CN101623584A - Hydrochloric acid full stripping method - Google Patents
Hydrochloric acid full stripping method Download PDFInfo
- Publication number
- CN101623584A CN101623584A CN200910181965A CN200910181965A CN101623584A CN 101623584 A CN101623584 A CN 101623584A CN 200910181965 A CN200910181965 A CN 200910181965A CN 200910181965 A CN200910181965 A CN 200910181965A CN 101623584 A CN101623584 A CN 101623584A
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- acid
- tower
- hydrogen chloride
- hcl
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a hydrochloric acid full stripping method which comprises the following steps: concentrated hydrochloric acid is heated in a double-effect concentrated hydrochloric acid heat exchanger and then enters the top of a concentrated hydrochloric acid desorption tower; heat transmission and mass transmission are carried out between the concentrated hydrochloric acid and high-temperature hydrogen chloride coming from a reboiler and vapor; hydrogen chloride gas containing saturated water is obtained at the top of the tower, and azeotropic acid is obtained at the bottom of the tower; the hydrogen chloride gas containing saturated water passes through a secondary condenser using cooling water as a cooling medium for removing carried acid mist and is further treated by a low-temperature demister to obtain dry hydrogen chloride gas which is transferred outside through a pipeline; and the azeotropic acid is treated by pressure changing and deep desorption. The invention has easy operation and less energy consumption, the content of hydrogen chloride in final waste water is less than or equal to 1 percent, and because the double-effect heat exchanger is adopted, the operation cost is reduced.
Description
Technical field:
The present invention relates to a kind of hydrochloric acid analytic method.
Background technology:
Existing Production of PVC by-product hydrochloric acid is generally handled by the combination extracting tower, synthesis gas comes out from the demercuration device, temperature is about 110 to 130 ℃, after entering the one-level syngas cooler and making cooling medium temperature is reduced to 45～60 ℃, send the secondary syngas cooler again to and make cooling medium with+5 ℃ of chilled waters temperature is reduced to 15 to 20 ℃ with recirculated water.Synthesis gas enters the combination extracting tower at the bottom of tower, come out at the bottom of tower, to enter the water scrubber of combination extracting tower after in the extracting tower of combination extracting tower, removing a large amount of hydrogen chloride from cat head, eject the synthesis gas that comes from water scrubber and at the bottom of tower, enter the caustic wash tower that makes up extracting tower, after cat head comes out, send compression section.Fresh water enters the washing cat head continuously, forms acidic circulation liquid, and acid liquid enters the extracting tower of combination extracting tower continuously, and extracting tower makes～and 31% hydrochloric acid delivers to hydrochloric acid and takes off and inhale the unit or sell outward.
Summary of the invention:
The object of the present invention is to provide a kind of easy to operate, energy consumption is little, the low hydrochloric acid full stripping method of hydrogen chloride content in the final waste water.
Technical solution of the present invention is:
A kind of hydrochloric acid full stripping method is characterized in that: comprise the following steps:
(1) will enter concentrated acid desorber top after the heating of concentrated hydrochloric acid process economic benefits and social benefits concentrated hydrochloric acid heat exchanger, with high-temp chlorination hydrogen and steam countercurrent heat-transfer, mass transfer in tower from reboiler, obtain containing the hydrogen chloride gas of saturation water at cat head, at the bottom of tower, obtain containing the azeotropic acid of 18.2～20% mass concentration HCl;
(2) hydrogen chloride gas that contains saturation water is through by cooling water being the acid mist that the secondary condenser cooling of refrigerant removes deentrainment, and further the low temperature demister is handled and obtained dry hydrogen chloride gas and sent by pipeline;
(3) the azeotropic acid that contains 18.2～20% mass concentration HCl is taken off the suction processing through the transformation degree of depth.
The described degree of depth of step (3) is taken off to inhale to handle and is comprised the following steps: that the azeotropic acid that contains 18.2～20% mass concentration HCl enters vacuum stripper through the vacuum stripper desorb, the mass concentration that cat head obtains is that the condenser cooling of refrigerant obtains concentration less than 1% HCl liquid less than 1% HCl gas via cooling water, and what obtain at the bottom of the tower is the diluted acid that contains the HCl of 22%～23% mass concentration.
The described transformation degree of depth of step (3) is taken off to inhale to handle and is comprised the following steps: the rectification under vacuum tower is sent in azeotropic acid, and the hydrochloric acid that obtains after the rectifying send the combination extracting tower to handle.
Concentrated hydrochloric acid described in the step (1) is the concentrated hydrochloric acid that obtains after the combination extracting tower is handled.
The present invention is easy to operate, energy consumption is little, hydrogen chloride content≤1% in the final waste water, adopts the economic benefits and social benefits heat exchanger, saves operating cost.
Description of drawings:
The invention will be further described below in conjunction with drawings and Examples.
Fig. 1 is the system diagram of the embodiment of the invention 1.
The specific embodiment:
Embodiment 1: a kind of hydrochloric acid full stripping method comprises the following steps:
(1) will enter concentrated acid desorber 3 tops after 2 heating of concentrated hydrochloric acid process economic benefits and social benefits concentrated hydrochloric acid heat exchanger, with high-temp chlorination hydrogen and steam countercurrent heat-transfer, mass transfer in tower from reboiler 4, obtain containing the hydrogen chloride gas of saturation water at cat head, at the bottom of tower, obtain containing the azeotropic acid of 18.2～20% (mass concentration) HCl; Concentrated hydrochloric acid described in the step (1) is the concentrated hydrochloric acid that obtains after combination extracting tower 1 is handled.
(2) hydrogen chloride gas that contains saturation water is through by cooling water being the acid mists that secondary condenser 5,6 coolings of refrigerant remove deentrainment, and further low temperature demister 7 is handled and obtained dry hydrogen chloride gas and sent by pipeline;
(3) the azeotropic acid that contains 18.2～20%HCl is taken off the suction processing through the transformation degree of depth, and cat head yield and quality concentration is produced the diluted acid that contains 22%～23% mass concentration HCl less than the waste water of 1%HCl at the bottom of the tower.
The described transformation degree of depth of step (3) is taken off inhale to handle and is comprised the following steps: that specifically mass concentration is that 18.2～20% azeotropic acid enters vacuum stripper through the vacuum stripper desorb, it is that the condenser cooling of refrigerant obtains mass concentration less than 1%HCl liquid less than the 1%HCl gas via cooling water that cat head obtains mass concentration, and what obtain at the bottom of the tower is the diluted acid that contains 22%～23% mass concentration HCl.
Also have among the figure: 5 ℃ of water remove refrigeration station pipeline 13,5 ℃ of water go out refrigeration station pipeline 14, HCl cooler 15, HCl circulation fluid cooler 16,17, HCl absorbs charge pump 18,19,19.5%HCl storage tank 20, HCl circulation absorption pump 21, cooling vinyl chloride conveyance conduit 22, the vinyl chloride lixiviating is washed operation pipeline 23, concentrated acid storage tank 24,31%HCl charge pump 25, heat exchanger 26,0.8MPa steam supply pipe road 27,19.5%HCl storage tank 28,19%HCl charge pump 29, calcium chloride charge pump 30, calcium chloride storage tank 31, heat exchanger 32, reboiler 33,0.8MPa steam supply pipe road 34,35, high-temp chlorination calcium charge pump 36,0.8MPa steam supply pipe road 37, reboiler 38, condenser 39,1%HCl storage tank 40,1%HCl delivery pump 41.
Embodiment 2:
Step (3) the transformation degree of depth is taken off to inhale to handle and changed into: the rectification under vacuum tower is sent in azeotropic acid, and the hydrochloric acid that obtains after the rectifying send the combination extracting tower to handle.All the other are with embodiment 1.
Claims (4)
1, a kind of hydrochloric acid full stripping method is characterized in that: comprise the following steps:
(1) will enter concentrated acid desorber top after the heating of concentrated hydrochloric acid process economic benefits and social benefits concentrated hydrochloric acid heat exchanger, with high-temp chlorination hydrogen and steam countercurrent heat-transfer, mass transfer in tower from reboiler, obtain containing the hydrogen chloride gas of saturation water at cat head, at the bottom of tower, obtain containing the azeotropic acid of 18.2～20% mass concentration HCl;
(2) hydrogen chloride gas that contains saturation water is through by cooling water being the acid mist that the secondary condenser cooling of refrigerant removes deentrainment, and further the low temperature demister is handled and obtained dry hydrogen chloride gas and sent by pipeline;
(3) the azeotropic acid that contains 18.2～20% mass concentration HCl is taken off the suction processing through the transformation degree of depth.
2, hydrochloric acid full stripping method according to claim 1, it is characterized in that: the described degree of depth of step (3) is taken off to inhale to handle and is comprised the following steps: that the azeotropic acid that contains 18.2～20% mass concentration HCl enters vacuum stripper through the vacuum stripper desorb, the mass concentration that cat head obtains is that the condenser cooling of refrigerant obtains concentration less than 1% HCl liquid less than 1% HCl gas via cooling water, and what obtain at the bottom of the tower is the diluted acid that contains the HCl of 22%～23% mass concentration.
3, hydrochloric acid full stripping method according to claim 1 is characterized in that: the described transformation degree of depth of step (3) is taken off to inhale to handle and is comprised the following steps: the rectification under vacuum tower is sent in azeotropic acid, and the hydrochloric acid that obtains after the rectifying send the combination extracting tower to handle.
4, according to claim 1,2 or 3 described hydrochloric acid full stripping methods, it is characterized in that: the concentrated hydrochloric acid described in the step (1) is the concentrated hydrochloric acid that obtains after the combination extracting tower is handled.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910181965A CN101623584A (en) | 2009-07-28 | 2009-07-28 | Hydrochloric acid full stripping method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910181965A CN101623584A (en) | 2009-07-28 | 2009-07-28 | Hydrochloric acid full stripping method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101623584A true CN101623584A (en) | 2010-01-13 |
Family
ID=41519669
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910181965A Pending CN101623584A (en) | 2009-07-28 | 2009-07-28 | Hydrochloric acid full stripping method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101623584A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103387573A (en) * | 2012-05-08 | 2013-11-13 | 江苏兄弟维生素有限公司 | Preparation process for thiamine hydrochloride |
| CN105947983A (en) * | 2016-05-09 | 2016-09-21 | 杭州中昊科技有限公司 | Preparation method of anhydrous hydrogen chloride |
| CN107161950A (en) * | 2017-06-29 | 2017-09-15 | 天津黄埔盐化工程技术有限公司 | The thickening device and method of a kind of low concentration waste hydrochloric acid |
| CN107998827A (en) * | 2017-12-22 | 2018-05-08 | 江苏天楹环保能源成套设备有限公司 | A kind of high temperature gas containing acid fume hydrogen chloride recovery system |
| CN108483399A (en) * | 2018-05-29 | 2018-09-04 | 杭州东日节能技术有限公司 | A kind of VCM purification hydrochloric acid full stripping device and technique |
| CN112239199A (en) * | 2019-07-19 | 2021-01-19 | 吴军祥 | Hydrochloric acid desorption tower and process using superheated steam as desorption gas in tower kettle |
| CN113398720A (en) * | 2021-07-20 | 2021-09-17 | 四川永祥股份有限公司 | Absorption tower and system for producing electronic-grade hydrochloric acid by utilizing hydrochloric acid resolution |
-
2009
- 2009-07-28 CN CN200910181965A patent/CN101623584A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103387573A (en) * | 2012-05-08 | 2013-11-13 | 江苏兄弟维生素有限公司 | Preparation process for thiamine hydrochloride |
| CN105947983A (en) * | 2016-05-09 | 2016-09-21 | 杭州中昊科技有限公司 | Preparation method of anhydrous hydrogen chloride |
| CN105947983B (en) * | 2016-05-09 | 2018-11-30 | 杭州中昊科技有限公司 | A kind of preparation method of anhydrous hydrogen chloride |
| CN107161950A (en) * | 2017-06-29 | 2017-09-15 | 天津黄埔盐化工程技术有限公司 | The thickening device and method of a kind of low concentration waste hydrochloric acid |
| CN107998827A (en) * | 2017-12-22 | 2018-05-08 | 江苏天楹环保能源成套设备有限公司 | A kind of high temperature gas containing acid fume hydrogen chloride recovery system |
| CN107998827B (en) * | 2017-12-22 | 2019-11-01 | 江苏天楹环保能源成套设备有限公司 | A kind of high temperature gas containing acid fume hydrogen chloride recovery system |
| CN108483399A (en) * | 2018-05-29 | 2018-09-04 | 杭州东日节能技术有限公司 | A kind of VCM purification hydrochloric acid full stripping device and technique |
| CN112239199A (en) * | 2019-07-19 | 2021-01-19 | 吴军祥 | Hydrochloric acid desorption tower and process using superheated steam as desorption gas in tower kettle |
| CN113398720A (en) * | 2021-07-20 | 2021-09-17 | 四川永祥股份有限公司 | Absorption tower and system for producing electronic-grade hydrochloric acid by utilizing hydrochloric acid resolution |
| CN113398720B (en) * | 2021-07-20 | 2023-03-17 | 四川永祥股份有限公司 | Absorption tower and system for producing electronic-grade hydrochloric acid by utilizing hydrochloric acid resolution |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101623584A (en) | Hydrochloric acid full stripping method | |
| CN102671510A (en) | Recovery process of flue gas CO2 | |
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN209630847U (en) | A kind of smoke stack emission gas collecting carbonic anhydride recyclable device | |
| CN205412614U (en) | Tail gas recycling apparatus of sucralose chlorination workshop section | |
| CN107754568B (en) | Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process | |
| CN101219773A (en) | Dry type acid making technique | |
| CN202146695U (en) | Gas-phase silicon dioxide tail gas treatment system | |
| CN113457381A (en) | Energy-saving process for capturing and recovering carbon dioxide from chimney exhaust gas | |
| CN103708993B (en) | A kind of vinylidene is thick cracking gas alkali cleaning and dehydrating process in producing | |
| CN102824818B (en) | Device for reducing energy consumption of flue gas CO2 capturing system and increasing CO2 recovery rate | |
| CN109319736A (en) | Ammonia tank periodic off-gases recyclable device and its technique | |
| CN202893154U (en) | Device for reducing energy consumption of smoke carbon dioxide (CO2) capturing system and improving recovery rate of CO2 | |
| CN110721493A (en) | Method for separating trichloroethane from crude sulfur dioxide | |
| CN217410284U (en) | Novel chemical absorption method flue gas CO2 entrapment system | |
| CN1686980A (en) | Method for preparing methane chloride from methane chloride through heat chlorination | |
| CN202829608U (en) | Urea deep-hydrolyzation gaseous-phase heat recovery system | |
| CN217264857U (en) | Concentration and reuse device for chlorine gas drying waste acid | |
| CN102584523B (en) | Semifinished chlorinated solution water washing and alkali washing device used during chlorobenzene production and water washing and alkali washing method | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source | |
| CN204933232U (en) | Carbon dioxide capture system | |
| CN203298522U (en) | Waste heat recovery and utilization system applied during production process of ethylene oxide equipment | |
| CN207102248U (en) | Improve the synthesis ammonia decarbonization system of lean solution regeneration degree | |
| CN104261428A (en) | Synthesis ammonia production method for improving net value of ammonia | |
| CN107335318B (en) | Hydrogen chloride recycling system and method in industrial organic waste gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Open date: 20100113 |