CN103657367A - Device and process for changing one-tower calcium desulphurization to double-tower ammonia desulphurization - Google Patents
Device and process for changing one-tower calcium desulphurization to double-tower ammonia desulphurization Download PDFInfo
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- CN103657367A CN103657367A CN201310713267.0A CN201310713267A CN103657367A CN 103657367 A CN103657367 A CN 103657367A CN 201310713267 A CN201310713267 A CN 201310713267A CN 103657367 A CN103657367 A CN 103657367A
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- 238000000034 method Methods 0.000 title claims abstract description 63
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 42
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 239000011575 calcium Substances 0.000 title claims abstract description 37
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 37
- 230000008569 process Effects 0.000 title claims abstract description 25
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 21
- 238000010521 absorption reaction Methods 0.000 claims abstract description 63
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 43
- 230000023556 desulfurization Effects 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000003546 flue gas Substances 0.000 claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 13
- 230000003647 oxidation Effects 0.000 claims abstract description 12
- 230000001590 oxidative effect Effects 0.000 claims description 45
- 239000007788 liquid Substances 0.000 claims description 32
- 230000003009 desulfurizing effect Effects 0.000 claims description 18
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims description 12
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 12
- 239000002250 absorbent Substances 0.000 claims description 10
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 10
- 230000002745 absorbent Effects 0.000 claims description 9
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 9
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 7
- 239000007921 spray Substances 0.000 claims description 7
- 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 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- ZETCGWYACBNPIH-UHFFFAOYSA-N azane;sulfurous acid Chemical compound N.OS(O)=O ZETCGWYACBNPIH-UHFFFAOYSA-N 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000002425 crystallisation Methods 0.000 claims description 3
- 239000003337 fertilizer Substances 0.000 claims description 3
- 239000000706 filtrate Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 229910000831 Steel Inorganic materials 0.000 abstract description 5
- 238000005260 corrosion Methods 0.000 abstract description 5
- 239000010959 steel Substances 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000013078 crystal Substances 0.000 abstract 1
- 238000007599 discharging Methods 0.000 abstract 1
- 239000000428 dust Substances 0.000 abstract 1
- 230000004048 modification Effects 0.000 abstract 1
- 238000012986 modification Methods 0.000 abstract 1
- 239000002002 slurry Substances 0.000 abstract 1
- 239000010410 layer Substances 0.000 description 5
- 230000009466 transformation Effects 0.000 description 5
- 238000010276 construction Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 206010058490 Hyperoxia Diseases 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 230000000222 hyperoxic effect Effects 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 230000002421 anti-septic effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 230000000638 stimulation Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
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Abstract
The invention belongs to the technical field of environmental protection, relates to a device and a process for ammonia desulphurization, which are changed by using a calcium desulphurization device, is especially suitable for modifying an original calcium desulphurization device or newly building an ammonia desulphurization device in a thermal power plant, and solves the problems of secondary pollution in a calcium desulphurization process, insufficient steel structure strength, insufficient layering height, difficulty for repairing an anti-corrosion layer, no high temperature resistance of an anti-corrosion material, rapidly changed temperature and the like in a calcium desulphurization tower during modification and low desulfurization amount in an existing technology of changing one-tower calcium desulphurization to double-tower ammonia desulphurization. According to the device and the process, an original dust remover, gas-gas heat exchanger, circulating pump, crystal slurry pump and cyclone are completely utilized, the calcium desulphurization tower is used as an oxidation tower, devices such as an absorption tower are configured, and the purposes of purifying and discharging flue gas and avoiding the secondary pollution are achieved.
Description
Technical field
The invention belongs to environmental technology field, relate to a kind of calcium method desulfurizer that utilizes, change into device and the technique of the ammonia process of desulfurization, be particularly useful for transformation or the newly-built ammonia desulfuration equipment of steam power plant's original calcium method desulfurizer.
Background technology
At present, known calcium method (being limestone-based process) the sulfur removal technology waste liquid that has been in operation produces, and also has waste residues calcium sulfate to generate simultaneously, causes secondary pollution.And the ammonia process of desulfurization can be without waste liquid, waste sludge discharge, the ammonium sulfate of generation can utilize.Therefore a lot of calcium method desulfurization change to the ammonia process of desulfurization of efficient and low power consuming.In the desulfurization of calcium method, cost maximum is desulfurizing tower, general calcium method desulfurization all adopts single tower mode, and desulfurizing tower is all single layer structure, and ammonia process desulfuration tower is all generally a plate column (at least two-layer), if directly become plate column for the ammonia process of desulfurization in original calcium method desulfurizing tower interior laminate layer, it is not enough that the height of each interval seems again, transformation also will inevitably destroy the anti-corrosion layer structure of desulfurizing tower, and do not reach original antiseptic effect through the anticorrosive coat of repairing, transformation is got up very difficult, after layering, desulfurizing tower epimere has increased liquid bearing, cause original steel construction undercapacity.
Summary of the invention
In order to overcome the deficiency of prior art, solve the secondary pollution that the desulfurization of calcium method produces, and the steel construction undercapacity of the calcium method desulfurizing tower existing in the transformation of calcium method desulfurizing tower, layer height is not enough, anticorrosive coat is difficult to repair, anti-corrosion material is Nai Gaore and thermal shocking etc. not, and the desulfurization of existing calcium method turns the desulfurization amount problem less than normal existing in ammonia-process desulfurization technique, the invention provides device and technique that the tower calcium method of a kind of list desulfurizer turns the multi-tower type ammonia process of desulfurization, utilized original deduster completely, gas-gas heat exchanger, circulating pump, magma pump, cyclone, using calcium method desulfurizing tower as oxidizing tower utilization, the devices such as absorption tower have been configured, do not change desulfurizing tower internal structure, reach stack gas cleaning discharge, do not cause the object of secondary pollution.
The desulfurization of the tower calcium method of list of the present invention turns the device of the multi-tower type ammonia process of desulfurization, includes absorption tower, oxidizing tower, gas-gas heat exchanger, deduster, absorbent recirculation pump, heavy liquor pump, oxidation cycle pump, cyclone, crystallisation by cooling groove, piece-rate system, drying system, booster fan, exhaust fan; Deduster, gas-gas heat exchanger, absorbent recirculation pump, heavy liquor pump, oxidation cycle pump, cyclone, booster fan are all the equipment having utilized in the desulfurization of original calcium method, and protocalcium method desulfurizing tower is used as oxidizing tower; Its top, absorption tower is provided with shower nozzle, and bottom is connected with top, absorption tower shower nozzle, oxidizing tower top shower nozzle respectively through absorbent recirculation pump by pipeline.
It is as follows that the desulfurization of the tower calcium method of list of the present invention turns the technological process of the double-tower type ammonia process of desulfurization:
A. first flue gas enter deduster by entering mouth, enter again gas-gas heat exchanger, after flue gas is lowered the temperature, through booster fan, introducing absorption tower contacts with the absorption liquid spraying by shower nozzle, sulfur dioxide in flue gas and the ammoniacal liquor in absorption liquid and sulfurous acid ammonia generation chemical reaction, generate ammonium sulfite and ammonium bisulfite etc. and be dissolved in absorption liquid, flue gas is by preliminary purification like this; Then, by absorption tower exhaust opening, by flue, enter oxidizing tower, sulfur dioxide of flue gases continues to occur chemical reaction with ammoniacal liquor or ammonium sulfite in the absorption liquid being ejected, flue gas is by smart desulfurization like this, after the demister demist in oxidizing tower, through exhaust fan, blast after gas gas interchanger heats up and discharged by chimney.
B. absorption liquid is from the shower nozzle spray on top, absorption tower, arrive bottom, absorption tower, then be absorbed circulating pump and be transported to respectively the shower nozzle of absorption tower internal upper part and the shower nozzle of oxidizing tower internal upper part, absorption liquid arrives bottom, absorption tower and oxidizing tower bottom from shower nozzle spray, and the ammonium bisulfite in absorption liquid is met ammoniacal liquor and is reduced into ammonium sulfite; In oxidizing tower, ammonium sulfite and gas distributor oxygen reaction out generates ammonium sulfate; The shower nozzle Sprayer Circulation that the absorption liquid of oxidizing tower bottom is transported to oxidizing tower internal upper part through oxidation cycle pump is used; The absorption liquid of oxidizing tower bottommost is sent into cyclone through heavy liquor pump, and overflow water flows in oxidizing tower, and magma part enters piece-rate system by cyclone bottom, and the filtrate after separation enters in oxidizing tower, and solid particle is partly sent into drying system, is processed into ammonium sulfate fertilizer.
Described piece-rate system comprises condensing crystallizing groove and filter, and filter has utilized original equipment.
Described piece-rate system is seperator.
Because the present invention designs, adopted technique scheme, effectively solved that steel construction undercapacity, layer height that the desulfurization of single tower calcium method turns desulfurizing tower in the calcium method desulfurizing tower transformation that the double-tower type ammonia process of desulfurization exists are not enough, anticorrosive coat is difficult to repair and the not high heat-proof problem of anti-corrosion material.It compared with prior art has following beneficial effect:
I. the desulfurization of calcium method turns the ammonia process of desulfurization, has eliminated secondary pollution, has improved environment protecting.
Ii. utilize original calcium method desulfurizing tower, circulating pump, heavy liquor pump, cyclone, piece-rate system, booster fan etc., reduced cost;
Iii. increase absorption tower, avoid problem in the separate zone stimulation of desulfurizing tower, the problem includes: height is not enough, anticorrosive coat is difficult to repair and the problem of steel construction undercapacity;
Iv. adopt gas-gas heat exchanger, effectively reduce the temperature of flue gas, desulfurizing tower need not increase the resistance to high hot material of inwall can be used, thereby reduces improvement cost; The temperature that simultaneously adds hot exhaust gases;
V. crystallisation by cooling groove improves ammonium sulfate size and concentration, reaches the object of utilizing filter, has saved equipment cost.
Vi. utilize booster fan, exhaust fan, make the design height on absorption tower unrestricted, increased the desulfurization amount on absorption tower, meet the needs of big-and-middle-sized coal-burning boiler desulfurization.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the present invention is further described.
Fig. 1 is apparatus structure and the process flow diagram of the embodiment of the present invention.
Fig. 2 is a kind of device combination schematic diagram of piece-rate system in the present invention.
Mark in figure: 1-flue gas, 2-deduster, 3-gas-gas heat exchanger, 4-booster fan, 5-absorption tower, 6-oxidizing tower, 7-cyclone, 8-piece-rate system, 9-drying system, 10-absorbent recirculation pump, 11-oxidation cycle pump, 12-heavy liquor pump, 13-fresh water (FW), 14-air or high concentration oxygen, 15-exhaust fan, 16-chimney, ammoniacal liquor-17, ammonium sulfate fertilizer-18, gas distributor-601, demister-602; 801-condensing crystallizing groove, 802-filter.
The specific embodiment
As shown in Figure 1, include deduster (2), gas-gas heat exchanger (3), booster fan (4), absorption tower (5), oxidizing tower (6), cyclone (7), piece-rate system (8), drying system (9), absorbent recirculation pump (10), oxidation cycle pump (11), heavy liquor pump (12), exhaust fan (15), chimney (16); Oxidizing tower (6) has utilized calcium method desulfurizing tower, and deduster (2), gas-gas heat exchanger (3), booster fan (4), cyclone (7), absorbent recirculation pump (10), oxidation cycle pump (11), heavy liquor pump (12) are all the equipment having utilized in the desulfurization of original calcium method; Its top, absorption tower (5) is provided with shower nozzle, and bottom is connected with top, absorption tower shower nozzle, oxidizing tower top shower nozzle respectively through absorbent recirculation pump (10) by pipeline.Gas distributor (601) is positioned at oxidizing tower (6) inner bottom part, and demister (602) is positioned at oxidizing tower (6) internal upper part, is all the device in original calcium method desulfurizing tower.
It is as follows that the desulfurization of the tower calcium method of list of the present invention turns the technological process of the double-tower type ammonia process of desulfurization:
A. flue gas (1) first enters deduster (2), enter again gas-gas heat exchanger (3), after flue gas (1) is lowered the temperature, through booster fan (4), introducing absorption tower (5) contacts with the absorption liquid spraying by shower nozzle, sulfur dioxide in flue gas (1) and the ammoniacal liquor in absorption liquid and sulfurous acid ammonia generation chemical reaction, generate ammonium sulfite and ammonium bisulfite etc. and be dissolved in absorption liquid, flue gas (1) is by preliminary purification like this; Then by absorption tower (5), by flue, enter oxidizing tower (6), in flue gas (1), sulfur dioxide continues to occur chemical reaction with ammoniacal liquor or ammonium sulfite in the absorption liquid being ejected, flue gas (1) is by smart desulfurization like this, after demister (602) demist in oxidizing tower (6), through exhaust fan (15), blast gas gas interchanger (3), flue gas is discharged by chimney (16) after heating up.The use of booster fan (4) and exhaust fan (15), make the exhaust opening on absorption tower (5) higher than system energy works fine in the situation of entering mouth of oxidizing tower (6), greatly increase height and the volume on absorption tower (5), thereby improved the gas cleaning ability of whole system.Demister in simultaneous oxidation tower efficiently solves smog problem, and aerosol is also had to good effect.By adjusting pH value, the degree of oxidation of absorption liquid, solve aerocolloidal problem completely.
B. the shower nozzle on absorption liquid (5) top from absorption tower sprays, arrive bottom, absorption tower, then be absorbed circulating pump (10) and be transported to respectively superposed shower nozzle and the interior superposed orlop shower nozzle of oxidizing tower (6) in absorption tower (5), absorption liquid arrives bottom, absorption tower (5) and oxidizing tower (6) bottom from shower nozzle spray, and the ammonium bisulfite in absorption liquid is met ammoniacal liquor and is reduced into ammonium sulfite; In oxidizing tower (6), ammonium sulfite and gas distributor (601) oxygen reaction out generates ammonium sulfate; The shower nozzle Sprayer Circulation that the absorption liquid of oxidizing tower (6) bottom is transported to oxidizing tower internal upper part through oxidation cycle pump (11) is used; The absorption liquid of oxidizing tower (6) bottommost enters cyclone (7) through heavy liquor pump (12), overflow water flows in oxidizing tower (6), magma part enters piece-rate system (8) by cyclone (7) bottom, filtrate after separation enters in oxidizing tower (6), solid particle is partly sent into drying system (9), is finally processed into ammonium sulfate fertilizer (18).
C. ammoniacal liquor (17) supplements by liquid supplementation pipe shower nozzle spray in tower.
D. fresh water (FW) (13) supplements by the shower nozzle of the Ta Nei the superiors.
E. the gas distributor (601) that air or hyperoxia gas (14) are transported to oxidizing tower (6) bottom enters in oxidizing tower (6), and in hyperoxia gas, the volume content of oxygen is at 22%--100%.
Claims (3)
1. the tower calcium method of list desulfurization turns the device of the multi-tower type ammonia process of desulfurization, include absorption tower, oxidizing tower, gas-gas heat exchanger, deduster, absorbent recirculation pump, heavy liquor pump, oxidation cycle pump, cyclone, crystallisation by cooling groove, piece-rate system, drying system, booster fan, exhaust fan, it is characterized in that: deduster, gas-gas heat exchanger, absorbent recirculation pump, heavy liquor pump, oxidation cycle pump, cyclone, booster fan are all the equipment having utilized in the desulfurization of original calcium method, and protocalcium method desulfurizing tower is used as oxidizing tower; Its top, absorption tower is provided with shower nozzle, and bottom is connected with top, absorption tower shower nozzle, oxidizing tower top shower nozzle respectively through absorbent recirculation pump by pipeline;
It is as follows that the desulfurization of the tower calcium method of list of the present invention turns the technological process of the double-tower type ammonia process of desulfurization:
A. first flue gas enter deduster by entering mouth, enter again gas-gas heat exchanger, after flue gas is lowered the temperature, through booster fan, introducing absorption tower contacts with the absorption liquid spraying by shower nozzle, sulfur dioxide in flue gas and the ammoniacal liquor in absorption liquid and sulfurous acid ammonia generation chemical reaction, generate ammonium sulfite and ammonium bisulfite etc. and be dissolved in absorption liquid, flue gas is by preliminary purification like this; Then, by absorption tower exhaust opening, by flue, enter oxidizing tower, sulfur dioxide of flue gases continues to occur chemical reaction with ammoniacal liquor or ammonium sulfite in the absorption liquid being ejected, flue gas is by smart desulfurization like this, after the demister demist in oxidizing tower, through exhaust fan, blast after gas gas interchanger heats up and discharged by chimney;
B. absorption liquid is from the shower nozzle spray on top, absorption tower, arrive bottom, absorption tower, then be absorbed circulating pump and be transported to respectively the shower nozzle of absorption tower internal upper part and the shower nozzle of oxidizing tower internal upper part, absorption liquid arrives bottom, absorption tower and oxidizing tower bottom from shower nozzle spray, and the ammonium bisulfite in absorption liquid is met ammoniacal liquor and is reduced into ammonium sulfite; In oxidizing tower, ammonium sulfite and gas distributor oxygen reaction out generates ammonium sulfate; The shower nozzle Sprayer Circulation that the absorption liquid of oxidizing tower bottom is transported to oxidizing tower internal upper part through oxidation cycle pump is used; The absorption liquid of oxidizing tower bottommost is sent into cyclone through heavy liquor pump, and overflow water flows in oxidizing tower, and magma part enters piece-rate system by cyclone bottom, and the filtrate after separation enters in oxidizing tower, and solid particle is partly sent into drying system, is processed into ammonium sulfate fertilizer.
2. the desulfurization of the tower calcium method of a kind of list turns the device of the multi-tower type ammonia process of desulfurization according to claim 1, it is characterized in that: piece-rate system includes condensing crystallizing groove and filter, and filter has utilized original equipment.
3. the desulfurization of the tower calcium method of a kind of list turns the device of the multi-tower type ammonia process of desulfurization according to claim 1, it is characterized in that: piece-rate system is seperator.
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|---|---|---|---|
| CN201310713267.0A CN103657367B (en) | 2013-12-13 | 2013-12-13 | The desulfurization of a kind of list tower calcium method turns device and the technique of the double-tower type ammonia process of desulfurization |
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| CN201310713267.0A CN103657367B (en) | 2013-12-13 | 2013-12-13 | The desulfurization of a kind of list tower calcium method turns device and the technique of the double-tower type ammonia process of desulfurization |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104180381A (en) * | 2014-08-18 | 2014-12-03 | 山东大学 | System and method for desulfurization cooling efficiency improvement and waste heat recovery |
| CN104190228A (en) * | 2014-08-14 | 2014-12-10 | 诸暨洁球环保科技有限公司 | Composite, efficient and energy-saving ammonia process desulfurization tower |
| CN104353344A (en) * | 2014-11-05 | 2015-02-18 | 朱忠良 | Method for removing sulfide from steel gas |
| CN106166434A (en) * | 2016-07-21 | 2016-11-30 | 浙江天地环保科技有限公司 | A kind of ozone oxidation double tower ammonia process of desulfurization denitrating technique and system thereof |
| CN106669405A (en) * | 2017-01-03 | 2017-05-17 | 江苏绿叶环境工程集团有限公司 | Wet desulphurization flue gas purification system |
| CN112521982A (en) * | 2020-09-28 | 2021-03-19 | 福建省气柜设备安装有限公司 | System and process for recycling coking tail gas by using gas purification system |
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| CN1360964A (en) * | 2000-12-29 | 2002-07-31 | 清华大学 | Fume desulfurizing method and apparatus with sprayed sea water column |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104190228A (en) * | 2014-08-14 | 2014-12-10 | 诸暨洁球环保科技有限公司 | Composite, efficient and energy-saving ammonia process desulfurization tower |
| CN104190228B (en) * | 2014-08-14 | 2016-04-13 | 诸暨洁球环保科技有限公司 | A kind of composite efficient energy-saving ammonia process desulfuration tower |
| CN104180381A (en) * | 2014-08-18 | 2014-12-03 | 山东大学 | System and method for desulfurization cooling efficiency improvement and waste heat recovery |
| CN104180381B (en) * | 2014-08-18 | 2017-02-15 | 山东大学 | System and method for desulfurization cooling efficiency improvement and waste heat recovery |
| CN104353344A (en) * | 2014-11-05 | 2015-02-18 | 朱忠良 | Method for removing sulfide from steel gas |
| CN104353344B (en) * | 2014-11-05 | 2016-08-24 | 朱忠良 | The method removing iron and steel sulfide in flue gas |
| CN106166434A (en) * | 2016-07-21 | 2016-11-30 | 浙江天地环保科技有限公司 | A kind of ozone oxidation double tower ammonia process of desulfurization denitrating technique and system thereof |
| CN106166434B (en) * | 2016-07-21 | 2018-11-27 | 浙江天地环保科技有限公司 | A kind of ozone oxidation double tower ammonia process of desulfurization denitrating technique and its system |
| CN106669405A (en) * | 2017-01-03 | 2017-05-17 | 江苏绿叶环境工程集团有限公司 | Wet desulphurization flue gas purification system |
| CN106669405B (en) * | 2017-01-03 | 2019-12-27 | 江苏绿叶环境工程集团有限公司 | Wet flue gas desulfurization purification system |
| CN112521982A (en) * | 2020-09-28 | 2021-03-19 | 福建省气柜设备安装有限公司 | System and process for recycling coking tail gas by using gas purification system |
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