CN101343040B - Liquefied chlorine flash evaporation purification preparation technique - Google Patents
Liquefied chlorine flash evaporation purification preparation technique Download PDFInfo
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- CN101343040B CN101343040B CN2008101395629A CN200810139562A CN101343040B CN 101343040 B CN101343040 B CN 101343040B CN 2008101395629 A CN2008101395629 A CN 2008101395629A CN 200810139562 A CN200810139562 A CN 200810139562A CN 101343040 B CN101343040 B CN 101343040B
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- chlorine
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- flash distillation
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- pressure liquid
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Abstract
The invention discloses a chlorine liquid flash vaporization purification production process; a flash vaporization purification tank is arranged to enable the flash vaporization purification tank to connect with a high pressure chlorine liquid storage tank through the high pressure chlorine liquid pipeline; meanwhile, the flash vaporization purification tank is connected with a chlorine presser through a mixture gas pipeline; the high pressure chlorine liquid in the high pressure chlorine liquid storage tank is fed to the flash vaporization purification tank; the pressure in the flash vaporization purification tank is more than 0.7 Mpa; the mixture gas in the flash vaporization purification tank is extracted by the chlorine presser to enable the pressure in the flash vaporization purification tank is reduced to be less than or equal to 0.4 Mpa; in this time, the high concentration chlorine liquid is produced in the flash vaporization purification tank; the high pressure chlorine liquid in the high pressure chlorine liquid storage tank is fed to the flash vaporization purification tank continuously; the high concentration chlorine liquid produced in the flash vaporization purification tank is directly fed into the user pressure tank. The chlorine liquid flash vaporization purification production can increase the concentration of the chlorine liquid obtained by the chlorine liquid high pressure method to be 99.75% through the process, be applicable to the production of the downstream products and have the advantages of reasonable design, easy operation, high production safety and low production cost.
Description
Technical field
The present invention relates to chlorine gas liquefaction, is a kind of liquefied chlorine flash evaporation purification preparation technique.
Background technology
Because chlorine is the raw material of inorganic chemical industry, so purposes is very extensive.At present, the method of producing chlorine mainly is the saline electrolysis method, though this method is simple to operation, production cost is lower, but the purity of chlorine gas feeding of Sheng Chaning is lower in this way, can not be directly used in the part organic chemical industry product, therefore, need be with vaporization behind the chlorine gas liquefaction to obtain the chlorine of higher degree.This area generally adopts low-pressure process and high-pressure process to make chlorine gas liquefaction.Though adopt low-pressure process to make chlorine gas liquefaction can obtain the chlorine of higher degree,, its energy consumption is higher, complex process, production cost height.Adopt high-pressure process to make chlorine gas liquefaction, though energy consumption is low, technology is simple relatively, and easy to operate, and the purity of chlorine gas feeding that obtains is lower, will directly influence the quality and the output of derived product when this chlorine is used for derived product.
Summary of the invention
The purpose of this invention is to provide a kind of liquefied chlorine flash evaporation purification preparation technique, the high pressure liquid chlorine that it utilizes chlorine liquid high-pressure process to obtain adopts purifying technique of the present invention, thereby reaches the purpose of further raising liquid chlorine purity.
The present invention for achieving the above object, be achieved through the following technical solutions: a kind of liquefied chlorine flash evaporation purification preparation technique, flash distillation purification jar is set, flash distillation purification jar is connected with high pressure liquid chlorine storage tank by high pressure liquid chlorine pipeline, the purification of flash distillation simultaneously jar is connected with the chlorine press by the mixed gas pipeline, high pressure liquid chlorine in the high pressure liquid chlorine storage tank is inserted in the flash distillation purification jar, flash distillation purification jar interior pressure is more than the 0.7Mpa, with the chlorine press a flash distillation purification jar interior mixed gas is taken away, a flash distillation purification jar internal pressure is reduced to be less than or equal to 0.4Mpa, at this moment, the flash distillation purification jar interior high purity liquid chlorine that produces, high pressure liquid chlorine in the high pressure liquid chlorine storage tank is added in jar is purified in flash distillation continuously, and the high purity liquid chlorine of generation directly enters in user's pressure-pot in the flash distillation purification jar.A flash distillation purification jar interior high pressure liquid chloro level is tank body volumetrical 1/2-2/3.Sewage draining exit is offered in a flash distillation purification jar bottom, right side.On the high pressure liquid chlorine pipeline that flash distillation is purified jar with high pressure liquid chlorine storage tank is connected the charging control valve is installed, flash distillation purify jar with the tank connected pipeline of user's pressure on installation discharging control valve, the installation control valve of bleeding on the mixed gas pipeline.
Positively effect of the present invention is: it can will utilize the liquid chlorine of liquid chlorine high-pressure process acquisition by technology of the present invention, make liquid chlorine purity be increased to 99.75%, can be directly used in the production of derived product, and can increase substantially the quality and the output of derived product, to produce the Benzyl Chloride product is example, the logical chlorine dose of single cover Benzyl Chloride chloridizing unit has on average improved 5.6%, Benzyl Chloride output has improved 5.6% every year, for enterprise has increased considerably economic benefit, be used for various products, the economic benefit of its acquisition is very considerable.Purifying technique of the present invention also has reasonable in design, easy handling, production security height, advantages such as low production cost.
Description of drawings
Accompanying drawing 1 is a process flow diagram of the present invention.
Embodiment
1 is flash distillation purification jar among the figure, the 2nd, sewage draining exit, the 3rd, high pressure liquid chlorine pipeline, the 4th, high pressure liquid chlorine storage tank, the 5th, high pressure liquid chlorine storage tank sewage draining exit, the 6th, chlorine press, the 7th, chlorine treatment system, the 8th, feed control valve, the 9th, the control valve of bleeding, the 10th, mixed gas pipeline, the 11st, discharging control valve, the 12nd, user's pressure-pot.
The air outlet of the chlorine press 6 shown in the figure of the present invention is connected with chlorine treatment system 7, by flash distillation purification jar 1 mixed gas of extracting out, by chlorine press 6 chlorine is delivered to chlorine treatment system 7 recyclings.
Production technique of the present invention is: flash distillation purification jar 1 at first is set, flash distillation purification jar 1 is connected with high pressure liquid chlorine storage tank 4 by high pressure liquid chlorine pipeline 3, the purification of flash distillation simultaneously jar 1 is connected with chlorine press 6 by mixed gas pipeline 10, high pressure liquid chlorine in the high pressure liquid chlorine storage tank 4 is inserted in the flash distillation purification jar 1, flash distillation purification jar 1 interior pressure is more than the 0.7Mpa, with chlorine press 6 flash distillation purification jar 1 an interior mixed gas is taken away again, flash distillation purification jar 1 interior pressure is reduced to be less than or equal to 0.4Mpa, at this moment, the flash distillation purification jar 1 interior high purity liquid chlorine that produces, then the high pressure liquid chlorine in the high pressure liquid chlorine storage tank 4 is added in flash distillation purification jar 1 continuously, the high purity liquid chlorine of flash distillation purification jar 1 interior generation directly enters in user's pressure-pot 12.
Flash distillation purification of the present invention jar 1 an interior high pressure liquid chloro level is tank body volumetrical 1/2-2/3, so that guarantee to reach pressure drop effect preferably.
Flash distillation of the present invention purify jar 1 with high pressure liquid chlorine pipeline 3 that high pressure liquid chlorine storage tank 4 is connected on installation charging control valve 8, flash distillation purify jar 1 with pipeline that user's pressure-pot 12 is connected on installation discharging control valve 11, the control valve 9 of bleeding is installed on the mixed gas pipeline 10, to be able to the rapid adjustment system balancing, make high purity liquid chlorine safety input user pressure-pot.
The high purity liquid chlorine that technology of the present invention obtains can directly be imported the user and use.
Chlorine press of the present invention is a known equipment, so its structure is not done detailed description.
The operation steps of production technique of the present invention is: open the feed control valve 8 on the high pressure liquid chlorine pipeline 3, the high pressure liquid chlorine is joined in the flash distillation purification jar 1 from high pressure liquid chlorine storage tank 4, reaching the 1/2-2/3 place to flash distillation purification jar 1 liquid level ends, open chlorine press 6 and open extraction valve 9, when flash distillation purify jar 1 internal pressure reduce to more than by 0.7Mpa be less than or equal to 0.4Mpa after, open discharging control valve 11, bleeding regulating control valve 9, the aperture of feed control valve 8 and discharging control valve 11 makes system reach balance, the high pressure liquid chlorine that utilizes high-pressure process to obtain is purified by flash distillation purification jar 1, and the high purity liquid chlorine directly enters in user's pressure-pot 12.
Claims (4)
1. liquefied chlorine flash evaporation purification preparation technique, it is characterized in that: flash distillation purification jar (1) is set, flash distillation purification jar (1) is connected with high pressure liquid chlorine storage tank (4) by high pressure liquid chlorine pipeline (3), the purification of flash distillation simultaneously jar (1) is connected with chlorine press (6) by mixed gas pipeline (10), high pressure liquid chlorine in the high pressure liquid chlorine storage tank (4) is inserted in the flash distillation purification jar (1), pressure in the flash distillation purification jar (1) is more than the 0.7MPa, with chlorine press (6) mixed gas in the flash distillation purification jar (1) is taken away, flash distillation purification jar (a 1) internal pressure is reduced to be less than or equal to 0.4MPa, at this moment, produce high purity liquid chlorine in the flash distillation purification jar (1), high pressure liquid chlorine in the high pressure liquid chlorine storage tank (4) is added in jar (1) is purified in flash distillation continuously, and the high purity liquid chlorine that produces in the flash distillation purification jar (1) directly enters in user's pressure-pot (12).
2. a kind of liquefied chlorine flash evaporation purification preparation technique according to claim 1 is characterized in that: the high pressure liquid chloro level in the flash distillation purification jar (1) is tank body volumetrical 1/2-2/3.
3. a kind of liquefied chlorine flash evaporation purification preparation technique according to claim 1 and 2 is characterized in that: sewage draining exit (2) is offered in a flash distillation purification jar bottom, (1) right side.
4. a kind of liquefied chlorine flash evaporation purification preparation technique according to claim 3, it is characterized in that: the high pressure liquid chlorine pipeline (3) that flash distillation purification jar (1) is connected with high pressure liquid chlorine storage tank (4) is gone up charging control valve (8) is installed, flash distillation is purified and discharging control valve (11) to be installed on jar (1) and the pipeline that user's pressure-pot (12) is connected, and mixed gas pipeline (10) is the installation control valve (9) of bleeding upward.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101395629A CN101343040B (en) | 2008-08-22 | 2008-08-22 | Liquefied chlorine flash evaporation purification preparation technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101395629A CN101343040B (en) | 2008-08-22 | 2008-08-22 | Liquefied chlorine flash evaporation purification preparation technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101343040A CN101343040A (en) | 2009-01-14 |
| CN101343040B true CN101343040B (en) | 2010-04-07 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101395629A Expired - Fee Related CN101343040B (en) | 2008-08-22 | 2008-08-22 | Liquefied chlorine flash evaporation purification preparation technique |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102612485B (en) * | 2010-03-06 | 2014-08-27 | 诺拉姆国际公司 | Method of processing liquid chlorine containing nitrogen trichloride |
| US10377629B2 (en) | 2010-03-06 | 2019-08-13 | Noram International Limited | Method and apparatus for vaporizing liquid chlorine containing nitrogen trichloride |
| CN113318470A (en) * | 2021-05-31 | 2021-08-31 | 鲁西化工集团股份有限公司氯碱化工分公司 | Fluorine direct cooling technology combined chlorine rectification purification system and method |
| CN113546439B (en) * | 2021-08-16 | 2023-02-21 | 聊城鲁西氯甲烷化工有限公司 | Liquid chlorine flash evaporation deoxidization system and process |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2045380U (en) * | 1989-01-07 | 1989-10-04 | 苏州市制冷设备厂 | Chlorine liquefying device |
| CN1144712A (en) * | 1995-05-19 | 1997-03-12 | 挪威海德罗公司 | Method for purification of chiorine gas |
| US5861049A (en) * | 1997-01-24 | 1999-01-19 | Membrane Technology And Research, Inc. | Chlorine separation process combining condensation, membrane separation and flash evaporation |
| CN1590279A (en) * | 1995-10-04 | 2005-03-09 | 巴斯福股份公司 | Method for separating and recovering chlorine from service gas containing chlorine |
-
2008
- 2008-08-22 CN CN2008101395629A patent/CN101343040B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2045380U (en) * | 1989-01-07 | 1989-10-04 | 苏州市制冷设备厂 | Chlorine liquefying device |
| CN1144712A (en) * | 1995-05-19 | 1997-03-12 | 挪威海德罗公司 | Method for purification of chiorine gas |
| CN1590279A (en) * | 1995-10-04 | 2005-03-09 | 巴斯福股份公司 | Method for separating and recovering chlorine from service gas containing chlorine |
| US5861049A (en) * | 1997-01-24 | 1999-01-19 | Membrane Technology And Research, Inc. | Chlorine separation process combining condensation, membrane separation and flash evaporation |
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| CN101343040A (en) | 2009-01-14 |
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Granted publication date: 20100407 Termination date: 20120822 |