CN103301718B - The device of a kind of recovery, concentrated sulfur dioxide in tail gas - Google Patents
The device of a kind of recovery, concentrated sulfur dioxide in tail gas Download PDFInfo
- Publication number
- CN103301718B CN103301718B CN201310246739.6A CN201310246739A CN103301718B CN 103301718 B CN103301718 B CN 103301718B CN 201310246739 A CN201310246739 A CN 201310246739A CN 103301718 B CN103301718 B CN 103301718B
- Authority
- CN
- China
- Prior art keywords
- tail gas
- gas
- liquid
- absorber
- deoxidation reactor
- 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.)
- Active
Links
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000011084 recovery Methods 0.000 title claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 63
- 239000006096 absorbing agent Substances 0.000 claims abstract description 32
- 238000010791 quenching Methods 0.000 claims abstract description 18
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 239000012530 fluid Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 83
- 239000000243 solution Substances 0.000 claims description 38
- 238000000034 method Methods 0.000 claims description 32
- 230000008569 process Effects 0.000 claims description 17
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000010521 absorption reaction Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000000047 product Substances 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 238000002425 crystallisation Methods 0.000 claims description 9
- 230000008025 crystallization Effects 0.000 claims description 9
- CEYULKASIQJZGP-UHFFFAOYSA-L disodium;2-(carboxymethyl)-2-hydroxybutanedioate Chemical compound [Na+].[Na+].[O-]C(=O)CC(O)(C(=O)O)CC([O-])=O CEYULKASIQJZGP-UHFFFAOYSA-L 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000011734 sodium Substances 0.000 claims description 8
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 239000006227 byproduct Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000007864 aqueous solution Substances 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000003595 mist Substances 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 3
- 235000011152 sodium sulphate Nutrition 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 238000004781 supercooling Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 238000006477 desulfuration reaction Methods 0.000 description 16
- 230000023556 desulfurization Effects 0.000 description 11
- 239000002250 absorbent Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 230000002745 absorbent Effects 0.000 description 5
- 150000001412 amines Chemical class 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000003963 antioxidant agent Substances 0.000 description 2
- 230000003078 antioxidant effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000002608 ionic liquid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 150000001449 anionic compounds Chemical class 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 229910001412 inorganic anion Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 150000002892 organic cations Chemical class 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
A kind of recovery, the device of concentrated sulfur dioxide in tail gas comprises: deoxidation reactor, Quench tank, tail gas absorber, absorbing liquid circulating pump, lean pump, lean solution tank and gas-liquid separator, tail gas enters deoxidation reactor and connects Quench tank by pipeline, gas in deoxidation reactor after deoxidation enters tail gas absorber from bottom to top after Quench cooling, go out the tail gas of tail gas absorber by qualified discharge, the bottom of tail gas absorber is connected with absorbing liquid circulating pump, absorbing liquid circulating pump connects gas-liquid separator and component loops liquid is delivered to gas-liquid separator, and send cycles left liquid back to tail gas absorber, the circulation fluid delivering to gas-liquid separator discharges sulfur dioxide gas and lean solution after resolving.
Description
Technical field
The present invention relates to a kind of recovery and concentrated device, especially for reclaiming and the device of concentrated sulfur dioxide in tail gas.
Background technology
It is a large amount of containing SO that the fields such as metallurgy, thermal power generation and Coal Chemical Industry produce
2tail gas severe contamination is caused to environment.In recent years, country is to SO
2discharge propose more and more stricter requirement, especially " overall control " requirement, even if the enterprise having reached discharging standards also will carry out the desulfurization of the more degree of depth, reduce SO further
2concentration.Meanwhile, because China's Sulphur ressource lacks relatively, for meeting industrial production needs, need a large amount of imported sulphur.Data in recent years show, the demand of China to sulphur is increasing, and major part all will depend on import; Therefore in the case, the more SO reclaimed in tail gas
2just seem particularly economical, make tail gas can qualified discharge on the one hand; Reclaim SO on the other hand
2, turn waste into wealth.
In current tail gas desulfurization technology, Wet Flue Gas Desulfurization Technique is the most ripe and desulfurization degree is the highest, is therefore used widely.And in Wet Flue Gas Desulfurization Technique, most widely used is limestone/lime-gypsum doctor treatment, account for 70% of desulfurization total installed capacity amount.This method is simple, easy, desulfuration efficiency is high.But its major defect is: desulfurization product is gypsum, is mainly used as cement raw material, industrial chemicals, filler etc., utilizes limited, market price only dozens of yuan one ton, stack volume large, be easy to cause secondary pollution, and there is problems such as absorbing wastewater treatment.Especially, this method is at process low concentration SO
2there is desulfuration efficiency during flue gas to reduce, process operation is unstable, the problems such as economic benefit is low.
In order to solve traditional desulfur technology for process low concentration SO
2the deficiency of tail gas, some the relevant SO also in succession occurred both at home and abroad
2recycling technology; Mainly contain WellmanLord doctor treatment, LABSORB regenerating desulfurization method, ClausMaster doctor treatment, CANSOLV regenerable amine process, activated coke method, ionic liquid absorption cycle etc.Wherein, WellmanLord doctor treatment utilizes sodium sulfite solution absorption SO
2, then heat resolve reclaims, and this method desulfuration efficiency is high, but more difficult to the control of oxidation side reaction in sweetening process, and power consumption is higher; LABSORB regenerating desulfurization method adopts the sodium radio-phosphate,P-32 solution prepared by NaOH and phosphoric acid to absorb SO
2, solution thermal regeneration and reclaim high concentration SO
2, this mature technology, absorbent expense is lower, but technological process is long, investment cost is high, electric and steam consumption is relatively high; ClausMaster doctor treatment adopts non-water physical solvent absorption SO
2, then by thermal regeneration, this technique absorption efficiency is high, environmental friendliness, operating cost are low; CANSOLV regenerable amine process adopts reproducible By Amine Solutions as SO
2absorbent, this method advantage is absorbent reusable edible, desulfuration efficiency is high, process gas flow and concentration range is large, by-product SO
2concentration is high, but low-pressure steam and power consumption higher, and need when processing flue gas during smelting to carry out preliminary clearning process to flue gas; Activated coke method is Shanghai Ke Liu environmental protection company desulfurization by dry method newly developed, and its advantage desulfurizing agent can Reusability, desulfurization and efficiency of dust collection is higher, strong adaptability after thermal regeneration, but activated coke loss is large, water, electricity and gas etc. consumes high; Ionic liquid absorption cycle and CANSOLV regenerable amine process type, absorbent adds the aqueous solution of a small amount of activator, antioxidant and corrosion inhibiter composition with organic cation and inorganic anion for main component, this method is applicable to the little tail gas for the treatment of capacity, technique is simple, desulfuration efficiency is high, absorbent loss is little, by-product concentration of SO 2 gas is high, but there is the shortcoming the same with amine method too.
Summary of the invention
Technical problem to be solved by this invention is to overcome the defect existed in above-mentioned prior art, and provides.
For solving the problems of the technologies described above, the device of a kind of recovery, concentrated sulfur dioxide in tail gas, it is characterized in that comprising: deoxidation reactor, Quench tank, tail gas absorber, absorbing liquid circulating pump, lean pump, lean solution tank and gas-liquid separator, tail gas enters deoxidation reactor and connects Quench tank by pipeline, by being equipped with the deoxidation reactor of efficient dehydrogenation catalyst after entering the mix with a certain proportion of H2 containing the tail gas of low-concentration sulfur dioxide of deoxidation reactor, occur wherein to react as follows:
H
2+O
2→H
2O
This reaction more easily occurs, even if do not need heating can carry out at normal temperatures yet, and the deoxidation degree of depth can reach below remaining oxygen 0.1ppm, deoxidation reactor connects Quench tank and Quench tank pipeline connects into tail gas absorber, gas in deoxidation reactor after deoxidation enters tail gas absorber from bottom to top after Quench cooling, contacts with the absorption cycle liquid containing natrium citricum lower from top spray is reverse; Compared to pure water, containing the natrium citricum meeting in the aqueous solution of natrium citricum and H
+form resiliency solution, thus the reduction of restriction pH value, make SO
2solubility increase.Its absorption reaction process can represent by following series reaction:
SO
2(gas) → SO
2(liquid)
SO
2(liquid)+H
2o → H
++ HSO
3 -
Cit
3 -+H
+→HCit
2 -
HCit
2 -+H
+→H
2Cit
-
H
2Cit
-+H
+→H
3Cit
3SO
2+3H
2O+Na
3Cit→3NaHSO
3+H
3Cit
By reflecting the tail gas of tail gas absorber above by qualified discharge, the bottom of tail gas absorber is connected with absorbing liquid circulating pump, and by the pH value of controlled circulation liquid, absorbing liquid circulating pump connects gas-liquid separator
Component loops liquid is delivered to gas-liquid separator, and sends cycles left liquid back to tail gas absorber; The circulation fluid delivering to gas-liquid separator discharges sulfur dioxide gas and lean solution after resolving, and lean solution is delivered to lean solution tank by pipeline and collected, and lean solution tank is connected with lean pump, lean pump is delivered to tail gas absorber and recycles.
Also comprise preheater, preheater is connected between tail gas air inlet and described deoxidation reactor, catalyst carrier in described deoxidation reactor is activated alumina, and before described deoxidation reactor device preheater, activated alumina is a kind of good drier, good hydrophilic property, water is a kind of polar molecule, be easy to be adsorbed to catalyst surface, the active surface of covering catalyst, and hydrogen and Oxygen Adsorption ability are all not as water, so just make catalyst lose activity, before deoxidation reactor, preheater is installed, mist is carried out preheating.
Also comprise rich solution heater, gas product cooler, crystallization tank; Rich solution heater is connected between absorbing liquid circulating pump and gas-liquid separator, the component loops absorbing liquid extracted out from tail gas absorber passes through the Steam Heating of rich solution heater to required resolution temperature, and then by described gas-liquid separator separates, gas product cooler is connected with described gas-liquid separator, the SO of higher temperature
2gas, through supercooling, cooling and separation, obtains the SO that purity is higher
2gas products; The pipeline that lean pump is connected to described tail gas absorber is connected with crystallization tank simultaneously, and a small amount of sodium sulphate byproduct that the oxidation of a small amount of sulfur dioxide dissolving and oxygen in tail gas in plant running process is produced enters crystallization tank and isolates Na
2sO
410H
2o, the lean solution after being separated is back to lean solution groove.
The device of recovery provided by the invention, concentrated sulfur dioxide in tail gas, is applicable to containing low concentration (0.5%-15%) SO
2the process of tail gas; The rate of recovery is high, can reach more than 99%; The tail gas entering device by deoxidation reactor, by tail gas the overwhelming majority (> 99%) O
2remove, citric acid has complexing SO in addition
2effect and make oxygenation efficiency be less than 1%, this just makes absorption tower without the need to adding antioxidant again, decreases accessory substance Na
2sO
410H
2the generation of O; Technological process is simple, easy to operate, and equipment structure is few, and gross investment economizes; Absorbent is renewable, only need be interrupted supplementary in practical operation; By-product SO
2purity is high, and economic benefit is obvious.In view of the needs of China's modernization construction, this invention has wide market prospects, and its release must bring good economic benefit and social benefit.
Accompanying drawing illustrates:
Fig. 1 is the schematic flow sheet reclaiming, concentrate sulfur dioxide in tail gas device.
Detailed description of the invention:
Below in conjunction with accompanying drawing, inventive embodiment is described in further detail.
Embodiment 1: as shown in Figure 1, the device of a kind of recovery, concentrated sulfur dioxide in tail gas comprises: deoxidation reactor 2, Quench tank 3, tail gas absorber 4, absorbing liquid circulating pump 5, lean pump 6, lean solution tank 7 and gas-liquid separator 9, tail gas enters deoxidation reactor 2 and connects Quench tank 3 by pipeline, enters the tail gas containing low-concentration sulfur dioxide of deoxidation reactor 2 and a certain proportion of H
2by being equipped with the deoxidation reactor 2 of efficient dehydrogenation catalyst after mixing, there is following reaction wherein:
H
2+O
2→H
2O
This reaction more easily occurs, even if do not need heating can carry out at normal temperatures yet, and the deoxidation degree of depth can reach below remaining oxygen 0.1ppm, deoxidation reactor 2 connects Quench tank 3 and Quench tank 3 pipeline connects into tail gas absorber, gas in deoxidation reactor 2 after deoxidation enters tail gas absorber 4 from bottom to top after Quench cooling, contacts with the absorption cycle liquid containing natrium citricum lower from top spray is reverse; Compared to pure water, containing the natrium citricum meeting in the aqueous solution of natrium citricum and H
+form resiliency solution, thus the reduction of restriction pH value, make SO
2solubility increase.Its absorption reaction process can represent by following series reaction:
SO
2(gas) → SO
2(liquid)
SO
2(liquid)+H
2o → H
++ HSO
3 -
Cit
3 -+H
+→HCit
2 -
HCit
2 -+H
+→H
2Cit
-
H
2Cit
-+H
+→H3Cit
3SO
2+3H
2O+Na
3Cit→3NaHSO
3+H
3Cit
By reflecting the tail gas of tail gas absorber 4 above by qualified discharge, the bottom of tail gas absorber 4 is connected with absorbing liquid circulating pump 5, by the pH value of controlled circulation liquid, absorbing liquid circulating pump 5 connects gas-liquid separator 9, component loops liquid is delivered to gas-liquid separator 9, and sends cycles left liquid back to tail gas absorber 4; The circulation fluid delivering to gas-liquid separator 9 discharges sulfur dioxide gas and lean solution after resolving, and lean solution is delivered to lean solution tank 7 by pipeline and collected, and lean solution tank 7 is connected with lean pump 6, lean solution 6 is pumped to tail gas absorber 4 and recycles.
Embodiment 2: difference from Example 1 also comprises preheater 1 as shown in Figure 1, preheater 1 is connected between tail gas air inlet and deoxidation reactor 2, catalyst carrier in deoxidation reactor 2 is activated alumina, and before described deoxidation reactor 2 device preheater 1, activated alumina is a kind of good drier, good hydrophilic property, water is a kind of polar molecule, be easy to be adsorbed to catalyst surface, the active surface of covering catalyst, and hydrogen and Oxygen Adsorption ability are all not as water, catalyst is so just made to lose activity, before deoxidation reactor, preheater is installed, mist is carried out preheating.
Embodiment 3: difference from Example 2 also comprises rich solution heater 8, gas product cooler 10, crystallization tank 11 as shown in Figure 1; Rich solution heater 8 is connected between absorbing liquid circulating pump 5 and gas-liquid separator 9, the component loops absorbing liquid extracted out from tail gas absorber 4 passes through the Steam Heating of rich solution heater 8 to required resolution temperature, and then be separated by gas-liquid separator 9, gas product cooler 10 is connected with described gas-liquid separator 9, the SO of higher temperature
2gas, through supercooling, cooling and separation, obtains the SO that purity is higher
2gas products; The pipeline that lean pump is connected to described tail gas absorber is connected with crystallization tank simultaneously, and a small amount of sodium sulphate byproduct that the oxidation of a small amount of sulfur dioxide dissolving and oxygen in tail gas in plant running process is produced enters crystallization tank and isolates Na
2sO
410H
2o, the lean solution after being separated is back to lean solution groove.
Above embodiments of the invention have been described in detail, but described content being only preferred embodiment of the present invention, can not being considered to for limiting practical range of the present invention.All equalizations done according to the present patent application scope change and improve, and all should still belong within patent covering scope of the present invention.
Claims (2)
1. the device of a recovery, concentrated sulfur dioxide in tail gas, it is characterized in that comprising: deoxidation reactor, Quench tank, tail gas absorber, absorbing liquid circulating pump, lean pump, lean solution tank and gas-liquid separator, tail gas enters deoxidation reactor and connects Quench tank by pipeline, enters the tail gas containing low-concentration sulfur dioxide of deoxidation reactor and a certain proportion of H
2by being equipped with the deoxidation reactor of efficient dehydrogenation catalyst after mixing, there is following reaction wherein:
H
2+O
2→H
2O
This reaction more easily occurs, even if do not need heating can carry out at normal temperatures yet, and the deoxidation degree of depth can reach below remaining oxygen 0.1ppm, deoxidation reactor connects Quench tank and Quench tank pipeline connects into tail gas absorber, gas in deoxidation reactor after deoxidation enters tail gas absorber from bottom to top after Quench cooling, contacts with the absorption cycle liquid containing natrium citricum lower from top spray is reverse; Compared to pure water, containing the natrium citricum meeting in the aqueous solution of natrium citricum and H
+form resiliency solution, thus the reduction of restriction pH value, make SO
2solubility increase, its absorption reaction process can represent by following series reaction:
SO
2(gas) → SO
2(liquid)
SO
2(liquid)+H
2o → H
++ HSO
3 -
Cit
3-+H
+→Hcit
2-
Hcit
2-+H
+→H
2Cit
-
H
2Cit
-+H
+→H
3Cit
3SO
2+3H
2O+Na
3Cit→3NaHSO
3+H
3Cit
By reflecting the tail gas of tail gas absorber above by qualified discharge, the bottom of tail gas absorber is connected with absorbing liquid circulating pump, by the pH value of controlled circulation liquid, absorbing liquid circulating pump connects gas-liquid separator and component loops liquid is delivered to gas-liquid separator, and sends cycles left liquid back to tail gas absorber; The circulation fluid delivering to gas-liquid separator discharges sulfur dioxide gas and lean solution after resolving, and lean solution is delivered to lean solution tank by pipeline and collected, and lean solution tank is connected with lean pump, lean pump is delivered to tail gas absorber and recycles; Also comprise preheater, preheater is connected between tail gas air inlet and described deoxidation reactor, catalyst carrier in described deoxidation reactor is activated alumina, and before described deoxidation reactor device preheater, activated alumina is a kind of good drier, good hydrophilic property, water is a kind of polar molecule, be easy to be adsorbed to catalyst surface, the active surface of covering catalyst, and hydrogen and Oxygen Adsorption ability are all not as water, so just make catalyst lose activity, before deoxidation reactor, preheater is installed, mist is carried out preheating.
2., according to the device of the recovery described in claim 1, concentrated sulfur dioxide in tail gas, it is characterized in that: also comprise rich solution heater, gas product cooler, crystallization tank; Rich solution heater is connected between absorbing liquid circulating pump and gas-liquid separator, the component loops absorbing liquid extracted out from tail gas absorber passes through the Steam Heating of rich solution heater to required resolution temperature, and then by described gas-liquid separator separates, gas product cooler is connected with described gas-liquid separator, the SO of higher temperature
2gas, through supercooling, cooling and separation, obtains the SO that purity is higher
2gas products; The pipeline that lean pump is connected to described tail gas absorber is connected with crystallization tank simultaneously, and a small amount of sodium sulphate byproduct that the oxidation of a small amount of sulfur dioxide dissolving and oxygen in tail gas in plant running process is produced enters crystallization tank and isolates Na
2sO
410H
2o, the lean solution after being separated is back to lean solution groove.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310246739.6A CN103301718B (en) | 2013-06-21 | 2013-06-21 | The device of a kind of recovery, concentrated sulfur dioxide in tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310246739.6A CN103301718B (en) | 2013-06-21 | 2013-06-21 | The device of a kind of recovery, concentrated sulfur dioxide in tail gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103301718A CN103301718A (en) | 2013-09-18 |
| CN103301718B true CN103301718B (en) | 2016-03-02 |
Family
ID=49127697
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310246739.6A Active CN103301718B (en) | 2013-06-21 | 2013-06-21 | The device of a kind of recovery, concentrated sulfur dioxide in tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103301718B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708427A (en) * | 2013-12-19 | 2014-04-09 | 中国平煤神马集团开封兴化精细化工有限公司 | Method for recycling sulfur dioxide tail gas in saccharin production process |
| CN106986313A (en) * | 2017-04-11 | 2017-07-28 | 付永全 | A kind of flue gas desulfurization with citrate solution and sulfur dioxide process for reclaiming |
| CN111450672A (en) * | 2020-03-31 | 2020-07-28 | 陕西聚能新创煤化科技有限公司 | Environment-friendly treatment system and treatment method for desulfurization tail gas and ammonia nitrogen liquid |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202046881U (en) * | 2011-03-16 | 2011-11-23 | 建业庆松集团有限公司 | Device for preparing high-concentration liquid SO2 with waste gas containing H2S of rectisol |
-
2013
- 2013-06-21 CN CN201310246739.6A patent/CN103301718B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202046881U (en) * | 2011-03-16 | 2011-11-23 | 建业庆松集团有限公司 | Device for preparing high-concentration liquid SO2 with waste gas containing H2S of rectisol |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103301718A (en) | 2013-09-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102151476B (en) | Method for removing hydrogen sulfide in gas phase through oxidization under high gravity field | |
| CN103303877B (en) | Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process | |
| CN102992351B (en) | Method and device for purifying ammonia recovered from coal chemical industry wastewater | |
| CN100427390C (en) | Method of purifying furnace gas of closed calcium carbide furnace | |
| WO2014134917A1 (en) | Catalyst system for desulfurization treatment of industrial sulphur-containing waste gas and process thereof | |
| CN104208985A (en) | Flue gas desulfurization method and system | |
| CN103113928B (en) | Optimization process of vacuum potassium carbonate method coke oven gas desulfurization and equipment thereof | |
| CN103301718B (en) | The device of a kind of recovery, concentrated sulfur dioxide in tail gas | |
| CN210826085U (en) | Blast furnace gas catalytic desulfurization device | |
| CN105505480A (en) | Desulfurization purification system applicable to coke oven gas | |
| CN103432879B (en) | The method of the ferrous flue gas desulfurization and denitrification of hypergravity complexing | |
| CN105214450B (en) | A kind of selective absorbing SO2Absorbent and absorb SO2Process | |
| CN104119947B (en) | A kind of catalytic cracking flue gas desulfurization and aftertreatment technology | |
| CN105080317B (en) | Method that is a kind of while reclaiming sulphur and nitre | |
| CN109351126A (en) | Sulphur-containing exhaust gas processing method | |
| CN105441140A (en) | Coke oven gas purifying system | |
| CN103801175B (en) | Polyoxometallate, preparation and application thereof | |
| CN102614768B (en) | Desulfurization reactor device | |
| CN204093274U (en) | Flue gas desulphurization system | |
| CN204412040U (en) | A kind of combined type Gas Purification Factory low concentration acid gas processing device | |
| CN110252090A (en) | A method of sodium sulfite sulfur removal technology absorptive capacity and utilization rate are improved using triethanolamine | |
| CN105542873A (en) | A purification process system for coke oven gas | |
| CN104511228A (en) | Process system and method for flue gas combined desulfurization and decarburization | |
| CN212383460U (en) | Treatment system for absorbing tail gas sulfur dioxide gas | |
| CN214319665U (en) | Claus tail gas treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20160511 Address after: 214200, Jiangsu, Wuxi province Yixing Xinzhuang Street industrial concentration zone Patentee after: JIANGSU HENGXIN ENERGY TECHNOLOGY CO., LTD. Address before: 214200, 22 floor, International Economic & Trade Building, 21 education West Road, Yixing, Jiangsu Patentee before: Shao Zhihui |