a method for recovering hexane from the production of high-density polyethylene, and mainly aiming to solve the problems on the loss of the hexane and the pollution of the discharged hexane to environment in the prior art. The method comprises the following steps: (a) feeding hexane flow 5 into a catalyst preparation tank 1, and mixing the hexane flow 5 with a catalyst, wherein a prepared catalyst 9 is obtained at the bottom of the catalyst preparation tank 1, and a hexane exhaust 6 is obtained on the top of the catalyst preparation tank 1; (b) feeding the hexane exhaust 6 into a suction tank 3 of a compressor to obtain a hexane exhaust 10 with pressure being stabilized; and (c) feeding the hexane exhaust 10 into a gas compressor 4, increasing the pressure to obtain a high-pressure hexane exhaust 11, and feeding the high-pressure hexane exhaust 11 into a subsequent drying gas system. Due to adoption of the technical scheme, the problems are well solved. The method disclosed by the invention can be applied to the industrial production on the recovery of the hexane from the production of the high-density polyethylene.
Description
Technical field
The present invention relates to the recovery method of hexane in a kind of high density polyethylene(HDPE) production process.
Background technology
High density polyethylene is that a kind of degree of crystallinity is high, nonpolar thermoplastic resin, and purposes is very extensive.Document CN200910090649.6 discloses a kind of preparation method of superfine polyethylene powder, and document CN 200910156643.4 discloses a kind of for the preparation of poly double series reactor process.When prior art is produced high density polyethylene(HDPE), in its catalyst preparation and charging system, the technical scheme that the hexane discharging is taked comprises: the equipment such as hexane drain tank, drain tank condenser, hexane sealed can, technical process is: hexane is discharged pneumatic transmission hexane drain tank, use the drain tank condenser condenses, a small amount of uncooled hexane discharging pneumatic transmission enters the hexane sealed can, and the high altitude discharge pipe by this tank is discharged into this part uncooled hexane discharging gas in the atmospheric environment.But, adopt this operational path, there is the hexane loss of material, the problem of the hexane contaminate environment of discharging.
In addition, in the flow process of the existing HDPE device dry gas recycle system, compressor suction tank and gas compressor have been comprised.Existing gas compressor need be used N
2Supercharging is with the pressure-stabilisation of keeping system.
Summary of the invention
Technical problem to be solved by this invention is that prior art exists the hexane loss of material, and the problem of the hexane contaminate environment of discharging provides the recovery method of hexane in a kind of new high density polyethylene(HDPE) production process.The method can make hexane be in and not be discharged in the closed system in the environment, and hexane is fully utilized.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: the recovery method of hexane in a kind of high density polyethylene(HDPE) production process may further comprise the steps:
A) hexane streams 5 enters catalyst preparation tank 1 and catalyst mix, obtains preparing the catalyzer 9 of finishing at the bottom of the tank, and tank deck obtains hexane discharging gas 6;
B) hexane discharging gas 6 enters compressor suction tank 3, obtains the hexane discharging gas 10 after the voltage stabilizing;
C) hexane discharging gas 10 enters gas compressor 4, obtains high pressure hexane discharging gas 11 after the supercharging and enters follow-up dry gas system.
In the technique scheme, catalyst preparation tank 1 service temperature is 0 ~ 120 ℃, and preferable range is 0 ~ 100 ℃, and more preferably scope is 10 ~ 60 ℃; Working pressure is 0.0 ~ 0.8MPaG, and preferable range is 0.0 ~ 0.5MPaG, and more preferably scope is 0.0 ~ 0.2MPaG.Compressor suction tank 3 service temperatures are-20 ~ 90 ℃, and preferable range is-15 ~ 60 ℃, and more preferably scope is-10 ~ 40 ℃; Working pressure is 0.0 ~ 0.10MPaG, and preferable range is 0.0 ~ 0.05MPaG, and more preferably scope is 0.0 ~ 0.01MPaG.Gas compressor 4 service temperatures are-20 ~ 120 ℃, and preferable range is-15 ~ 100 ℃, and more preferably scope is-10 ~ 90 ℃; Working pressure is 0.0 ~ 0.80MPaG, and preferable range is 0.0 ~ 0.60MPaG, and more preferably scope is 0.0 ~ 0.40MPaG.
In the technique scheme, preferred version is that hexane discharging gas 6 is introduced into hexane condenser 2, obtains gaseous stream 7 and liquid phase stream 8 after the condensation; Logistics 8 return catalizer preparing tank recycles; Logistics 7 enters compressor suction tank 3.Wherein, hexane condenser 2 service temperatures are-20 ~ 120 ℃, and preferable range is-15 ~ 100 ℃, and more preferably scope is-10 ~ 60 ℃.
The inventive method, in the catalyst preparation cellular system, the hexane material is in closed system and is not discharged among the atmospheric environment, makes the hexane quantity discharged be reduced to 0.00 kg/tonne of HDPE by 0.05 kg/tonne of HDPE of prior art, has solved the problem of environmental pollution.Simultaneously, the hexane closed circulation is used, hexane is fully used, reduced the N of gas compressor
2Consumption has been obtained preferably technique effect.
Description of drawings
Fig. 1 is the prior art schematic flow sheet.
Fig. 2 is the inventive method schematic flow sheet.
Among Fig. 1 and among Fig. 2,1 is the catalyst preparation tank, 2 is the hexane condenser, 3 is the compressor suction tank, 4 is gas compressor, 5 is hexane streams, and 6 is hexane discharging gas, and 7 is the gaseous stream that obtains after 2 condensations of hexane condenser, 8 are the liquid phase stream through obtaining after 2 condensations of hexane condenser, 9 for preparing the catalyzer of finishing, and 10 is hexane discharging gas, and 11 is high pressure hexane discharging gas, 12 is the hexane drain tank, 13 is the drain tank condenser, and 14 is the hexane sealed can, and 15 is hexane drain tank overhead stream, 16 is the gaseous stream that obtains after the drain tank condenser condenses, 17 is the liquid phase stream that obtains after the drain tank condenser condenses, and 18 is hexane drain tank bottoms, and 19 is the logistics of hexane sealed can high altitude discharge.
Among Fig. 1, hexane streams 5 enters catalyst preparation tank 1 and catalyst mix, obtains preparing the catalyzer 9 of finishing at the bottom of the tank, and tank deck obtains hexane discharging gas 6.Hexane discharging gas 6 enters hexane drain tank 12, obtains overhead stream 15 and bottoms 18, and logistics 18 is sent outside as sump oil, processes in addition.Overhead stream 15 enters drain tank condenser 13, obtains gaseous stream 16 and liquid phase stream 17 after the condensation, and gaseous stream 16 is a small amount of uncooled hexane discharging gas.Logistics 16 enters hexane sealed can 14, and the high altitude discharge pipe 19 by this tank is discharged into this part uncooled hexane discharging gas in the atmospheric environment.
Among Fig. 2, hexane streams 5 enters catalyst preparation tank 1 and catalyst mix, obtains preparing the catalyzer 9 of finishing at the bottom of the tank, and tank deck obtains hexane discharging gas 6.Hexane discharging gas 6 enters compressor suction tank 3, obtains the hexane discharging gas 10 after the voltage stabilizing.Hexane discharging gas 10 enters gas compressor 4, obtains high pressure hexane discharging gas 11 after the supercharging and enters follow-up dry gas system.
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
Adopt flow process shown in Figure 2, hexane condenser hexane discharging gas service temperature is reduced to-8 ℃ by 35 ℃; Working pressure is 0.01MPaG.Catalyst preparation tank service temperature is 35 ℃; Working pressure is 0.01MPaG.Compressor suction tank service temperature is-8 ℃; Working pressure is 0.001MPaG; The gas compressor service temperature rises to 90 ℃ for-8 ℃; Working pressure is pressurized to 0.40MPaG by 0.001MPaG.Adopt the present invention to utilize existing compressor suction tank and gas compressor equipment, hexane is discharged gas directly send the hexane condenser condenses, the liquid phase return catalizer preparing tank recycling of the part that is condensed, the technical process that enters the dry gas system after the hexane discharging pneumatic transmission compressor suction tank supercharging of uncooled part, make hexane Reducing exhaust emission to 0.00 kg/tonne HDPE, reduced simultaneously N
20.05 kg/tonne of HDPE of consumption.
[embodiment 2]
With [embodiment 1], adopt Fig. 2 flow process, just operational condition changes, and hexane condenser hexane discharging gas service temperature is reduced to-6 ℃ by 38 ℃; Working pressure is 0.012MPaG.Catalyst preparation tank service temperature is 38 ℃; Working pressure is 0.012MPaG.Compressor suction tank service temperature is-6 ℃; Working pressure is 0.002MPaG; The gas compressor service temperature rises to 90 ℃ for-6 ℃; Working pressure is pressurized to 0.40MPaG by 0.002MPaG.Adopt the present invention to utilize existing compressor suction tank and gas compressor equipment, hexane is discharged gas directly send the hexane condenser condenses, the liquid phase return catalizer preparing tank recycling of the part that is condensed, the technical process that enters the dry gas system after the supercharging of uncooled hexane discharging pneumatic transmission compressor suction tank, make hexane Reducing exhaust emission to 0.00 kg/tonne HDPE, reduced simultaneously N
20.05 kg/tonne of HDPE of consumption.
[embodiment 3]
With [embodiment 1], adopt Fig. 2 flow process, just operational condition changes, and hexane condenser hexane discharging gas service temperature is reduced to-5 ℃ by 45 ℃; Working pressure is 0.015MPaG.Catalyst preparation tank service temperature is 45 ℃; Working pressure is 0.015MPaG.Compressor suction tank service temperature is-5 ℃; Working pressure is 0.003MPaG; The gas compressor service temperature rises to 90 ℃ for-5 ℃; Working pressure is pressurized to 0.40MPaG by 0.003MPaG.Adopt the present invention to utilize existing compressor suction tank and gas compressor equipment, hexane is discharged gas directly send the hexane condenser condenses, the liquid phase return catalizer preparing tank recycling of the part that is condensed, the technical process that enters the dry gas system after the hexane discharging pneumatic transmission compressor suction tank supercharging of uncooled part, make hexane Reducing exhaust emission to 0.00 kg/tonne HDPE, reduced simultaneously N
20.05 kg/tonne of HDPE of consumption.
[comparative example 1]
Adopt flow process shown in Figure 1, prior art hexane condenser hexane discharging gas service temperature is reduced to-8 ℃ by 35 ℃; Working pressure is 0.01MPaG.Catalyst preparation tank service temperature is 35 ℃; Working pressure is 0.01MPaG.Compressor suction tank service temperature is-8 ℃; Working pressure is 0.001MPaG; The gas compressor service temperature rises to 90 ℃ for-8 ℃; Working pressure is pressurized to 0.40MPaG by 0.001MPaG.Among the hexane discharging pneumatic transmission atmospheric environment of uncooled part, the hexane quantity discharged is 0.05 kg/tonne of HDPE.
Claims (8)
1. the recovery method of hexane in the high density polyethylene(HDPE) production process may further comprise the steps:
A) hexane streams 5 enters catalyst preparation tank 1 and catalyst mix, obtains preparing the catalyzer 9 of finishing at the bottom of the tank, and tank deck obtains hexane discharging gas 6;
B) hexane discharging gas 6 enters compressor suction tank 3, obtains the hexane discharging gas 10 after the voltage stabilizing;
C) hexane discharging gas 10 enters gas compressor 4, obtains high pressure hexane discharging gas 11 after the supercharging and enters follow-up dry gas system.
2. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 1 is characterized in that catalyst preparation tank 1 service temperature is 0 ~ 120 ℃, and working pressure is 0.0 ~ 0.8MPaG; Compressor suction tank 3 service temperatures are-20 ~ 90 ℃, and working pressure is 0.0 ~ 0.10MPaG; Gas compressor 4 service temperatures are-20 ~ 120 ℃, and working pressure is 0.0 ~ 0.80MPaG.
3. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 2 is characterized in that catalyst preparation tank 1 service temperature is 0 ~ 100 ℃, and working pressure is 0.0 ~ 0.5MPaG; Compressor suction tank 3 service temperatures are-15 ~ 60 ℃, and working pressure is 0.0 ~ 0.05MPaG; Gas compressor 4 service temperatures are-15 ~ 100 ℃, and working pressure is 0.0 ~ 0.60MPaG.
4. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 3 is characterized in that catalyst preparation tank 1 service temperature is 10 ~ 60 ℃, and working pressure is 0.0 ~ 0.2MPaG; Compressor suction tank 3 service temperatures are-10 ~ 40 ℃, and working pressure is 0.0 ~ 0.01MPaG; Gas compressor 4 service temperatures are-10 ~ 90 ℃, and working pressure is 0.0 ~ 0.40MPaG.
5. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 1 is characterized in that hexane discharging gas 6 is introduced into hexane condenser 2, obtains gaseous stream 7 and liquid phase stream 8 after the condensation; Logistics 8 return catalizer preparing tank recycles; Logistics 7 enters compressor suction tank 3.
6. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 5 is characterized in that hexane condenser 2 service temperatures are-20 ~ 120 ℃, and working pressure is 0.0 ~ 1.0MPaG.
7. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 6 is characterized in that hexane condenser 2 service temperatures are-15 ~ 100 ℃, and working pressure is 0.0 ~ 0.8MPaG.
8. the recovery method of hexane in the high density polyethylene(HDPE) production process according to claim 7 is characterized in that hexane condenser 2 service temperatures are-10 ~ 60 ℃, and working pressure is 0.0 ~ 0.6MPaG.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104448383A (en) * | 2014-11-24 | 2015-03-25 | 天华化工机械及自动化研究设计院有限公司 | Recovering, washing and steam-stripping method for ultra-high molecular weight polyethylene hexene |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2592814A (en) * | 1947-12-20 | 1952-04-15 | Du Pont | Isolation of chlorosulfonated polymers of ethylene from solution |
| CN201915053U (en) * | 2010-12-20 | 2011-08-03 | 大连欧科膜技术工程有限公司 | Hydrocarbon recovery device used in polyethylene production process |
-
2012
- 2012-03-28 CN CN201210084909.0A patent/CN103360620B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2592814A (en) * | 1947-12-20 | 1952-04-15 | Du Pont | Isolation of chlorosulfonated polymers of ethylene from solution |
| CN201915053U (en) * | 2010-12-20 | 2011-08-03 | 大连欧科膜技术工程有限公司 | Hydrocarbon recovery device used in polyethylene production process |
Non-Patent Citations (1)
| Title |
|---|
| 闫庆贺: ""低压聚乙烯装置己烷回收系统操作能力分析"", 《黑龙江石油化工》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104448383A (en) * | 2014-11-24 | 2015-03-25 | 天华化工机械及自动化研究设计院有限公司 | Recovering, washing and steam-stripping method for ultra-high molecular weight polyethylene hexene |
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