CN105481640B - A kind of VCM rectification technique of the low loss of low energy consumption - Google Patents
A kind of VCM rectification technique of the low loss of low energy consumption Download PDFInfo
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- CN105481640B CN105481640B CN201510945426.9A CN201510945426A CN105481640B CN 105481640 B CN105481640 B CN 105481640B CN 201510945426 A CN201510945426 A CN 201510945426A CN 105481640 B CN105481640 B CN 105481640B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
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Abstract
The invention discloses a kind of VCM rectification techniques of the low loss of low energy consumption, comprising: (1) most thick vinyl chloride gas is carried out condensed in two stages liquefaction with recirculated water and chilled water respectively, liquid enters separator I and feeds pumped to low boiling tower middle and upper part；(2) uncooled gas enters tail gas condenser deep cooling, and condensate liquid enters separator II, flow to the charging of low boiling tower top certainly, and fixed gas send exhaust gas processing device；(3) low boiling tower overhead gas returns to conversion unit, and the thick vinyl chloride liquid of tower bottom enters high boiling tower；(4) high boiling tower top obtains vinyl chloride product, and tower is low to send residue treatment device for high-boiling components.The advance of this technique is: (1) using condensed in two stages low boiling tower overhead gas can be made to be recycled to front end conversion unit direct reuse, reduce Matter Transfer, reduce material and energy consumption effectively departing from the oxygen in light component；(2) water into rectifying column can be effectively reduced, the degree of vinyl chloride autohemagglutination in rectifying column is mitigated；(3) rectification efficiency and yield are improved, is economical and environmentally friendly worth with very big.
Description
Technical field
The present invention relates to a kind of VCM rectification technique of the low loss of low energy consumption, especially carbides to produce vinyl chloride process
It is middle to reduce energy consumption, reduce vinyl chloride and the rectification process of acetylene loss.
Background technique
Vinyl chloride (abbreviation VCM) be produce polyvinyl chloride (abbreviation PVC) raw material, due to PVC material extensive use and
It is mass produced.There are mainly two types of the methods for producing vinyl chloride, and process for oxychlorination of ethylene and acetylene method, acetylene method are also referred to as calcium carbide
Method, domestic PVC manufacturing enterprise generally use carbide to produce vinyl chloride.In the thick vinyl chloride gas obtained from carbide toward
Toward containing weights composition impurities such as acetylene, acetaldehyde, nitrogen, oxygen, dichloroethylene, dichloroethanes, trichloro ethylenes, need by essence
The very high vinyl chloride product of purity could be obtained for PVC polymerization by evaporating process removing impurity.
The distillation process of vinyl chloride is usually made of processes such as gas liquefaction dehydration, removing light component, removing heavy constituents.Pressure
The thick vinyl chloride gas that compression process comes is introduced into complete condenser and most vinyl chloride gas liquefies, and liquid enters separator
Low boiling tower is transported to through pump after removing partial moisture；The light component in thick vinyl chloride such as acetylene, acetaldehyde, nitrogen are removed in low boiling tower
Gas, oxygen etc., the light-component gas containing vinyl chloride that tower top obtains enter tail gas condenser with the not solidifying gas of complete condenser together
Further condensing recovery vinyl chloride；The condensate liquid of tail gas condenser enters separator and enters back into low boiling tower, and solidifying tail gas is not gone
Pressure-variable adsorption or other recyclable devices recycle acetylene and vinyl chloride therein；The vinyl chloride liquid without light component of low boiling tower tower bottom
Body flows automatically by pressure difference or enters high boiling tower with the mode of pump conveying, removes heavy constituent such as dichloroethylene, two in high boiling tower
Chloroethanes, trichloro ethylene etc., the vinyl chloride gas that tower top obtains high-purity is that final products use for PVC polymerization, tower bottom
The further rectifying of high-boiling components recycle the products such as vinyl chloride and dichloroethanes.
Although PVC manufacturing enterprise is most widely used at home for this rectification process, there are some unreasonable places to lead to energy
Source consumes the problems such as more, vinyl chloride and more acetylene loss:
(1) complete condenser uses 5 DEG C of chilled waters to be condensed completely, consumes a large amount of chilled waters, is unfavorable for energy conservation, meanwhile, entirely
Condenser condensation temperature is higher (25~30 DEG C), since solubility with temperature of the water in vinyl chloride increases and increases, Gu Shui separation
The water that device is isolated is less, and the water into rectifying column is more, to exacerbate the degree of vinyl chloride autohemagglutination in tower；
(2) vinyl chloride of the overwhelming majority is condensed into liquid in an equipment, it will make the acetylene carried secretly in liquid, lazy
The gases such as gas are more, participate in low boiling tower-tail gas condenser-separator-vinyl chloride of low boiling tower circulation and the amount of other components
Also it increases with it, increasing produce load influences product quality；
(3) since the condensate liquid of tail gas condenser and the composition of thick vinyl chloride liquid and temperature are different, after mixing again into
Enter low boiling tower, reduces the rectification efficiency of low boiling tower, increase energy consumption；
(4) contain acetylene and a large amount of vinyl chloride in the tail gas of tail gas condenser discharge, become although some enterprises use
Pressure absorption or other methods are recycled, but the efficiency for being limited recycling by many-sided condition is lower, consumes many energy in vain
Source is discharged into a large amount of acetylene and vinyl chloride in atmosphere, not only causes very big economic loss to enterprise, also polluted
Environment.
Chinese patent CN102516023B discloses a kind of rectification process of vinyl chloride, will be outside the overhead condenser of low boiling tower
Set, condensate liquid enters a surge tank, pumped and condensate liquid be driven at the top of low boiling tower, the reflux ratio of adjustable low boiling tower into
And control the content of acetylene in vinyl chloride.Chinese patent CN102675034B discloses a kind of method of vinyl chloride monomer purification,
Inorganic impurity and water in vinyl chloride gas first are removed with the mode of physical absorption, then the rectifying under low temperature, vacuum environment again
The substance for separating different boiling, obtains vinyl chloride gas.Above-mentioned first patent is from the angle of reflux ratio is adjusted to low boiling
Tower is improved, and could not be optimized on the whole to existing rectification process；Second patent uses entirely different side
Formula cleaning vinyl chloride monomer, but the requirement of operating process conditional is harsh, energy consumption is high, the residence time is long, utilization rate of equipment and installations is low, no
Suitable for industrializing continuous mass production.
Summary of the invention
It is an object of the invention to solve common problem in existing VCM rectification technique, it is low to provide a kind of low energy consumption
The VCM rectification technique of loss, improves optimization to existing rectification process on the whole, to reduce energy consumption, reduce chloroethene
The loss of alkene and acetylene.
To achieve the goals above, the present invention improves existing rectification process, is mainly reflected in: thick vinyl chloride gas
Condensation liquefaction be divided into two-stage: the first order is that thick vinyl chloride gas is condensed into liquid, the second level in complete condenser I with recirculated water
It is further to condense the condensed liquid of complete condenser I with chilled water in complete condenser II, uncooled thick vinyl chloride gas is used
Chilled water further condenses in complete condenser III；The thick vinyl chloride liquid condensed out in complete condenser II and complete condenser III enters
It is delivered to low boiling tower through pump after dehydration in first order separator I, uncooled gas enters tail gas condenser in complete condenser III
Deep cooling, gravity flow enters low boiling tower after the thick vinyl chloride liquid condensed out is dehydrated in the separator II of the second level；Low boiling tower tower
Top gas body returns to conversion unit；The thick vinyl chloride liquid of low boiling tower tower bottom enters high boiling tower removing high-boiling components, high boiling column overhead
Obtain vinyl chloride gas product；The waste water and high boiling tower tower bottom of first order separator I and second level separator II removing
High-boiling components collect storage respectively, recycle vinyl chloride and dichloroethanes therein.
Thick vinyl chloride liquefaction process of the present invention needs two separators: first order separator I and the second level
Separator II；Three complete condensers are needed, complete condenser I is condensed thick vinyl chloride gas to 30~40 DEG C with recirculated water, condensation
Liquid enters after complete condenser II freezing is water-cooled to 15~25 DEG C and enters separator I；The uncooled gas of complete condenser I enters
Complete condenser III is with freezing water condensation to 15~25 DEG C, and condensate liquid also enters first order separator I, and uncooled gas is gone
Tail gas condenser；Arrange from high to low complete condenser I, complete condenser II, the position of first order separator I and complete condenser III with
There is certain difference in height to guarantee that liquid can flow automatically under entrance from an equipment for the position of first order separator I, two equipment rooms
One equipment.
- 35 DEG C of tail gas condenser use of chilled brine condensation of the present invention, gaseous phase outlet temperature are -10~-20 DEG C,
Tail gas removes pressure-variable adsorption or other recyclable devices recycle acetylene and vinyl chloride, and condensate liquid flows after second level separator II dehydration
Enter low boiling tower；From high to low arrange tail gas condenser, second level separator II, low boiling tower position, two equipment rooms have one
Fixed difference in height guarantees that liquid can flow automatically from an equipment and enters next equipment；The row of first order separator I and second level II
The frequency for putting waste water is 2h/ times, and waste water uniform effluent is recycled vinyl chloride therein into waste water tank.
Each equipment of the present invention pressure control be respectively tail gas condenser gaseous phase outlet pressure be 0.45~
(MPa is pressure unit to 0.55MPa, and the present invention refers to gauge pressure, 1MPa=1 × 106Pa, similarly hereinafter)；Low boiling tower tower top pressure is 0.45
~0.55MPa, tower reactor pressure are 0.48~0.58MPa；High boiling tower tower top pressure is 0.25~0.35MPa, and tower reactor pressure is 0.3
~0.4MPa.
Low boiling tower and high boiling tower of the present invention are the sieve-plate tower with interior reflux condenser and reboiler, the number of plates
It is 30~50 pieces；The feed entrance point of low boiling tower compares the first order in liquid feedstock position in the top of tower, second level separator II
High 2~4 blocks of column plates of the feed entrance point of separator I, the condensate liquid of tower top deep freezer is the same as the liquid in the separator II of the second level
Enter low boiling tower in same feed inlet；Low boiling tower reflux ratio is 1~10, and the temperature of overhead condenser is 25~35 DEG C, and tower top is deep
The temperature of cooler is 10~20 DEG C, and bottom temperature is 38~42 DEG C；The feed entrance point of high boiling tower is in the middle and lower part of tower, reflux ratio
0.01~1, the temperature of overhead condenser is 20~30 DEG C, and bottom temperature is 30~40 DEG C, and tower bottom high-boiling components are discharged into storage tank recycling
VCM and dichloroethanes.
Compared with existing rectification process, the invention has the following advantages that first is that slightly the vinyl chloride gas condensation liquefaction stage makes
Partial freeze water is replaced with recirculated water, saves 50% or more water consumption of freezing, and can with the cooling vinyl chloride liquid of freezing water depth
The liquid for entering separator is cooled to lower temperature, so that increase separator divides water effect, it is lowered into low
Boil the water content in the vinyl chloride of tower；Second is that the thick vinyl chloride gas of fractional condensaion, drastically reduces the liquid into low boiling tower
The amount of middle noble gas alleviates the produce load of low boiling tower, improves rectification yield, saved the energy；Third is that eliminating low boiling tower-
Tail gas condenser-separator-low boiling tower cyclic process, largely reduces energy consumption, improves rectifying effect
Rate；Fourth is that low boiling tower overhead gas returns to conversion unit after level-one deep cooling, the fluctuation of low boiling tower tower top pressure is alleviated,
A large amount of unconverted acetylene are directly applied to conversion, not only shorten the process of acetylene reuse, have saved the energy, and reduce
The loss of acetylene；Fifth is that the gas of low boiling column overhead does not enter back into tail gas condenser, the amount of tail gas is drastically reduced, is mitigated
The burden of pressure-variable adsorption or other recyclable devices, to reduce the consumption of the energy, and reduces the damage of vinyl chloride and acetylene
It loses.
Detailed description of the invention
Fig. 1 is existing VCM rectification process flow diagram.
Fig. 2 is VCM rectification process flow diagram provided by the invention.
Wherein, 1 is complete condenser I, and 2 be complete condenser II, and 3 be complete condenser III, and 4 be first order separator I, and 5 be that tail gas is cold
Condenser, 6 be low boiling tower feed pump, and 7 be low boiling tower, and 8 be high boiling tower, and 9 be second level separator II, and 10 be that low boiling column overhead is deep
Cooler, S1 are thick vinyl chloride gas, and S2 is waste water, and S3 is tail gas, and S4 is vinyl chloride product, and S5 is high-boiling components, and S6 is revolutionization
Gas.
Specific embodiment
The present invention provides a kind of VCM rectification techniques of the low loss of low energy consumption, with reference to the accompanying drawings and examples and
The present invention is further illustrated with the comparative example of existing rectification process comparison.
The process flow of embodiment 1,2 is cooled with circulating water as shown in Fig. 2, thick vinyl chloride gas S1 enters complete condenser I 1
Thick vinyl chloride gas, condensate liquid enter complete condenser II 2, and fixed gas enters complete condenser III 3；In complete condenser II 2, complete condenser
The III 3 interior cooling thick vinyl chloride liquid of chilled water, gas, condensate liquid enter first order separator I 4, and on-condensible gas enters
Tail gas condenser 5；The upper of low boiling tower 7 is transported to through low boiling tower feed pump 6 after dehydrate liquids in first order separator I 4
Portion, the chilled brine cooling gas of tail gas condenser 5, condensate liquid also enter low after being dehydrated in second level separator II 9
The top of tower 7 is boiled, solidifying tail gas S3 does not remove pressure-variable adsorption then or other recyclable devices recycle vinyl chloride and acetylene, two water separation
The frequency of device waste discharge is 2h/ times, and waste water S2 enters waste water tank to recycle vinyl chloride；Light component is removed in low boiling tower 7,
Tower bottom obtains the thick vinyl chloride liquid without light component, and the gas that tower top contains vinyl chloride enters tower top deep freezer 10 and uses chilled water
Cooling, in liquid reflux to tower, on-condensible gas S6 then returns to conversion unit；The thick vinyl chloride liquid of 7 tower bottom of low boiling tower enters
The middle and lower part of high boiling tower 8, controls the operating condition of high boiling tower 8, and tower top obtains vinyl chloride gas product S4, the high-boiling components S5 of tower bottom
Into storage tank to recycle vinyl chloride and dichloroethanes etc..
The process of existing rectification process is as shown in Figure 1, thick vinyl chloride gas S1 enters complete condenser I 1, with freezing water condensation
To 25~35 DEG C, condensate liquid enters dehydration, fixed gas in first order separator I 4 and enters tail gas condenser 5 and use chilled brine
- 10~-20 DEG C are cooled to, the condensate liquid of tail gas condenser also enters in first order separator I 4, and tail gas S3 then goes transformation to inhale
Attached or other recyclable device recycling vinyl chloride and acetylene；Thick vinyl chloride liquid in first order separator I 4 through low boiling tower into
Material pump 6 is delivered to the top of low boiling tower 7, and the frequency of waste discharge is 2h/ times, and waste water S2 enters waste water tank to recycle vinyl chloride；
Light-component gas is separated from thick vinyl chloride in low boiling tower 7, overhead gas enters tail gas condenser condensation, and tower bottom is not
Thick vinyl chloride liquid containing light component enters the middle and lower part of high boiling tower 8；The operating condition for controlling high boiling tower 8, obtains chlorine in tower top
Ethylene gas product S4, the high-boiling components S5 of tower bottom enter storage tank recycling vinyl chloride and dichloroethanes etc..
Percentage composition composition in stock is respectively flowed in embodiment and comparative example each means that mass percent, reflux ratio each mean quality
Reflux ratio, pressure each mean gauge pressure.
Embodiment 1:
The heat exchanger addressed is tubular heat exchanger, and low boiling tower, high boiling tower are vertical sieve plate column, number of plates difference
It is 36,44.The flow of thick vinyl chloride gas S1 is 10000kg/h, temperature is 50 DEG C, pressure 0.51MPa, composition are as follows: chloroethene
Alkene 98.62%, acetylene 0.21%, water 0.42%, dichloroethanes etc. 0.37%, nitrogen etc. 0.38%.Thick vinyl chloride gas is complete
36 DEG C are cooled in condenser I, about 90% gas is condensed into liquid, 20 DEG C is cooled in complete condenser II, III, in tail gas
- 15 DEG C are cooled in condenser, the gas outlet pressure of tail gas condenser is 0.5MPa；It is removed water by two separators
Afterwards, thick vinyl chloride liquid enters low boiling tower, low boiling tower tower top pressure 0.5MPa, tower reactor pressure at the 4th, 6 block of column plate respectively
0.52MPa, reflux ratio 8,25 DEG C of tower top temperature；Low boiling column overhead deep freezer is cooled to low boiling tower overhead gas with chilled water
10 DEG C, condensate liquid is back in tower in the 4th block of column plate, and fixed gas S6 returns conversion unit；The thick vinyl chloride liquid that low boiling tower comes
Enter high boiling tower, high boiling tower tower top pressure 0.3MPa, tower reactor pressure 0.325MPa, reflux ratio 0.1, tower reactor in the 30th block of column plate
Temperature is 35 DEG C, obtains vinyl chloride product S4 in tower top.Waste water S2, tail gas S3 and high-boiling components S5 are required to be further processed to return
Receive acetylene therein, vinyl chloride, dichloroethanes etc..
Resulting vinyl chloride product the results are shown in Table shown in 1, table 2.
Embodiment 2:
The heat exchanger addressed is tubular heat exchanger, and low boiling tower, high boiling tower are vertical sieve plate column, number of plates difference
It is 36,44.The flow of thick vinyl chloride gas S1 is 10000kg/h, temperature is 50 DEG C, pressure 0.51MPa, composition are as follows: chloroethene
Alkene 98.62%, acetylene 0.21%, water 0.42%, dichloroethanes etc. 0.37%, nitrogen etc. 0.38%.Thick vinyl chloride gas is complete
40 DEG C are cooled in condenser I, about 55% gas is condensed into liquid, 20 DEG C is cooled in complete condenser II, III, in tail gas
- 15 DEG C are cooled in condenser, the gas outlet pressure of tail gas condenser is 0.5MPa；It is removed water by two separators
Afterwards, thick vinyl chloride liquid enters low boiling tower, low boiling tower tower top pressure 0.5MPa, tower reactor pressure at the 4th, 6 block of column plate respectively
0.52MPa, reflux ratio 8,25 DEG C of tower top temperature；Low boiling column overhead deep freezer is cooled to low boiling tower overhead gas with chilled water
10 DEG C, condensate liquid is back in tower in the 4th block of column plate, and fixed gas S6 returns conversion unit；The thick vinyl chloride liquid that low boiling tower comes
Enter high boiling tower, high boiling tower tower top pressure 0.3MPa, tower reactor pressure 0.325MPa, reflux ratio 0.1, tower reactor in the 30th block of column plate
Temperature is 35 DEG C, obtains vinyl chloride product S4 in tower top.Waste water S2, tail gas S3 and high-boiling components S5 are required to be further processed to return
Receive acetylene therein, vinyl chloride, dichloroethanes etc..
Resulting vinyl chloride product the results are shown in Table shown in 1, table 2.
Comparative example:
The heat exchanger addressed is tubular heat exchanger, and low boiling tower, high boiling tower are vertical sieve plate column, number of plates difference
It is 36,44.The flow of thick vinyl chloride gas S1 is 10000kg/h, temperature is 50 DEG C, pressure 0.51MPa, composition are as follows: chloroethene
Alkene 98.62%, acetylene 0.21%, water 0.42%, dichloroethanes etc. 0.37%, nitrogen etc. 0.38%.Thick vinyl chloride gas is complete
25 DEG C are cooled in condenser I, about 98% gas is condensed into liquid, -15 DEG C are cooled in tail gas condenser, tail gas condenser
Gas outlet pressure is 0.5MPa；After two separators remove water, thick vinyl chloride liquid respectively at the 4th, 6 block of column plate into
Enter low boiling tower, low boiling tower tower top pressure 0.5MPa, tower reactor pressure 0.52MPa, reflux ratio 8,25 DEG C of tower top temperature；Low boiling tower mistake
The thick vinyl chloride liquid come enters high boiling tower in the 30th block of column plate, high boiling tower tower top pressure 0.3MPa, tower reactor pressure 0.325MPa,
Reflux ratio is 0.1, and bottom temperature is 35 DEG C, obtains vinyl chloride product S4 in tower top.Waste water S2, tail gas S3 and high-boiling components S5 are both needed to
It is further processed to recycle acetylene therein, vinyl chloride, dichloroethanes etc..
By the result data in table 1,2 as it can be seen that rectification process provided by the invention is compared with existing rectification process, can incite somebody to action
The purity of vinyl chloride product is increased to 99.91% by 99.83%, and yield is increased to 99.6% by 98.39%, and acetylene content reduces
To 1~2ppm, 700ppm and 200ppm is also greatly reduced to for the content of water and high-boiling components hereinafter, obtained vinyl chloride product can
For the special industry more demanding to product purity.The characteristic that recirculated water is at low cost is made full use of, freezing is significantly reduced
The dosage of water and chilled brine reduces the situation of vinyl chloride autohemagglutination in the water mitigation tower for enter rectifying column.Meanwhile it directly recycling
Low boiling tower overhead gas goes to convert, and reduces the amount of the acetylene and vinyl chloride i.e. loss of acetylene and vinyl chloride in emission, subtracts
The light load of vent gas treatment.
Resulting vinyl chloride product the results are shown in Table shown in 1, table 2.
The Comparative result of 1 embodiment of table and the obtained vinyl chloride product of comparative example
| Raw material S1 | Embodiment 1S4 | Embodiment 2S4 | Comparative example S4 | |
| Vinyl chloride | 98.62% | 99.91% | 99.91% | 99.83% |
| Acetylene | 0.21% | 2ppm | 1ppm | 12ppm |
| Water | 0.42% | 700ppm | 690ppm | 1230ppm |
| High-boiling components | 0.37% | 173ppm | 194ppm | 414 |
| Chloro ethylene yield | 98.62% | 98.57 | 98.39% |
The Comparative results such as 2 embodiment of table and comparative example energy consumption
Claims (6)
1. a kind of VCM rectification technique of the low loss of low energy consumption, which is characterized in that including following operating procedure: thick vinyl chloride gas
The condensation liquefaction of body is divided into two-stage: the first order is that thick vinyl chloride gas is condensed into liquid in complete condenser I with recirculated water, second
Grade is further to condense the condensed liquid of complete condenser I with chilled water in complete condenser II, uncooled thick vinyl chloride gas
It is further condensed in complete condenser III with chilled water；The thick vinyl chloride liquid condensed out in complete condenser II and complete condenser III into
Enter in first order separator I and be delivered to low boiling tower through pump after dehydration, uncooled gas enters tail gas condensing in complete condenser III
Device deep cooling, gravity flow enters low boiling tower after the thick vinyl chloride liquid condensed out is dehydrated in the separator II of the second level；Low boiling tower
Overhead gas returns to conversion unit；The thick vinyl chloride liquid of low boiling tower tower bottom enters high boiling tower removing high-boiling components, high boiling tower tower
Top obtains vinyl chloride gas product；The waste water and high boiling tower tower of first order separator I and second level separator II removing
The high-boiling components at bottom collect storage respectively, recycle vinyl chloride and dichloroethanes therein.
2. a kind of VCM rectification technique of the low loss of low energy consumption according to claim 1, which is characterized in that there are two water
Separator, the first order separator I namely for complete condenser condensate liquid and the second level for tail gas condenser condensate liquid
The frequency of the waste discharge of separator II, first order separator I and second level separator II is 2h/ times, waste water row
Enter waste water tank and recycles vinyl chloride therein.
3. according to claim 1 with a kind of low energy consumption as claimed in claim 2 low loss VCM rectification technique, feature exists
Three complete condensers are needed in thick vinyl chloride liquefaction process, complete condenser I is condensed thick vinyl chloride gas to 30~40 DEG C with recirculated water,
The liquid of condensation enters after complete condenser II freezing is water-cooled to 15~25 DEG C and enters first order separator I；Complete condenser I is not cold
Solidifying gas enters complete condenser III with freezing water condensation to 15~25 DEG C, and condensate liquid also enters first order separator I, not
The gas of condensation removes tail gas condenser；The position of complete condenser I, complete condenser II, first order separator I are arranged from high to low, with
And there is certain difference in height to guarantee that liquid can be set from one for the position of complete condenser III and first order separator I, two equipment rooms
Standby gravity flow enters next equipment.
4. according to claim 1 with a kind of low energy consumption as claimed in claim 2 low loss VCM rectification technique, feature exists
In low boiling tower and high boiling tower are the sieve-plate towers with interior reflux condenser and reboiler, and the number of plates is 30~50 pieces；Low boiling tower
Feed entrance point in the top of tower, the second level separator II feed position of the liquid feedstock position than first order separator I
High 2~4 blocks of column plates are set, the condensate liquid of tower top deep freezer enters with the liquid in the separator II of the second level in same feed inlet low
Boil tower；The feed entrance point of high boiling tower is in the middle and lower part of tower.
5. a kind of VCM rectification technique of the low loss of low energy consumption according to claim 1, which is characterized in that tail gas condensing
The pressure of the gaseous phase outlet of device is 0.45~0.55MPa；Low boiling tower tower top pressure is 0.45~0.55MPa, and tower reactor pressure is
0.48~0.58MPa；High boiling tower tower top pressure is 0.25~0.35MPa, and tower reactor pressure is 0.3~0.4MPa.
6. a kind of VCM rectification technique of the low loss of low energy consumption according to claim 1, which is characterized in that low boiling tower is returned
For stream than being 1~10, the temperature of overhead condenser is 25~35 DEG C, and the temperature of tower top deep freezer is 10~20 DEG C, and bottom temperature is
38~42 DEG C；The reflux ratio of high boiling tower is 0.01~1, and the temperature of overhead condenser is 20~30 DEG C, and bottom temperature is 30~40
DEG C, tower bottom high-boiling components are discharged into storage tank recycling VCM and dichloroethanes.
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| CN107235823B (en) * | 2017-06-27 | 2021-11-16 | 山东新龙科技股份有限公司 | Process and equipment for recovering and refining calcium carbide VCM high-boiling residues |
| CN109651066B (en) * | 2018-12-29 | 2023-08-22 | 南通东港化工有限公司 | Production system of 1, 2-trichloroethane |
| CN113121306B (en) * | 2019-12-31 | 2022-11-29 | 蓝星（北京）技术中心有限公司 | Chloroprene concentrating system and refrigerant control method thereof |
| CN113121305B (en) * | 2019-12-31 | 2023-02-03 | 蓝星（北京）技术中心有限公司 | Chloroprene concentrating system |
| CN111440066A (en) * | 2020-04-16 | 2020-07-24 | 太原理工大学 | Pre-separation process for synthesizing dimethyl carbonate product by chlorine-free catalysis |
| CN112717669A (en) * | 2020-12-15 | 2021-04-30 | 内蒙古亿利化学工业有限公司 | Polymerization tail gas processing system in chloroethylene production |
| 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 |
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| DE4342042A1 (en) * | 1993-12-09 | 1995-06-14 | Hoechst Ag | Process and apparatus for cleaning vinyl chloride |
| CN203355329U (en) * | 2013-06-09 | 2013-12-25 | 内蒙古三联金山化工有限责任公司 | Coarse vinyl chloride distillation system |
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