CN104926581A - Process flow for dry separation of propylene and hydrogen chloride - Google Patents
Process flow for dry separation of propylene and hydrogen chloride Download PDFInfo
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- CN104926581A CN104926581A CN201410119088.9A CN201410119088A CN104926581A CN 104926581 A CN104926581 A CN 104926581A CN 201410119088 A CN201410119088 A CN 201410119088A CN 104926581 A CN104926581 A CN 104926581A
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- Prior art keywords
- propylene
- hydrogenchloride
- tower
- hydrogen chloride
- temperature
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 94
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 86
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 86
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 71
- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000000926 separation method Methods 0.000 title claims abstract description 21
- 238000005057 refrigeration Methods 0.000 claims abstract description 18
- 230000006835 compression Effects 0.000 claims abstract description 14
- 238000007906 compression Methods 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 238000005516 engineering process Methods 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 5
- 238000002309 gasification Methods 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 238000007701 flash-distillation Methods 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 239000003507 refrigerant Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 238000004821 distillation Methods 0.000 abstract 4
- 238000009834 vaporization Methods 0.000 abstract 1
- 230000008016 vaporization Effects 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 13
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- 238000005660 chlorination reaction Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 239000004230 Fast Yellow AB Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 description 2
- KNKRKFALVUDBJE-UHFFFAOYSA-N 1,2-dichloropropane Chemical compound CC(Cl)CCl KNKRKFALVUDBJE-UHFFFAOYSA-N 0.000 description 2
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical group ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002151 riboflavin Substances 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000004229 Alkannin Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000004172 quinoline yellow Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000004149 tartrazine Substances 0.000 description 1
Classifications
-
- 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
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Epoxy Compounds (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a process flow for dry separation of propylene and hydrogen chloride. The process flow comprises a compression refrigeration unit, a heat exchange unit, a distillation unit and a cold energy recovery unit. The concrete process flow comprises the following steps: the mixed gas of propylene and hydrogen chloride is condensed through the compression refrigeration unit and then pressurized via a pump and enters a hydrogen chloride distillation tower, so high-purity hydrogen chloride is obtained from the tower top of the hydrogen chloride distillation tower, and propylene mixed gas containing trace hydrogen chloride is obtained from the tower bottom of the hydrogen chloride distillation tower; the obtained mixed gas is transported to a hydrogen chloride stripping tower via the pump and further purified, so high-purity recovered propylene is obtained; the recovered propylene undergoes heat exchanging through a heat exchanger 2 and then enters a flash vaporization tank, so one part of heat-exchanged recovered propylene is gasified, and the other part of heat-exchanged recovered propylene is changed into low-temperature-level propylene; one part of the low-temperature-level propylene enters the heat exchanger 2 and exchanges heat with the recovered propylene; and the other part of the low-temperature-level propylene enters the compression refrigeration unit and is used for the cooling of a refrigeration system. According to the invention, the separated high-purity hydrogen chloride and propylene are fully utilized, so the environment can be protected; resources are saved; economic losses are reduced; and high economic values are obtained.
Description
Technical field
The present invention relates to a kind of method of propylene and hydrogen chloride mixture separation and purification, by in epoxy chloropropane production process specifically, after acrylonitrile-chlorinated reaction, unreacted propylene and byproduct hydrogen chloride separation and purification obtain highly purified hydrogenchloride and propylene, hydrogenchloride is as product, and the method that propylene can be recycled.
Background technology
The production of epoxy chloropropane adopts high-temperature chlorization craft, and propylene and chlorine reaction generate propenyl chloride, and by-product hydrogen chloride.Excessive propylene and hydrogenchloride can be caused like this to mix, current most of device adopts water absorption extraction technique, absorb the hydrogenchloride in propylene, produce low value-added hydrochloric acid, hydrochloric acid is worth low on the one hand, and a large amount of low-concentration hcls can cause corrosion to equipment on the other hand.If can be recycled into the hydrogenchloride of high density, the oxychlorination unit can delivering to TOWER OUTLET IN VINYL CHLORIDE UNIT is used as raw material, produces propylene dichloride; Or the high purity hydrochloric acid device delivering to caustic soda makes raw material, substitute the chlorine production high purity hydrochloric acid used at present, thus save a large amount of chlorine, realize cyclic production, and can increase economic efficiency.Meanwhile, isolated propylene reuse can be made refrigeration agent or enters high-temperature chlorination reactor, produces epoxy chloropropane.
Summary of the invention
For solving the problems of the technologies described above, the invention provides the technical process of a kind of dry method separation of propylene and hydrogenchloride, both preserving the ecological environment to reach, and economized on resources again, accomplishing to make the best use of everything, reduce the object of the financial loss in producing.
For achieving the above object, technical scheme of the present invention is as follows:
The technical process of a kind of dry method separation of propylene and hydrogenchloride, comprise compression refrigeration unit, heat exchange unit, rectification cell and cold recovery unit, described heat exchange unit comprises interchanger one, interchanger two, condenser, reboiler and well heater, described rectification cell comprises hydrogenchloride rectifying tower and hydrogenchloride stripping tower, described cold recovery unit comprises flash tank, concrete technology flow process is, after the compressed refrigeration unit condensation of mixed gas of propylene and hydrogenchloride, pressurizeed by pump and enter hydrogenchloride rectifying tower, hydrogenchloride rectifying tower pressure on top surface scope is at 2.0 ~ 2.50MPa, tower top temperature is at-10 ~-40 DEG C, column bottom temperature-20 ~ 50 DEG C, tower top obtains high purity hydrogenchloride, the propylene mixed gas containing micro-hydrogenchloride is obtained at the bottom of tower, described mixed gas is purified to hydrogenchloride stripping tower further by pump delivery, hydrogenchloride stripper overhead pressure range is at 2.00 ~ 2.7MPa, tower top temperature 10 DEG C ~ 50 DEG C, column bottom temperature 10 DEG C ~ 50 DEG C, obtain highly purified Propylene recovery, described Propylene recovery enters described flash tank after interchanger two heat exchange, partial gasification, part becomes low-temperature level propylene, a described low-temperature level propylene part enters described interchanger two and described Propylene recovery heat exchange, another part enters the cooling of compression refrigeration unit for refrigeration system.
Preferably, mixed gas and the refrigerant condensation in interchanger one from compression refrigeration unit of described propylene and hydrogenchloride, temperature controls at-60 ~-40 DEG C, separating tank is entered after condensation, flash distillation is gas-liquid two-phase, gaseous stream returns interchanger one entrance, enters hydrogenchloride rectifying tower after liquid phase stream pumps up.
Preferably, described hydrogenchloride rectifying tower tower top is provided with condenser, is provided with reboiler at the bottom of tower.
Preferably, be provided with well heater at the bottom of described hydrogenchloride stripping tower tower, top gaseous phase logistics returns hydrogenchloride rectifying tower hypomere as backflow.
Preferably, reclaim after the logistics mixing of gasifying in described interchanger two, flash tank and compression refrigerating system.
Preferably, the tower top pressure of described hydrogenchloride rectifying tower is 2.17MPa, and tower top temperature is-24.8 DEG C, and column bottom temperature is-30 DEG C.
Preferably, the tower top pressure 2.27MPa of described hydrogenchloride stripping tower, tower top temperature is 30 DEG C, and column bottom temperature is 33 DEG C.
Pass through technique scheme, the technical process of dry method separation of propylene provided by the invention and hydrogenchloride is in whole sepn process, do not relate to water or other solvent absorbing, therefore be named as " dry method " to be separated, through hydroperoxide rectifying tower can obtain content up to 99.6% high purity chlorination hydrogen production, after the further purification of hydrogenchloride stripping tower, highly purified propylene product can be obtained at the bottom of tower, the oxychlorination unit that highly purified hydrogenchloride can deliver to TOWER OUTLET IN VINYL CHLORIDE UNIT makes raw material, for the production of propylene dichloride; Or the high purity hydrochloric acid device delivering to caustic soda makes raw material production high purity hydrochloric acid, has higher economic benefit; Highly purified propylene reuse can make refrigeration agent or enters high-temperature chlorination reactor, and for the production of epoxy chloropropane, separated hydrogenchloride and propylene are all fully used; alleviate the corrosion to production unit; protection of the environment, accomplishes to make the best use of everything, and reduces the object of financial loss.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below.
The process flow diagram that Fig. 1 is a kind of dry method separation of propylene disclosed in the embodiment of the present invention and hydrogenchloride.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is clearly and completely described.
The invention provides the technical process of a kind of dry method separation of propylene and hydrogenchloride, schematic flow sheet as shown in Figure 1, the method is separated with byproduct hydrogen chloride at propenyl chloride pre-separation column overhead unreacted propylene out in epoxy chloropropane can being produced, reduce the corrosion to production unit, and can make the best use of everything, there is very high economic worth.
Embodiment one:
In order to illustrate technological process of the present invention and effect, by heat and the material balance of the technical process to propylene and HCl separation purge process, simulation embodiment of the present invention, process the operating mode of propylene and hydrogen chloride mixture 120,000 tons simulation year.
Logistics 1 comprise mass content be 15.5% hydrogenchloride, the propylene of 84.3%, the propane mixture of 0.2% be condensed into logistics 2 by the refrigerant from compression refrigeration unit through interchanger one E101 with 15000kg/hr flow, temperature controls at-60 ~-40 DEG C, after entering separating tank U101, flash distillation is gas-liquid two-phase, separating tank U101 tank deck gaseous stream 4 returns interchanger one E101 entrance, and liquid phase stream 3 at the bottom of separating tank U101 tank is pressurized to certain pressure with pump P101 and enters hydrogenchloride rectifying tower T101 by logistics 5.Hydrogenchloride rectifying tower T101 tower top pressure is 2.17MPa, tower top temperature-24.8 DEG C, column bottom temperature-30 DEG C, tower top establishes condenser E102, reboiler E103 is established at the bottom of tower, it is the hydrogenchloride of 99.97% that T101 tower top obtains logistics 6 purity, and obtain the propylene stream 8 containing micro-hydrogenchloride at the bottom of tower, purified propylene is 99.67%.
Be delivered to hydrogenchloride stripping tower T102 containing the propylene stream of micro-hydrogenchloride by pump P102 at the bottom of hydrogenchloride rectifying tower T101 tower to purify further, hydrogenchloride stripping tower T102 tower top temperature 30 DEG C, pressure 2.27MPa, column bottom temperature 33 DEG C, well heater E104 is established at the bottom of hydrogenchloride stripping tower T102 tower, top gaseous phase logistics 7 returns hydrogenchloride rectifying tower T101 hypomere as backflow, obtains the Propylene recovery 9 that purity is 99.78% at the bottom of hydrogenchloride stripping tower T102 tower.Propylene recovery logistics 9 through pump P103 pressurize after with low-temperature level propylene stream 14 through interchanger two E105 heat exchange, partial gasification is logistics 10, by the gasification cooling of flash tank U102 decompression rear section, tank deck obtains gas-phase propene logistics 12, liquid phase low temperature propylene stream 13 is obtained at the bottom of tank, liquid phase low temperature propylene stream 13 is divided into logistics 14 and logistics 15, interchanger two E105 is entered in logistics 14 and logistics 9 heat exchange becomes logistics 10, logistics 15 enters compression refrigerating system K101, as refrigeration agent, from interchanger two E105, the logistics 10 gasified in flash tank U102 and compression refrigerating system K101, high-temperature chlorination reactor (workshop section of epoxy chloropropane production above) is entered through preheating after logistics 12 and logistics 16 mix, carry out the recycling of propylene.
Here it may be noted that the propane of minute quantity is directly discharged from the production of epoxy chloropropane, be blended in the mixed gas of propylene and hydrogenchloride, in whole sepn process, any impact can not be produced on the separation of hydrogenchloride, finally along with propylene is discharged together.
The invention provides the technical process being obtained high purity hydrogenchloride and propylene by the unreacted propylene of epoxy chloropropane production process and byproduct hydrogen chloride mixture separation purifying; according to the nature difference of each component; carry out comprehensively to the rectifying tower being separated different components; and adopt supercharging technology means; obtain high-purity propylene and hydrogenchloride product, namely preserve the ecological environment, economize on resources again; accomplish to make the best use of everything, reduce the financial loss in producing.
To the above-mentioned explanation of the disclosed embodiments, professional and technical personnel in the field are realized or uses the present invention.To be apparent for those skilled in the art to the multiple amendment of these embodiments, General Principle as defined herein can without departing from the spirit or scope of the present invention, realize in other embodiments.Therefore, the present invention can not be restricted to these embodiments shown in this article, but will meet the widest scope consistent with principle disclosed herein and features of novelty.
Claims (7)
1. the technical process of a dry method separation of propylene and hydrogenchloride, it is characterized in that, comprise compression refrigeration unit, heat exchange unit, rectification cell and cold recovery unit, described heat exchange unit comprises interchanger one, interchanger two, condenser, reboiler and well heater, described rectification cell comprises hydrogenchloride rectifying tower and hydrogenchloride stripping tower, described cold recovery unit comprises flash tank, concrete technology flow process is, after the compressed refrigeration unit condensation of mixed gas of propylene and hydrogenchloride, pressurizeed by pump and enter hydrogenchloride rectifying tower, hydrogenchloride rectifying tower pressure on top surface scope is at 2.00 ~ 2.50MPa, tower top temperature is at-10 ~-40 DEG C, column bottom temperature-20 ~ 50 DEG C, tower top obtains high purity hydrogenchloride, the propylene mixed gas containing micro-hydrogenchloride is obtained at the bottom of tower, described mixed gas is purified to hydrogenchloride stripping tower further by pump delivery, hydrogenchloride stripper overhead pressure range is at 2.00 ~ 2.7MPa, tower top temperature 10 DEG C ~ 50 DEG C, column bottom temperature 10 DEG C ~ 50 DEG C, obtain highly purified Propylene recovery, described Propylene recovery enters described flash tank after interchanger two heat exchange, partial gasification, part becomes low-temperature level propylene, a described low-temperature level propylene part enters described interchanger two and described Propylene recovery heat exchange, another part enters the cooling of compression refrigeration unit for refrigeration system.
2. the technical process of a kind of dry method separation of propylene according to claim 1 and hydrogenchloride, it is characterized in that, mixed gas and the refrigerant condensation in interchanger one from compression refrigeration unit of described propylene and hydrogenchloride, temperature controls at-60 ~-40 DEG C, separating tank is entered after condensation, flash distillation is gas-liquid two-phase, and gaseous stream returns interchanger one entrance, enters hydrogenchloride rectifying tower after liquid phase stream pumps up.
3. the technical process of a kind of dry method separation of propylene according to claim 1 and hydrogenchloride, is characterized in that, described hydrogenchloride rectifying tower tower top is provided with condenser, is provided with reboiler at the bottom of tower.
4. the technical process of a kind of dry method separation of propylene according to claim 1 and hydrogenchloride, is characterized in that, is provided with well heater at the bottom of described hydrogenchloride stripping tower tower, and top gaseous phase logistics returns hydrogenchloride rectifying tower hypomere as backflow.
5. the technical process of a kind of dry method separation of propylene according to claim 1 and hydrogenchloride, is characterized in that, reclaims after the logistics mixing of gasifying in described interchanger two, flash tank and compression refrigerating system.
6. the technical process of a kind of dry method separation of propylene according to claim 1 and hydrogenchloride, is characterized in that, the tower top pressure of described hydrogenchloride rectifying tower is 2.17MPa, and tower top temperature is-24.8 DEG C, and column bottom temperature is-30 DEG C.
7. the technical process of according to claim 1 ~ kind of dry method separation of propylene and hydrogenchloride, is characterized in that, the tower top pressure 2.27MPa of described hydrogenchloride stripping tower, and tower top temperature is 30 DEG C, and column bottom temperature is 33 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410119088.9A CN104926581B (en) | 2014-03-21 | 2014-03-21 | Process flow for dry separation of propylene and hydrogen chloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410119088.9A CN104926581B (en) | 2014-03-21 | 2014-03-21 | Process flow for dry separation of propylene and hydrogen chloride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104926581A true CN104926581A (en) | 2015-09-23 |
| CN104926581B CN104926581B (en) | 2017-02-15 |
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| CN201410119088.9A Active CN104926581B (en) | 2014-03-21 | 2014-03-21 | Process flow for dry separation of propylene and hydrogen chloride |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106629605A (en) * | 2016-12-23 | 2017-05-10 | 上海建安化工设计有限公司 | Dry separation refining method and dry separation refining device for byproduct hydrogen chloride in production of vinylidene difluoride |
| CN108083971A (en) * | 2017-12-27 | 2018-05-29 | 山东凯泰科技股份有限公司 | A kind of refrigerating method in chloropropene production process |
| CN109437108A (en) * | 2018-11-22 | 2019-03-08 | 衡阳恒荣高纯半导体材料有限公司 | A kind of waste acidity recovery 26%-28% hydrogen chloride new process |
| CN113546439A (en) * | 2021-08-16 | 2021-10-26 | 聊城鲁西氯甲烷化工有限公司 | Liquid chlorine flash evaporation deoxidization system and process |
| CN117018653A (en) * | 2023-08-14 | 2023-11-10 | 山东天海能源科技发展有限公司 | Method for coproducing high-purity hydrogen chloride gas by high-temperature chloridizing chloropropene device |
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| CN102661654B (en) * | 2012-05-02 | 2014-04-30 | 北京华宇同方化工科技开发有限公司 | Method and system for preparing high purity gas by rectification method |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106629605A (en) * | 2016-12-23 | 2017-05-10 | 上海建安化工设计有限公司 | Dry separation refining method and dry separation refining device for byproduct hydrogen chloride in production of vinylidene difluoride |
| CN108083971A (en) * | 2017-12-27 | 2018-05-29 | 山东凯泰科技股份有限公司 | A kind of refrigerating method in chloropropene production process |
| CN108083971B (en) * | 2017-12-27 | 2020-12-04 | 山东凯泰科技股份有限公司 | Refrigeration method in chloropropene production process |
| CN109437108A (en) * | 2018-11-22 | 2019-03-08 | 衡阳恒荣高纯半导体材料有限公司 | A kind of waste acidity recovery 26%-28% hydrogen chloride new process |
| CN113546439A (en) * | 2021-08-16 | 2021-10-26 | 聊城鲁西氯甲烷化工有限公司 | Liquid chlorine flash evaporation deoxidization system and process |
| CN113546439B (en) * | 2021-08-16 | 2023-02-21 | 聊城鲁西氯甲烷化工有限公司 | Liquid chlorine flash evaporation deoxidization system and process |
| CN117018653A (en) * | 2023-08-14 | 2023-11-10 | 山东天海能源科技发展有限公司 | Method for coproducing high-purity hydrogen chloride gas by high-temperature chloridizing chloropropene device |
| CN117018653B (en) * | 2023-08-14 | 2024-02-02 | 山东天海能源科技发展有限公司 | Method for coproducing high-purity hydrogen chloride gas by high-temperature chloridizing chloropropene device |
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| CN104926581B (en) | 2017-02-15 |
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