CN100584766C - Full- desorption system for hydrochloride - Google Patents
Full- desorption system for hydrochloride Download PDFInfo
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- CN100584766C CN100584766C CN200810024336A CN200810024336A CN100584766C CN 100584766 C CN100584766 C CN 100584766C CN 200810024336 A CN200810024336 A CN 200810024336A CN 200810024336 A CN200810024336 A CN 200810024336A CN 100584766 C CN100584766 C CN 100584766C
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- heat exchanger
- graphite heat
- full
- reboiler
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Abstract
The invention discloses a full desorption system for hydrochloric acid, which comprises a vacuum system and a high pressure system. The invention recycles boiling acid by utilizing the difference of azeotropic point of the hydrochloric acid; a reboiler of the hydrochloric acid in the vacuum system heats diluted acid at tower bottom by utilizing HCl gas evaporated by the high pressure system, thus reducing energy consumption.
Description
Technical field:
The present invention relates to a kind of hydrochloric acid and take off desorption system.
Background technology:
Existing hydrochloric acid takes off the suction device, and content of hydrochloric acid still has certain proportion in the waste water after the processing, and recovering effect is undesirable.
Summary of the invention:
The object of the present invention is to provide a kind of rational in infrastructure, the full-desorption system for hydrogenchloride that the hydrochloric acid recovering effect is good.
Technical solution of the present invention is:
A kind of full-desorption system for hydrogenchloride, it is characterized in that: comprise that the bottom is provided with the first full graphite heat exchanger of stoste import, the first full graphite heat exchanger top communicates with the middle and upper part of first packing tower of vacuum system, the first full graphite heat exchanger communicates with first reboiler, first reboiler communicates with the first packing tower bottom, first packing tower bottom communicates with pipe connecting between the first full graphite heat exchanger and first reboiler, the first full graphite heat exchanger is connected with the concentrated acid water cooler, the first packing tower top communicates with first condenser inlet, and first condensator outlet communicates with waste pipe; Described concentrated acid water cooler is connected with the concentrated acid storage tank, the concentrated acid storage tank communicates with the second full graphite heat exchanger by pump, the second full graphite heat exchanger communicates with the top of second packing tower of high-pressure system, the second full graphite heat exchanger communicates with second reboiler, second reboiler communicates with the second packing tower bottom, second packing tower bottom communicates with pipe connecting between the second full graphite heat exchanger and second reboiler, the second full graphite heat exchanger is connected with the diluted acid water cooler, the second packing tower top communicates with second condenser, and first reboiler communicates with second condenser.
First condenser is connected with the vacuum extractor of vacuum system.The diluted acid water cooler communicates with the diluted acid storage tank, and the diluted acid storage tank is connected with the stoste import of the first full graphite heat exchanger.
The present invention utilizes the difference of hydrochloric acid azeotropic point, reclaims the acid of boiling, and the HCl gas that the hydrochloric acid reboiler of vacuum system makes full use of the high-pressure system evaporation comes diluted acid at the bottom of the heating tower, has reduced system energy consumption; The present invention adopts the packing tower form, and the concentration of the finished product HCl is more than 99%, and the massfraction of HCl is less than 1% in the waste water.
Description of drawings:
The invention will be further described below in conjunction with drawings and Examples.
Accompanying drawing is the configuration diagram of one embodiment of the invention.
Embodiment:
A kind of full-desorption system for hydrogenchloride, comprise that the bottom is provided with the first full graphite heat exchanger 1 of stoste import, the first full graphite heat exchanger, 1 top communicates with the middle and upper part of first packing tower 2 of vacuum system, the first full graphite heat exchanger 1 communicates with first reboiler 3, first reboiler 3 communicates with first packing tower, 2 bottoms, first packing tower bottom 2 communicates with pipe connecting between the first full graphite heat exchanger and first reboiler, the first full graphite heat exchanger 1 is connected with concentrated acid water cooler 4, first packing tower, 2 tops communicate with 5 imports of first condenser, and 5 outlets of first condenser communicate with waste pipe 6; Described concentrated acid water cooler 4 is connected with concentrated acid storage tank 7, concentrated acid storage tank 7 communicates with the second full graphite heat exchanger 9 by pump 8, the second full graphite heat exchanger 9 communicates with the top of second packing tower 10 of high-pressure system, the second full graphite heat exchanger 9 communicates with second reboiler 11, second reboiler 11 communicates with second packing tower, 10 bottoms, second packing tower, 10 bottoms communicate with pipe connecting between the second full graphite heat exchanger 9 and second reboiler 11, the second full graphite heat exchanger 9 is connected with diluted acid water cooler 12, the second packing tower top communicates with second condenser 13, and first reboiler 3 communicates with second condenser 13.Second packing tower, 10 tops communicate with first reboiler 3.The first packing tower top is connected with waste pipe 6.
First condenser is connected with the vacuum extractor of vacuum system.Diluted acid water cooler 12 communicates with the diluted acid storage tank, and the diluted acid storage tank is connected with the stoste import of the first full graphite heat exchanger.
Working process of the present invention is: the diluted acid in the diluted acid jar and enter vacuum system from the diluted acid of high-pressure system, carry out hot mass transfer with gas mixture from first reboiler 3, because under the vacuum condition, azeotropic acid point is higher, therefore during caloic exchanges in first packing tower 2, water vapor becomes waste water aftertreatment discharging by first condenser, enter the concentrated acid storage tank after the concentrated acid cooling at the bottom of the first filler Tata, squeeze into the second full graphite heat exchanger 9 by pump 8, enter desorption tower (i.e. second packing tower 10) through second full graphite heat exchanger 9 heating, enter high-pressure system, fully contact with the hydrogenchloride that is evaporated of desorption tower bottom and the gas mixture of water, gas-liquid mixture is finished in tower and is conducted heat and mass transfer, and the hydrogenchloride in the concentrated acid obtains heat and desorbed, after the cooling of second condenser, obtain exsiccant hydrogenchloride.The diluted acid of desorption tower bottom enters the recirculation of diluted acid jar through behind the interchanger.
Claims (2)
1, a kind of full-desorption system for hydrogenchloride, it is characterized in that: comprise that the bottom is provided with the first full graphite heat exchanger of stoste import, the first full graphite heat exchanger top communicates with the middle and upper part of first packing tower of vacuum system, the first full graphite heat exchanger communicates with first reboiler, first reboiler communicates with the first packing tower bottom, first packing tower bottom communicates with pipe connecting between the first full graphite heat exchanger and first reboiler, the first full graphite heat exchanger is connected with the concentrated acid water cooler, the first packing tower top communicates with first condenser inlet, first condensator outlet communicates with waste pipe, and first condenser is connected with the vacuum extractor of vacuum system; Described concentrated acid water cooler is connected with the concentrated acid storage tank, the concentrated acid storage tank communicates with the second full graphite heat exchanger by pump, the second full graphite heat exchanger communicates with the top of second packing tower of high-pressure system, the second full graphite heat exchanger communicates with second reboiler, second reboiler communicates with the second packing tower bottom, second packing tower bottom communicates with pipe connecting between the second full graphite heat exchanger and second reboiler, the second full graphite heat exchanger is connected with the diluted acid water cooler, the second packing tower top communicates with second condenser, first reboiler communicates with second condenser, and the second packing tower top communicates with first reboiler.
2, full-desorption system for hydrogenchloride according to claim 1 is characterized in that: the diluted acid water cooler communicates with the diluted acid storage tank, and the diluted acid storage tank is connected with the stoste import of the first full graphite heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810024336A CN100584766C (en) | 2008-05-20 | 2008-05-20 | Full- desorption system for hydrochloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810024336A CN100584766C (en) | 2008-05-20 | 2008-05-20 | Full- desorption system for hydrochloride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101289233A CN101289233A (en) | 2008-10-22 |
| CN100584766C true CN100584766C (en) | 2010-01-27 |
Family
ID=40033716
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200810024336A Expired - Fee Related CN100584766C (en) | 2008-05-20 | 2008-05-20 | Full- desorption system for hydrochloride |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100584766C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708571A (en) * | 2013-12-19 | 2014-04-09 | 天津普莱化工技术有限公司 | Technology for treating dilute hydrochloric acid waste liquid generated in production process of ADC (azodicarbonamide) foaming agent |
| CN111422833A (en) * | 2020-03-20 | 2020-07-17 | 安徽相邦化工有限公司 | Method for preparing ultra-clean high-purity hydrochloric acid by separating hydrogen chloride from hydrochloric acid-containing mother liquor |
| CN114452668B (en) * | 2022-02-28 | 2023-07-14 | 中船(邯郸)派瑞特种气体股份有限公司 | Method for preparing hydrogen chloride by using device for preparing hydrogen chloride through hydrochloric acid analysis |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3565573A (en) * | 1965-01-23 | 1971-02-23 | Power Gas Ltd | Removal of acidic gases from gaseous mixtures |
| JP2939306B2 (en) * | 1990-06-19 | 1999-08-25 | 三井化学株式会社 | Method for recovering hydrogen chloride from waste gas from bisphenol compound production |
| CN2934207Y (en) * | 2005-11-29 | 2007-08-15 | 天津渤天化工有限责任公司 | Hydrochloric acid purification device |
-
2008
- 2008-05-20 CN CN200810024336A patent/CN100584766C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3565573A (en) * | 1965-01-23 | 1971-02-23 | Power Gas Ltd | Removal of acidic gases from gaseous mixtures |
| JP2939306B2 (en) * | 1990-06-19 | 1999-08-25 | 三井化学株式会社 | Method for recovering hydrogen chloride from waste gas from bisphenol compound production |
| CN2934207Y (en) * | 2005-11-29 | 2007-08-15 | 天津渤天化工有限责任公司 | Hydrochloric acid purification device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101289233A (en) | 2008-10-22 |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100127 Termination date: 20130520 |