CN102432426A - Method for separating and purifying dichloropropane and dichloropropylene - Google Patents
Method for separating and purifying dichloropropane and dichloropropylene Download PDFInfo
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- CN102432426A CN102432426A CN201110415024XA CN201110415024A CN102432426A CN 102432426 A CN102432426 A CN 102432426A CN 201110415024X A CN201110415024X A CN 201110415024XA CN 201110415024 A CN201110415024 A CN 201110415024A CN 102432426 A CN102432426 A CN 102432426A
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- dichloropropylene
- rectifying tower
- rectifying
- tower
- extraction
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- KNKRKFALVUDBJE-UHFFFAOYSA-N 1,2-dichloropropane Chemical compound CC(Cl)CCl KNKRKFALVUDBJE-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 23
- ZAIDIVBQUMFXEC-UHFFFAOYSA-N 1,1-dichloroprop-1-ene Chemical group CC=C(Cl)Cl ZAIDIVBQUMFXEC-UHFFFAOYSA-N 0.000 title claims abstract description 8
- UOORRWUZONOOLO-OWOJBTEDSA-N (E)-1,3-dichloropropene Chemical compound ClC\C=C\Cl UOORRWUZONOOLO-OWOJBTEDSA-N 0.000 claims abstract description 56
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 238000009835 boiling Methods 0.000 claims abstract description 14
- 238000000746 purification Methods 0.000 claims abstract description 11
- VRTNIWBNFSHDEB-UHFFFAOYSA-N 3,3-dichloroprop-1-ene Chemical group ClC(Cl)C=C VRTNIWBNFSHDEB-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000000203 mixture Substances 0.000 claims description 46
- 238000000605 extraction Methods 0.000 claims description 43
- 239000000463 material Substances 0.000 claims description 34
- 241000282326 Felis catus Species 0.000 claims description 28
- 238000009833 condensation Methods 0.000 claims description 16
- 230000005494 condensation Effects 0.000 claims description 16
- 239000012071 phase Substances 0.000 claims description 16
- 239000002994 raw material Substances 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 13
- 239000007791 liquid phase Substances 0.000 claims description 12
- 239000002699 waste material Substances 0.000 claims description 9
- 238000005516 engineering process Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- UOORRWUZONOOLO-UPHRSURJSA-N (Z)-1,3-dichloropropene Chemical group ClC\C=C/Cl UOORRWUZONOOLO-UPHRSURJSA-N 0.000 claims description 6
- 239000004615 ingredient Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- UOCLXMDMGBRAIB-UHFFFAOYSA-N 1,1,1-trichloroethane Chemical compound CC(Cl)(Cl)Cl UOCLXMDMGBRAIB-UHFFFAOYSA-N 0.000 claims description 3
- XSTXAVWGXDQKEL-UHFFFAOYSA-N Trichloroethylene Chemical compound ClC=C(Cl)Cl XSTXAVWGXDQKEL-UHFFFAOYSA-N 0.000 claims description 3
- 239000000284 extract Substances 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 17
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000006227 byproduct Substances 0.000 abstract description 4
- 238000005660 chlorination reaction Methods 0.000 abstract description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 abstract description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000003905 agrochemical Substances 0.000 description 3
- 239000004229 Alkannin Substances 0.000 description 2
- 239000004230 Fast Yellow AB Substances 0.000 description 2
- 239000004231 Riboflavin-5-Sodium Phosphate Substances 0.000 description 2
- 239000004234 Yellow 2G Substances 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 239000003973 paint Substances 0.000 description 2
- 239000004172 quinoline yellow Substances 0.000 description 2
- 239000002151 riboflavin Substances 0.000 description 2
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000004148 curcumin Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 230000002363 herbicidal effect Effects 0.000 description 1
- 239000004009 herbicide Substances 0.000 description 1
- 239000005645 nematicide Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000001577 simple distillation Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000004149 tartrazine Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of separation and purification of chemical substances, and relates to a method for separating and purifying dichloropropane and dichloropropylene by Dorlone, particularly a method for separating and purifying dichloropropane and dichloropropylene from a byproduct Dorlone discharged from a rectification tower in a propylene high-temperature chlorination production process. The method can effectively utilize the Dorlone, and comprises the steps of 1,2-dichloropropane rectification, high-boiling substance separation, 3,3-dichloropropylene separation and 1,3-dichloropropylene separation. By using the method, the recovery rate of the 1,2-dichloropropane is up to more than 80%, the recovery rate of the 1,3-dichloropropylene is up to more than 90%, the two cis-trans-isomers of the 1,3-dichloropropylene can be well separated, the purity of the recovered products 1,2-dichloropropane and 1,3-dichloropropylene is up to more than 99%, and thus, the method has high economic benefit; and the invention has the advantages of simple overall technique, high separation and purification efficiency, good quality and production environment friendliness.
Description
Technical field:
The invention belongs to chemical substance separates and the purification technique field; Relate to a kind of method by D-D mixture separation and purification propylene dichloride and dichloropropylene; Particularly a kind of in propylene high-temperature chlorination production process from the by product D-D mixture that rectifying tower is discharged the method for separation and purification propylene dichloride and dichloropropylene, can effectively utilize the D-D mixture.
Background technology:
Along with China's production of propylene oxide ability strengthens year by year; Produce the by product D-D mixture that produces in the 3-vinylchlorid process in acrylonitrile-chlorinated method also increases thereupon, contain in the D-D mixture a large amount of 1,2-propylene dichloride, 3; 3-dichloropropylene, 1,3-dichloropropylene and a spot of high boiling material.Because the D-D mixture has nematicide medicament and herbicide action, all be widely used at world wide, be 1 as the staple of agricultural chemicals, the 3-dichloropropylene, a large amount of 1, the 2-propylene dichloride is dispersed in soil and the air, can cause serious pollution to environment; 1, the 2-propylene dichloride can be used for preparing paint, printing ink, thinner and PVC sizing agent as a kind of good organic solvent.Present domestic processing D-D mixture generally is directly to use as paint thinner or agricultural chemicals after the process simple distillation, also has part D-D mixture directly as the boiler oil burning disposal, and this is the root that produces the three wastes, has promptly wasted resource and has also polluted environment.Have report can adopt rectification method with 1,3-dichloropropylene cut purity is increased to more than 90%, is used for the synthetic of agricultural chemicals or other fine-chemical intermediate; The somebody attempts to adopt rectification method with 1 in the D-D mixture, 3-dichloropropylene and 1, and the 2-propylene dichloride separates; But because the component boiling point is close; Be difficult to the warp separation fully of each component is decomposited HCl after the D-D mixture is heated, the column efficiency and the erosion resistance of rectifier unit are had higher requirement.Therefore, reasonable development goes out the approach of effective D-D mixture comprehensive utilization, therefrom isolate respectively purity higher 1,3-dichloropropylene and 1, the 2-propylene dichloride has important environment protection significance and economic benefit.
Summary of the invention:
The objective of the invention is to overcome the shortcoming that prior art exists, seek to provide a kind of by the by product D-D mixture separation and purification propylene dichloride that produces in the propylene high-temperature chlorination reaction process and the technical process of dichloropropylene, to 1; The 2-propylene dichloride recovery reaches more than 80%, and to 1, the 3-dichloropropylene recovery reaches more than 90%; And can be with 1; Two kinds of cis-trans-isomers that the 3-dichloropropylene exists separate 1 of recovery, 2-propylene dichloride and 1 preferably; 3-dichloropropylene product gas purity can reach more than 99%, has high economic benefit.
To achieve these goals, the inventive method comprises 1,2 propylene dichloride rectifying, high boiling material separation, 3,3-dichloropropylene separation and 1; The 3-dichloropropylene separates four steps, will contain 1,2 propylene dichloride, 3 earlier, 3-dichloropropylene, cis 1; 3-dichloropropylene, trans 1, the D-D mixture raw material of 3-dichloropropylene, trieline and trichloroethane gets into first rectifying tower through the pressure pump back of boosting, and the first rectifying tower cat head is provided with condensing surface, and the pressure of being controlled first rectifying tower by vacuum pump is lower than 80kPa; Temperature is controlled at below 80 ℃, and the tower still is provided with reboiler, and the temperature of reboiler is controlled at below 140 ℃; D-D mixture raw material through the first rectifying tower rectifying after, vapour phase gets into drainer by the rectifying tower top extraction after condensation; Partial reflux, it is subsequent use that all the other get into drainer as product 1,2 propylene dichloride extraction; After the separation of first rectifying tower, 1 more than 99%, the 2-propylene dichloride is recovered; The surplus materials raw material is squeezed into second rectifying tower by pressure pump after by the first rectifier bottoms extraction and is carried out rectifying, and the second rectifying tower cat head is provided with condensing surface, and the pressure of being controlled second rectifying tower by vacuum pump is lower than 90kPa; Temperature is controlled at below 90 ℃, and the tower still is provided with reboiler, and its temperature is controlled at below 150 ℃; The surplus materials raw material through second rectifying tower after, liquid phase by the tower of second rectifying tower at the bottom of extraction, high boiling material is separated from blending ingredients; Get into the waste oil storage tank as waste oil, vapour phase gets into drainer by the cat head extraction of second rectifying tower after condensation; Partial reflux gets into the 3rd rectifying tower after the extraction of remaining mixture material; Comprise 3 in the mixture of the cat head extraction of second rectifying tower; 3-dichloropropylene, cis and trans 1, the 3-dichloropropylene, the mixture that will comprise above-mentioned three kinds of components is squeezed into the 3rd rectifying tower by pressure pump; The 3rd rectifying Tata still is provided with reboiler; Its temperature is controlled at below 140 ℃, and tower top temperature is controlled at below 120 ℃, and pressure is 102-160kPa; Mixture through the 3rd rectifying tower rectifying after, vapour phase gets into drainer at cat head after the water cooler condensation, partial reflux, remaining mixture material be as 3, the extraction of 3-dichloropropylene product gets into storage tank; Liquid phase by tower at the bottom of extraction, squeeze in the 4th rectifying tower subsequent use by pressure pump; The material of extraction comprises cis and trans 1 at the bottom of the 3rd rectifying Tata; The 3-dichloropropylene, the mixture that will comprise above-mentioned two kinds of components is squeezed in the 4th rectifying tower by pressure pump, and the 4th rectifying Tata still is provided with reboiler; Temperature is controlled at below 100 ℃; Cat head is provided with vacuum pump, and its temperature is controlled at below 60 ℃, and pressure is lower than 25kPa; Mixture through the 4th rectifying tower rectifying after, vapour phase gets into drainer at cat head after the water cooler condensation, partial reflux, rest materials is as trans 1, the extraction of 3-dichloropropylene product gets into storage tank; Liquid phase extracts as cis 1 at the bottom of by the tower of the 4th rectifying tower, and it is subsequent use that 3-dichloropropylene product gets into storage tank stores.
The present invention compared with prior art according to the nature difference of each component of material, carries out comprehensively the rectifying tower that is used to separate different components; And the means that adopt decompression technology and supercharging technology to combine, can realize separation and purification efficiently 1,2-propylene dichloride and 1; The 3-dichloropropylene is removed high boiling material, preserves the ecological environment; Economize on resources again, accomplish to make the best use of everything, reduce the financial loss in producing; Its overall craft process is simple, and condition control is convenient, and product goes out the rate height, quality better, and production environment is friendly, the conservation resource, economic worth is high, and social benefit is good.
Description of drawings:
Fig. 1 is that equipment of the present invention is formed structure and technical process principle schematic.
Embodiment:
Below through embodiment and combine accompanying drawing to be described further.
Present embodiment will contain 1,2 propylene dichloride, 3 earlier, 3-dichloropropylene, cis 1; 3-dichloropropylene, trans 1, the D-D mixture raw material of 3-dichloropropylene, trieline and trichloroethane gets into the first rectifying tower T101 through the pressure pump P101 back of boosting, and the first rectifying tower cat head is provided with condensing surface E102; The pressure of being controlled first rectifying tower by vacuum pump P200 is lower than 80kPa, and temperature is controlled at below 80 ℃, and the tower still is provided with reboiler E101; The temperature of reboiler is controlled at below 140 ℃, D-D mixture raw material through the first rectifying tower T101 rectifying after, vapour phase is by the rectifying tower top extraction; After condensation, get into drainer U100; Partial reflux, it is subsequent use that all the other get into the U200 drainer as product 1,2 propylene dichloride extraction; After first rectifying tower T101 separation, 1 more than 99%, the 2-propylene dichloride is recovered; The surplus materials raw material is squeezed into the second rectifying tower T102 by pressure pump P103 after the extraction and is carried out rectifying bottom the first rectifying tower T101, the second rectifying tower T102 cat head is provided with condensing surface E103, and the pressure of being controlled the second rectifying tower T102 by vacuum pump P201 is lower than 90kPa; Temperature is controlled at below 90 ℃, and the tower still is provided with reboiler E104, and its temperature is controlled at below 150 ℃; The surplus materials raw material through the second rectifying tower T102 after, liquid phase by the tower of the second rectifying tower T102 at the bottom of extraction, high boiling material is separated from blending ingredients; Get into waste oil storage tank U101 as waste oil, vapour phase gets into drainer U102 by the cat head extraction of the second rectifying tower T102 after condensation; Partial reflux gets into the 3rd rectifying tower T103 after the extraction of remaining mixture material; Comprise 3 in the mixture of the cat head extraction of the second rectifying tower T102; 3-dichloropropylene, cis and trans 1, the 3-dichloropropylene, the mixture that will comprise above-mentioned three kinds of components is squeezed into the 3rd rectifying tower T103 by pressure pump; The 3rd rectifying tower T103 tower still is provided with reboiler E105; Go temperature to be controlled at below 140 ℃, tower top temperature is controlled at below 120 ℃, and pressure is 102-160kPa; Mixture through the 3rd rectifying tower T103 rectifying after, vapour phase gets into drainer U103 at cat head after water cooler E106 condensation, partial reflux, remaining mixture material be as 3, the extraction of 3-dichloropropylene product gets into storage tank U104; Liquid phase by tower at the bottom of extraction, squeeze among the 4th rectifying tower T104 subsequent use by pressure pump P106; The material of extraction comprises cis and trans 1 at the bottom of the 3rd rectifying tower T103 tower; The 3-dichloropropylene, the mixture that will comprise above-mentioned two kinds of components is squeezed among the 4th rectifying tower T104 by pressure pump, and the 4th rectifying tower T104 tower still is provided with reboiler E107; Temperature is controlled at below 100 ℃; Cat head is provided with vacuum pump P202, and temperature is controlled at below 60 ℃, and pressure is lower than 25kPa; Mixture through the 4th rectifying tower T104 rectifying after, vapour phase gets into drainer U105 at cat head after water cooler E108 condensation, partial reflux, rest materials is as trans 1, the extraction of 3-dichloropropylene product gets into storage tank U106; Liquid phase extracts as cis 1 at the bottom of by the tower of the 4th rectifying tower T104, and 3-dichloropropylene product gets into storage tank U107 and stores for future use.
Embodiment 1:
Present embodiment is through heat and material balance to the technical process of D-D mixture separation and purification process, and the operating mode of 40,000 tons of D-D mixtures year is handled in simulation, will comprise mass content and be 82.1% 1; The 2-propylene dichloride, 0.6% 3,3-dichloropropylene, 5.3% cis 1, the 3-dichloropropylene, 10.8% trans 1; The D-D mixture raw material of 3-dichloropropylene and 1.1% high boiling material is squeezed into the first rectifying tower T101 with the 4600kg/hr flow by pressure pump P101, and the first rectifying tower T101 cat head is established condensing surface E100, is 40kPa by vacuum pump P200 control tower top pressure; Temperature is controlled at 67 ℃, and the tower still is established reboiler E101, and temperature is controlled at 118 ℃; Raw material through first rectifying tower after, vapour phase is by the cat head extraction, after condensation, gets into drainer U100; Part is refluxed by pump P102; All the other are as product 1,2 propylene dichloride extraction to product jar U200, and product purity is 99.8%;
After the separation of first rectifying tower, 1 more than 99%, the 2-propylene dichloride is recovered; All the other materials are squeezed into the second rectifying tower T102 by pressure pump P103 after the extraction at the bottom of by tower; The second rectifying tower cat head is established condensing surface E103, is 40kPa by vacuum pump P201 control tower top pressure, and temperature is controlled at 77 ℃; The tower still is established reboiler E104, and temperature is controlled at 131 ℃; Raw material through the second rectifying tower T102 after; Liquid phase by tower at the bottom of extraction, high boiling material is separated from blending ingredients, by pressure pump P104 as among the waste oil input waste oil storage tank U101; Vapour phase is by the cat head extraction; After condensation, get into drainer U102, part refluxes via pressure pump P105, gets into the 3rd rectifying tower T103 after all the other extraction; After second rectifying tower T102 separation, all high boiling material separate cat head mass flow of materials 760kg/hr at the bottom of tower; Wherein 3,3 dichloropropylene content are 3.1%, 1; 2-propylene dichloride content is 0.6%; Cis 1,3-dichloropropylene content be 30.8% and 65.5% trans 1, the 3-dichloropropylene;
The second rectifying tower cat head production mainly comprises 3,3-dichloropropylene and cis, trans 1,3-dichloropropylene and a spot of 1,2-propylene dichloride; The partial confounding compound is squeezed among the 3rd rectifying tower T103 by pressure pump P105, and the 3rd rectifying Tata still is established reboiler E105, and temperature is controlled at 131 ℃, and tower top temperature is controlled to be 113 ℃; Pressure 152kPa, mixture through the 3rd rectifying tower T103 after, vapour phase gets into drainer U103 at cat head after water cooler E106 condensation; Part is refluxed by pressure pump P107, and all the other contain 3,3-dichloropropylene, cis and trans 1; 3-dichloropropylene mixture gets into a jar U104 by the cat head extraction, and wherein 3,3-dichloropropylene concentration is 73.5%; Liquid phase by tower at the bottom of extraction, the production mass rate is 728kg/hr, wherein cis 1,3-dichloropropylene content 32.2% is trans 1,3-dichloropropylene content 67.8%, this mixture is squeezed among the 4th rectifying tower T104 subsequent use by pressure pump P106;
Production mainly comprises cis and trans 1,3-dichloropropylene at the bottom of the 3rd rectifying Tata.The mixture that will comprise these two kinds of components is squeezed among the 4th rectifying tower T104 by pressure pump P103, and the tower still of the 4th rectifying tower T104 is established reboiler E107, and temperature is controlled at 90 ℃; Cat head is established vacuum pump P202, and temperature is controlled at 47 ℃, pressure 13.3kPa; Raw material through the 4th rectifying tower T104 rectifying after, vapour phase gets into drainer U105 at cat head after water cooler E108 condensation, part is refluxed by pressure pump P108, all the other are as trans 1, the extraction of 3-dichloropropylene product gets among the storage tank U106, purity is 99.9%; Liquid phase by tower at the bottom of as cis 1,3-dichloropropylene product is got among the storage tank U107 by pressure pump P109 extraction, purity is 99.9%.
Present embodiment is according to the nature difference of each component, the rectifying tower that is used to separate different components carried out comprehensively, and the means that adopt decompression technology and supercharging technology to combine; Remove 3,3-dichloropropylene and high boiling material are realized separation and purification efficiently 1; 2-propylene dichloride and 1,3-dichloropropylene, product 1; 2-propylene dichloride and cis, trans 1,3-dichloropropylene purity all reaches more than 99%.
Claims (1)
1. the separation purification method of propylene dichloride and dichloropropylene, it is characterized in that comprising 1,2 propylene dichloride rectifying, high boiling material separate, 3, the 3-dichloropropylene separates and 1; The 3-dichloropropylene separates four steps, and 1,2 propylene dichloride rectification process is: will contain 1 earlier; 2 propylene dichlorides, 3,3-dichloropropylene, cis 1,3-dichloropropylene, trans 1; The D-D mixture raw material of 3-dichloropropylene, trieline and trichloroethane gets into first rectifying tower after boosting through pressure pump, and the first rectifying tower cat head is provided with condensing surface, and the pressure of being controlled first rectifying tower by vacuum pump is lower than 80kPa; Temperature is controlled at below 80 ℃, and the tower still is provided with reboiler, and the temperature of reboiler is controlled at below 140 ℃; D-D mixture raw material through the first rectifying tower rectifying after, vapour phase gets into drainer by the rectifying tower top extraction after condensation; Partial reflux, it is subsequent use that all the other get into drainer as product 1,2 propylene dichloride extraction; The high boiling material separating technology is: after separating through first rectifying tower, and 1 more than 99%, the 2-propylene dichloride is recovered; The surplus materials raw material is squeezed into second rectifying tower by pressure pump after by the first rectifier bottoms extraction and is carried out rectifying, and the second rectifying tower cat head is provided with condensing surface, and the pressure of being controlled second rectifying tower by vacuum pump is lower than 90kPa; Temperature is controlled at below 90 ℃, and the tower still is provided with reboiler, and its temperature is controlled at below 150 ℃; The surplus materials raw material through second rectifying tower after, liquid phase by the tower of second rectifying tower at the bottom of extraction, high boiling material is separated from blending ingredients; Get into the waste oil storage tank as waste oil, vapour phase gets into drainer by the cat head extraction of second rectifying tower after condensation; Partial reflux gets into the 3rd rectifying tower after the extraction of remaining mixture material; 3,3-dichloropropylene separating technology is: comprise 3 in the mixture of the cat head extraction of second rectifying tower, 3-dichloropropylene, cis and trans 1; The 3-dichloropropylene; The mixture that will comprise above-mentioned three kinds of components is squeezed into the 3rd rectifying tower by pressure pump, and the 3rd rectifying Tata still is provided with reboiler, and its temperature is controlled at below 140 ℃; Tower top temperature is controlled at below 120 ℃, and pressure is 102-160kPa; Mixture through the 3rd rectifying tower rectifying after, vapour phase gets into drainer at cat head after the water cooler condensation, partial reflux, remaining mixture material be as 3, the extraction of 3-dichloropropylene product gets into storage tank; Liquid phase by tower at the bottom of extraction, squeeze in the 4th rectifying tower subsequent use by pressure pump; 1,3-dichloropropylene separating technology is: the material of extraction comprises cis and trans 1,3-dichloropropylene at the bottom of the 3rd rectifying Tata; The mixture that will comprise above-mentioned two kinds of components is squeezed in the 4th rectifying tower by pressure pump; The 4th rectifying Tata still is provided with reboiler, and temperature is controlled at below 100 ℃, and cat head is provided with vacuum pump; Its temperature is controlled at below 60 ℃, and pressure is lower than 25kPa; Mixture through the 4th rectifying tower rectifying after, vapour phase gets into drainer at cat head after the water cooler condensation, partial reflux, rest materials is as trans 1, the extraction of 3-dichloropropylene product gets into storage tank; Liquid phase extracts as cis 1 at the bottom of by the tower of the 4th rectifying tower, and it is subsequent use that 3-dichloropropylene product gets into storage tank stores.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110415024.XA CN102432426B (en) | 2011-12-14 | 2011-12-14 | Method for separating and purifying dichloropropane and dichloropropylene |
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| CN201110415024.XA CN102432426B (en) | 2011-12-14 | 2011-12-14 | Method for separating and purifying dichloropropane and dichloropropylene |
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| CN102432426A true CN102432426A (en) | 2012-05-02 |
| CN102432426B CN102432426B (en) | 2013-11-06 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104387226A (en) * | 2014-11-20 | 2015-03-04 | 闾正军 | Purification method of dichloropropene |
| CN107879891A (en) * | 2017-11-20 | 2018-04-06 | 天津辰力工程设计有限公司 | A kind of method that dichloropropane and dichloropropylene are purified using DD mixtures |
| CN111807925A (en) * | 2020-07-23 | 2020-10-23 | 山东海益化工科技有限公司 | D-D mixture rectification separation process |
| CN111848334A (en) * | 2020-07-30 | 2020-10-30 | 江苏扬农化工集团有限公司 | Method for treating by-products in process of preparing chloropropene by chlorination of propylene |
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| CN1282724A (en) * | 1999-07-31 | 2001-02-07 | 崔英武 | Process for extracting dichloropropene from D-D mixture |
| CN1847205A (en) * | 2005-03-31 | 2006-10-18 | 沈阳化工学院 | Method of separating 1,2-dichloropropane with DD mixture |
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- 2011-12-14 CN CN201110415024.XA patent/CN102432426B/en active Active
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| GB1231127A (en) * | 1968-12-18 | 1971-05-12 | ||
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104387226A (en) * | 2014-11-20 | 2015-03-04 | 闾正军 | Purification method of dichloropropene |
| CN104387226B (en) * | 2014-11-20 | 2017-05-17 | 闾正军 | Purification method of dichloropropene |
| CN107879891A (en) * | 2017-11-20 | 2018-04-06 | 天津辰力工程设计有限公司 | A kind of method that dichloropropane and dichloropropylene are purified using DD mixtures |
| CN107879891B (en) * | 2017-11-20 | 2020-09-29 | 天津辰力工程设计有限公司 | Method for purifying dichloropropane and dichloropropene by using DD (DD) mixing agent |
| CN111807925A (en) * | 2020-07-23 | 2020-10-23 | 山东海益化工科技有限公司 | D-D mixture rectification separation process |
| CN111807925B (en) * | 2020-07-23 | 2021-11-02 | 山东海益化工科技有限公司 | D-D mixture rectification separation process |
| WO2022016631A1 (en) * | 2020-07-23 | 2022-01-27 | 山东海益化工科技有限公司 | Rectification separation process for d-d mixture |
| CN111848334A (en) * | 2020-07-30 | 2020-10-30 | 江苏扬农化工集团有限公司 | Method for treating by-products in process of preparing chloropropene by chlorination of propylene |
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