CN210934373U - Chloroethylene rectification tail gas solvent method absorption device - Google Patents
Chloroethylene rectification tail gas solvent method absorption device Download PDFInfo
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- CN210934373U CN210934373U CN201921463025.XU CN201921463025U CN210934373U CN 210934373 U CN210934373 U CN 210934373U CN 201921463025 U CN201921463025 U CN 201921463025U CN 210934373 U CN210934373 U CN 210934373U
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Abstract
The utility model relates to a tail gas treatment technical field is a chloroethylene rectification tail gas solvent method absorbing device, and it includes absorbent cooler, absorption tower, top of the tower condensation cooler, tower cauldron cooler, defroster, absorption fluid reservoir, and the fixed intercommunication in the first import of absorbent cooler bottom has absorbent feed line, and the fixed intercommunication in absorption tower middle part import has chloroethylene rectification tail gas line, and fixed intercommunication has top of the tower condensation cooler feed line between the export of absorption tower top and the import of top of the tower condensation cooler upper portion. The utility model has the advantages of reasonable and compact structure, convenient to use, it utilizes refined dichloroethane to absorb chloroethylene rectification tail gas, has reduced impurity content among tail gas flow, the chloroethylene content in the tail gas, the chloroethylene monomer, realizes tail gas absorption processing, resource cyclic utilization, makes chloroethylene rectification tail gas discharge to reach standard, has safety, with low costs, simple and convenient efficient characteristics.
Description
Technical Field
The utility model relates to a tail gas treatment technical field is a vinyl chloride rectification tail gas solvent method absorbing device.
Background
The production of polyvinyl chloride resin by calcium carbide method is the main production process of polyvinyl chloride resin in China, the total domestic polyvinyl chloride energy is 2500 ten thousand tons/year, the calcium carbide method capacity is 1925 ten thousand tons, and the proportion is nearly 80%. The calcium carbide method is a production method for synthesizing polyvinyl chloride resin by polymerizing Vinyl Chloride Monomer (VCM) by using calcium carbide as a raw material to produce acetylene, using acetylene and hydrogen chloride as raw materials to produce VCM. In the production process of chloroethylene, low-boiling-point substances are discharged from the top of the rectification low-boiling tower,and (4) conveying the condensed tail gas to a pressure swing adsorption device for treatment, and feeding the recovered acetylene gas and chloroethylene gas into a conversion system again for synthesis reaction. The part of the vinyl chloride gas participates in the reaction along with the converter to form a side reaction product, and the content of impurities in the vinyl chloride monomer is increased. Meanwhile, GB15581-2016 emission Standard of Industrial pollutants for caustic soda and polyvinyl chloride relates to that the content of chloroethylene in a chloroethylene rectification tail discharge outlet of a pollutant facility purification discharge outlet is 36mg/m3Adjusted to 10mg/m3And it is clear that the existing commissioned devices and new-start construction devices all implement this new standard since 7/1/2018. The prior chloroethylene rectifying device adopts a pressure swing adsorption tail gas treatment process, and the emission of rectifying tail gas can reach 36mg/m3But to meet the new standard of 10mg/m3The requirement of (2) is that enterprises have the problems that the discharge amount of chloroethylene rectification tail gas is large, impurities are easily generated in a chloroethylene monomer, the production load has to be reduced or production is stopped, and a matched pressure swing adsorption device is increased.
Disclosure of Invention
The utility model provides a chloroethylene rectification tail gas solvent method absorbing device has overcome above-mentioned prior art not enough, and it can effectively solve current chloroethylene production process, and the enterprise has chloroethylene rectification tail gas emission big, produce impurity easily among the chloroethylene monomer, has to reduce the production load or produce the problem of stopping, increase supporting pressure swing adsorption equipment.
The technical scheme of the utility model is realized through following measure: a chloroethylene rectification tail gas solvent absorption device comprises an absorbent cooler, an absorption tower, a tower top condensation cooler, a tower kettle cooler, a demister and an absorption liquid tank, wherein a first inlet at the bottom of the absorbent cooler is fixedly communicated with an absorbent feeding pipeline, a second inlet at the bottom of the absorbent cooler is fixedly communicated with a first chilled brine feeding pipeline, an absorbent discharging pipeline is fixedly communicated between a first outlet at the top of the absorbent cooler and a first inlet at the upper part of the absorption tower, a second outlet at the top of the absorbent cooler is fixedly communicated with a first chilled brine return pipeline, a tail gas pipeline of chloroethylene rectification is fixedly communicated with an inlet at the middle part of the absorption tower, a feeding pipeline of the tower top condensation cooler is fixedly communicated between an outlet at the top of the absorption tower and an inlet at the upper part of the tower top condensation cooler, a first outlet at the upper part of the tower top condensation cooler is fixedly communicated with a second chilled brine return pipeline, a demister feeding pipeline is fixedly communicated between a second outlet at the upper part of the tower top condensing cooler and an inlet at the lower part of the demister, a second frozen brine upper water pipeline is fixedly communicated with an inlet at the lower part of the tower top condensing cooler, a tower top condensing cooler discharging pipeline is fixedly communicated with an outlet at the bottom of the tower top condensing cooler, a first demister discharging pipeline is fixedly communicated with an outlet at the top of the demister, a second demister discharging pipeline is fixedly communicated with an outlet at the bottom of the demister, an outlet of the tower top condensing cooler discharging pipeline is fixedly communicated with the second demister discharging pipeline, a tower kettle cooler discharging pipeline is fixedly communicated between a second inlet at the upper part of the absorption tower and a first outlet at the top of the tower kettle cooler, a third frozen brine return pipeline is fixedly communicated with a second outlet at the top of the tower kettle cooler, a tower kettle cooler feeding pipeline is fixedly communicated between the first inlet at the bottom of the tower kettle cooler and the, the fixed intercommunication of tower cauldron cooler bottom second import has third frozen brine water pipeline, and second defroster discharge line export is linked together with tower cauldron cooler feed line is fixed, and fixed intercommunication has absorption fluid reservoir feed line between absorption fluid reservoir top import and the tower cauldron cooler feed line, and the fixed intercommunication of absorption fluid reservoir top export has the first discharge line of absorption fluid reservoir, and the fixed intercommunication of absorption fluid reservoir bottom export has absorption fluid reservoir second discharge line.
The following are further optimization or/and improvement of the technical scheme of the utility model:
an emptying pipeline is fixedly communicated with the first demister discharging pipe line.
And a third discharge pipeline of the absorption liquid tank is fixedly communicated with the second discharge pipeline of the absorption liquid tank.
A tower kettle cooler feed pump is fixedly mounted on the tower kettle cooler feed line, and a feed pump circulating line is fixedly communicated with the inlet of the tower kettle cooler feed pump and the tower kettle cooler feed line at the outlet of the tower kettle cooler feed pump.
A demister circulating pipeline is fixedly communicated between the second demister discharge pipeline and the absorption liquid tank feeding pipeline, and an absorption liquid tank feeding pump is fixedly mounted on the demister circulating pipeline.
And a first absorption liquid conveying pump is fixedly arranged on the second discharge pipe line of the absorption liquid tank, an absorption liquid circulating pipeline is fixedly communicated with the second discharge pipe line of the absorption liquid tank at the inlet and the outlet of the first absorption liquid conveying pump, and a second absorption liquid conveying pump is fixedly arranged on the absorption liquid circulating pipeline.
An absorbent thermometer is fixedly installed on the absorbent discharging pipe line, an overhead condensation cooler thermometer is fixedly installed on the overhead condensation cooler discharging pipe line, and a tower kettle cooler thermometer is fixedly installed on the tower kettle cooler discharging pipe line.
The utility model has the advantages of reasonable and compact structure, convenient to use, it utilizes refined dichloroethane to absorb chloroethylene rectification tail gas, has reduced impurity content among tail gas flow, the chloroethylene content in the tail gas, the chloroethylene monomer, realizes tail gas absorption processing, resource cyclic utilization, makes chloroethylene rectification tail gas discharge to reach standard, has safety, with low costs, simple and convenient efficient characteristics.
Drawings
FIG. 1 is a schematic process flow diagram of the preferred embodiment of the present invention.
The codes in the figures are respectively: 1 is an absorbent cooler, 2 is an absorption tower, 3 is a tower top condensing cooler, 4 is a tower kettle cooler, 5 is a demister, 6 is an absorption liquid tank, 7 is an absorbent feeding pipeline, 8 is a first frozen brine water feeding pipeline, 9 is an absorbent discharging pipeline, 10 is a first frozen brine water returning pipeline, 11 is a chloroethylene rectification tail gas pipeline, 12 is a tower top condensing cooler feeding pipeline, 13 is a second frozen brine water returning pipeline, 14 is a demister feeding pipeline, 15 is a second frozen brine water feeding pipeline, 16 is a tower top condensing cooler discharging pipeline, 17 is a first demister discharging pipeline, 18 is a second demister discharging pipeline, 19 is a tower kettle cooler discharging pipeline, 20 is a third frozen brine water returning pipeline, 21 is a tower kettle cooler feeding pipeline, 22 is a third frozen brine water feeding pipeline, 23 is an absorption liquid tank feeding pipeline, and 24 is an absorption first discharging pipeline, 25 is a second discharge pipeline of the absorption liquid tank, 26 is an emptying pipeline, 27 is a third discharge pipeline of the absorption liquid tank, 28 is a feeding pump of a tower bottom cooler, 29 is a feeding pump circulation pipeline, 30 is a demister circulation pipeline, 31 is a feeding pump of the absorption liquid tank, 32 is a first absorption liquid conveying pump, 33 is an absorption liquid circulation pipeline, 34 is a second absorption liquid conveying pump, 35 is an absorbent thermometer, 36 is a thermometer of a condensation cooler at the top of the tower, and 37 is a thermometer of the tower bottom cooler.
Detailed Description
The utility model discloses do not receive the restriction of following embodiment, can be according to the utility model discloses a technical scheme and actual conditions determine concrete implementation.
In the present invention, for convenience of description, the description of the relative position relationship of the components is described according to the layout mode of the attached drawing 1 in the specification, such as: the positional relationship of front, rear, upper, lower, left, right, etc. is determined in accordance with the layout direction of fig. 1 of the specification.
The invention will be further described with reference to the following examples and drawings:
as shown in figure 1, the chloroethylene rectification tail gas solvent method absorption device comprises an absorbent cooler 1, an absorption tower 2, a tower top condensation cooler 3, a tower bottom cooler 4, a demister 5 and an absorption liquid tank 6, wherein a first inlet at the bottom of the absorbent cooler 1 is fixedly communicated with an absorbent feeding pipeline 7, a second inlet at the bottom of the absorbent cooler 1 is fixedly communicated with a first frozen brine feeding pipeline 8, an absorbent discharging pipeline 9 is fixedly communicated between a first outlet at the top of the absorbent cooler 1 and a first inlet at the upper part of the absorption tower 2, a second outlet at the top of the absorbent cooler 1 is fixedly communicated with a first frozen brine return pipeline 10, an inlet at the middle part of the absorption tower 2 is fixedly communicated with a chloroethylene rectification tail gas pipeline 11, a feeding pipeline 12 of the tower top condensation cooler is fixedly communicated between an outlet at the top of the absorption tower 2 and an inlet at the upper part of the tower top condensation cooler 3, a first outlet at the upper part of the tower top condensation cooler 3 is fixedly communicated with a second frozen brine return pipeline 13, a demister feeding pipeline 14 is fixedly communicated between a second outlet at the upper part of the tower top condensing cooler 3 and an inlet at the lower part of the demister 5, a second frozen brine upper water pipeline 15 is fixedly communicated with an inlet at the lower part of the tower top condensing cooler 3, a tower top condensing cooler discharging pipeline 16 is fixedly communicated with an outlet at the bottom of the tower top condensing cooler 3, a first demister discharging pipeline 17 is fixedly communicated with an outlet at the top of the demister 5, a second demister discharging pipeline 18 is fixedly communicated with an outlet at the bottom of the demister 5, an outlet of the tower top condensing cooler discharging pipeline 16 is fixedly communicated with the second demister discharging pipeline 18, a tower still cooler discharging pipeline 19 is fixedly communicated between a second inlet at the upper part of the absorption tower 2 and a first outlet at the top of the tower still cooler 4, a third frozen brine return pipeline 20 is fixedly communicated with a second outlet at the top of the tower still cooler 4, a tower still cooler feeding pipeline 21 is fixedly communicated between the first inlet at the bottom of the tower still cooler 4, a second inlet at the bottom of the tower bottom cooler 4 is fixedly communicated with a third frozen brine water inlet pipeline 22, an outlet of a second demister discharge pipeline 18 is fixedly communicated with a tower bottom cooler feed pipeline 21, an absorption liquid tank feed pipeline 23 is fixedly communicated between an inlet at the top of the absorption liquid tank 6 and the tower bottom cooler feed pipeline 21, a first discharge pipeline 24 of the absorption liquid tank is fixedly communicated with an outlet at the top of the absorption liquid tank 6, and a second discharge pipeline 25 of the absorption liquid tank is fixedly communicated with an outlet at the bottom of the absorption liquid tank 6.
Among the prior art, chloroethylene rectification tail gas adopts single pressure swing adsorption processing mode, and pressure swing adsorption processing apparatus load can cause the influence to normal production and environmental protection greatly, the utility model discloses utilize the nature that dichloroethane and chloroethylene are mutual soluble, adopt refined dichloroethane to absorb chloroethylene rectification tail gas, changed the single pressure swing adsorption processing mode of chloroethylene rectification tail gas, will refine dichloroethane absorption and the ally oneself with usefulness of pressure swing adsorption, make chloroethylene rectification tail gas discharge to reach standard, refined dichloroethane can cyclic utilization, has realized bigger environmental protection benefit.
The absorbing device of the vinyl chloride rectification tail gas solvent method can be further optimized or/and improved according to actual needs:
as shown in fig. 1, a vent line 26 is fixedly communicated with the first demister discharge line 17.
As shown in the attached figure 1, a third discharge pipeline 27 of the absorption liquid tank is fixedly communicated with the second discharge pipeline 25 of the absorption liquid tank.
As shown in fig. 1, a column cooler feed pump 28 is fixedly installed on the column cooler feed line 21, and a feed pump circulation line 29 is fixedly communicated with the column cooler feed line 21 at the inlet and the outlet of the column cooler feed pump 28.
As shown in fig. 1, a demister circulation line 30 is fixedly communicated between the second demister discharge line 18 and the absorption liquid tank feed line 23, and an absorption liquid tank feed pump 31 is fixedly installed on the demister circulation line 30.
As shown in fig. 1, a first absorption liquid delivery pump 32 is fixedly installed on the second discharge pipeline 25 of the absorption liquid tank, an absorption liquid circulation pipeline 33 is fixedly communicated with the second discharge pipeline 25 of the absorption liquid tank at the inlet and the outlet of the first absorption liquid delivery pump 32, and a second absorption liquid delivery pump 34 is fixedly installed on the absorption liquid circulation pipeline 33.
As shown in fig. 1, an absorbent thermometer 35 is fixedly installed on the absorbent discharge line 9, an overhead condensing cooler thermometer 36 is fixedly installed on the overhead condensing cooler discharge line 16, and a column bottom cooler thermometer 37 is fixedly installed on the column bottom cooler discharge line 19.
Above technical feature constitutes the utility model discloses a best embodiment, it has stronger adaptability and best implementation effect, can increase and decrease unnecessary technical feature according to actual need, satisfies the demand of different situation.
The utility model discloses best embodiment's use: introducing absorbent refined dichloroethane into an absorbent cooler 1 through an absorbent feeding pipeline 7, cooling the refined dichloroethane with the frozen brine entering the absorbent cooler 1 through a first frozen brine water feeding pipeline 8, cooling the refined dichloroethane to-5 to-15 ℃, then introducing the refined dichloroethane into an absorption tower 2 along an absorbent discharging pipeline 9, discharging the cooled frozen brine with the temperature lower than-10 ℃ from a first frozen brine water return pipeline 10, introducing the vinyl chloride rectification tail gas into the absorption tower 2 through a vinyl chloride rectification tail gas pipeline 11, continuously absorbing the vinyl chloride rectification tail gas by the refined dichloroethane in the absorption tower 2, introducing a part of the refined dichloroethane liquid absorbing the vinyl chloride rectification tail gas into a tower bottom cooler feeding pipeline 21, a feeding pump circulating pipeline 29 and an absorption rectification feeding pipeline 23 respectively into a tower bottom cooler 4 and an absorption liquid tank 6, and converting the other part of the refined dichloroethane liquid absorbing the vinyl chloride rectification tail gas into gas in the absorption tower 2 to flow into gas flowing into the tower top A condensation cooler 3, wherein the refined dichloroethane gas absorbing the chloroethylene rectification tail gas is cooled to-5 ℃ to-15 ℃ by the frozen brine entering the tower top condensation cooler 3 from a second frozen brine water inlet pipeline 15, a part of uncondensed liquid drops enter a demister 5 from a demister feeding pipeline 14, the other part of condensed liquid flows out from a tower top condensation cooler discharging pipeline 16, the frozen brine with the temperature lower than-10 ℃ after being cooled flows out from a second frozen brine water return pipeline 13, the uncondensed liquid drops entering the demister 5 are subjected to gas-liquid separation under the action of the demister 5, the separated gas is discharged from a first demister discharging pipeline 17 and an emptying pipeline 26, the separated liquid flows out from a second demister discharging pipeline 18, and the liquid flowing out from the tower top condensation cooler discharging pipeline 16 and the second demister discharging pipeline 18 flows along the second demister discharging pipeline 18, The demister circulating pipeline 30 and the absorption liquid tank feeding pipeline 23 enter the absorption liquid tank 6, the refined dichloroethane liquid which has absorbed the chloroethylene rectification tail gas is cooled to-5 ℃ to-15 ℃ by the frozen brine which enters the tower bottom cooler 4 from the third frozen brine upper water pipeline 22, then enters the absorption tower 2 from the tower bottom cooler discharging pipeline 19 to continuously absorb the chloroethylene rectification tail gas, the frozen brine which is cooled to be lower than-10 ℃ flows out from the third frozen brine water return pipeline 20, enters the absorption liquid tank 6 to absorb the refined dichloroethane liquid of the chloroethylene rectification tail gas, one part of the refined dichloroethane liquid is converted into gas and discharged from the absorption liquid tank first discharging pipeline 24, and the other part of the refined liquid flows through the absorption liquid circulating pipeline 33 and then is discharged from the absorption liquid tank second discharging pipeline 25 and the absorption liquid tank third discharging pipeline 27.
Claims (7)
1. A chloroethylene rectification tail gas solvent method absorption device is characterized by comprising an absorbent cooler, an absorption tower, a tower top condensation cooler, a tower kettle cooler, a demister and an absorption liquid tank, wherein a first inlet at the bottom of the absorbent cooler is fixedly communicated with an absorbent feeding pipeline, a second inlet at the bottom of the absorbent cooler is fixedly communicated with a first frozen brine feeding pipeline, an absorbent discharging pipeline is fixedly communicated between a first outlet at the top of the absorbent cooler and a first inlet at the upper part of the absorption tower, a second outlet at the top of the absorbent cooler is fixedly communicated with a first frozen brine return pipeline, a tail gas pipeline for chloroethylene rectification is fixedly communicated with an inlet at the middle part of the absorption tower, a feeding pipeline for the tower top condensation cooler is fixedly communicated between an outlet at the top of the absorption tower and an inlet at the upper part of the tower top condensation cooler, a first outlet at the upper part of the tower top condensation cooler is fixedly communicated with a second frozen brine return pipeline, a demister feeding pipeline is fixedly communicated between a second outlet at the upper part of the tower top condensing cooler and an inlet at the lower part of the demister, a second frozen brine upper water pipeline is fixedly communicated with an inlet at the lower part of the tower top condensing cooler, a tower top condensing cooler discharging pipeline is fixedly communicated with an outlet at the bottom of the tower top condensing cooler, a first demister discharging pipeline is fixedly communicated with an outlet at the top of the demister, a second demister discharging pipeline is fixedly communicated with an outlet at the bottom of the demister, an outlet of the tower top condensing cooler discharging pipeline is fixedly communicated with the second demister discharging pipeline, a tower kettle cooler discharging pipeline is fixedly communicated between a second inlet at the upper part of the absorption tower and a first outlet at the top of the tower kettle cooler, a third frozen brine return pipeline is fixedly communicated with a second outlet at the top of the tower kettle cooler, a tower kettle cooler feeding pipeline is fixedly communicated between the first inlet at the bottom of the tower kettle cooler and the, the fixed intercommunication of tower cauldron cooler bottom second import has third frozen brine water pipeline, and second defroster discharge line export is linked together with tower cauldron cooler feed line is fixed, and fixed intercommunication has absorption fluid reservoir feed line between absorption fluid reservoir top import and the tower cauldron cooler feed line, and the fixed intercommunication of absorption fluid reservoir top export has the first discharge line of absorption fluid reservoir, and the fixed intercommunication of absorption fluid reservoir bottom export has absorption fluid reservoir second discharge line.
2. The absorption apparatus of vinyl chloride rectification tail gas solvent method according to claim 1, characterized in that a discharge pipeline is fixedly communicated with a discharge pipeline of the first demister.
3. The vinyl chloride rectification tail gas solvent method absorption device according to claim 1 or 2, characterized in that a third discharge pipeline of the absorption liquid tank is fixedly communicated with a second discharge pipeline of the absorption liquid tank.
4. The absorption apparatus for vinyl chloride rectification tail gas solvent method according to claim 1 or 2, characterized in that a tower cooler feed pump is fixedly installed on the tower cooler feed line, and a feed pump circulation line is fixedly communicated with the inlet of the tower cooler feed pump and the tower cooler feed line at the outlet.
5. The vinyl chloride rectification tail gas solvent method absorption device according to claim 1 or 2, which is characterized in that a demister circulating pipeline is fixedly communicated between the second demister discharge pipeline and the absorption liquid tank feeding pipeline, and an absorption liquid tank feeding pump is fixedly installed on the demister circulating pipeline.
6. The vinyl chloride rectification tail gas solvent method absorption device according to claim 1 or 2, characterized in that a first absorption liquid delivery pump is fixedly installed on the second discharge pipe line of the absorption liquid tank, an absorption liquid circulation pipeline is fixedly communicated with the second discharge pipe line of the absorption liquid tank at the inlet and the outlet of the first absorption liquid delivery pump, and a second absorption liquid delivery pump is fixedly installed on the absorption liquid circulation pipeline.
7. The absorption apparatus for vinyl chloride rectification tail gas solvent method according to claim 1 or 2, characterized in that an absorbent thermometer is fixedly installed on an absorbent discharge pipe line, an overhead condensation cooler thermometer is fixedly installed on an overhead condensation cooler discharge pipe line, and a column bottom cooler thermometer is fixedly installed on a column bottom cooler discharge pipe line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921463025.XU CN210934373U (en) | 2019-09-04 | 2019-09-04 | Chloroethylene rectification tail gas solvent method absorption device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921463025.XU CN210934373U (en) | 2019-09-04 | 2019-09-04 | Chloroethylene rectification tail gas solvent method absorption device |
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| Publication Number | Publication Date |
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| CN210934373U true CN210934373U (en) | 2020-07-07 |
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| CN201921463025.XU Active CN210934373U (en) | 2019-09-04 | 2019-09-04 | Chloroethylene rectification tail gas solvent method absorption device |
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| Country | Link |
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| CN (1) | CN210934373U (en) |
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- 2019-09-04 CN CN201921463025.XU patent/CN210934373U/en active Active
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