CN111689833A - VCM high-boiling-point substance purification device and purification method - Google Patents
VCM high-boiling-point substance purification device and purification method Download PDFInfo
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- CN111689833A CN111689833A CN202010636275.XA CN202010636275A CN111689833A CN 111689833 A CN111689833 A CN 111689833A CN 202010636275 A CN202010636275 A CN 202010636275A CN 111689833 A CN111689833 A CN 111689833A
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- 238000000746 purification Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000000126 substance Substances 0.000 title claims abstract description 12
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims abstract description 33
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000009835 boiling Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 59
- 238000010992 reflux Methods 0.000 claims description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 47
- 239000002994 raw material Substances 0.000 claims description 25
- 239000012267 brine Substances 0.000 claims description 23
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 23
- 239000000463 material Substances 0.000 claims description 15
- 239000012046 mixed solvent Substances 0.000 claims description 9
- 230000001276 controlling effect Effects 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000000112 cooling gas Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000005070 sampling Methods 0.000 claims description 3
- 239000005997 Calcium carbide Substances 0.000 abstract description 7
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 abstract description 7
- 230000009286 beneficial effect Effects 0.000 abstract description 4
- 238000011084 recovery Methods 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000002894 chemical waste Substances 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
-
- 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
-
- 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
- B01D3/42—Regulation; Control
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a VCM high-boiling-point substance purification device and a purification method, and belongs to the field of chemical waste treatment. The VCM high-boiling residue purification technology can produce the following beneficial effects: 1. the recovery rate of the chloroethylene in the dichloroethane generated by the PVC by the calcium carbide method can reach more than 99.5 percent (w). 2. The 1, 1-dichloroethane in the dichloroethane generated by PVC by calcium carbide method is purified to more than 98 percent (w) and can be directly sold as a product.
Description
Technical Field
The invention relates to the field of chemical waste treatment, in particular to a VCM high-boiling-point substance purification device and a purification method.
Background
At present, the common treatment method of the residual liquid of the tower bottom of the vinyl chloride rectification tower in domestic calcium carbide method PVC enterprises is to filter, separate oil from water, decolor, remove water and impurities, and recycle most substances to be used as a mixed solvent. The treatment process comprises the following steps: the residual liquid of high-boiling-point substance obtained from the fractionation of the high-boiling tower is further removed with chloroethylene in a recovery device, so that after the quality of the residual liquid is partially improved, the prior art only recovers part of chloroethylene monomers, the content of chloroethylene in the recovered high-boiling-point substance is more than 20% (w) of 1, 1-dichloroethane 75% (w), and the residual liquid of high-boiling-point substance is treated as a dangerous waste according to the national environmental protection requirement.
Disclosure of Invention
The invention aims to solve the technical problem of providing a high-boiling residue purification device and a high-boiling residue purification method, which can extract and recycle high-boiling residual liquid.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: a VCM high-boiling-point substance purification device comprises a raw material tank, a rectifying tower, a water cooler, a brine cooler, a circulating water cooler, a reflux pump, a reflux tank, a circulating water cooler, an intermediate tank, a mixed solvent tank and a finished product tank, wherein the raw material tank is connected with the rectifying tower through a pipeline, a feed pump is arranged on a connecting pipeline of the raw material tank and the rectifying tower, the top of the rectifying tower is connected with the water cooler through a pipeline, the water cooler is connected with the brine cooler through a pipeline, the brine cooler is connected with the circulating water cooler I through a pipeline, the rectifying tower is connected with the finished product tank through a pipeline, a reflux pump is arranged on a connecting pipeline between the rectifying tower and the connecting pipeline of the finished product tank, the reflux pump is connected with the reflux tank through a pipeline, the reflux tank is connected with the water cooler through a pipeline, the bottom of the rectifying tower is connected with the circulating water cooler II through a pipeline, the circulating water cooler II is connected with the intermediate, and a kettle liquid pump is arranged on a connecting pipeline between the rectifying tower and the circulating water cooler II, the intermediate tank is connected with the rectifying tower through a pipeline, and an intermediate tank delivery pump is arranged on the connecting pipeline between the rectifying tower and the intermediate tank.
The VCM high-boiling-point substance purification method comprises the following steps:
(1) performing pressure distillation, opening an inlet valve of a feed pump, starting the feed pump, and conveying the raw materials from a raw material tank to the 60 th to 62 th layers of the upper part of the distillation tower at a feed rate of 950-;
(2) opening hand valves of a water cooler and a brine cooler at the top of the rectifying tower, and cooling gas distilled from the top of the rectifying tower by the water cooler and the brine cooler;
(3) when the liquid level of the tower kettle of the rectifying tower reaches 20 percent, the liquid can be heated and heated to slowly heat the tower kettle, the pressure of the rectifying tower is gradually increased to an operation value, the temperature of the tower kettle is controlled to be 85-100 ℃, the pressure of the tower kettle is controlled to be 0.2-0.25 MPa (gauge pressure), the temperature of the top of the tower is controlled to be 25-35 ℃, the liquid level of the rectifying tower is controlled to be 30-60 percent, and the pressure of the top of the tower is controlled to be 0.2-0.25 MPa (gauge pressure);
(4) after the liquid level of the reflux tank reaches 30-40%, a reflux pump is started to feed materials to the rectifying tower, reflux operation is carried out, and the liquid levels of the tower kettle and the reflux tank are kept stable;
(5) starting a kettle liquid pump when the tower kettle material is unqualified and the liquid level is higher, and starting the kettle liquid pump to return the material to the raw material tank;
(6) when the temperature at the top of the tower and the temperature at the bottom of the tower reach operating values, sampling and analyzing that the content of gaseous chloroethylene at the top of the tower is more than 90 percent (v) and the content of chloroethylene at the bottom of the tower is less than 0.01 percent (w), opening a gas phase extraction regulating valve at the top of the tower to convey chloroethylene to a gas holder after the chloroethylene at the top of the tower is qualified, opening a liquid pump at the bottom of the tower, cooling the liquid pump to 35 ℃ through a condenser, and conveying;
(7) rectifying under normal pressure, opening an inlet valve of a transfer pump of the intermediate tank, starting a feed pump, and transferring raw materials from the raw material tank to the 5 th to 6 th layers of the upper part of the rectifying tower at the feeding amount of 750-;
(8) opening hand valves of a circulating water cooler II and a brine cooler on the top of the rectifying tower, and cooling gas distilled from the top of the rectifying tower by a circulating water condenser II and the brine cooler;
(9) when the liquid level of the tower kettle of the rectifying tower reaches 20%, heating and slowly heating the tower kettle, gradually raising the pressure of the rectifying tower to an operation value, controlling the temperature of the tower kettle to be 75-80 ℃, the pressure of the tower kettle to be 0.001-0.07 MPa (gauge pressure), the temperature of the tower top to be 55-60 ℃, the liquid level of the rectifying tower to be 30-60%, the pressure of the tower top to be 0.001-0.07 MPa (gauge pressure), and the reflux amount of the tower top to be 3800-5300 kg/h;
(10) after the liquid level of the reflux tank reaches 30-40%, feeding the material to a rectifying tower by starting a reflux pump, keeping the liquid levels of a tower kettle and the reflux tank stable, wherein the reflux amount at the top of the tower is 3800-5300 kg/h, and when the reflux amount of 1, 1-dichloroethane in the reflux tank is more than 98% (w), discharging the material to a finished product tank;
(11) when the content of 1, 1-dichloroethane in the tower kettle is less than 30% (w), a kettle liquid pump is started to convey kettle liquid to the mixed solvent tank after the kettle liquid pump is cooled to 35 ℃ by a condenser.
By adopting the technical scheme of the invention, the following beneficial effects can be obtained:
the VCM high-boiling residue purification technology of the invention can produce the following beneficial effects: 1. the recovery rate of the chloroethylene in the dichloroethane generated by the PVC by the calcium carbide method can reach more than 99.5 percent (w). 2. The 1, 1-dichloroethane in the dichloroethane generated by PVC by calcium carbide method is purified to more than 98 percent (w) and can be directly sold as a product.
Drawings
The contents of the description and the references in the drawings are briefly described as follows:
FIG. 1 is a schematic view of the purification apparatus;
the labels in the above figures are: 1. a raw material tank; 2. a feed pump; 3. a rectifying tower; 4. a water cooler; 5. A brine cooler; 6. a first circulating water cooler; 7. a reflux pump; 8. a reflux tank; 9. a second circulating water cooler; 10. A kettle liquid pump; 11. a tundish delivery pump; 12. an intermediate tank; 13. a mixed solvent tank; 14. and (5) a finished product can.
Detailed Description
The embodiments of the present invention, such as the shapes and structures of the respective members, the mutual positions and connection relationships between the respective portions, the functions and operation principles of the respective portions, will be described in further detail below with reference to the accompanying drawings.
As shown in figure 1, the VCM high-boiling residue purification device comprises a raw material tank 1, a rectifying tower 3, a water cooler 4, a brine cooler 5, a circulating water cooler 6, a reflux pump 7, a reflux tank 8, a circulating water cooler 9, an intermediate tank 12, a mixed solvent tank 13 and a finished product tank 14, wherein the raw material tank 1 is connected with the rectifying tower 3 through a pipeline, a feeding pump 2 is arranged on a connecting pipeline of the raw material tank 1 and the rectifying tower 3, the top of the rectifying tower 3 is connected with the water cooler 4 through a pipeline, the water cooler 4 is connected with the brine cooler 5 through a pipeline, the brine cooler 5 is connected with the circulating water cooler 6 through a pipeline, the rectifying tower 3 is connected with the finished product tank 14 through a pipeline, the reflux pump 7 is arranged on a connecting pipeline between the rectifying tower 3 and the connecting pipeline of the finished product tank 14, the reflux pump 7 is connected with the reflux tank 8 through a pipeline, the reflux tank 8 is connected with the water cooler 4 through a pipeline, the bottom of the rectifying tower 3 is connected with a second circulating water cooler 9 through a pipeline, the second circulating water cooler 9 is connected with an intermediate tank 12 and a mixed solvent tank 13 through a pipeline, a kettle liquid pump 10 is arranged on a connecting pipeline between the rectifying tower 3 and the second circulating water cooler 9, the intermediate tank 12 is connected with the rectifying tower 3 through a pipeline, and an intermediate tank delivery pump 11 is arranged on the connecting pipeline between the rectifying tower 3 and the intermediate tank 12.
As shown in figure 1, the VCM high boiling point substance purification method comprises the following steps: pressure rectification
(1) Opening an inlet valve of the feed pump 2, starting the feed pump 2, and conveying the raw material from the raw material tank 1 to the 60 th-62 th layer of the upper part of the rectifying tower 3, wherein the feeding amount is 950-;
(2) opening hand valves of a water cooler 4 and a brine cooler 5 at the top of the rectifying tower 3, and cooling gas distilled from the top of the rectifying tower 3 by the water cooler 4 and the brine cooler 5;
(3) when the liquid level of a tower kettle 3 of the rectifying tower reaches 20 percent, heating and raising the temperature to slowly raise the temperature of the tower kettle 3, gradually raising the pressure of the rectifying tower 3 to an operation value, controlling the temperature of the tower kettle to be 85-100 ℃, controlling the pressure of the tower kettle to be 0.2-0.25 MPa (gauge pressure), controlling the temperature of the tower top to be 25-35 ℃, controlling the liquid level of the rectifying tower to be 30-60 percent, and controlling the pressure of the tower top to be 0.2-0.25 MPa (gauge pressure);
(4) after the liquid level of the reflux tank 8 reaches 30-40%, a reflux pump 7 is started to feed materials to the rectifying tower 3, reflux operation is carried out, and the liquid levels of the tower kettle and the reflux tank 8 are kept stable;
(5) when the tower kettle material is unqualified and the liquid level is higher, the kettle liquid pump 10 is started, and the kettle liquid pump 10 is started to return the material to the raw material tank 1;
(6) when the temperature at the top of the tower and the temperature at the bottom of the tower reach the operating values, sampling and analyzing that the content of gaseous chloroethylene at the top of the tower is more than 90 percent (v) and the content of chloroethylene at the bottom of the tower is less than 0.01 percent (w), opening a gas phase extraction regulating valve at the top of the tower to convey chloroethylene to a gas holder after the chloroethylene at the top of the tower is qualified, opening a liquid pump at the bottom of the tower to be cooled to 35 ℃ by a condenser, and conveying a liquid.
The technological parameters of the pressure distillation are as follows:
1050kg/h of feeding amount of the rectifying tower 3, 85-100 ℃ of tower kettle temperature of the rectifying tower 3, 0.2-0.25 MPa (gauge pressure) of tower kettle pressure, 25-35 ℃ of tower top temperature, 30-60% of rectifying tower liquid level, 0.2-0.25 MPa (gauge pressure) of tower top pressure, 160-230 kg/h of tower top reflux amount, more than 90% (v) of gaseous chloroethylene at an outlet of a brine cooler, and less than 0.01% (w) of tower kettle chloroethylene.
Then, normal pressure rectification is carried out: comprises the following steps
(1) Opening an inlet valve of a transfer pump of the intermediate tank 12, starting a feed pump 2, and transferring raw materials from the raw material tank 1 to the 5 th-6 th layer at the upper part of the rectifying tower 3 at a feeding amount of 750-;
(2) opening a second circulating water cooler 9 at the top of the rectifying tower 3 and hand valves of the brine cooler 5, and cooling gas distilled from the top of the rectifying tower 3 by a second circulating water condenser 9 and the brine cooler 5;
(3) when the liquid level of a tower kettle of the rectifying tower 3 reaches 20%, heating and slowly heating the tower kettle, gradually raising the pressure of the rectifying tower 3 to an operation value, controlling the temperature of the tower kettle to be 75-80 ℃, the pressure of the tower kettle to be 0.001-0.07 MPa (gauge pressure), the temperature of the tower top to be 55-60 ℃, the liquid level of the rectifying tower to be 30-60%, the pressure of the tower top to be 0.001-0.07 MPa (gauge pressure), and the reflux amount of the tower top to be 3800-5300 kg/h;
(4) after the liquid level of the reflux tank 8 reaches 30-40%, starting a reflux pump 7 to feed materials to the rectifying tower 3, keeping the liquid levels of the tower kettle and the reflux tank 8 stable, wherein the reflux amount at the tower top is 3800-5300 kg/h, and when the reflux tank 81 and 1-dichloroethane are more than 98% (w), discharging materials to a finished product tank 14;
(5) when the content of 1, 1-dichloroethane in the tower kettle tower is less than 30% (w), a kettle opening pump 10 is used for cooling the tower kettle tower 1, 1-dichloroethane to 35 ℃ through a condenser and conveying the kettle liquid to a mixed solvent tank 13.
The process parameters of the normal pressure rectification are as follows:
the feeding amount of the rectifying tower 3 is 750-800kg/h, the tower kettle temperature of the rectifying tower 3 is 75-80 ℃, the tower kettle pressure is 0.001-0.07 MPa (gauge pressure), the tower top temperature is 55-60 ℃, the liquid level of the rectifying tower is 30-60%, the tower top pressure is 0.001-0.07 MPa (gauge pressure), the tower top reflux amount is 3800-5300 kg/h, and the reflux tank 1, 1-dichloroethane is more than 98% (w).
The VCM high-boiling residue purification technology can produce the following beneficial effects: 1. the recovery rate of the chloroethylene in the dichloroethane generated by the PVC by the calcium carbide method can reach more than 99.5 percent (w). 2. The 1, 1-dichloroethane in the dichloroethane generated by PVC by calcium carbide method is purified to more than 98 percent (w) and can be directly sold as a product.
The invention has been described above with reference to the accompanying drawings, it is obvious that the invention is not limited to the specific implementation in the above-described manner, and it is within the scope of the invention to apply the inventive concept and solution to other applications without substantial modification.
Claims (2)
1. The utility model provides a VCM high boiling thing purification device which characterized in that: comprises a raw material tank, a rectifying tower, a water cooler, a brine cooler, a circulating water cooler, a reflux pump, a reflux tank, a circulating water cooler, an intermediate tank, a mixed solvent tank and a finished product tank, wherein the raw material tank is connected with the rectifying tower through a pipeline, a feed pump is arranged on a connecting pipeline of the raw material tank and the rectifying tower, the top of the rectifying tower is connected with the water cooler through a pipeline, the water cooler is connected with the brine cooler through a pipeline, the brine cooler is connected with the circulating water cooler I through a pipeline, the rectifying tower is connected with the finished product tank through a pipeline, the reflux pump is arranged on a connecting pipeline between the connecting pipelines of the rectifying tower and the finished product tank, the reflux pump is connected with the reflux tank through a pipeline, the reflux tank is connected with the water cooler through a pipeline, the bottom of the rectifying tower is connected with a circulating water cooler II through a pipeline, the circulating water cooler II is connected with the intermediate tank and, and a kettle liquid pump is arranged on a connecting pipeline between the rectifying tower and the circulating water cooler II, the intermediate tank is connected with the rectifying tower through a pipeline, and an intermediate tank delivery pump is arranged on the connecting pipeline between the rectifying tower and the intermediate tank.
2. A VCM high boiling substance purification method is characterized by comprising the following steps:
(1) performing pressure distillation, opening an inlet valve of a feed pump, starting the feed pump, and conveying the raw materials from a raw material tank to the 60 th to 62 th layers of the upper part of the distillation tower at a feed rate of 950-;
(2) opening hand valves of a water cooler and a brine cooler at the top of the rectifying tower, and cooling gas distilled from the top of the rectifying tower by the water cooler and the brine cooler;
(3) when the liquid level of the tower kettle of the rectifying tower reaches 20 percent, the liquid can be heated and heated to slowly heat the tower kettle, the pressure of the rectifying tower is gradually increased to an operation value, the temperature of the tower kettle is controlled to be 85-100 ℃, the pressure of the tower kettle is controlled to be 0.2-0.25 MPa (gauge pressure), the temperature of the top of the tower is controlled to be 25-35 ℃, the liquid level of the rectifying tower is controlled to be 30-60 percent, and the pressure of the top of the tower is controlled to be 0.2-0.25 MPa (gauge pressure);
(4) after the liquid level of the reflux tank reaches 30-40%, a reflux pump is started to feed materials to the rectifying tower, reflux operation is carried out, and the liquid levels of the tower kettle and the reflux tank are kept stable;
(5) starting a kettle liquid pump when the tower kettle material is unqualified and the liquid level is higher, and starting the kettle liquid pump to return the material to the raw material tank;
(6) when the temperature at the top of the tower and the temperature at the bottom of the tower reach operating values, sampling and analyzing that the content of gaseous chloroethylene at the top of the tower is more than 90 percent (v) and the content of chloroethylene at the bottom of the tower is less than 0.01 percent (w), opening a gas phase extraction regulating valve at the top of the tower to convey chloroethylene to a gas holder after the chloroethylene at the top of the tower is qualified, opening a liquid pump at the bottom of the tower, cooling the liquid pump to 35 ℃ through a condenser, and conveying;
(7) rectifying under normal pressure, opening an inlet valve of a transfer pump of the intermediate tank, starting a feed pump, and transferring raw materials from the raw material tank to the 5 th to 6 th layers of the upper part of the rectifying tower at the feeding amount of 750-;
(8) opening hand valves of a circulating water cooler II and a brine cooler on the top of the rectifying tower, and cooling gas distilled from the top of the rectifying tower by a circulating water condenser II and the brine cooler;
(9) when the liquid level of the tower kettle of the rectifying tower reaches 20%, heating and slowly heating the tower kettle, gradually raising the pressure of the rectifying tower to an operation value, controlling the temperature of the tower kettle to be 75-80 ℃, the pressure of the tower kettle to be 0.001-0.07 MPa (gauge pressure), the temperature of the tower top to be 55-60 ℃, the liquid level of the rectifying tower to be 30-60%, the pressure of the tower top to be 0.001-0.07 MPa (gauge pressure), and the reflux amount of the tower top to be 3800-5300 kg/h;
(10) after the liquid level of the reflux tank reaches 30-40%, feeding the material to a rectifying tower by starting a reflux pump, keeping the liquid levels of a tower kettle and the reflux tank stable, wherein the reflux amount at the top of the tower is 3800-5300 kg/h, and when the reflux amount of 1, 1-dichloroethane in the reflux tank is more than 98% (w), discharging the material to a finished product tank;
(11) when the content of 1, 1-dichloroethane in the tower kettle is less than 30% (w), a kettle liquid pump is started to convey kettle liquid to the mixed solvent tank after the kettle liquid pump is cooled to 35 ℃ by a condenser.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920453A (en) * | 2021-02-24 | 2021-06-08 | 唐山三友氯碱有限责任公司 | Special resin recovery monomer upgrading system for vinyl chloride and operation method thereof |
| CN113527043A (en) * | 2021-08-24 | 2021-10-22 | 天津市普莱特科技发展有限公司 | Treatment method of chloroethylene high-boiling residue |
| CN113648674A (en) * | 2021-08-31 | 2021-11-16 | 鄂尔多斯市君正能源化工有限公司 | Chloroethylene high-boiling residue treatment and purification system |
| WO2022261288A3 (en) * | 2021-06-09 | 2023-04-06 | Cemvita Factory, Inc. | Methods and compositions |
| CN116036626A (en) * | 2022-11-22 | 2023-05-02 | 安徽海华科技集团有限公司 | Quick high-efficient dewatering system of reaction raw materials |
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Application publication date: 20200922 |