CN104208994A - Sodium metabisulfite exhaust gas desulfurization process - Google Patents
Sodium metabisulfite exhaust gas desulfurization process Download PDFInfo
- Publication number
- CN104208994A CN104208994A CN201410418232.9A CN201410418232A CN104208994A CN 104208994 A CN104208994 A CN 104208994A CN 201410418232 A CN201410418232 A CN 201410418232A CN 104208994 A CN104208994 A CN 104208994A
- Authority
- CN
- China
- Prior art keywords
- gas
- tail gas
- liquid
- tower
- exhaust gas
- 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.)
- Granted
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a sodium metabisulfite exhaust gas desulfurization process. Sodium metabisulfite is synthesized by three-stage series absorption, namely SO2 firstly enters a first-stage absorption synthesis kettle; a reaction exhaust gas is conveyed to a second-stage absorption synthesis kettle; an unreacted exhaust gas is conveyed to a third-stage absorption synthesis kettle, and then is conveyed to an exhaust gas absorption system; and the synthesized exhaust gas which is absorbed by the three stages of reaction kettles, and centrifugal exhaust gas are synthesized on an exhaust gas master pipe, and the synthesized gas enters a two-stage exhaust gas packing absorption tower to be absorbed. By adopting the method disclosed by the invention, the target of desulfurization of the sodium metabisulfite exhaust gas can be achieved, the environmental pollution is alleviated, the energy consumption is low, and the treatment method is simple.
Description
Technical field
The present invention relates to sulfur removal technology field, mainly a kind of sodium pyrosulfite tail gas desulfurization technique.
Background technology
Produce at home after pyrosulfurous acid process for producing sodium majority adopts soda ash washing and directly discharge.Fail the SO sponged
2surrounding enviroment pollution, the wasting of resources can be caused.Current employing " thtee-stage shiplock absorption " synthesis sodium pyrosulfite, i.e. SO
2be introduced into first order absorption synthesis reactor, reaction end gas is sent into secondary and is absorbed synthesis reactor, and unreacted tail gas enters feeding three grades again and absorbs synthesis reactor, and unreacted tail gas delivers to tail gas absorbing system again, qualified discharge.Reaction mother liquor at different levels reach adverse current after certain concentration and under, keep certain concentration gradient, maintaining system response stablizes, and also improves SO
2absorptivity.Following reaction is there is: 2SO in reactor
2+ Na
2cO
3→ Na
2s
2o
5+ CO
2.
Following reaction is produced in absorption process:
2SO
2+Na
2CO
3+H
2O→2NaHSO
3+CO
2
2NaHSO
3+Na
2CO
3→2Na
2SO
3+H
2O+CO
2
Na
2SO
3+SO
2+H
2O→2NaHSO
3
As the Na in absorption mother liquor
2sO
3, NaHSO
3when concentration reaches certain value, with transport pump to joining alkali still, recycling, supplementing fresh soda ash solution simultaneously.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of sodium pyrosulfite tail gas desulfurization technique, and it can reach the object of process sodium pyrosulfite tail gas desulfurization, and decrease the pollution to environment, energy consumption is low, and processing method is simple.
For solving the problems of the technologies described above, the technical solution adopted in the present invention is:
A kind of sodium pyrosulfite tail gas desulfurization technique, is characterized in that: the SO come from purification section
2gas passes into and generates sodium pyrosulfite containing carrying out reaction in soda ash feed liquid reactor, reactor adopts thtee-stage shiplock reaction composition, the gas that purification section comes is introduced into the first order reaction still containing soda ash feed liquid, reaction control temperature 50 ~ 60 DEG C, terminal PH is 5, after reaction, tail gas enters containing soda ash feed liquid, second order reaction still, reaction control temperature 50 ~ 60 DEG C, terminal PH is 6, after reaction, tail gas enters the third-order reaction still containing soda ash feed liquid again, reaction control temperature 50 ~ 60 DEG C, terminal PH is 6.8, soda ash material adds from three grades, ladder flows to second level reactor again, first order reactor, sulfur dioxide is absorbed fully, improve SO
2absorptivity.(unreacted is SO completely for third-order reaction still tail gas out
2gas) and the centrifugal tail gas (SO of trace
2gas) and in synthesis tail gas house steward, the centrifugal synthesis tail gas scrubbing tower entering two-stage series connection, adopt one-level soda ash absorption+one-level liquid caustic soda packed tower counter-current absorption, tail gas is emptying after alkali cleaning, after the alkali lye pH value of scrubbing tower reaches requirement, send into alkali-prepared tank and join alkali, return sodium pyrosulfite synthesis system.
Described tail gas adopts two-stage tail gas packed absorber to absorb: one-level soda ash absorption+one-level liquid caustic soda packed tower absorbs, (SO
2) absorption efficiency is greater than 99.5%, pollutant (SO
2) qualified discharge.
Every grade of tail gas packed absorber internal structure top is wire mesh demister, and middle part is gas-liquid distributor, and bottom is filling-material structure, and packed tower is the mass transfer apparatus using the filler in tower as gas-liquid two-phase Contact component.The tower body of packed tower is vertical cylinder always, and supporting plate is equipped with in bottom, and filler is placed on support plate in the mode of whole block.Hold-down grid is installed, in case blown by ascending air in the top of filler.Liquid sprays filler from tower top through liquid distribution trough, and flows down along filling surface.Gas is sent at the bottom of tower, and after distribution device in gas-fluid (minor diameter tower does not generally establish distribution device in gas-fluid) distribution, be the space that adverse current continues through packing layer with liquid, on filling surface, gas-liquid two-phase close contact carries out mass transfer.Packed tower belongs to continuous contact gas-liquid mass transfer (contact) equipment, and two phase compositions are along tower height consecutive variations, and under normal operating condition, gas phase is continuous phase, and liquid phase is decentralized photo.It is large that packed tower has production capacity, the advantages such as separative efficiency is high, and pressure drop is little, and liquid holdup is little, and operating flexibility is large.
Advantage of the present invention is:
The present invention can reach the object of process sodium pyrosulfite tail gas desulfurization, and decrease the pollution to environment, energy consumption is low, and processing method is simple.
Accompanying drawing explanation
Fig. 1 is process chart of the present invention.
Detailed description of the invention
See Fig. 1, from the SO that purification section comes
2gas passes into and generates sodium pyrosulfite containing carrying out reaction in soda ash feed liquid reactor, reactor adopts thtee-stage shiplock reaction composition, the gas that purification section comes is introduced into the first order reaction still containing soda ash feed liquid, reaction control temperature 50 ~ 60 DEG C, terminal PH is 5, after reaction, tail gas enters containing soda ash feed liquid, second order reaction still, reaction control temperature 50 ~ 60 DEG C, terminal PH is 6, after reaction, tail gas enters the third-order reaction still containing soda ash feed liquid again, reaction control temperature 50 ~ 60 DEG C, terminal PH is 6.8, soda ash material adds from three grades, ladder flows to second level reactor again, first order reactor, sulfur dioxide is absorbed fully, improve SO
2absorptivity.(unreacted is SO completely for third-order reaction still tail gas out
2gas) and the centrifugal tail gas (SO of trace
2gas) and in synthesis tail gas house steward, the centrifugal synthesis tail gas scrubbing tower entering two-stage series connection, adopt one-level soda ash absorption+one-level liquid caustic soda packed tower counter-current absorption, tail gas is emptying after alkali cleaning, after the alkali lye pH value of scrubbing tower reaches requirement, send into alkali-prepared tank and join alkali, return sodium pyrosulfite synthesis system.
Claims (3)
1. a sodium pyrosulfite tail gas desulfurization technique, is characterized in that: the SO come from purification section
2gas passes into and generates sodium pyrosulfite containing carrying out reaction in soda ash feed liquid reactor, reactor adopts thtee-stage shiplock reaction composition, the gas that purification section comes is introduced into the first order reaction still containing soda ash feed liquid, reaction control temperature 50 ~ 60 DEG C, terminal PH is 5, after reaction, tail gas enters containing soda ash feed liquid, second order reaction still, reaction control temperature 50 ~ 60 DEG C, terminal PH is 6, after reaction, tail gas enters the third-order reaction still containing soda ash feed liquid again, reaction control temperature 50 ~ 60 DEG C, terminal PH is 6.8, soda ash material adds from three grades, ladder flows to second level reactor again, first order reactor, sulfur dioxide is absorbed fully, improve the absorptivity of SO2.(unreacted is SO completely for third-order reaction still tail gas out
2gas) and the centrifugal tail gas (SO of trace
2gas) and in synthesis tail gas house steward, the centrifugal synthesis tail gas scrubbing tower entering two-stage series connection, adopt one-level soda ash absorption+one-level liquid caustic soda packed tower counter-current absorption, tail gas is emptying after alkali cleaning, after the alkali lye pH value of scrubbing tower reaches requirement, send into alkali-prepared tank and join alkali, return sodium pyrosulfite synthesis system.
2. a kind of sodium pyrosulfite tail gas desulfurization technique according to claim 1, is characterized in that: described tail gas adopts two-stage tail gas packed absorber to absorb: one-level soda ash absorption+one-level liquid caustic soda packed tower absorbs, (SO
2) absorption efficiency is greater than 99.5%, pollutant (SO
2) qualified discharge.
3. a kind of sodium pyrosulfite tail gas desulfurization technique according to claim 1, it is characterized in that: every grade of tail gas packed absorber internal structure top is wire mesh demister, middle part is gas-liquid distributor, bottom is filling-material structure, and packed tower is the mass transfer apparatus using the filler in tower as gas-liquid two-phase Contact component.The tower body of packed tower is vertical cylinder always, and supporting plate is equipped with in bottom, and filler is placed on support plate in the mode of whole block.Hold-down grid is installed, in case blown by ascending air in the top of filler.Liquid sprays filler from tower top through liquid distribution trough, and flows down along filling surface.Gas is sent at the bottom of tower, and after distribution device in gas-fluid (minor diameter tower does not generally establish distribution device in gas-fluid) distribution, be the space that adverse current continues through packing layer with liquid, on filling surface, gas-liquid two-phase close contact carries out mass transfer.Packed tower belongs to continuous contact gas-liquid mass transfer (contact) equipment, and two phase compositions are along tower height consecutive variations, and under normal operating condition, gas phase is continuous phase, and liquid phase is decentralized photo.It is large that packed tower has production capacity, the advantages such as separative efficiency is high, and pressure drop is little, and liquid holdup is little, and operating flexibility is large.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410418232.9A CN104208994B (en) | 2014-08-22 | 2014-08-22 | Sodium metabisulfite exhaust gas desulfurization process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410418232.9A CN104208994B (en) | 2014-08-22 | 2014-08-22 | Sodium metabisulfite exhaust gas desulfurization process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104208994A true CN104208994A (en) | 2014-12-17 |
| CN104208994B CN104208994B (en) | 2017-05-10 |
Family
ID=52091139
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410418232.9A Expired - Fee Related CN104208994B (en) | 2014-08-22 | 2014-08-22 | Sodium metabisulfite exhaust gas desulfurization process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104208994B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108202055A (en) * | 2018-02-13 | 2018-06-26 | 鞍钢股份有限公司 | Cleaning method for upper section of desulfurizing tower and acid-making tail gas alkaline washing tower |
| CN108744907A (en) * | 2018-06-27 | 2018-11-06 | 湖北鼎创泰裕科技有限公司 | A kind of exhaust gas treating method and processing unit containing sulfur dioxide |
| CN109970081A (en) * | 2019-03-22 | 2019-07-05 | 扬州康龙环保工程有限公司 | A method of sodium pyrosulfite is prepared using coking sulphur cream |
| CN110960961A (en) * | 2019-12-18 | 2020-04-07 | 北京中航泰达环保科技股份有限公司 | Resource recycling system and method for activated coke regeneration gas |
| CN111153418A (en) * | 2020-01-21 | 2020-05-15 | 北京中航泰达环保科技股份有限公司 | System and method for resource preparation of multi-salt by using regenerated gas of active coke |
| WO2021114851A1 (en) * | 2019-12-13 | 2021-06-17 | 江苏德义通环保科技有限公司 | System for producing sodium pyrosulfite |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4740362A (en) * | 1987-01-05 | 1988-04-26 | Central Illinois Public Service Company | Regeneration and use of SO2 gas scrubber liquid in dual alkali system |
| CN102659142A (en) * | 2012-04-17 | 2012-09-12 | 伍立君 | Preparation device and preparation method of sodium pyrosulfite and anhydrous sodium sulphite |
| CN203006961U (en) * | 2013-01-20 | 2013-06-19 | 伍立君 | Device for preparing sodium metabisulfite and anhydrous sodium sulfite |
-
2014
- 2014-08-22 CN CN201410418232.9A patent/CN104208994B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4740362A (en) * | 1987-01-05 | 1988-04-26 | Central Illinois Public Service Company | Regeneration and use of SO2 gas scrubber liquid in dual alkali system |
| CN102659142A (en) * | 2012-04-17 | 2012-09-12 | 伍立君 | Preparation device and preparation method of sodium pyrosulfite and anhydrous sodium sulphite |
| CN203006961U (en) * | 2013-01-20 | 2013-06-19 | 伍立君 | Device for preparing sodium metabisulfite and anhydrous sodium sulfite |
Non-Patent Citations (3)
| Title |
|---|
| 周家华: "《食品添加剂》", 30 April 2008 * |
| 喻朝善: "《石油化工传质单元操作》", 31 July 2012 * |
| 潘长华: "《实用小化工生产大全 第一卷》", 31 January 1999 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108202055A (en) * | 2018-02-13 | 2018-06-26 | 鞍钢股份有限公司 | Cleaning method for upper section of desulfurizing tower and acid-making tail gas alkaline washing tower |
| CN108744907A (en) * | 2018-06-27 | 2018-11-06 | 湖北鼎创泰裕科技有限公司 | A kind of exhaust gas treating method and processing unit containing sulfur dioxide |
| CN109970081A (en) * | 2019-03-22 | 2019-07-05 | 扬州康龙环保工程有限公司 | A method of sodium pyrosulfite is prepared using coking sulphur cream |
| WO2021114851A1 (en) * | 2019-12-13 | 2021-06-17 | 江苏德义通环保科技有限公司 | System for producing sodium pyrosulfite |
| CN110960961A (en) * | 2019-12-18 | 2020-04-07 | 北京中航泰达环保科技股份有限公司 | Resource recycling system and method for activated coke regeneration gas |
| CN111153418A (en) * | 2020-01-21 | 2020-05-15 | 北京中航泰达环保科技股份有限公司 | System and method for resource preparation of multi-salt by using regenerated gas of active coke |
| CN111153418B (en) * | 2020-01-21 | 2024-03-01 | 北京中航泰达环保科技股份有限公司 | System and method for preparing multiple salts by recycling active coke regenerated gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104208994B (en) | 2017-05-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104208994A (en) | Sodium metabisulfite exhaust gas desulfurization process | |
| CN103223292B (en) | Ammonia process flue gas treatment method for acidic tail gas and device | |
| CN201179415Y (en) | Flue gas desulfurization purification column | |
| CN104096468A (en) | Tail gas absorption process and equipment for bis(trichloromethyl)carbonate production | |
| CN102992351B (en) | Method and device for purifying ammonia recovered from coal chemical industry wastewater | |
| CN203183905U (en) | Low-content carbon dioxide absorption and analysis system in industrial waste gas | |
| CN108079762A (en) | Flue gas desulphurization system and the method that flue gas desulfurization is carried out using the flue gas desulphurization system | |
| CN105944544A (en) | Petrochemical acidic tail gas treatment system | |
| CN103657352A (en) | High-purity hydrogen sulfide recovery device and recovery method | |
| CN102580504A (en) | Novel ammonia desulphurization absorption device | |
| CN104495757A (en) | System for removing low-temperature thermal energy generated during adsorption of SO3 from sulfuric acid production device | |
| CN201214046Y (en) | Ammonia process desulphurizing device for reducing ammonia escape | |
| CN103550989B (en) | The integrated conduct method of tail gas in a kind of mercury chloride production process | |
| CN202506306U (en) | Novel ammonia process desulfurization absorption device | |
| CN109232171B (en) | Method for completely removing acidic substances in crude vinyl chloride gas | |
| CN204911189U (en) | Device of hydrogen phosphate in desorption yellow phosphoric tail gas | |
| CN202590600U (en) | Desulfurization device for preparing ammonium bisulfite solution through ammonia process | |
| CN112452114A (en) | Process and device for treating HCl-containing gas and by-producing high-concentration hydrochloric acid | |
| CN201889156U (en) | Combined alkaline washing tower | |
| CN104324569B (en) | Exhaust gas cleaner | |
| CN205886572U (en) | Petrochemical acidic tail gas processing system | |
| CN202590601U (en) | Production device for ammonium bisulfate solution | |
| CN101884872A (en) | Double-oxidation, double-loop and double-demisting desulfurization tower and processing device | |
| CN214020023U (en) | Preparation facilities of hydrogen chloride methanol solution | |
| CN103301718A (en) | Device capable of recovering and concentrating sulfur dioxide in tail 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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170510 Termination date: 20210822 |