CN203447967U - Combined smoke desulfuration, denitration and demercuration device of industrial boiler - Google Patents
Combined smoke desulfuration, denitration and demercuration device of industrial boiler Download PDFInfo
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- CN203447967U CN203447967U CN201320471845.XU CN201320471845U CN203447967U CN 203447967 U CN203447967 U CN 203447967U CN 201320471845 U CN201320471845 U CN 201320471845U CN 203447967 U CN203447967 U CN 203447967U
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- absorption tower
- industrial boiler
- denitration
- flue gas
- calcium
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 28
- 239000000779 smoke Substances 0.000 title abstract description 11
- 238000010521 absorption reaction Methods 0.000 claims abstract description 26
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910052753 mercury Inorganic materials 0.000 claims abstract description 26
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 39
- 239000003546 flue gas Substances 0.000 claims description 39
- 230000023556 desulfurization Effects 0.000 claims description 23
- 230000003134 recirculating effect Effects 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 22
- 239000006096 absorbing agent Substances 0.000 claims description 17
- 230000008602 contraction Effects 0.000 claims description 10
- 238000013459 approach Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 15
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 8
- 239000003344 environmental pollutant Substances 0.000 abstract description 8
- 231100000719 pollutant Toxicity 0.000 abstract description 7
- 239000012530 fluid Substances 0.000 abstract description 6
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- 239000000428 dust Substances 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract 3
- 239000011575 calcium Substances 0.000 abstract 3
- 229910052791 calcium Inorganic materials 0.000 abstract 3
- 239000002594 sorbent Substances 0.000 abstract 3
- 238000006243 chemical reaction Methods 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 13
- 238000000034 method Methods 0.000 description 8
- 239000002250 absorbent Substances 0.000 description 7
- 230000002745 absorbent Effects 0.000 description 7
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 6
- 239000003245 coal Substances 0.000 description 6
- 230000001590 oxidative effect Effects 0.000 description 6
- 239000007800 oxidant agent Substances 0.000 description 5
- 230000003009 desulfurizing effect Effects 0.000 description 4
- 238000000889 atomisation Methods 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- 235000012255 calcium oxide Nutrition 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- -1 sulfate radical Chemical class 0.000 description 2
- 241001520221 Alligator sinensis Species 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000004568 cement Substances 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
- 230000000779 depleting effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Treating Waste Gases (AREA)
Abstract
The utility model relates to a combined smoke desulfuration, denitration and demercuration device of an industrial boiler. The combined smoke desulfuration, denitration and demercuration device comprises an ozone generating device, a circulating fluid bed absorption tower, a calcium-based sorbent storage bin, a cyclone separator, a bag-type dust collector as well as a chimney, wherein the bottom of the circulating fluid bed absorption tower is provided with a smoke inlet, and a main discharge flue is connected to the smoke inlet; the ozone generating device is connected with an ozone nozzle which is arranged on the main discharge flue, and the calcium-based sorbent storage bin is connected to the circulating fluid bed absorption tower; the circulating fluid bed absorption tower, the cyclone separator, the bag-type dust collector and the chimney are sequentially connected. The combined smoke desulfuration, denitration and demercuration device of the industrial boiler provided by the utility model has the advantages that O3 and a calcium-based sorbent are utilized as a consumption agent, a circulating fluid bed is utilized as a basic system, and multiple pollutants such as sulfur dioxide (SO2), nitrogen oxide (NOx) and mercury in the industrial boiler smoke are removed in a combined manner.
Description
[technical field]
The utility model relates to a kind of emission-control equipment, is specifically related to a kind of Industrial Boiler flue gas combined desulfurization and denitration mercury removal device, and it is for Industrial Boiler sulfur dioxide in flue gas (SO
2), nitrogen oxide (NO
x) and mercury etc. remove combining of multiple pollutant, belong to environmental protection equipment technical field.
[background technology]
China is that an Industrial Boiler is used big country, according to statistics, and approximately more than 50 ten thousand of the nearly Industrial Boilers of current China.China's coal-burned industrial boiler has following features: (1) separate unit boiler average size is little, and boiler overall energy consumption level is high, and energy-saving and emission-reduction managerial skills are low, and energy waste and environmental pollution are serious; (2) steam coal kind is changeable, ature of coal is poor, burn deterioration, and combustion system is backward, take grate firing boiler as main, and efficiency of combustion is lower, and pollutants emission intensity is high; (3) short, the high fume temperature of boiler chimney, pollution are large; (4) active boiler has a large capacity and a wide range, and layout is quite disperseed, and it is large that pollution control reduces discharging difficulty.
In recent years, the developed countries such as the U.S., Japan are comparatively active to the integrated research that removes technology of coal-fired multi-pollutant, and some of them technology (as urea desulphurization denitration technology etc. simultaneously) is in early stage commercialization stage.But these technology are not also all very ripe, mostly in demonstration phase, unrealized heavy industrialization application.Although the integrated control technology research of coal-fired flue-gas pollutant has obtained preliminary progress, needs time from industrial applications, need the key technical problems such as resolution system design, technology controlling and process, technology be integrated.
Circulating fluid bed semi-drying method be take recirculating fluidized bed (CFB) principle as basis, by German LURGI, developed in nineteen seventies, originally the HF that is applied to smeltery's tail gas processes, developed into afterwards the gas cleaning of the industries such as power plant, waste incineration, cement, single tower disposal ability maximum, the superior a kind of dry method flue gas purification techniques of gas cleaning comprehensive benefit in current business application, and successively in deep and remote families such as Germany, Austria, Poland, Czech, U.S. are deep and remote, Irish, Chinese, obtaining numb use, it is 2.2 * 10 that people has moved single tower flue gas Chinese alligator
6m
3/ h (operating mode, hygrometric state).The method is after quicklime slaking, to introduce in desulfurizing tower, under fluidized state, carry out desulphurization reaction with the flue gas passing into, after flue gas desulfurization, enter sack cleaner dedusting, by air-introduced machine, through chimney, discharged, the material major part under sack cleaner removes is returned to fluidized bed circulation through absorbent circulation delivery chute and is used again.Due to ciculation fluidized, make the whole formation of desulfurizing agent compared with large reaction surface, the SO in desulfurizing agent and flue gas
2fully contact, desulfuration efficiency is higher.This technology can effectively be removed sour gas and (be mainly SO
2, HF and HCl), the pollutant such as particle, but to NO
xand the removal efficiency of heavy metal (as mercury) is very limited.
Chinese invention patent 201110251067.9 has been reported a kind of fire coal boiler fume method of dust-removal and desulfurizing denitration simultaneously, boiler smoke is introduced to venturi spraying Combined Electrostatic reactor, at venturi collapsible tube, be raised flow velocity, make the absorbent atomization spraying into, flue gas, after the absorbent droplet collision with after atomization reacts, is realized preliminary sedimentation and the SO of dust
2tentatively remove.Then through diffuser, enter wet static dedusting section, realize the trapping to absorbent drop.In addition, the NO in the oxidable flue gas of oxidative free radical that high humility corona discharge produces becomes NO
2, HNO
2and HNO
3, realize NO
xremove.The high-pressure electrostatic power consumption of this patented technology is high, and inferior sulfate radical, sulfate radical and the nitrate anion of drop absorption are larger to reactor corrosion, and removal efficiency is stable not.
Therefore, for solving the problems of the technologies described above, necessaryly provide a kind of structure improved Industrial Boiler flue gas combined desulfurization and denitration mercury removal device that has, to overcome described defect of the prior art.
[utility model content]
For addressing the above problem, the purpose of this utility model is to provide a kind of O of utilization
3as depleting agents, using recirculating fluidized bed as fundamental system with calcium-base absorbing agent, to the sulfur dioxide (SO in Industrial Boiler flue gas
2), nitrogen oxide (NO
x) and the multiple pollutant such as mercury combine the Industrial Boiler flue gas combined desulfurization and denitration mercury removal device removing.
For achieving the above object, the technical scheme that the utility model is taked is: a kind of Industrial Boiler flue gas combined desulfurization and denitration mercury removal device, and it comprises ozone generating-device, recirculating fluidized bed absorption tower, calcium-base absorbing agent warehouse, cyclone separator, sack cleaner and chimney; Wherein, bottom, described recirculating fluidized bed absorption tower is provided with gas approach, and a main smokejack is connected on this gas approach; On described ozone generating-device, be connected with an ozone nozzle, this ozone nozzle is arranged on main smokejack; Described calcium-base absorbing agent warehouse is connected on recirculating fluidized bed absorption tower; Described recirculating fluidized bed absorption tower, cyclone separator, sack cleaner are connected successively with chimney.
Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model is further set to: the bottom on described recirculating fluidized bed absorption tower is followed successively by contraction section, trunnion and diffuser from the bottom up; On described contraction section, be provided with calcium-base absorbing agent entrance and circulating ash entrance; Described diffuser arranges water spout along axis direction.
Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model is further set to; The top on described recirculating fluidized bed absorption tower is provided with exhanst gas outlet along axis direction, and this exhanst gas outlet is communicated with the import of cyclone separator by pipeline.
Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model is further set to: described cyclone separator lower end hopper is provided with two outlets, wherein an outlet is connected with an ash silo by conveying device, and another outlet is connected with described circulating ash entrance by spiral reverse material machine.
Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model is further set to: the bottom of described sack cleaner is also connected in ash silo.
Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model is also set to: described calcium-base absorbing agent warehouse is connected on contraction section by calcium-base absorbing agent entrance.
Compared with prior art, the utlity model has following beneficial effect:
1) realized Industrial Boiler SO 2 from fume (SO
2), nitrogen oxide (NO
x) and mercury etc. remove combining of multiple pollutant.
2) desulfurization and denitration demercuration functional independence.This device is on the basis of original semi-dry desulphurization technology, by increasing oxidant add-on system, realizes the denitration demercuration function of system.Oxidant add-on system independent operating, regulation and control flexibly, can realize the function of system desulfurization and denitration demercuration as required.
3) adopt dry state feeding manner, the problems such as burn into obstruction of having avoided hygrometric state feeding manner to bring, compare and have saved pulping system with slurry state feeding manner simultaneously, and floor space is little, and investment and operating cost reduce.
4) desulfurization denitration demercuration function all completes in a reaction tower, system is taken up an area province, cost of investment is suitable with semi-dry desulphurization equipment, operating cost only increases oxidant consumption part, compare with SCR or SNCR denitration series connection wet method/semi-dry desulphurization technology, present technique device is simple, and investment and operating cost are with the obvious advantage.
5) apparatus control system flexibility and reliability.This device is main to be realized to determining the control of removal efficiency key process parameter, to guarantee higher removal efficiency.By the control to feeding coal, confluent, recycle stock amount, realize the parameters such as reaction temperature, particle concentration are regulated.The control of absorbent, oxidant feeding coal is according to reaction tower inlet flue gas flow and SO
2, NO
xconcentration regulates, the SO of reaction tower outlet
2, NO
xconcentration, is used as and checks and accurately regulate the assistant regulating and controlling parameter of quick lime, oxidant feeding coal, to guarantee to meet the requirements of removal efficiency.The control of confluent is to regulate reaction temperature according to reaction tower exit gas temperature, to guarantee and to promote quick lime and SO
2, NO
2reaction.The control of recycle stock amount is to carry out adjusting tower endoparticle substrate concentration according to reaction tower inlet flue gas flow and tower internal drop, to guarantee that reaction tower is in good operating condition.
[accompanying drawing explanation]
Fig. 1 is the schematic diagram of Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model.
[specific embodiment]
Refer to shown in Figure of description 1, the utility model is a kind of Industrial Boiler flue gas combined desulfurization and denitration mercury removal device, and it is comprised of several parts such as ozone generating-device 14, recirculating fluidized bed absorption tower 1, calcium-base absorbing agent warehouse 5, cyclone separator 4, sack cleaner 16 and chimneys 18.
Wherein, 1 bottom, described recirculating fluidized bed absorption tower is provided with the main smokejack of gas approach 2, (not label) and is connected on this gas approach 2, and this main smokejack is used for passing into boiler smoke.On described ozone generating-device 14, be connected with an ozone nozzle 15, this ozone nozzle 15 is arranged on main smokejack.Described calcium-base absorbing agent warehouse 5 is connected on recirculating fluidized bed absorption tower 1.Described recirculating fluidized bed absorption tower 1, cyclone separator 4, sack cleaner 16 and chimney 18 are connected successively.
Further, 1 bottom, described recirculating fluidized bed absorption tower adopts Venturi tube structure 8, and this structure is followed successively by contraction section, trunnion and diffuser from the bottom up; Boiler smoke enters recirculating fluidized bed absorption tower 1 from bottom to top via described gas approach 2, contraction section; Contraction section arranges calcium-base absorbing agent entrance 9 and circulating ash entrance 10; Diffuser arranges water spout 11 along axis direction, for jet atomization water.Described calcium-base absorbing agent warehouse 16 is connected on contraction section by calcium-base absorbing agent entrance 9.
The top on described recirculating fluidized bed absorption tower 1 is provided with exhanst gas outlet 3 along axis direction.This exhanst gas outlet 3 is communicated with cyclone separator import 12 by pipeline.
Described cyclone separator 4 is arranged between described exhanst gas outlet 3 and described sack cleaner 16.Described cyclone separator 4 lower end hoppers are provided with two outlets, and an outlet is connected with ash silo 17 by conveying device 6, and another outlet is connected with circulating ash entrance 10 by spiral reverse material machine 7.
The bottom of described sack cleaner 16 is also connected in ash silo 17.The top of described cyclone separator is provided with gas vent 13, and this gas vent 13 is connected with described sack cleaner 17.
The job step of Industrial Boiler flue gas combined desulfurization and denitration mercury removal device of the present utility model is as follows:
Step 1, the ozone that boiler smoke sprays into ozone nozzle 14 at main smokejack mixes generation oxidation reaction, and the NO in flue gas is oxidized to NO
2, Hg
0be oxidized to Hg
2+.Flue gas is entered by 1 bottom, recirculating fluidized bed absorption tower afterwards, at reaction tower bottom Venturi tube structure 8, accelerates; Calcium-base absorbing agent and circulating ash spray into recirculating fluidized bed absorption tower 1 via described Venturi tube structure 8 simultaneously;
Step 2, atomized water sprays to accelerated flow of flue gas cross section, for accelerating the SO of absorbent and flue gas
2and NO
2deng the reaction of sour gas, and the divalence mercury in solubilized flue gas.The straying quatity of water is controlled according to exhaust gas volumn and flue-gas temperature, need to regulate the straying quatity of water that the temperature of reaction tower is remained between 70～85 ℃;
Step 3, flue gas enters sack cleaner 16 and carries out gas solid separation together with after absorbent reaction, and flue gas finally enters atmosphere by chimney 18.Final reactant is for containing CaSO
3, CaSO
4, CaCO
3, particle mercury and boiler dust etc. mixture, directly enter ash silo 17, by ash discharge tank car, transported outward.
The above specific embodiment is only the preferred embodiment of this creation, not in order to limit this creation, any modification of making, is equal to replacement, improvement etc., within all should being included in the protection domain of this creation within all spirit in this creation and principle.
Claims (6)
1. an Industrial Boiler flue gas combined desulfurization and denitration mercury removal device, is characterized in that: comprise ozone generating-device, recirculating fluidized bed absorption tower, calcium-base absorbing agent warehouse, cyclone separator, sack cleaner and chimney; Wherein, bottom, described recirculating fluidized bed absorption tower is provided with gas approach, and a main smokejack is connected on this gas approach; On described ozone generating-device, be connected with an ozone nozzle, this ozone nozzle is arranged on main smokejack; Described calcium-base absorbing agent warehouse is connected on recirculating fluidized bed absorption tower; Described recirculating fluidized bed absorption tower, cyclone separator, sack cleaner are connected successively with chimney.
2. Industrial Boiler flue gas combined desulfurization and denitration mercury removal device as claimed in claim 1, is characterized in that: the bottom on described recirculating fluidized bed absorption tower is followed successively by contraction section, trunnion and diffuser from the bottom up; On described contraction section, be provided with calcium-base absorbing agent entrance and circulating ash entrance; Described diffuser arranges water spout along axis direction.
3. Industrial Boiler flue gas combined desulfurization and denitration mercury removal device as claimed in claim 2, is characterized in that: the top on described recirculating fluidized bed absorption tower is provided with exhanst gas outlet along axis direction, and this exhanst gas outlet is communicated with the import of cyclone separator by pipeline.
4. Industrial Boiler flue gas combined desulfurization and denitration mercury removal device as claimed in claim 3, it is characterized in that: described cyclone separator lower end hopper is provided with two outlets, wherein an outlet is connected with an ash silo by conveying device, and another outlet is connected with described circulating ash entrance by spiral reverse material machine.
5. Industrial Boiler flue gas combined desulfurization and denitration mercury removal device as claimed in claim 4, is characterized in that: the bottom of described sack cleaner is also connected in ash silo.
6. Industrial Boiler flue gas combined desulfurization and denitration mercury removal device as claimed in claim 5, is characterized in that: described calcium-base absorbing agent warehouse is connected on contraction section by calcium-base absorbing agent entrance.
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|---|---|---|---|
| CN201320471845.XU CN203447967U (en) | 2013-08-05 | 2013-08-05 | Combined smoke desulfuration, denitration and demercuration device of industrial boiler |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320471845.XU CN203447967U (en) | 2013-08-05 | 2013-08-05 | Combined smoke desulfuration, denitration and demercuration device of industrial boiler |
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Cited By (16)
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| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
| CN103933841A (en) * | 2014-04-09 | 2014-07-23 | 中国科学院过程工程研究所 | Device and method for simultaneously desulfurizing and denitrating sintering smoke |
| CN104984656A (en) * | 2015-06-23 | 2015-10-21 | 哈尔滨工业大学 | Multistage internal circulation semi-dry method desulfurization, denitrification and demercuration integrated device |
| WO2016011681A1 (en) * | 2014-07-21 | 2016-01-28 | 中国科学院过程工程研究所 | Equipment and method for circulating fluidized bed semidry simultaneous desulfurization and denitration of sintering flue gas |
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| CN108273375A (en) * | 2017-12-29 | 2018-07-13 | 铜陵铜冠神虹化工有限责任公司 | The hot carbonizer flue gas desulfurization device and technique in vulcanized sodium production |
| CN108310952A (en) * | 2018-05-07 | 2018-07-24 | 龙净科杰环保技术（上海）有限公司 | A kind of desulfurization and denitrification integral system and its build bed process |
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- 2013-08-05 CN CN201320471845.XU patent/CN203447967U/en not_active Expired - Fee Related
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| US9656206B2 (en) | 2013-10-15 | 2017-05-23 | Institute Of Process Engineering, Chinese Academy Of Sciences | Combined desulfuration, denitration, and demercuration apparatus and method using semi-dry process in circulating fluidized bed |
| WO2015054929A1 (en) * | 2013-10-15 | 2015-04-23 | 中国科学院过程工程研究所 | Combined desulfuration, denitration, and mercury removal apparatus and method using semidry process in circulating fluidized bed |
| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
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| WO2016011681A1 (en) * | 2014-07-21 | 2016-01-28 | 中国科学院过程工程研究所 | Equipment and method for circulating fluidized bed semidry simultaneous desulfurization and denitration of sintering flue gas |
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