CN101450935B - Purification process for producing propylene oxide by chlorohydrination method - Google Patents
Purification process for producing propylene oxide by chlorohydrination method Download PDFInfo
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- CN101450935B CN101450935B CN2007101153220A CN200710115322A CN101450935B CN 101450935 B CN101450935 B CN 101450935B CN 2007101153220 A CN2007101153220 A CN 2007101153220A CN 200710115322 A CN200710115322 A CN 200710115322A CN 101450935 B CN101450935 B CN 101450935B
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- propylene oxide
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Abstract
The invention provides a technology for producing and purifying propylene oxide. The technology is characterized in that the crude propylene oxide undergoes rectification and purification through passing through three levels of rectifying towers. The technology of three-level rectification effectively recycle the propylene oxide in the byproducts and water phase through reasonably control of a first two levels of rectifying parameters and a further separation and treatment on a last level of rectifying pot liquid, thereby improving the yield of the product and lowering the consumption. The technology has simple procedures, easy operation and low investment.
Description
Technical field
The present invention relates to the purifying technique of propylene oxide in the producing propylene oxide by chlorohydrination method technology.
Background technology
Domestic technology with producing propylene oxide by chlorohydrination method, what the propylene oxide purification phase adopted is two-stage rectification.Internal structure is similar, and process control parameter is also different, and purpose is in order to improve product yield, to reduce the propylene oxide that propylene dichloride (DCP) and aqueous phase are carried secretly.After back one-level rectifying was finished, the rectifying tower bottoms produced byproduct through after the condensation, handled at a low price.Facts have proved at back one-level rectifying tower bottoms and still contain minor amount of propylene oxide, this part product or be entrained in propylene dichloride and fall or be entrained in aqueous phase to enter sewage work when byproduct for treatment.
Summary of the invention
Technical problem to be solved by this invention provides a kind of purifying technique of improved producing propylene oxide by chlorohydrination method, improves the propylene oxide yield, reduces consuming.
The purifying technique of producing propylene oxide by chlorohydrination method of the present invention is characterized in that crude propene oxide carries out rectification and purification by three grades of rectifying tower successively.
Three grades of rectification process of the present invention carry out further separating treatment by two stage rectification parameter before the reasonable control and with back one-level rectifying tower bottoms, and efficient recovery is present in the propylene oxide of byproduct and aqueous phase, improves product yield, reduces consuming.
Whole technology mainly comprises one-level rectifying tower, one-level reboiler, two-stage rectification tower, secondary reboiler, three grades of rectifying tower, three grades of reboilers and respective pump, control instruments, condenser.The discharging of first step rectifying tower is smart propylene oxide, and the second stage, third stage discharging are crude propene oxide, needs to beat to be recycled to the first step and to carry out rectifying again.Each grade rectifying tower all is furnished with corresponding reboiler, condenser, cat head tower still discharging pump.The charging of second and third grade rectifying tower is from the tower still discharging of upper level, the temperature height, and consumes energy is low, and temperature controlling range is big at the bottom of the two-stage rectification Tata.
The rectification process condition of three grades of rectifying tower is respectively: 35 ± 2 ℃ of one-level rectifying tower tower top temperatures, 60 ± 10 ℃ of column bottom temperatures, reflux ratio 〉=2.2,40 ± 3 ℃ of two-stage rectification column overhead temperature, column bottom temperature 80-92 ℃, 65 ± 5 ℃ of reflux ratio 〉=1, three grade rectifying tower tower top temperatures, 83 ± 3 ℃ of column bottom temperatures, reflux ratio 〉=1.
Advantage of the present invention:
1, simple, simple to operate, the less investment of technology has made full use of the heat of previous stage, has reduced energy consumption.
2, through three grades of rectifying, the propylene oxide in the byproduct reduces gradually, efficient recovery propylene oxide, reduced environmental protection pressure simultaneously.
3, temperature controlling range is big at the bottom of the two-stage rectification Tata.
Description of drawings
Fig. 1 is a process flow sheet of the present invention;
Among the figure: 1, one-level rectifying tower 2, one-level reboiler 3, one-level tower still pump 4,6,7,15,17,18,24,26,27. flowrate control valve group 5, one-level discharging pump 8, first-stage condenser 9, one-level return tank 10, discharging condenser 11, basin 12, two-stage rectification tower 13, secondary reboiler 14, secondary tower still pump 16, secondary reflux pump 19, secondary condenser 20, secondary return tank 21, three grades of rectifying tower 22, three grades of reboilers 23, three grades of tower still pumps 25, three grades of reflux pumps 28, three grades of condensers 29, three grades of return tanks 30, byproduct condenser 31, separating tank
Embodiment
The present invention is further illustrated below in conjunction with Fig. 1.
Contain propylene oxide 65-80% (mass percent) crude propene oxide (PO) and entered after dominant discharge by pump and carry out rectifying separation in the one-level rectifying tower 1, tower still temperature is controlled at 60 ± 10 ℃, and tower top temperature is controlled at 35 ± 2 ℃.Smart PO steams from cat head, PO liquid enters PO return tank 9 after first-stage condenser 8 condensations, by 5 outputs of one-level discharging pump, by the phegma of dominant discharge as the one-level rectifying tower, discharging shows flow by variable valve, under meter control, again through the laggard PO basin 11 of PO condenser 10 coolings.Contain water (accounting for 26%), PO (accounting for 41%), DCP (accounting for 11%) and propionic aldehyde PA components such as (accounting for 15%) and enter two-stage rectification tower 12 by one-level kettle liquid column still pump 3, be heated to 80-92 ℃ for two-stage rectification tower reboiler 13 with steam, tower top temperature is controlled at 40 ± 3 ℃, volatile components PO, PA enter the thick PO return tank 20 of secondary after 19 condensations of cat head process condenser, a part by reflux pump 16 by dominant discharge as two-stage rectification tower phegma, another part is regulated control by valve group 17, gets to one-level rectifying tower 1 as secondary feeds.Contain water (accounting for 32%), PO (accounting for 3%), DCP (accounting for 41%) and PA (accounting for 12%) component enter three grades of rectifying tower 21 by secondary kettle liquid column still pump 14, be heated to 83 ± 3 ℃ for three grades of rectifying tower reboilers 22 with steam, tower top temperature is controlled at 65 ± 5 ℃, volatile components PO, PA enters three grades of thick PO return tanks 29 after 28 condensations of cat head process condenser, a part by pump 25 by dominant discharge as three grades of rectifying tower 21 phegmas, another part is by regulating control through valve group 27, get to the smart tower level of one-level rectifying tower 1 as charging once more or get to thick PO return tank 20 recirculation of two-stage rectification tower, tower still heavy constituent DCP (accounting for 42%) and water (accounting for 44%) etc. enter DCP separator 31 by pump 23 after condenser 30 condensations separates.Propylene oxide from one-level to three grade tower bottoms reduces gradually, and whole process is continuous.
The technical parameter of above-mentioned technology is:
35 ± 2 ℃ of one-level rectifying tower tower top temperatures, 60 ± 10 ℃ of column bottom temperatures, reflux ratio 〉=2.2,40 ± 3 ℃ of two-stage rectification column overhead temperature, column bottom temperature 80-92 ℃, reflux ratio 〉=1,65 ± 5 ℃ of three grades of rectifying tower tower top temperatures, 83 ± 3 ℃ of column bottom temperatures, reflux ratio 〉=1.
Rectifying tower progression and propylene oxide yield such as following table:
| Rectifying tower progression | 1 grade | 2 grades | Three grades |
| The propylene oxide yield | 83％ | 97％ | 99.5％ |
Claims (1)
1. the purifying technique of a producing propylene oxide by chlorohydrination method, it is characterized in that crude propene oxide carries out rectification and purification by three grades of rectifying tower successively, the rectification process condition of three grades of rectifying tower is respectively: 35 ± 2 ℃ of one-level rectifying tower tower top temperatures, 60 ± 10 ℃ of column bottom temperatures, reflux ratio 〉=2.2,40 ± 3 ℃ of two-stage rectification column overhead temperature, column bottom temperature 80-92 ℃, 65 ± 5 ℃ of reflux ratio 〉=1, three grade rectifying tower tower top temperatures, 83 ± 3 ℃ of column bottom temperatures, reflux ratio 〉=1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007101153220A CN101450935B (en) | 2007-12-08 | 2007-12-08 | Purification process for producing propylene oxide by chlorohydrination method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007101153220A CN101450935B (en) | 2007-12-08 | 2007-12-08 | Purification process for producing propylene oxide by chlorohydrination method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101450935A CN101450935A (en) | 2009-06-10 |
| CN101450935B true CN101450935B (en) | 2011-05-11 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2007101153220A Expired - Fee Related CN101450935B (en) | 2007-12-08 | 2007-12-08 | Purification process for producing propylene oxide by chlorohydrination method |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942539B (en) * | 2012-11-09 | 2014-10-15 | 南阳中聚天冠低碳科技有限公司 | Epoxy propane recovery and purification process |
| CN105399606B (en) * | 2015-12-18 | 2018-02-02 | 山东蓝星东大化工有限责任公司 | Technique for recovering propylene in expoxy propane subtractive process |
| CN106397362B (en) * | 2016-09-06 | 2018-05-01 | 南京英斯派工程技术有限公司 | Deamination and the method and apparatus of propylene oxide, propylene is recycled in a kind of propylene oxide unit |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1389461A (en) * | 2001-12-18 | 2003-01-08 | 锦化化工（集团）有限责任公司 | Chlorohydrination process of producing epoxypropane and its production equipment |
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- 2007-12-08 CN CN2007101153220A patent/CN101450935B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1389461A (en) * | 2001-12-18 | 2003-01-08 | 锦化化工（集团）有限责任公司 | Chlorohydrination process of producing epoxypropane and its production equipment |
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| Publication number | Publication date |
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| CN101450935A (en) | 2009-06-10 |
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Granted publication date: 20110511 Termination date: 20171208 |