CN104923028A - Method for dehydrating coarse pyrolysis gas in production of vinylidene fluoride and dehydration device - Google Patents
Method for dehydrating coarse pyrolysis gas in production of vinylidene fluoride and dehydration device Download PDFInfo
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- CN104923028A CN104923028A CN201510292704.5A CN201510292704A CN104923028A CN 104923028 A CN104923028 A CN 104923028A CN 201510292704 A CN201510292704 A CN 201510292704A CN 104923028 A CN104923028 A CN 104923028A
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Abstract
The invention discloses a method for dehydrating coarse pyrolysis gas in production of vinylidene fluoride. According to the method, the coarse pyrolysis gas generated in production of vinylidene fluoride is treated in the manner that three-stage compression and freeze-dehydration are carried out simultaneously, the step of silica gel drying is eliminated, most moisture in coarse pyrolysis gas can be removed, and moreover, partial HCFC-142b is condensed out, so that the workloads of a subsequent VDF degassing tower and a VDF rectifying tower are reduced and energy consumption of the work is reduced.
Description
Technical field
The invention belongs to vinylidene production technical field, be specifically related to dewatering and the dewater unit of thick cracking gas in the production of a kind of vinylidene.
Background technology
Vinylidene CH2CF2(VDF) be one of important kind of Fluorine containing olefine, as the important monomer of synthesis Kynoar (PVDF), there is very high economic benefit.Current domestic industryization generally adopts HCFC-142b thermal cracking to produce vinylidene, although it is simple that the method has flow process, product purity advantages of higher, but a large amount of HCL accessory substances can be generated due to thermal cracking, so cracking gas needs to wash thorough deacidification through scale, inevitably, the moisture carried secretly in cracking gas to be easy in distillation process occluding device and pipeline because of low temperature crystallization.
Traditional dewatering process is as follows: after caustic wash tower thoroughly deacidifies, be introduced into calcium chloride spray column, by low temperature chlorination calcium Saline Absorbent moisture, make the moisture in cracking gas drop to 400Ppm, and then make the moisture in cracking gas drop to below 200PPM through overcompression, silica dehydrator to carry out rectifying again.But in above-mentioned technique, directly using silica dehydrator upon compression, silica gel activating can be made frequent, and silica gel shortens service life, operation often there will be and make cracking gas Moisture high UCL because not activating in time.
Summary of the invention
Technical problem to be solved by this invention is to provide dewatering and the dewater unit of thick cracking gas in the production of a kind of vinylidene, thus effectively improves the dewatering efficiency of thick cracking gas.
For solving the problems of the technologies described above, the technical solution used in the present invention is:
The dewatering of a kind of vinylidene thick cracking gas in producing, comprise the following steps: the thick cracking gas that thermal cracking produces, by the low temperature chlorination calcium Saline Absorbent moisture in spray column after caustic wash tower alkali cleaning, the moisture in thick cracking gas is made to drop to 486 ~ 495Ppm, then send into the condensation of one-level deep cooling dehydrator by one stage of compression chamber and go out most of moisture, one-level deep cooling dehydrator control temperature at 2 ~ 10 DEG C, by first-level buffer tank controlled pressure at 0.25 ~ 0.4MPa; Thick cracking gas continues through two-stage compression chamber and sends into the condensation of secondary deep cooling dehydrator and go out portion of water and part HCFC-142b, secondary deep cooling dehydrator control temperature at-8 ~-2 DEG C, by level 2 buffering tank controlled pressure at 0.65 ~ 0.8MPa; Cracking gas continues through three stage compression chamber, is condensed into liquid phase enters VDF degassing tower after being compressed to 1.58 ~ 1.62Mpa by forecooler.
A kind of dewater unit, the dewatering of thick cracking gas in producing for above-mentioned vinylidene, it comprises one stage of compression chamber, two-stage compression chamber and three stage compression chamber, the air intake access spray column in one stage of compression chamber, gas outlet are connected with first-level buffer tank by one-level deep cooling dehydrator, first-level buffer tank is connected with the air intake in two-stage compression chamber, the gas outlet in two-stage compression chamber is connected with level 2 buffering tank by secondary deep cooling dehydrator, level 2 buffering tank is connected with the air intake in three stage compression chamber, the gas outlet in three stage compression chamber is connected with forecooler, forecooler access VDF degassing tower.
Described forecooler adopts-35 DEG C of chilled brines as refrigerant.
Compared with prior art, advantage of the present invention is: the thick cracking gas that the mode that the present invention adopts three grades of limits to compress just lyophilization produces in producing vinylidene processes, abandon this step of silica dehydrator, most moisture in thick cracking gas can not only be removed, and can coagulate part HCFC-142b simultaneously, reduce the work load of follow-up VDF degassing tower and VDF rectifying column, also reduce operating power consumption.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
Fig. 1 is the structural representation of dewater unit in the present invention.
Wherein, 1, one stage of compression chamber, 2, one-level deep cooling dehydrator, 3, first-level buffer tank, 4, two-stage compression chamber, 5, secondary deep cooling dehydrator, 6, level 2 buffering tank, 7, three stage compression chamber, 8, forecooler.
Detailed description of the invention:
As shown in Figure 1, a kind of dewater unit, it comprises one stage of compression chamber 1, two-stage compression chamber 4 and three stage compression chamber 7, the air intake access spray column in one stage of compression chamber 1, gas outlet are connected with first-level buffer tank 3 by one-level deep cooling dehydrator 2, first-level buffer tank 3 is connected with the air intake in two-stage compression chamber 4, the gas outlet in two-stage compression chamber 4 is connected with level 2 buffering tank 6 by secondary deep cooling dehydrator 5, level 2 buffering tank 6 is connected with the air intake in three stage compression chamber 7, the gas outlet in three stage compression chamber 7 is connected with forecooler 8, and forecooler 8 accesses VDF degassing tower; Wherein, forecooler 8 adopts-35 DEG C of chilled brines as refrigerant; Compression chamber adopts the compression chamber of three series connection in VSW-90/2.0 type oil-free lubrication process gas compressor, carries out implements spatial scalable compression to thick cracking gas.
Below in conjunction with embodiment, the present invention is described in further details.
Embodiment 1
The thick cracking gas that 1000t/a vinylidene process units obtains, by the low temperature chlorination calcium Saline Absorbent moisture in spray column after caustic wash tower alkali cleaning, the moisture in thick cracking gas is made to drop to 486Ppm, then send into the condensation of one-level deep cooling dehydrator 2 by one stage of compression chamber 1 and go out most of moisture, one-level deep cooling dehydrator 2 control temperature at 10 DEG C, by first-level buffer tank 3 controlled pressure at 0.25MPa; Thick cracking gas continues through two-stage compression chamber 4 and sends into the condensation of secondary deep cooling dehydrator 5 and go out portion of water and part HCFC-142b, secondary deep cooling dehydrator 5 control temperature at-2 DEG C, by level 2 buffering tank 6 controlled pressure at 0.65MPa; Cracking gas continues through three stage compression chamber 7, is condensed into liquid phase enters VDF degassing tower after being compressed to 1.58Mpa by forecooler 8.
Cracking gas sample analysis is carried out to the outlet in three stage compression chamber 7, obtains cracking gas water content and drop to 240Ppm.
Embodiment 2
The thick cracking gas that 1000t/a vinylidene process units obtains, by the low temperature chlorination calcium Saline Absorbent moisture in spray column after caustic wash tower alkali cleaning, the moisture in thick cracking gas is made to drop to 495Ppm, then send into the condensation of one-level deep cooling dehydrator 2 by one stage of compression chamber 1 and go out most of moisture, one-level deep cooling dehydrator 2 control temperature at 5 DEG C, by first-level buffer tank 3 controlled pressure at 0.3MPa; Thick cracking gas continues through two-stage compression chamber 4 and sends into the condensation of secondary deep cooling dehydrator 5 and go out portion of water and part HCFC-142b, secondary deep cooling dehydrator 5 control temperature at-5 DEG C, by level 2 buffering tank 6 controlled pressure at 0.75MPa; Cracking gas continues through three stage compression chamber 7, is condensed into liquid phase enters VDF degassing tower after being compressed to 1.6Mpa by forecooler 8.
Cracking gas sample analysis is carried out to the outlet in three stage compression chamber 7, obtains cracking gas water content and drop to 197Ppm.
Embodiment 3
The thick cracking gas that 1000t/a vinylidene process units obtains, by the low temperature chlorination calcium Saline Absorbent moisture in spray column after caustic wash tower alkali cleaning, the moisture in thick cracking gas is made to drop to 488Ppm, then send into the condensation of one-level deep cooling dehydrator 2 by one stage of compression chamber 1 and go out most of moisture, one-level deep cooling dehydrator 2 control temperature at 2 DEG C, by first-level buffer tank 3 controlled pressure at 0.38MPa; Thick cracking gas continues through two-stage compression chamber 4 and sends into the condensation of secondary deep cooling dehydrator 5 and go out portion of water and part HCFC-142b, secondary deep cooling dehydrator 5 control temperature at-8 DEG C, by level 2 buffering tank 6 controlled pressure at 0.79MPa; Cracking gas continues through three stage compression chamber 7, is condensed into liquid phase enters VDF degassing tower after being compressed to 1.62Mpa by forecooler 8.
Cracking gas sample analysis is carried out to the outlet in three stage compression chamber 7, obtains cracking gas water content and drop to 175Ppm.
Claims (3)
1. the dewatering of a vinylidene thick cracking gas in producing, it is characterized in that: comprise the following steps: the thick cracking gas that thermal cracking produces, by the low temperature chlorination calcium Saline Absorbent moisture in spray column after caustic wash tower alkali cleaning, the moisture in thick cracking gas is made to drop to 486 ~ 495Ppm, then send into the condensation of one-level deep cooling dehydrator by one stage of compression chamber and go out most of moisture, one-level deep cooling dehydrator control temperature at 2 ~ 10 DEG C, by first-level buffer tank controlled pressure at 0.25 ~ 0.4MPa; Thick cracking gas continues through two-stage compression chamber and sends into the condensation of secondary deep cooling dehydrator and go out portion of water and part HCFC-142b, secondary deep cooling dehydrator control temperature at-8 ~-2 DEG C, by level 2 buffering tank controlled pressure at 0.65 ~ 0.8MPa; Cracking gas continues through three stage compression chamber, is condensed into liquid phase enters VDF degassing tower after being compressed to 1.58 ~ 1.62Mpa by forecooler.
2. a dewater unit, the dewatering of thick cracking gas in producing for vinylidene according to claim 1, it is characterized in that: comprise one stage of compression chamber, two-stage compression chamber and three stage compression chamber, the air intake access spray column in described one stage of compression chamber, gas outlet is connected with first-level buffer tank by one-level deep cooling dehydrator, described first-level buffer tank is connected with the air intake in two-stage compression chamber, the gas outlet in described two-stage compression chamber is connected with level 2 buffering tank by secondary deep cooling dehydrator, described level 2 buffering tank is connected with the air intake in three stage compression chamber, the gas outlet in described three stage compression chamber is connected with forecooler, described forecooler access VDF degassing tower.
3. dewater unit according to claim 2, is characterized in that: described forecooler adopts-35 DEG C of chilled brines as refrigerant.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510292704.5A CN104923028A (en) | 2015-06-02 | 2015-06-02 | Method for dehydrating coarse pyrolysis gas in production of vinylidene fluoride and dehydration device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107586252A (en) * | 2016-07-07 | 2018-01-16 | 中昊晨光化工研究院有限公司 | Dewatering and dewatering system in a kind of vinylidene production |
| CN112955421A (en) * | 2019-03-26 | 2021-06-11 | 日本瑞翁株式会社 | Method for dehydrating organic solvent and method for purifying organic solvent |
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| CN203346305U (en) * | 2013-06-08 | 2013-12-18 | 山东瑞特新材料有限公司 | Refining device of tetrafluoroethylene cracked gas |
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| KR100276415B1 (en) * | 1997-09-17 | 2000-12-15 | 오세 코노수케 | Method and apparatus for producing super clean air |
| RU2175882C2 (en) * | 1999-12-22 | 2001-11-20 | ООО "Уренгойгазпром" ОАО "Газпром" | Method of treating hydrocarbon gas for transportation |
| WO2008092604A1 (en) * | 2007-01-30 | 2008-08-07 | Dge Dr.-Ing. Günther Engineering Gmbh | Method and plant for treating crude gas, in particular biogas, containing methane and carbon dioxide, in order to produce methane |
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| CN107586252A (en) * | 2016-07-07 | 2018-01-16 | 中昊晨光化工研究院有限公司 | Dewatering and dewatering system in a kind of vinylidene production |
| CN112955421A (en) * | 2019-03-26 | 2021-06-11 | 日本瑞翁株式会社 | Method for dehydrating organic solvent and method for purifying organic solvent |
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Application publication date: 20150923 |