CN101187443A - Chlorine steam liquefying method - Google Patents
Chlorine steam liquefying method Download PDFInfo
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- CN101187443A CN101187443A CNA2007101142438A CN200710114243A CN101187443A CN 101187443 A CN101187443 A CN 101187443A CN A2007101142438 A CNA2007101142438 A CN A2007101142438A CN 200710114243 A CN200710114243 A CN 200710114243A CN 101187443 A CN101187443 A CN 101187443A
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Abstract
The invention relates to a chlorine steam-age method in the field of chemical materials productive technology. The technical scheme is that chlorine gas after compressed by a high-pressure compressor enters a shell-and-tube liquefier when the pressure reaches to 0.65 MPa, and temperature is 50 DEG C, chlorine gas in the pipe is cooled and liquefied through the water circulation on the outer side of the pipe, liquefied chlorine, partial foul gas, and non-liquefied chlorine enter a separator to be separated from vapor and liquid, the liquefied chlorine flows into a liquefied chlorine storage tank from the bottom of the separator, and the foul gas and tail chlorine flow to a chlorhydric acid lack tank from the top portion of the separator. The cooling of the liquefier is processed by below 12 DEG C low temperature pure water which is prepared by a steam type lithium bromide refrigerating machine, liquefied chlorine enters the separator to separate when the temperature of the liquefied chlorine reduces to below 12 DEG C, and cool water returns to the lithium bromide machine to be cooled down when the temperature of the cool water increases to 10-15 DEG C and then is cyclically used. The invention adopts the methods that low pressure chlorine gas compressing and low temperature chlorine gas liquefying, which reduces the leakage of the liquefier, decreases working strength, increases safe coefficient, and increases liquefied chlorine output efficiency.
Description
Technical field
The present invention relates to a kind of chlorine steam liquefying method in the industrial chemicals production technology field.
Background technique
The method high temperature and high pressure method of present chlorine gas liquefaction, its technological process comprise that referring to accompanying drawing 1 chlorine is after the high-pressure unit compression, pressure reaches 1.1MPa, after forming high pressure chlorine, about 50 ℃ of chlorine temperatures enter in the tube still type liquifier, chlorine is in pipe, pipe is outer by circulating water, about 30 ℃ of circulating water temperatures, and circulating water carries out cooling liquid to chlorine, temperature is elevated to about 32 ℃, chlorine is emitted heat take out of.The chlorine that the liquid chlorine temperature drops to about 32 ℃ with part incoagulable gas, not liquefaction enters separator, carries out vapor-liquid separation in separator, and liquid chlorine flows into the liquid chlorine storage tank from the separator bottom, and the acid of coming out to desalt from the top of non-condensition and tail chlorine body is irritated.The drawback that this liquifying method exists:
(1) equipment maintenance cost height, owing to utilize circulating water with chlorine gas liquefaction, high-pressure unit exports up to 1.1MPa, causes high-pressure unit machine envelope and H2SO4 recycle pump machine envelope often to reveal, liquifier pressure height, liquifier is revealed, the Cost of repair and maintenance height.(2) energy consumption height, liquifier cooling medium are circulating water, high-pressure unit outlet temperature height, about 50 ℃ of temperature, tubulation fouling in the liquifier, heat-transfer coefficient is low, the heat exchange weak effect, according to the liquefaction tracing analysis, temperature is high more, and pressure raises, the circulating water consumption increases, liquefaction efficiency is low more, and chlorine is arranged to exhaust gas absorption device, and liquefaction output reduces.(3) circulating water temperature is subjected to weather effect bigger, when temperature is high, and the liquefaction weak effect, the pressure height, a large amount of chlorine rows are to exhaust gas absorption device.
Summary of the invention
Purpose of the present invention is exactly the defective that exists at prior art, and low pressure, the low temperature chlorine steam liquefying method of a kind of energy-saving safe, high-efficiency environment friendly is provided.
Its technological scheme is: after the chlorine high pressure compressed, pressure 0.6-0.75MPa, temperature 45-55 ℃ laggard goes into the tube still type liquifier, chlorine is in pipe, carry out cooling liquid by managing outer water cycle, the chlorine of liquid chlorine and part incoagulable gas, not liquefaction enters separator, carries out vapor-liquid separation in separator, liquid chlorine flows into the liquid chlorine storage tank from separator bottom, the acid of coming out to desalt from the top of non-condensition and tail chlorine body is irritated.Described liquifier cooling is to utilize-10 to-15 ℃ of low temperature pure water of steam type lithium bromide refrigerator preparation to liquefy, the liquid chlorine temperature drops to and enters separator about 10-15 ℃ and separate, and cold water temperature raises 10～15 ℃ and recycles after returning the cooling of lithium bromide unit.
Effect of the present invention: what the present invention adopted is the method for the compression of low pressure chlorine, low temperature chlorine gas liquefaction, what made full use of that large-scale chlorine production enterprise possesses enriches the steam resource, adopt the steam type lithium bromide unit of safety and environmental protection to implement cooling, annual temperature-resistant, simple to operate, reduced the liquifier leakage, high-pressure unit envelope frequent breakage situation, reduce labor intensity, increased safety coefficient, improved the liquid chlorine output efficiency.
Description of drawings
Fig. 1 is existing chlorine gas liquefaction process flow diagram; Fig. 2 is a chlorine gas liquefaction process flow diagram of the present invention.
Specific embodiment
With reference to accompanying drawing 2, with Membrane Cell Installation for Caustic Soda Production is 100,000 t/a, be example: chlorine is after high-pressure unit compression, and pressure reaches 0.65MPa, and 50 ℃ of temperature are laggard goes into the tube still type liquifier, chlorine is in pipe, carry out cooling liquid by managing outer water cycle, the chlorine of liquid chlorine and part incoagulable gas, not liquefaction enters separator, carries out vapor-liquid separation in separator, liquid chlorine flows into the liquid chlorine storage tank from separator bottom, the acid of coming out to desalt from the top of non-condensition and tail chlorine body is irritated.Described liquifier cooling is to utilize-12 ℃ of low temperature pure water of steam type lithium bromide refrigerator preparation to liquefy, the liquid chlorine temperature drops to and enters the separator separation about 12 ℃, and cold water temperature raises 10～15 ℃ and recycles after returning the cooling of lithium bromide unit, and the cold water circulating load is 330m
2About.
Adopt high temperature and high pressure method in the past, equipment frequently keeps in repair, and liquifier is revealed, and has potential safety hazard.By technical innovation, make liquifier pressure drop to 0.65MPa by 1.1MPa, condensing temperature drops to about 12 ℃, reaches energy-saving and cost-reducing, ensures safety in production.
Claims (1)
1. chlorine steam liquefying method, chlorine is after the high-pressure unit compression, pressure reaches 0.6-0.75MPa, temperature 45-55 ℃ laggard goes into the tube still type liquifier, chlorine is in pipe, carry out cooling liquid by managing outer water cycle, liquid chlorine and part incoagulable gas, Ye Hua chlorine does not enter separator, in separator, carry out vapor-liquid separation, liquid chlorine flows into the liquid chlorine storage tank from the separator bottom, the acid of coming out to desalt from the top of non-condensition and tail chlorine body is irritated, described liquifier cooling is to utilize-10 to-15 ℃ of low temperature pure water of steam type lithium bromide refrigerator preparation to liquefy, the liquid chlorine temperature drops to 10 to 15 ℃ and enters separator and separate, and cold water temperature raises 10～15 ℃ and recycles after returning the cooling of lithium bromide unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101142438A CN101187443A (en) | 2007-12-07 | 2007-12-07 | Chlorine steam liquefying method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101142438A CN101187443A (en) | 2007-12-07 | 2007-12-07 | Chlorine steam liquefying method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101187443A true CN101187443A (en) | 2008-05-28 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007101142438A Pending CN101187443A (en) | 2007-12-07 | 2007-12-07 | Chlorine steam liquefying method |
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| CN (1) | CN101187443A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101608872B (en) * | 2009-07-03 | 2012-07-04 | 中国天辰工程有限公司 | Device for washing and cooling chlorine |
| CN102564058A (en) * | 2012-02-09 | 2012-07-11 | 东营华泰化工集团有限公司 | Technology for liquefying chlorine through medium-temperature and medium-pressure method |
| CN105179940A (en) * | 2015-08-13 | 2015-12-23 | 湖北兴发化工集团股份有限公司 | Liquid chlorine conveying equipment and process thereof |
| CN105271120A (en) * | 2015-10-28 | 2016-01-27 | 成都兴业雷安电子有限公司 | Liquid-chlorine production system |
| CN110195822A (en) * | 2019-06-21 | 2019-09-03 | 江苏准信环保科技有限公司 | A kind of device and method automatically controlling chlorine gas liquefaction efficiency |
| CN110375520A (en) * | 2019-07-24 | 2019-10-25 | 王彪 | A kind of new high-efficiency chlorine liquefier |
| CN112604431A (en) * | 2020-11-19 | 2021-04-06 | 衡阳鸿宇化工有限责任公司 | Tail gas treatment device for aluminum trichloride production and use method thereof |
| CN113203249A (en) * | 2021-05-13 | 2021-08-03 | 遵义钛业股份有限公司 | Liquefying and purifying device for chlorine in electrolytic magnesium chloride |
-
2007
- 2007-12-07 CN CNA2007101142438A patent/CN101187443A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101608872B (en) * | 2009-07-03 | 2012-07-04 | 中国天辰工程有限公司 | Device for washing and cooling chlorine |
| CN102564058A (en) * | 2012-02-09 | 2012-07-11 | 东营华泰化工集团有限公司 | Technology for liquefying chlorine through medium-temperature and medium-pressure method |
| CN105179940A (en) * | 2015-08-13 | 2015-12-23 | 湖北兴发化工集团股份有限公司 | Liquid chlorine conveying equipment and process thereof |
| CN105179940B (en) * | 2015-08-13 | 2017-11-07 | 湖北兴发化工集团股份有限公司 | A kind of Liquid chlorine equipment and its technique |
| CN105271120A (en) * | 2015-10-28 | 2016-01-27 | 成都兴业雷安电子有限公司 | Liquid-chlorine production system |
| CN105271120B (en) * | 2015-10-28 | 2017-10-31 | 成都兴业雷安电子有限公司 | Liquid chlorine production system |
| CN110195822A (en) * | 2019-06-21 | 2019-09-03 | 江苏准信环保科技有限公司 | A kind of device and method automatically controlling chlorine gas liquefaction efficiency |
| CN110195822B (en) * | 2019-06-21 | 2021-04-02 | 江苏准信化学工程有限公司 | Device and method for automatically controlling chlorine liquefaction efficiency |
| CN110375520A (en) * | 2019-07-24 | 2019-10-25 | 王彪 | A kind of new high-efficiency chlorine liquefier |
| CN112604431A (en) * | 2020-11-19 | 2021-04-06 | 衡阳鸿宇化工有限责任公司 | Tail gas treatment device for aluminum trichloride production and use method thereof |
| CN113203249A (en) * | 2021-05-13 | 2021-08-03 | 遵义钛业股份有限公司 | Liquefying and purifying device for chlorine in electrolytic magnesium chloride |
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Open date: 20080528 |