CN112717669A - Polymerization tail gas processing system in chloroethylene production - Google Patents
Polymerization tail gas processing system in chloroethylene production Download PDFInfo
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- CN112717669A CN112717669A CN202011474496.8A CN202011474496A CN112717669A CN 112717669 A CN112717669 A CN 112717669A CN 202011474496 A CN202011474496 A CN 202011474496A CN 112717669 A CN112717669 A CN 112717669A
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- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical group ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 238000006116 polymerization reaction Methods 0.000 title claims abstract description 32
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 15
- 238000009835 boiling Methods 0.000 claims abstract description 88
- 238000010992 reflux Methods 0.000 claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 238000011045 prefiltration Methods 0.000 claims abstract description 11
- 238000005406 washing Methods 0.000 claims abstract description 10
- 239000000463 material Substances 0.000 claims description 15
- 238000003860 storage Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 239000000126 substance Substances 0.000 description 11
- 239000012535 impurity Substances 0.000 description 5
- 150000003254 radicals Chemical class 0.000 description 5
- 239000000178 monomer Substances 0.000 description 4
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 239000004800 polyvinyl chloride Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- UOCLXMDMGBRAIB-UHFFFAOYSA-N 1,1,1-trichloroethane Chemical compound CC(Cl)(Cl)Cl UOCLXMDMGBRAIB-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 125000000816 ethylene group Chemical group [H]C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229920000915 polyvinyl chloride Polymers 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000009736 wetting Methods 0.000 description 2
- 230000000621 autoagglutination Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000357 carcinogen Toxicity 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 125000000963 oxybis(methylene) group Chemical group [H]C([H])(*)OC([H])([H])* 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000002940 repellent Effects 0.000 description 1
- 239000005871 repellent Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention discloses a polymerization tail gas treatment system in vinyl chloride production, which comprises a polymerization kettle, a discharge chute, a stripping tower feed chute, a stripping tower, a centrifugal dryer, a recovery separator, a primary condenser, a secondary condenser, a gas-liquid separation tank, an alkaline washing tower, a pre-cooler, a vinyl chloride compressor, a post-cooler, a first-stage total condenser, a second-stage total condenser, a crude vinyl chloride buffer tank, a pre-filter, a coalescer, a crude vinyl chloride dryer, a low-boiling tower, a high-boiling tower, a finished product condenser, a fine vinyl chloride dryer and a high-boiling tower reflux tank. The invention avoids the problem that the stable production is influenced by the fact that the non-condensable gas directly enters the rectifying tower to generate VCM self-polymerization and is attached to the tower plate of the rectifying tower in the traditional treatment system.
Description
The technical field is as follows:
the invention relates to a tail gas treatment system, in particular to a polymerization tail gas treatment system in vinyl chloride production.
Background art:
vinyl Chloride (VC) is a colorless gas at room temperature, and the main industrial application is in the production of polyvinyl chloride (PVC), so it is often called Vinyl Chloride Monomer (VCM) with a molecular formula of C2H3And (3) carrying out polymerization reaction on the Cl and the vinyl chloride monomer to obtain the polyvinyl chloride.
In the polymerization process of Vinyl Chloride (VCM), in order to realize the economical efficiency of the process operation and ensure the quality of resin, the final conversion rate of the VCM is generally controlled to be 80-85 percent, so that 15-20 percent of VCM is unreacted in each polymerization period, and after the tail gas is subjected to secondary compression and condensation treatment, a large amount of VCM still exists in non-condensable gas. If this polymerization tail gas is direct if empty, not only cause the wasting of resources, manufacturing cost increases, more importantly VCM is carcinogen, discharge into in the atmosphere, can serious environmental pollution, harm people's health, consequently, also there is the research and send this part noncondensable gas back to vinyl chloride gas cabinet, send polymerization reaction to the polymeric kettle again after the rectification, the problem that exists is that partly have the catalyst of active free radical in the noncondensable gas in addition, VCM auto-agglutination takes place easily in the rectifying column, the polyvinyl chloride viscosity of formation is great, adhere to the stable of influence production on the rectifying column plate and go on.
The invention content is as follows:
in order to solve the technical problems, the invention aims to provide a system for treating polymerization tail gas in vinyl chloride production, which can remove active free radicals and realize stable production.
The invention is implemented by the following technical scheme: a polymerization tail gas treatment system in vinyl chloride production comprises a polymerization kettle, a discharge chute, a stripping tower feed chute, a stripping tower, a centrifugal dryer, a recovery separator, a primary condenser, a secondary condenser and a gas-liquid separation tank, wherein a material outlet of the polymerization kettle is communicated with an inlet of the discharge chute, and the discharge chute, the stripping tower feed chute, the stripping tower and the centrifugal dryer are sequentially communicated; the gas outlet of the polymerization kettle, the gas phase outlet of the discharge chute and the gas phase outlet of the feeding chute of the stripping tower are communicated with the inlet of a recovery separator, and the recovery separator, the primary condenser, the secondary condenser and the gas-liquid separation tank are communicated in sequence;
the device also comprises an alkaline washing tower, a pre-cooler, a vinyl chloride compressor, a post-cooler, a first-stage total condenser, a second-stage total condenser, a crude vinyl chloride buffer tank, a pre-filter, a coalescer, a crude vinyl chloride dryer, a low-boiling tower, a high-boiling tower, a finished product condenser, a fine vinyl chloride dryer and a high-boiling tower reflux tank, wherein the gas inlet of the alkaline washing tower is communicated with the gas outlet of the gas-liquid separation tank, polymerization tail gas enters the alkaline washing tower, and active free radicals in the polymerization tail gas are removed by using alkali liquor in the alkaline washing tower. The outlet of the alkaline tower, the vinyl chloride compressor of the pre-cooler, the post-cooler, the first-stage total condenser, the second-stage total condenser, the crude vinyl chloride buffer tank, the pre-filter, the coalescer, the crude vinyl chloride dryer and the low-boiling tower are sequentially communicated, the outlet of the bottom of the low-boiling tower is communicated with the inlet of the high-boiling tower, the outlet of the top of the high-boiling tower is communicated with the inlet of the finished product condensing tank, the outlet of the finished product condenser is communicated with the inlet of the refined vinyl chloride dryer, the outlet of the refined vinyl chloride dryer is communicated with the inlet of the reflux tank of the high-boiling tower, and the outlet of the reflux tank of the high-boiling tower is communicated with the finished vinyl chloride storage.
Further, the outlet of the high-boiling tower reflux tank is communicated with a high-boiling tower reflux opening.
Further, an outlet of the chloroethylene finished product storage tank is communicated with a feed inlet of the polymerization kettle.
Liquid crude chloroethylene material containing emulsified water, free water and trace impurity particles from a crude chloroethylene buffer tank is firstly filtered by an external prefilter arranged at the front end of a coalescer to remove trace solid impurities in the chloroethylene material, the prefiltered clean chloroethylene containing the free water enters the coalescer, emulsified small water drops dispersed in the chloroethylene material are coalesced and grow in the process of passing through a filter bed of the coalescer until the dispersed-phase water drops form large bubbles on the outer surface of a filter element and are settled into a settling water collecting tank of the coalescer by self gravity, in order to ensure the dehydration effect of the device, a plurality of water repellent filter elements made of special polar materials are arranged at an outlet of the device, the filter elements have good hydrophobicity by depending on the difference of wetting angles of the special materials, only allow the chloroethylene to pass and do not allow the water to pass, thereby achieving high efficiency, High precision, large flow and continuous separation and water removal.
In the low-boiling column, low-boiling substances are removed. The reflux of the low-boiling tower top liquid is mainly realized by sending condensate in a low-boiling tower reflux tank to the top of the low-boiling tower through a low-boiling tower reflux pump. Condensing the low-boiling tower top steam in a low-boiling tower condenser and then feeding the low-boiling tower top steam into a low-boiling tower reflux tank. The noncondensable gas in the low-boiling tower condenser and the tail gas-removing condenser in the second-stage total condenser is continuously condensed by brine at the temperature of minus 35 ℃, and the condensate enters a reflux tank of the low-boiling tower. And a tail gas recovery system is used for removing non-condensable gas in the tail gas condenser. After removing low-boiling substances in the low-boiling tower, vinyl chloride is sent to the high-boiling tower by a high-boiling tower feeding pump, and high-boiling substances (such as dichloroethane, trichloroethane and the like) are collected from the bottom of the tower and then sent to a high-boiling substance buffer tank. The steam rising from the tower top is cooled by a finished product condenser and then enters a refined chloroethylene dryer, the steam is dried and then enters a high-boiling tower reflux tank, then a part of the steam is sent to the top of the high-boiling tower by a high-boiling tower reflux pump for reflux, the other part of the steam is sent to a spherical tank, and the steam is discharged from the high-boiling tower reflux pump and is checked to be a qualified monomer dechlorinated ethylene finished product storage tank.
The invention has the advantages that: the invention obtains qualified finished products by arranging an alkaline washing tower, a pre-cooler, a vinyl chloride compressor, a post-cooler, a first-stage total condenser, a second-stage total condenser, a crude vinyl chloride buffer tank, a pre-filter, a coalescer, a crude vinyl chloride dryer, a low-boiling tower, a high-boiling tower, a finished product condenser, a refined vinyl chloride dryer and a high-boiling tower reflux tank, and removing active free radicals from polymerization tail gas through alkaline washing, trace solid impurities and low-boiling substances through dehydration, and then removing the low-boiling substances and the high-boiling substances, thereby avoiding the problem that the stable production is influenced by VCM auto-polymerization when non-condensable gas directly enters a rectifying tower in a traditional treatment system and is attached to a rectifying tower plate.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of a polymerization off-gas treatment system in vinyl chloride production according to example 1.
In the figure: the device comprises a polymerization kettle 1, a discharge chute 2, a stripping tower feed chute 3, a stripping tower 4, a centrifugal dryer 5, a recovery separator 6, a first-stage condenser 7, a second-stage condenser 8, a gas-liquid separation tank 9, an alkaline tower 10, a pre-machine cooler 11, a vinyl chloride compressor 12, a post-machine cooler 13, a first-stage total condenser 14, a second-stage total condenser 15, a crude vinyl chloride buffer tank 16, a pre-filter 17, a coalescer 18, a crude vinyl chloride dryer 19, a low-boiling tower 20, a high-boiling tower 21, a finished product condenser 22, a refined vinyl chloride dryer 23, a high-boiling tower reflux tank 24 and a vinyl chloride finished product storage tank 25.
The specific implementation mode is as follows:
the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1:
a polymerization tail gas treatment system in vinyl chloride production comprises a polymerization kettle 1, a discharge chute 2, a stripping tower feed chute 3, a stripping tower 4, a centrifugal dryer 5, a recovery separator 6, a primary condenser 7, a secondary condenser 8, a gas-liquid separation tank 9, an alkaline tower 10, a pre-cooler 11, a vinyl chloride compressor 12, a post-cooler 13, a primary total condenser 14, a secondary total condenser 15, a crude vinyl chloride buffer tank 16, a pre-filter 17, a coalescer 18, a crude vinyl chloride dryer 19, a low-boiling tower 20, a high-boiling tower 21, a finished product condenser 22, a fine vinyl chloride dryer 23 and a high-boiling tower reflux tank 24, wherein a material outlet of the polymerization kettle 1 is communicated with an inlet of the discharge chute 2, the stripping tower feed chute 3, the stripping tower 4 and the centrifugal dryer 5 are sequentially communicated; a gas outlet of the polymerizer 1, a gas-phase outlet of the discharge chute 2 and a gas-phase outlet of the feeding chute 3 of the stripping tower are communicated with an inlet of a recovery separator 6, and the recovery separator 6, a primary condenser 7, a secondary condenser 8 and a gas-liquid separation tank 9 are communicated in sequence; an air inlet of the alkaline tower 10 is communicated with an air outlet of the gas-liquid separation tank 9, the polymerization tail gas enters the alkaline tower 10, and active free radicals in the polymerization tail gas are removed by using alkali liquor of the alkaline tower 10. An air outlet of the alkaline tower 10, a vinyl chloride compressor 12 of a pre-machine cooler 11, a post-machine cooler 13, a first-section full condenser 14, a second-section full condenser 15, a crude vinyl chloride buffer tank 16, a pre-filter 17, a coalescer 18, a crude vinyl chloride dryer 19 and a low-boiling tower 20 are sequentially communicated, a tower bottom outlet of the low-boiling tower 20 is communicated with an inlet of a high-boiling tower 21, a tower top outlet of the high-boiling tower 21 is communicated with an inlet of a finished product condensing tank, an outlet of a finished product condenser 22 is communicated with an inlet of a refined vinyl chloride dryer 23, an outlet of the refined vinyl chloride dryer 23 is communicated with an inlet of a high-boiling tower reflux tank 24, an outlet of the high-boiling tower reflux tank 24 is respectively communicated with a reflux port of the high-boiling tower 21 and a vinyl chloride finished product storage tank 25, and.
Liquid crude chloroethylene material containing emulsified water, free water and trace impurity particles from a crude chloroethylene buffer tank 16 firstly passes through a prefilter 17 arranged outside the front end of a coalescer 18 to remove trace solid impurities in the chloroethylene material, the prefiltered clean chloroethylene containing the free water enters the coalescer 18, emulsified small water drops dispersed in the chloroethylene material are coalesced and grow in the process of passing through a filter bed of the coalescer 18 until the dispersed water drops form large liquid bubbles on the outer surface of a filter element, the large liquid bubbles are settled in a settling water collecting tank of the coalescer 18 by self gravity, in order to ensure the dehydration effect of the device, a plurality of water filter elements made of special polar materials are arranged at the outlet of the device, the filter elements have good hydrophobicity by depending on the difference of wetting angles of the special materials, only allow the chloroethylene to pass through, and do not allow the water to pass through, thereby achieving high efficiency, High precision, large flow and continuous separation and water removal.
In the low-boiling column 20, low-boiling substances are removed. The reflux of the liquid at the top of the low-boiling tower 20 is mainly realized by sending the condensate in the reflux tank of the low-boiling tower to the top of the low-boiling tower 20 through a vinyl chloride finished product storage tank. The steam at the top of the low-boiling tower 20 is condensed in a low-boiling tower condenser and then enters a low-boiling tower reflux tank. The non-condensable gas in the low-boiling tower condenser and the tail gas-removing condenser in the second-stage total condenser 15 is continuously condensed by brine at the temperature of minus 35 ℃, and the condensate enters a reflux tank of the low-boiling tower. And a tail gas recovery system is used for removing non-condensable gas in the tail gas condenser. After removing low boiling substances in the low boiling column 20, vinyl chloride is sent to the high boiling column 21 by a high boiling column feed pump, and high boiling substances (such as dichloroethane, trichloroethane, etc.) are collected from the bottom of the column and then sent to a high boiling substance buffer tank. The steam rising from the top of the tower is cooled by a finished product condenser 22 and then enters a refined vinyl chloride dryer 23, the steam is dried and then enters a high-boiling tower reflux tank 24, then a part of the steam is sent to the top of the high-boiling tower 21 by a high-boiling tower reflux pump for reflux, the other part of the steam is sent to a spherical tank, and the steam is discharged from the high-boiling tower reflux pump and is detected to be a qualified monomer dechlorinated ethylene finished product storage tank 25.
The material coming out of the reflux pump of the high-boiling tower is analyzed and judged whether to be qualified or not through sampling, and the qualified material requires C2H2<0.0005％，C2H4O<0.0005% of dichloroethane<0.003％。
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (3)
1. A polymerization tail gas treatment system in vinyl chloride production comprises a polymerization kettle, a discharge chute, a stripping tower feed chute, a stripping tower, a centrifugal dryer, a recovery separator, a primary condenser, a secondary condenser and a gas-liquid separation tank, wherein a material outlet of the polymerization kettle is communicated with an inlet of the discharge chute, and the discharge chute, the stripping tower feed chute, the stripping tower and the centrifugal dryer are sequentially communicated; the gas outlet of the polymerization kettle, the gas phase outlet of the discharge chute and the gas phase outlet of the feeding chute of the stripping tower are communicated with the inlet of a recovery separator, and the recovery separator, the primary condenser, the secondary condenser and the gas-liquid separation tank are communicated in sequence;
it is characterized by also comprising an alkaline washing tower, a pre-cooler, a vinyl chloride compressor, a post-cooler, a first-stage total condenser, a second-stage total condenser, a crude vinyl chloride buffer tank, a pre-filter, a coalescer, a crude vinyl chloride dryer, a low-boiling tower, a high-boiling tower, a finished product condenser, a refined vinyl chloride dryer and a high-boiling tower reflux tank, wherein the gas inlet of the alkaline washing tower is communicated with the gas outlet of the gas-liquid separation tank, the gas outlet of the alkaline washing tower, the vinyl chloride compressor of the pre-cooler, the post-cooler, the first-stage total condenser, the second-stage total condenser, the crude vinyl chloride buffer tank, the pre-filter, the coalescer, the crude vinyl chloride dryer and the low-boiling tower are sequentially communicated, the tower bottom outlet of the low-boiling tower is communicated with the inlet of the high-boiling tower, the tower top outlet of the high-boiling tower is communicated with the inlet of the finished product condenser, and the outlet of, the outlet of the refined chloroethylene dryer is communicated with the inlet of the reflux tank of the high-boiling tower, and the outlet of the reflux tank of the high-boiling tower is respectively communicated with the reflux port of the high-boiling tower and the chloroethylene finished product storage tank.
2. The system of claim 1, wherein the outlet of the reflux drum of the high-boiling tower is further communicated with the reflux port of the high-boiling tower.
3. The system as claimed in claim 1, wherein the outlet of the storage tank is connected to the inlet of the polymerizer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011474496.8A CN112717669A (en) | 2020-12-15 | 2020-12-15 | Polymerization tail gas processing system in chloroethylene production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011474496.8A CN112717669A (en) | 2020-12-15 | 2020-12-15 | Polymerization tail gas processing system in chloroethylene production |
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| CN112717669A true CN112717669A (en) | 2021-04-30 |
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| CN202011474496.8A Pending CN112717669A (en) | 2020-12-15 | 2020-12-15 | Polymerization tail gas processing system in chloroethylene production |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3063728D1 (en) * | 1979-05-02 | 1983-07-21 | Goodrich Co B F | Improved process for removal and recovery of vinyl chloride monomer from vent gas stream in polyvinyl chloride plant |
| JP2002012411A (en) * | 2000-04-26 | 2002-01-15 | Tokuyama Corp | Recovering method for hydrogen chloride gas |
| CN103694079A (en) * | 2013-09-27 | 2014-04-02 | 新疆天业（集团）有限公司 | Method for refining and purifying vinyl chloride monomer |
| CN105481640A (en) * | 2015-12-17 | 2016-04-13 | 青岛科技大学 | Low-energy consumption low-loss vinyl chloride rectifying technology |
| CN205803358U (en) * | 2016-07-13 | 2016-12-14 | 青海盐湖工业股份有限公司 | A kind of knot screen of vinyl chloride |
| CN212092200U (en) * | 2020-04-17 | 2020-12-08 | 内蒙古亿利化学工业有限公司 | Recovery system of polymerization tail gas |
-
2020
- 2020-12-15 CN CN202011474496.8A patent/CN112717669A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3063728D1 (en) * | 1979-05-02 | 1983-07-21 | Goodrich Co B F | Improved process for removal and recovery of vinyl chloride monomer from vent gas stream in polyvinyl chloride plant |
| JP2002012411A (en) * | 2000-04-26 | 2002-01-15 | Tokuyama Corp | Recovering method for hydrogen chloride gas |
| CN103694079A (en) * | 2013-09-27 | 2014-04-02 | 新疆天业（集团）有限公司 | Method for refining and purifying vinyl chloride monomer |
| CN105481640A (en) * | 2015-12-17 | 2016-04-13 | 青岛科技大学 | Low-energy consumption low-loss vinyl chloride rectifying technology |
| CN205803358U (en) * | 2016-07-13 | 2016-12-14 | 青海盐湖工业股份有限公司 | A kind of knot screen of vinyl chloride |
| CN212092200U (en) * | 2020-04-17 | 2020-12-08 | 内蒙古亿利化学工业有限公司 | Recovery system of polymerization tail gas |
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Application publication date: 20210430 |