CN102658016A - Method for ammonia method desulfurization of flue gas and high-purity ammonium hydrogen sulfite by-producing - Google Patents
Method for ammonia method desulfurization of flue gas and high-purity ammonium hydrogen sulfite by-producing Download PDFInfo
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- CN102658016A CN102658016A CN2012101313574A CN201210131357A CN102658016A CN 102658016 A CN102658016 A CN 102658016A CN 2012101313574 A CN2012101313574 A CN 2012101313574A CN 201210131357 A CN201210131357 A CN 201210131357A CN 102658016 A CN102658016 A CN 102658016A
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- absorption tower
- washing
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 239000003546 flue gas Substances 0.000 title claims abstract description 61
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 25
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 20
- ZETCGWYACBNPIH-UHFFFAOYSA-N azane;sulfurous acid Chemical compound N.OS(O)=O ZETCGWYACBNPIH-UHFFFAOYSA-N 0.000 title claims abstract description 11
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 9
- 230000023556 desulfurization Effects 0.000 title abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims abstract description 71
- 239000007789 gas Substances 0.000 claims abstract description 43
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 30
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000005406 washing Methods 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 239000007787 solid Substances 0.000 claims abstract description 8
- 239000000243 solution Substances 0.000 claims description 51
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 24
- 230000003009 desulfurizing effect Effects 0.000 claims description 15
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 claims description 12
- 238000007872 degassing Methods 0.000 claims description 10
- 239000005864 Sulphur Substances 0.000 claims description 9
- 239000006227 byproduct Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 239000012266 salt solution Substances 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 4
- 239000002244 precipitate Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 2
- 239000011800 void material Substances 0.000 claims description 2
- 230000008021 deposition Effects 0.000 claims 1
- 229910052717 sulfur Inorganic materials 0.000 abstract description 12
- 239000011593 sulfur Substances 0.000 abstract description 12
- 230000002378 acidificating effect Effects 0.000 abstract description 2
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- XWGJFPHUCFXLBL-UHFFFAOYSA-M rongalite Chemical compound [Na+].OCS([O-])=O XWGJFPHUCFXLBL-UHFFFAOYSA-M 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- JVBXVOWTABLYPX-UHFFFAOYSA-L sodium dithionite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])=O JVBXVOWTABLYPX-UHFFFAOYSA-L 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a method for ammonia method desulfurization of flue gas and high-purity ammonium hydrogen sulfite by-producing. The method comprises the following steps that: solid substances rich in sulfur are firstly burnt to generate the flue gas rich in high concentration sulfur dioxide gas; the flue gas enters into a cyclone separator for dedusting, and the dedusted flue gas enters into a heat exchanger for temperature reduction; then the flue gas enters into a washing and purifying tower to be washed; the flue gas respectively enters into a primary absorption tower, a secondary absorption tower and a third absorption tower for absorption, the high concentration ammonium hydrogen sulfite solution generated through reaction is taken out from a bottom groove of the primary absorption tower as a finished product for package; and the flue gas enters into a washing tower to discharge after washing. By the method, SO2 and other harmful acidic gas are highly purified; the utilization ratio of an ammonia absorption agent is effectively improved; high-purity ammonium hydrogen sulfite solution can be obtained; and the ammonium hydrogen sulfite solution has excellent special industrial use and prospect.
Description
Technical field
The gas that the present invention relates to utilize rich sulfur material burning to produce prepares the ammonium bisulfite technical field, the method for particularly a kind of flue gas ammonia method desulfurizing and by-product high-purity ammonium bisulfite.
Background technology
Ammonium bisulfite (NH
4HSO
3) solution is a kind of important raw material of industry, is the raw material of producing liquid sulfur dioxide, sodium hydrosulfite and sodium formaldehyde sulfoxylate, in pharmaceuticals industry, is used as reducing agent.Preparation method commonly used is to absorb relieving haperacidity tail gas with ammoniacal liquor, obtains the bisulfite ammonium salt solution.Its chemical reaction formula is:
2NH
3+SO
2+H
2O→(NH
4)
2SO
3 (1)?；
(NH
4)
2SO
3+SO
2+H
2O→2NH
4HSO
3 (2)?。
Discharge tail gas contains sulfur dioxide, also contains sulfur dioxide in the waste gas of the tail gas of gas washing in SA production and sulfur-bearing raw ore sintering, and these sulfurous gas absorb with ammoniacal liquor usually, and ammonium sulfite is the byproduct of its desulfurization.Because content of sulfur dioxide is lower usually in these gases, therefore can react usually (1), it is incomplete that reaction (2) is carried out.If impurity is more in the gas, perhaps SO
2Gas concentration is not enough, and its product purity of producing is not enough, has influenced its industrial use.
Publication number is the ammonia type flue gas desulfurizing apparatus that the patent of CN201609633U discloses a kind of by-product ammonium bisulfite and ammonium sulfite; Comprise the two-step desulfurization tower; Be specially first grade desulfurizing tower and secondary desulfurizing tower; Feed liquid in first grade desulfurizing tower and the secondary desulfurizing tower all through circulated sprinkling with the absorption acidic gas in flue gas, the first grade desulfurizing tower bottom is provided with the slurries pond, is mainly the ammonium bisulfite feed liquid in the slurries pond.Can find out for the 15th section from this patent specification, the gas of this method desulfurization be plant tail gas from flue gas, usually sulfur dioxide in flue gas concentration is lower.Gangue, when containing burning such as sulfur mineral, SO in the flue gas
2Content is lower usually, and usually at 300-5000ppm, so the desulfurizer of secondary just can satisfy absorption, and discharges flue gas and can reach environmental requirement.But this device is not suitable for the high concentration sulfur dioxide gas that the secondary sulfur material of burning produces.The concentration of SO 2 gas that the secondary sulfur material that burns produces is very high.For example sulfur burning is not if sufficient combustion has remaining O
2, SO in the burning gases then
2The ratio of gas comprises volume of gas can reach 21%, certainly exists excess air in the Actual combustion, nonetheless, and the SO of generation
2The volume ratio of gas also can reach 10% to 15%; If burning is troilite, the SO of generation
2The volume ratio of gas also can reach 7%; Form the active carbon that is rich in sulphur in the activated carbon desulfurization, its sulfur content is also very high, SO in the gas that the burning back produces
2Content is also very high.The high concentration sulfur dioxide gas that the secondary sulfur material that burns produces is through behind the first grade absorption tower; The sulfur dioxide concentration of residual gas is still very high; After two-level absorption tower absorbed, the concentration of SO 2 gas of discharging was difficult to reach emission request, if strengthen the concentration of the ammonia of two-level absorption tower; Though sulfur dioxide can absorb fully, possibly have the escaping of ammonia.
Summary of the invention
The object of the present invention is to provide a kind of flue gas that is rich in high concentration sulfur dioxide that secondary sulfur material burning is produced to carry out the method for the ammonia process of desulfurization and production high-purity bisulfite ammonium salt solution; Make it when having than high desulfurization efficiency; Ammonia in the cleaning of off-gas; Loss reduces, and reduces production costs.
For realizing above-mentioned purpose, the present invention proposes technical scheme and is: the method for a kind of flue gas ammonia method desulfurizing and by-product high-purity ammonium bisulfite, and it is characterized in that: the solid matter that will be rich in sulphur burns, and produces the flue gas that is rich in the high concentration sulfur dioxide gas; Flue gas gets into cyclone separator and carries out dedusting, and the flue gas after the dedusting gets into heat exchanger, cools the temperature to 60～70 ℃; Flue gas gets into the washing, purifying tower, and washing, purifying tower structure and cyclone separator are similar, just are provided with shower nozzle on top, sprays the water that has atomized by shower nozzle, and the solid matter in the flue gas is washed; Flue gas gets into first grade absorption tower subsequently; First grade absorption tower inside comprises shower nozzle, several clean rooms and kerve from top to bottom at least; The tower outside is provided with circulating pump, and the solution in the kerve constantly is transported in the shower nozzle through pipeline, and the base plate of said clean room has some apertures; By the solution that shower nozzle ejection has atomized, this solution is by ammoniacal liquor and (NH
4)
2SO
3Form, the pH value of solution is controlled at 5～6, and the bisulfite ammonium salt solution of the high concentration that reaction generates falls into the kerve of first grade absorption tower, after concentration reaches requirement, from kerve, takes out and packs as finished product; Flue gas gets into two-level absorption tower subsequently, and the structure of two-level absorption tower is identical with first grade absorption tower, and by the solution that the shower nozzle ejection has atomized, this solution is by ammoniacal liquor and (NH
4)
2SO
3Form, the pH value of solution is controlled at 6～7; Flue gas gets into three grades of absorption towers subsequently, and the structure on three grades of absorption towers is identical with first grade absorption tower, and by the solution that the shower nozzle ejection has atomized, this solution is by ammoniacal liquor and (NH
4)
2SO
3Form, the pH value of solution is controlled at 6～7; Three grades of flue gas discharges after the water scrubber washing that discharge on the absorption tower, the water scrubber structure is identical with the washing, purifying tower structure.
Further, can in water scrubber, set up the net demister, carry out foam removal.
Further, in the washing, purifying tower flue gas is washed the back solution entering degassing tower that produces and outgas, degassing tower is the void tower structure, and the top is provided with gas vent; The solution that the degassing is accomplished gets into the wash cycle pond and precipitates, and after being rich in the solid precipitate and separate such as biochemical sulphur that do not have completing combustion, burns once more, carries out recycle; The gas that degassing tower produces is admitted to first grade absorption tower.
Further, the solution of the participation reaction in three grades of absorption towers can be transported in the two-level absorption tower and react, and the solution of the participation reaction in the two-level absorption tower can be transported to first grade absorption tower and react.
The invention has the beneficial effects as follows: through cyclone separator flue gas has been carried out dedusting, gas has been lowered the temperature through cooling system; If when secondary sulfur material such as sulphur can not fully burn, wherein possibly contain certain solid impurities such as biochemical sulphur, through the washing, purifying tower rich sulphur gas is washed, can impurity such as not having clean-burning biochemical sulphur be washed out, in slag liquid accumulator tank, reclaim.The solution that washing, purifying tower washing back produces contains certain SO
2, can in degassing tower, further outgas, reclaim SO wherein
2Carry out SO with three absorption towers
2Absorption, wherein first grade absorption tower mainly is used for to high concentration SO
2Concentrating of the absorption of gas and ammonium bisulfite is because SO
2Gas concentration is very high, and participates in the ammoniacal liquor of reaction and the concentration generally lower (pure ammonia concn is 25%-33%) of ammonium sulfite solution, and the bisulfite ammonium salt solution purity that therefore produces is very high.Generally at first grade absorption tower, through constantly circulation, nearly 75% SO in the gas
2Be absorbed.Two-level absorption tower mainly is used for absorbing SO
2And for the first grade desulfurizing tower provides the ammonium sulfite absorption liquid, at this moment, SO in the gas
2Concentration significantly reduces, and main component is an ammonium sulfite in the product.Generally at two-level absorption tower, through constantly circulation, nearly 75% SO in the gas
2Be absorbed.Sulfur dioxide concentration is very low in three grades of absorption towers, and the ammonia concentration in the absorption liquid is also very low at this moment, reacts remaining ammonia also seldom; Gas after the absorption is again through washing, SO in the gas
2Very low with the discharge capacity of ammonia, the removal efficiency of main acid contaminant can reach in the gas: SO
2:>=98%; SO
3:>=95%, can reach emission request fully.Desulfurizing tower is provided with the multilayer clean room, has solved in the prior art gas and has contacted insufficiently with circulation fluid, has the dead angle easily, the problem that desulfuration efficiency is low.Therefore the present invention has high purification SO
2And other harmful sour gas, effectively improve characteristics such as ammonia absorbent utilization rate, and can obtain high concentration bisulfite ammonium salt solution, have good special industry purposes and prospect.
Description of drawings
Fig. 1 is a method of using a kind of flue gas ammonia method desulfurizing of the present invention and by-product high-purity ammonium bisulfite.
Wherein: the 1-sulfur furnace; The 2-cyclone separating tower; The 3-heat exchanger; 4-washing, purifying tower; The 5-first grade absorption tower; The 6-two-level absorption tower; Three grades of absorption towers of 7-; The 8-water scrubber; The 9-circulating pump; The 10-shower nozzle; The 11-clean room; The 12-base plate; The 13-kerve; 14-one-level circulating tank; 15-secondary circulation pipe; Three grades of circulation pipes of 16-; The 17-tank; The 18-ammonia water tank; 19-wash cycle pond; The 20-degassing tower.
The specific embodiment
Experiment Introduction: at when experiment simulated flue gas of being made up of mixed air of flue gas, experiment flow is identical with Fig. 1, but flow process begins from first grade absorption tower, and simulated flue gas is preheating to 60 ℃ and laggardly goes into flow process.
Embodiment 1: simulated flue gas is formed: 78% N
2, 3% O
2, 15% SO
2, 3% CO
2And steam.Flue gas flow: 1m
3/ min.Participate in the ammoniacal liquor and (NH of circulation in the first grade absorption tower
4)
2SO
3The pH value of solution is 5～6; Participate in the ammoniacal liquor and (NH of circulation in the two-level absorption tower
4)
2SO
3The pH value of solution is 6～7; Participate in the ammoniacal liquor and (NH of circulation in three grades of absorption towers
4)
2SO
3The pH value of solution is 6～7.The result is following:
| Flue gas flow (m 3/min) | Purify back SO 2Content (ppm) | Purify back NH 3Content (ppm) | NH 4HSO 3Solution concentration |
| 1 | 58 | 32 | 75% |
Embodiment 2: simulated flue gas is formed: 78% N
2, 3% O
2, 12% SO
2, 7% CO
2And steam.Flue gas flow: 1m
3/ min.Participate in the ammoniacal liquor and (NH of circulation in the first grade absorption tower
4)
2SO
3The pH value of solution is 5～6; Participate in the ammoniacal liquor and (NH of circulation in the two-level absorption tower
4)
2SO
3The pH value of solution is 6～7; Participate in the ammoniacal liquor and (NH of circulation in three grades of absorption towers
4)
2SO
3The pH value of solution is 6～7.The result is following:
| Flue gas flow (m 3/min) | Purify back SO 2Content (ppm) | Purify back NH 3Content (ppm) | NH 4HSO 3Solution concentration |
| 1 | 65 | 28 | 70% |
Embodiment 3: simulated flue gas is formed: 78% N
2, 8 O
2SO %, 8%
2, 5% CO
2And steam.Flue gas flow: 1m
3/ min.Participate in the ammoniacal liquor and (NH of circulation in the first grade absorption tower
4)
2SO
3The pH value of solution is 5～6; Participate in the ammoniacal liquor and (NH of circulation in the two-level absorption tower
4)
2SO
3The pH value of solution is 6～7; Participate in the ammoniacal liquor and (NH of circulation in three grades of absorption towers
4)
2SO
3The pH value of solution is 5～6.The result is following:
| Flue gas flow (m 3/min) | Purify back SO 2Content (ppm) | Purify back NH 3Content (ppm) | NH 4HSO 3Solution concentration |
| 1 | 58 | 62 | 72% |
Embodiment 4: simulated flue gas is formed: 78% N
2, 3% O
2SO %, 10%
2, 8% CO
2And steam.Flue gas flow: 1m
3/ min.Participate in the ammoniacal liquor and (NH of circulation in the first grade absorption tower
4)
2SO
3The pH value of solution is 5～6; Participate in the ammoniacal liquor and (NH of circulation in the two-level absorption tower
4)
2SO
3The pH value of solution is 6～7; Participate in the ammoniacal liquor and (NH of circulation in three grades of absorption towers
4)
2SO
3The pH value of solution is 6～7.The result is following:
| Flue gas flow (m 3/min) | Purify back SO 2Content (ppm) | Purify back NH 3Content (ppm) | NH 4HSO 3Solution concentration |
| 1 | 62 | 27 | 73% |
Embodiment 5: simulated flue gas is formed: 78% N
2, 3% O
2SO %, 12%
2, 6% CO
2And steam.Flue gas flow: 1m
3/ min.Participate in the ammoniacal liquor and (NH of circulation in the first grade absorption tower
4)
2SO
3The pH value of solution is 5～6; Participate in the ammoniacal liquor and (NH of circulation in the two-level absorption tower
4)
2SO
3The pH value of solution is 6～7; Participate in the ammoniacal liquor and (NH of circulation in three grades of absorption towers
4)
2SO
3The pH value of solution is 6～7.The result is following:
| Flue gas flow (m 3/min) | Purify back SO 2Content (ppm) | Purify back NH 3Content (ppm) | NH 4HSO 3Solution concentration |
| 1 | 65 | 26 | 72% |
Claims (3)
1. the method for flue gas ammonia method desulfurizing and by-product high-purity ammonium bisulfite, it is characterized in that: the solid matter that will be rich in sulphur burns, and produces the flue gas that is rich in the high concentration sulfur dioxide gas; Flue gas gets into cyclone separator and carries out dedusting, and the flue gas after the dedusting gets into heat exchanger, cools the temperature to 60～70 ℃; Flue gas gets into the washing, purifying tower, and washing, purifying tower structure and cyclone separator are similar, just are provided with shower nozzle on top, sprays the water that has atomized by shower nozzle, and the solid matter in the flue gas is washed; Flue gas gets into first grade absorption tower subsequently; First grade absorption tower inside comprises shower nozzle, several clean rooms and kerve from top to bottom at least; The tower outside is provided with circulating pump, and the solution in the kerve constantly is transported in the shower nozzle through pipeline, and the base plate of said clean room has some apertures; By the solution that shower nozzle ejection has atomized, this solution is by ammoniacal liquor and (NH
4)
2SO
3Form, the pH value of solution is controlled at 5～6, and the bisulfite ammonium salt solution of the high concentration that reaction generates falls into the kerve of first grade absorption tower, after concentration reaches requirement, from kerve, takes out and packs as finished product; Flue gas gets into two-level absorption tower subsequently, and the structure of two-level absorption tower is identical with first grade absorption tower, and by the solution that the shower nozzle ejection has atomized, this solution is by ammoniacal liquor and (NH
4)
2SO
3Form, the pH value of solution is controlled at 6～7; Flue gas gets into three grades of absorption towers subsequently, and the structure on three grades of absorption towers is identical with first grade absorption tower, and by the solution that the shower nozzle ejection has atomized, this solution is by ammoniacal liquor and (NH
4)
2SO
3Form, the pH value of solution is controlled at 6～7; Three grades of flue gas discharges after the water scrubber washing that discharge on the absorption tower, the water scrubber structure is identical with the washing, purifying tower structure.
2. the method for a kind of flue gas ammonia method desulfurizing as claimed in claim 1 and by-product high-purity ammonium bisulfite; It is characterized in that: in the washing, purifying tower flue gas is washed the back solution entering degassing tower that produces and outgas; Degassing tower is the void tower structure, and the top is provided with gas vent; The solution that the degassing is accomplished gets into the wash cycle pond and precipitates, and with burning once more after being rich in solids such as the biochemical sulphur deposition that does not have completing combustion and collecting, carries out recycle; The gas that degassing tower produces is admitted to first grade absorption tower.
3. the method for a kind of flue gas ammonia method desulfurizing as claimed in claim 1 and by-product high-purity ammonium bisulfite; It is characterized in that: the solution of the participation reaction in three grades of absorption towers can be transported in the two-level absorption tower and react, and the solution of the participation reaction in the two-level absorption tower can be transported to first grade absorption tower and react.
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|---|---|---|---|
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210131357.4A CN102658016B (en) | 2012-05-02 | 2012-05-02 | Method for ammonia method desulfurization of flue gas and high-purity ammonium hydrogen sulfite by-producing |
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|---|---|
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| CN104474849A (en) * | 2014-12-04 | 2015-04-01 | 中国钢研科技集团有限公司 | Acid regeneration acid gas absorption and exhaust emission reduction system and utilization method thereof |
| CN110002472A (en) * | 2019-02-21 | 2019-07-12 | 武汉青江化工黄冈有限公司 | The industrial method of by-product sodium sulphate continuous production sodium hydrogensulfite |
| CN113082959A (en) * | 2021-04-02 | 2021-07-09 | 江苏新世纪江南环保股份有限公司 | Flue gas pretreatment method and device for ammonia desulphurization |
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| CN115041007A (en) * | 2022-06-23 | 2022-09-13 | 河北冀衡药业股份有限公司 | Sulfur dioxide gas recovery system and method |
| CN115624851A (en) * | 2022-12-21 | 2023-01-20 | 联仕(昆山)化学材料有限公司 | Treatment process and treatment device for tail gas in electronic-grade sulfuric acid production |
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