CN103301718A - Device capable of recovering and concentrating sulfur dioxide in tail gas - Google Patents
Device capable of recovering and concentrating sulfur dioxide in tail gas Download PDFInfo
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- CN103301718A CN103301718A CN2013102467396A CN201310246739A CN103301718A CN 103301718 A CN103301718 A CN 103301718A CN 2013102467396 A CN2013102467396 A CN 2013102467396A CN 201310246739 A CN201310246739 A CN 201310246739A CN 103301718 A CN103301718 A CN 103301718A
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- tail gas
- gas
- sulfur dioxide
- liquid
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000010521 absorption reaction Methods 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims description 84
- 239000007788 liquid Substances 0.000 claims description 48
- 239000000243 solution Substances 0.000 claims description 41
- 239000006096 absorbing agent Substances 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 26
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000010791 quenching Methods 0.000 claims description 15
- 238000011084 recovery 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
- 238000006243 chemical reaction Methods 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
- 230000008569 process Effects 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
- 238000001816 cooling Methods 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 6
- 239000007864 aqueous solution Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 238000000926 separation method 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
- 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
- 230000003635 deoxygenating effect Effects 0.000 abstract 3
- 238000006477 desulfuration reaction Methods 0.000 description 15
- 230000023556 desulfurization Effects 0.000 description 10
- 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
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 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
- 238000007599 discharging Methods 0.000 description 2
- 230000005611 electricity 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
- 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
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 239000000428 dust Substances 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
- 230000035800 maturation Effects 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
- 238000002360 preparation method 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
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- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a device capable of recovering and concentrating sulfur dioxide in tail gas. The device comprises a deoxygenating reactor, a chilling tank, a tail gas absorption tower, an absorption liquor circulating pump, a barren liquor pump, a barren liquor tank and a gas-liquor separator, wherein tail gas enters in the deoxygenating reactor and connected with the chilling tank by a pipeline, the gas deoxygenated from the deoxygenating reactor enters the tail gas absorption tower from bottom to top after being chilled and cooled, the tail gas from the tail gas absorption tower is standard and emitted, the bottom of the tail gas absorption tower is connected with the absorption liquor circulating pump, the absorption liquor circulating pump is connected with the gas-liquor separator so as to deliver a part of circulating liquor to the gas-liquor separator and send the remaining circulating liquor back to the tail gas absorption tower, and the circulating liquor delivered to the gas-liquor separator emits sulfur dioxide gas and barren liquor.
Description
Technical field
The present invention relates to a kind of the recovery and concentrated device, especially for the device of recovery and concentrated sulfur dioxide in tail gas.
Background technology
The fields such as metallurgical, thermal power generation and Coal Chemical Industry produce contains SO in a large number
2Tail gas environment is caused severe contamination.In recent years, country is to SO
2Discharging more and more stricter requirement has been proposed, especially " overall control " requirement also will be carried out the more desulfurization of the degree of depth even reached the enterprise of discharging standards, further reduces SO
2Concentration.Meanwhile, because China's sulphur resource lacks relatively, for satisfying the industrial production needs, need a large amount of imported sulphur.Data in recent years show, China is increasing to the demand of sulphur, and major part all will depend on import; Therefore in the case, more reclaim SO in the tail gas
2Just seem particularly economical, but make on the one hand the tail gas qualified discharge; Reclaim on the other hand SO
2, turn waste into wealth.
In the present tail gas desulfur technology, Wet Flue Gas Desulfurization Technique is that maturation and desulfurization degree are the highest the most, therefore is used widely.And in Wet Flue Gas Desulfurization Technique, most widely used is the limestone/lime-gypsum doctor treatment, accounts for 70% of desulfurization total installed capacity amount.This method is simple, easily row, desulfuration efficiency are high.But its major defect is: desulfurization product is gypsum, mainly as cement raw material, industrial chemicals, filler etc., utilizes limitedly, and the market price is one ton of dozens of yuan only, stacks volume large, is easy to cause secondary pollution, and has problems such as absorbing wastewater treatment.Especially, this method is being processed low concentration SO
2Exist desulfuration efficiency to reduce during flue gas, the problem such as process operation is unstable, and economic benefit is low.
In order to solve traditional desulfur technology for processing low concentration SO
2The deficiency of tail gas, the SO that some that also in succession occur both at home and abroad are relevant
2The recycling technology; Mainly contain the WellmanLord doctor treatment, LABSORB regenerating desulfurization method, ClausMaster doctor treatment, the renewable amine method of CANSOLV, activated coke method, ionic liquid absorption cycle etc.Wherein, the WellmanLord doctor treatment is to utilize sodium sulfite solution absorption SO
2, then heating recovery, this method desulfuration efficiency is high, but the control to the oxidation side reaction is difficult in the sweetening process, and power consumption is higher; LABSORB regenerating desulfurization method adopts the sodium radio-phosphate,P-32 solution by NaOH and phosphoric acid preparation to absorb SO
2, solution thermal regeneration and recovery high concentration SO
2, this technology is ripe, and the absorbent expense is lower, but technological process is long, investment cost is high, electricity and steam consumption are relatively high; The ClausMaster doctor treatment adopts non-water physical solvent to absorb SO
2, then by thermal regeneration, this technique absorption efficiency is high, environmental friendliness, operating cost are low; The renewable amine method of CANSOLV adopts reproducible By Amine Solutions as SO
2Absorbent, this method advantage be absorbent reusable edible, desulfuration efficiency high, process gas flow and concentration range is large, by-product SO
2Concentration is high, but low-pressure steam and power consumption are higher, and need to carry out preliminary clearning to flue gas when processing flue gas during smelting and process; The activated coke method is Shanghai gram sulphur environmental protection company desulfurization by dry method newly developed, but Reusability, desulfurization and efficiency of dust collection is higher, strong adaptability behind its advantage desulfurizing agent thermal regeneration, but the activated coke loss is large, water, electricity and gas etc. consumes high; The renewable amine method of ionic liquid absorption cycle and CANSOLV type, absorbent is take organic cation and inorganic anion as main component and adds the aqueous solution that a small amount of activator, antioxidant and corrosion inhibiter form, this method is applicable to the little tail gas for the treatment of capacity, technique is simple, desulfuration efficiency is high, the absorbent loss is little, the by-product concentration of SO 2 gas is high, but exists too the shortcoming the same with the amine method.
Summary of the invention
Technical problem to be solved by this invention is to overcome the defective that exists in the 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, absorption liquid circulating pump, lean pump, lean solution tank and gas-liquid separator, tail gas enters deoxidation reactor and connects the Quench tank by pipeline, after mixing with a certain proportion of H2, the tail gas that contains low-concentration sulfur dioxide that enters deoxidation reactor by the deoxidation reactor of efficient dehydrogenation catalyst is housed, following reaction occurs therein:
H
2+O
2→H
2O
This reaction more easily occurs, can not carry out even need not heat at normal temperatures yet, and the deoxidation degree of depth can reach below the remaining oxygen 0.1ppm, deoxidation reactor connects the Quench tank and Quench tank pipeline connects into tail gas absorber, gas in the deoxidation reactor after the deoxidation enters tail gas absorber from bottom to top after through the Quench cooling, with from top spray and under reverse contact of absorption cycle liquid that contains natrium citricum; Than pure water, the natrium citricum that contains in the aqueous solution of natrium citricum can form resiliency solution with H+, thereby reducing of restriction pH value makes SO
2Solubility increase.Its absorption reaction process can represent with 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
With qualified discharge, the bottom of tail gas absorber links to each other with the absorption liquid circulating pump by the above tail gas that reflects tail gas absorber, and by the pH value of controlled circulation liquid, the absorption liquid circulating pump connects gas-liquid separator
The part circulation fluid is delivered to gas-liquid separator, and send cycles left liquid back to tail gas absorber; The circulation fluid of delivering to gas-liquid separator discharges sulfur dioxide gas and lean solution after resolving, lean solution is delivered to the lean solution tank by pipeline and collected, and the lean solution tank links to each other with lean pump, lean pump is delivered to tail gas absorber recycle.
Also comprise preheater, preheater is connected between tail gas air inlet and the described deoxidation reactor, catalyst carrier in described deoxidation reactor is activated alumina, and before described deoxidation reactor, install 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 so just make catalyst lose activity all not as water, preheater is installed before deoxidation reactor, mist is carried out preheating.
Also comprise rich solution heater, gas product cooler, crystallization tank; The rich solution heater is connected between absorption liquid circulating pump and the gas-liquid separator, the part circulating absorption solution of extracting 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, the gas product cooler links to each other with described gas-liquid separator, the SO of higher temperature
2Gas obtains the higher SO of purity through supercooling, cooling and separation
2Gas products; The pipeline that lean pump is connected to described tail gas absorber links to each other with crystallization tank simultaneously, a small amount of sulfur dioxide in the tail gas is dissolved and a small amount of sodium sulphate byproduct that the oxidation of oxygen produces enters crystallization tank and isolates Na
2SO
4.10H
2O, the lean solution after separating is back to the lean solution groove.
The device of recovery provided by the invention, concentrated sulfur dioxide in tail gas is applicable to contain low concentration (0.5%-15%) SO
2The processing of tail gas; The rate of recovery is high, can reach more than 99%; The tail gas of motion device is by deoxidation reactor, with the O of the overwhelming majority (＞99%) in the tail gas
2Remove, citric acid has complexing SO in addition
2Effect and make oxygenation efficiency less than 1%, this has reduced accessory substance Na just so that the absorption tower need not to add antioxidant again
2SO
410H
2The generation of O; Technological process is simple, and is easy to operate, and the equipment structure is few, and gross investment economizes; Absorbent is renewable, only needs to be interrupted in the practical operation to replenish; 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.
Description of drawings:
Fig. 1 is the schematic flow sheet that reclaims, concentrates the sulfur dioxide in tail gas device.
The specific embodiment:
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, absorption 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, the tail gas that contains low-concentration sulfur dioxide that enters deoxidation reactor 2 mixes rear deoxidation reactor 2 by efficient dehydrogenation catalyst is housed with a certain proportion of H2, following reaction occurs therein:
H
2+O
2→H
2O
This reaction more easily occurs, can not carry out even need not heat at normal temperatures yet, and the deoxidation degree of depth can reach below the remaining oxygen 0.1ppm, deoxidation reactor 2 connects Quench tank 3 and Quench tank 3 pipelines connect into tail gas absorber, gas after the deoxidation reactor 2 interior deoxidations enters tail gas absorber 4 from bottom to top after through the Quench cooling, with from top spray and under reverse contact of absorption cycle liquid that contains natrium citricum; Than pure water, contain natrium citricum meeting and H in the aqueous solution of natrium citricum
+Form resiliency solution, thereby reducing of restriction pH value makes SO
2Solubility increase.Its absorption reaction process can represent with 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 the above tail gas of tail gas absorber 4 that reflects with qualified discharge, the bottom of tail gas absorber 4 links to each other with absorption liquid circulating pump 5, pH value by controlled circulation liquid, absorption liquid circulating pump 5 connects gas-liquid separator 9, the part circulation fluid is delivered to gas-liquid separator 9, and send cycles left liquid back to tail gas absorber 4; The circulation fluid of delivering to gas-liquid separator 9 discharges sulfur dioxide gas and lean solution after resolving, lean solution is delivered to lean solution tank 7 by pipeline and collected, and lean solution tank 7 links to each other with lean pump 6, lean solution 6 is pumped to tail gas absorber 4 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 the deoxidation reactor 2, catalyst carrier in deoxidation reactor 2 is activated alumina, and at described deoxidation reactor 2 front device preheaters 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 so just make catalyst lose activity all not as water, preheater is installed before deoxidation reactor, 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 absorption liquid circulating pump 5 and the gas-liquid separator 9, the part circulating absorption solution of extracting out from tail gas absorber 4 passes through the Steam Heating of rich solution heater 8 to required resolution temperature, and then by gas-liquid separator 9 separation, gas product cooler 10 links to each other the SO of higher temperature with described gas-liquid separator 9
2Gas obtains the higher SO of purity through supercooling, cooling and separation
2Gas products; The pipeline that lean pump is connected to described tail gas absorber links to each other with crystallization tank simultaneously, a small amount of sulfur dioxide in the tail gas is dissolved and a small amount of sodium sulphate byproduct that the oxidation of oxygen produces enters crystallization tank and isolates Na
2SO
4.10H
2O, the lean solution after separating is back to the lean solution groove.
Above embodiments of the invention are had been described in detail, but described content only is preferred embodiment of the present invention, can not be considered to be used to limiting practical range of the present invention.All equalizations of doing according to the present patent application scope change and improve etc., all should still belong within the patent covering scope of the present invention.
Claims (3)
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, absorption liquid circulating pump, lean pump, lean solution tank and gas-liquid separator, tail gas enters deoxidation reactor and connects the Quench tank by pipeline, enters the tail gas that contains low-concentration sulfur dioxide and a certain proportion of H of deoxidation reactor
2After mixing by the deoxidation reactor of efficient dehydrogenation catalyst is housed, following reaction occurs therein:
H
2+O
2→H
2O
This reaction more easily occurs, can not carry out even need not heat at normal temperatures yet, and the deoxidation degree of depth can reach below the remaining oxygen 0.1ppm, deoxidation reactor connects the Quench tank and Quench tank pipeline connects into tail gas absorber, gas in the deoxidation reactor after the deoxidation enters tail gas absorber from bottom to top after through the Quench cooling, with from top spray and under reverse contact of absorption cycle liquid that contains natrium citricum; Than pure water, the natrium citricum that contains in the aqueous solution of natrium citricum can form resiliency solution with H+, thereby reducing of restriction pH value makes SO
2Solubility increase.Its absorption reaction process can represent with 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 the above tail gas of tail gas absorber that reflects with qualified discharge, the bottom of tail gas absorber links to each other with the absorption liquid circulating pump, pH value by controlled circulation liquid, the absorption liquid circulating pump connects gas-liquid separator the part circulation fluid is delivered to gas-liquid separator, and sends cycles left liquid back to tail gas absorber; The circulation fluid of delivering to gas-liquid separator discharges sulfur dioxide gas and lean solution after resolving, lean solution is delivered to the lean solution tank by pipeline and collected, and the lean solution tank links to each other with lean pump, lean pump is delivered to tail gas absorber recycle.
2. the recovery described in according to claim 1, the device of concentrated sulfur dioxide in tail gas, it is characterized in that: also comprise preheater, preheater is connected between tail gas air inlet and the described deoxidation reactor, catalyst carrier in described deoxidation reactor is activated alumina, and before described deoxidation reactor, install preheater, activated alumina is a kind of good drier, good hydrophilic property, water is a kind of polar molecule, is 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 lost activity, preheater is installed before deoxidation reactor, mist is carried out preheating.
3. the device of the recovery described in according to claim 1, concentrated sulfur dioxide in tail gas is characterized in that: also comprise rich solution heater, gas product cooler, crystallization tank; The rich solution heater is connected between absorption liquid circulating pump and the gas-liquid separator, the part circulating absorption solution of extracting 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, the gas product cooler links to each other with described gas-liquid separator, the SO of higher temperature
2Gas obtains the higher SO of purity through supercooling, cooling and separation
2Gas products; The pipeline that lean pump is connected to described tail gas absorber links to each other with crystallization tank simultaneously, a small amount of sulfur dioxide in the tail gas is dissolved and a small amount of sodium sulphate byproduct that the oxidation of oxygen produces enters crystallization tank and isolates Na
2SO
410H
2O, the lean solution after separating is back to the lean solution groove.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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| 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 |
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|---|---|
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| CN103301718B CN103301718B (en) | 2016-03-02 |
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Cited By (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 |
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| 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 |
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2013
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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 |
Cited By (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 |
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