CN101648112A - Flue gas purifying device and flue gas purifying method for trapping inhalable particulate - Google Patents
Flue gas purifying device and flue gas purifying method for trapping inhalable particulate Download PDFInfo
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- CN101648112A CN101648112A CN200910112432A CN200910112432A CN101648112A CN 101648112 A CN101648112 A CN 101648112A CN 200910112432 A CN200910112432 A CN 200910112432A CN 200910112432 A CN200910112432 A CN 200910112432A CN 101648112 A CN101648112 A CN 101648112A
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- flue gas
- coalescence
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- trapping
- tower
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 239000003546 flue gas Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 74
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000002250 absorbent Substances 0.000 claims abstract description 25
- 230000002745 absorbent Effects 0.000 claims abstract description 25
- 239000000463 material Substances 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 17
- 238000005507 spraying Methods 0.000 claims abstract description 5
- 238000004581 coalescence Methods 0.000 claims description 71
- 239000002245 particle Substances 0.000 claims description 19
- 238000006477 desulfuration reaction Methods 0.000 claims description 15
- 230000023556 desulfurization Effects 0.000 claims description 13
- 239000008188 pellet Substances 0.000 claims description 12
- 239000000779 smoke Substances 0.000 claims description 10
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical group [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 8
- 239000003500 flue dust Substances 0.000 claims description 8
- 230000001143 conditioned effect Effects 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000000292 calcium oxide Substances 0.000 claims description 5
- 235000012255 calcium oxide Nutrition 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 239000000428 dust Substances 0.000 abstract description 17
- 238000005516 engineering process Methods 0.000 description 9
- 230000005684 electric field Effects 0.000 description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000012717 electrostatic precipitator Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001962 electrophoresis Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000006249 magnetic particle Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
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Abstract
The invention discloses a flue gas purifying device and flue gas purifying method for trapping inhalable particulates, relates to flue gas purifying treatment and provides a flue gas purifying deviceand flue gas purifying method which can efficiently trap and desulfurate the inhalable particulates and is used for trapping the absorbable particulate matters. The device is provided with a reactioncondensing and merging tower, an absorbent bin, a water spraying device, a bag-type dust remover and a material circulating chute. Flue gas enters in the reaction condensing and merging tower, is mixed with an absorbent and desulfurating dust in a mixing area; flue gas which is subject to the desulfurating reaction enters in the reaction condensing area via a Venturi accelerating area; water is sprayed into a pipe expanding section of the Venturi accelerating area by the water spraying device; thick particulates and inhalable particulates are condensed and merged in the reaction condensing andmerging area; meanwhile, the desulfurating reaction is continuously carried out to obtain the purified dust which enters in the bag-type dust remover through an outlet flue of the reaction condensingand merging tower; the condensed and merged particulates are trapped by the bag-type dust remover and returned to the mixing area through the material circulating chute; and purified gas of particulates condensed and merged by the bag-type dust remover are exhausted through a chimney.
Description
Technical field
The present invention relates to a kind of gas cleaning and handle, especially relate to the device and method of a kind of trapping inhalable particulate (RSP) and desulfurization simultaneously.
Background technology
Coal is one of main energy sources of China, and 75% raw coal is used for direct burning.And coal can produce a large amount of flue dust in combustion process.The flue dust of coal-burning power plant's discharging is one of main source of pellet in the atmosphere.Pellet (PM
10) especially particle diameter is less than 2.5 microns particle (PM
2.5) become the primary air pollutants of Chinese many big and medium-sized cities gradually, health, weather and atmospheric visibility etc. have been caused certain harm and influence.Therefore, strengthening the discharging of controlling pellet by all means has been the task of top priority.Several pellet control technologys are arranged at present: (1) injects the vapor sorbent technology, can reach the purpose that efficiently removes and reduce discharging of particle, but still under test; (2) magnetic dust removal technology, this technology successful Application in collecting the magnetic dust, as the gas cleaning in the smelting iron and steel, removal efficiency to pellet is higher, but can't large-scale industrial application, its main cause is that the collection of weak magnetic-particle and the removing of collecting the surface are also had problems; (3) electro-catalytic oxidation technology can remove NO simultaneously
X, SO
2, fine grained and trace element, but energy consumption is higher; (4) acoustic agglomeration technology, also at the experimental stage.
The most of power plant of China all adopts electrostatic precipitator (ESP) collection dust in flue gas, the supporting wet desulfurizing process in downstream to remove the technology of sulfur in smoke gas at present.Electrostatic precipitator is to having very high collection efficiency than the major diameter particle, but not high to the collection efficiency of a large amount of pellets.
Application number is that 200710068431.1 Chinese invention patent application discloses a kind of combined electrostatic dust separator, and it has 4 electrion dust collection electric fields, and the first direct-current discharge electric field links to each other with the harmful smoke pipeline, as the level of gathering dust in advance; The first pulsed discharge electric field links to each other with first DC electric field, as charged level; The second direct-current discharge electric field and the 3rd direct-current discharge electric field are positioned at after the first pulsed discharge electric field successively, as the coalescence level of gathering dust.This invention is by adopting electric coalescence and common dedusting complex method, to improve the ability that removes to pellet.But the coalescence mode that adopts is comparatively complicated, and also will just can reach the purpose of desulfurization at the supporting sulfur removal technology in deduster downstream.
The efficient that traditional deduster captures less than the particle of 1 μ m is very low, because applied dust-cleaning principle such as gravity sedimentation, inertial deposition, electrophoresis etc. are for the particle not significantly effect of this particle size range.In at present conventional dust collection method, adopt inertia, whirlwind method, for the removal efficiency of fine particle only 20%～40%.
Summary of the invention
The objective of the invention is to pellet be captured problems such as effect is relatively poor at existing deduster, provide a kind of efficiently trapping inhalable particulate and can the while desulfurization be used for trapping inhalable particulate smoke eliminator and purification method.
Technical scheme of the present invention is by adopting coalescence and the compound mode of bag-type dust.
The trapping inhalable particulate smoke eliminator that is used for of the present invention is provided with ciculation fluidized reaction coalescence tower, absorbent storehouse, water injector, sack cleaner and material circulation skewed slot, ciculation fluidized reaction coalescence tower is respectively equipped with mixed zone, venturi accelerating region and ciculation fluidized reaction coalescence district from bottom to up, the import of mixed zone connects the tower gas approach, and the mixed zone is connected by the venturi accelerating region with ciculation fluidized reaction coalescence district; The outlet in absorbent storehouse is connected with the absorbent import of mixed zone, the nozzle of water injector is located on the expander section of venturi accelerating region, the flue gas discharge opening in ciculation fluidized reaction coalescence district is connected with the gas approach of sack cleaner through the tower exhaust pass, the desulfurization ash outlet of being located at the ash bucket of sack cleaner bottom is connected with the mixed zone through material circulation skewed slot, and the pure qi (oxygen) of sack cleaner exports external chimney.
The trapping inhalable particulate flue gas purifying method that is used for of the present invention may further comprise the steps:
1) flue gas at first enters ciculation fluidized reaction coalescence tower from the tower gas approach, with the absorbent that adds from the absorbent storehouse and from the desulfurization ash premixed that material circulation skewed slot loops back, carries out preliminary desulphurization reaction in the mixed zone in the mixed zone;
2) flue gas behind preliminary desulphurization reaction enters ciculation fluidized reaction coalescence district by the venturi accelerating region, the water that is used for conditioned reaction temperature and coalescence particle is sprayed into the expander section of venturi accelerating region separately by water injector, in ciculation fluidized reaction coalescence district, finish coalescence than coarseparticulate and pellet, continue to finish desulphurization reaction simultaneously, the flue dust after must purifying;
3) flue dust after the purification enters sack cleaner through the tower exhaust pass of ciculation fluidized reaction coalescence tower, particle behind the coalescence is captured by sack cleaner, return the mixed zone through material circulation skewed slot, thereby guarantee ciculation fluidized reaction and the required bed pressure drop of coalescence;
4) pure qi (oxygen) of the material thing after sack cleaner captures coalescence is discharged through chimney.
In step 1), described flue gas at first enters ciculation fluidized reaction coalescence tower from the tower gas approach, is preferably 10～20m/s in the mixed zone with the absorbent that adds from the absorbent storehouse and from the premixed speed of desulfurization ash that material circulation skewed slot loops back; Described absorbent can be selected quick lime (CaO) or calcium hydroxide (Ca (OH) for use
2).
In step 2) in, described flue gas behind preliminary desulphurization reaction enters ciculation fluidized reaction coalescence district by the venturi accelerating region the speed of flue gas in ciculation fluidized reaction coalescence district is preferably 4～9m/s, and flue gas is preferably 33～65m/s in the speed of venturi accelerating region; The described water that is used for conditioned reaction temperature and coalescence particle sprays into the expander section of venturi accelerating region separately by water injector, guarantees the water rapid evaporation, realizes quick coalescence, and described water injector is preferably atomizing water spraying device.
In step 3), described ciculation fluidized reaction and the required bed pressure drop of coalescence are preferably 1000～1500Pa.
Compare with existing smoke eliminator and purification method, the present invention has following outstanding advantage:
1) the present invention adopts simple coalescence mode, and the fine particle coalescence is become than coarse granule.
2) owing to be used for the water of conditioned reaction temperature and coalescence particle is sprayed into the venturi accelerating region separately by water injector expander section, therefore guarantee the water rapid evaporation, realize quick coalescence, and in ciculation fluidized reaction coalescence district, finish coalescence than coarseparticulate and pellet, continue to finish desulphurization reaction simultaneously, can be at this regional desulfuration efficiency up to more than 95%.
3) because the flue dust after purifying enters sack cleaner through the tower exhaust pass of ciculation fluidized reaction coalescence tower, so the particle behind the coalescence captured by sack cleaner, efficiently trapping inhalable particulate.The sack cleaner downstream has 99% PM approximately
10Be removed the PM more than 95%
0.1～1(particle of particle diameter 0.1～1 μ m) is removed, and efficiency of dust collection is higher than the dust collection method of present routine far away.
4),, carry out preliminary desulphurization reaction in this zone at the absorbent of mixed zone and adding and from the fully premixed of desulfurization ash that material circulation skewed slot loops back because flue gas at first enters ciculation fluidized reaction coalescence tower from the tower gas approach; Then, flue gas enters ciculation fluidized reaction coalescence district by the venturi accelerating region, continues to finish desulphurization reaction at this, therefore can realize desulfurization simultaneously.
Description of drawings
Fig. 1 forms schematic diagram for the structure that is used for trapping inhalable particulate smoke eliminator embodiment of the present invention.
The specific embodiment
Referring to Fig. 1, the trapping inhalable particulate smoke eliminator embodiment that is used for of the present invention is provided with ciculation fluidized reaction coalescence tower 2, absorbent storehouse 3, water injector 5, sack cleaner 8 and material circulation skewed slot 9, ciculation fluidized reaction coalescence tower 2 is respectively equipped with mixed zone 21, venturi accelerating region 22 and ciculation fluidized reaction coalescence district 23 from bottom to up, the import of mixed zone 21 connects tower gas approach 1, and mixed zone 21 and ciculation fluidized reaction coalescence district 23 are connected by venturi accelerating region 22; The outlet in absorbent storehouse 3 is connected with the absorbent import of mixed zone 21, the nozzle of water injector 5 is located on the expander section of venturi accelerating region 22, the flue gas discharge opening in ciculation fluidized reaction coalescence district 23 is connected through the gas approach of tower exhaust pass 7 with sack cleaner 8, the desulfurization ash outlet of being located at the ash bucket 81 of sack cleaner 8 bottoms is connected with mixed zone 21 through material circulation skewed slot 9, and the pure qi (oxygen) of sack cleaner 8 exports external chimney.Water injector 5 can adopt atomizing water spraying device.
Below provide the described concrete steps that are used for the trapping inhalable particulate flue gas purifying method:
1) former flue gas (inlet sulfur dioxide concentration 4000mg/Nm
3More than) at first enter ciculation fluidized reaction coalescence tower 2 from tower gas approach 1, in the mixed zone 21 with absorbent that adds by absorbent storehouse 3 and the fully premixed of desulfurization ash that loops back from material circulation skewed slot 9,21 carry out preliminary desulphurization reaction in the mixed zone; Absorbent can be selected quick lime (CaO) or calcium hydroxide (Ca (OH) for use
2), the calcium hydroxide consumption is less than 6t/h.
2) flue gas behind preliminary desulphurization reaction enters ciculation fluidized reaction coalescence district 23 by venturi accelerating region 22, the water that is used for conditioned reaction temperature (reaction temperature is below 75 ℃) and coalescence particle is sprayed into the expander section of venturi accelerating region 22 separately by water injector 5, guarantee the water rapid evaporation, realize quick coalescence.In ciculation fluidized reaction coalescence district 23, finish coalescence, continue to finish desulphurization reaction simultaneously than coarseparticulate and pellet, can be at this regional desulfuration efficiency up to more than 95%; Described flue gas behind preliminary desulphurization reaction enters ciculation fluidized reaction coalescence district 23 by venturi accelerating region 22 the speed of flue gas in ciculation fluidized reaction coalescence district 23 is 4～9m/s; 21 speed is 10～20m/s to flue gas in the mixed zone; Mixed zone 21 and ciculation fluidized reaction coalescence district 23 are connected by venturi accelerating region 22, and flue gas is 33～65m/s in the speed of venturi accelerating region 22.
3) flue dust after the purification enters sack cleaner 8 through the tower exhaust pass 7 of ciculation fluidized reaction coalescence tower 2, particle behind the coalescence is captured by sack cleaner 8, return mixed zone 21 through material circulation skewed slot 9, thereby guarantee ciculation fluidized reaction and the required bed pressure drop (about 1000～1500Pa) of coalescence.
4) removing gases such as sulfur dioxide and the clean flue gas after sack cleaner 8 trap particulate matter through ciculation fluidized reaction coalescence tower 2 discharges through chimney.
Claims (9)
1. be used for the trapping inhalable particulate smoke eliminator, it is characterized in that being provided with ciculation fluidized reaction coalescence tower, absorbent storehouse, water injector, sack cleaner and material circulation skewed slot, ciculation fluidized reaction coalescence tower is respectively equipped with mixed zone, venturi accelerating region and ciculation fluidized reaction coalescence district from bottom to up, the import of mixed zone connects the tower gas approach, and the mixed zone is connected by the venturi accelerating region with ciculation fluidized reaction coalescence district; The outlet in absorbent storehouse is connected with the absorbent import of mixed zone, the nozzle of water injector is located on the expander section of venturi accelerating region, the flue gas discharge opening in ciculation fluidized reaction coalescence district is connected with the gas approach of sack cleaner through the tower exhaust pass, the desulfurization ash outlet of being located at the ash bucket of sack cleaner bottom is connected with the mixed zone through material circulation skewed slot, and the pure qi (oxygen) of sack cleaner exports external chimney.
2. be used for the trapping inhalable particulate flue gas purifying method, adopt to be used for the trapping inhalable particulate smoke eliminator according to claim 1, it is characterized in that may further comprise the steps:
1) flue gas at first enters ciculation fluidized reaction coalescence tower from the tower gas approach, with the absorbent that adds from the absorbent storehouse and from the desulfurization ash premixed that material circulation skewed slot loops back, carries out preliminary desulphurization reaction in the mixed zone in the mixed zone;
2) flue gas behind preliminary desulphurization reaction enters ciculation fluidized reaction coalescence district by the venturi accelerating region, the water that is used for conditioned reaction temperature and coalescence particle is sprayed into the expander section of venturi accelerating region separately by water injector, in ciculation fluidized reaction coalescence district, finish coalescence than coarseparticulate and pellet, continue to finish desulphurization reaction simultaneously, the flue dust after must purifying;
3) flue dust after the purification enters sack cleaner through the tower exhaust pass of ciculation fluidized reaction coalescence tower, particle behind the coalescence is captured by sack cleaner, return the mixed zone through material circulation skewed slot, thereby guarantee ciculation fluidized reaction and the required bed pressure drop of coalescence;
4) pure qi (oxygen) of the material thing after sack cleaner captures coalescence is discharged through chimney.
3. the trapping inhalable particulate flue gas purifying method that is used for as claimed in claim 2, it is characterized in that in step 1), described flue gas at first enters ciculation fluidized reaction coalescence tower from the tower gas approach, and reaching the premixed speed of desulfurization ash that loops back from material circulation skewed slot in the mixed zone with the absorbent that adds from the absorbent storehouse is 10～20m/s.
4. as claim 2 or the 3 described trapping inhalable particulate flue gas purifying methods that are used for, it is characterized in that in step 1) described absorbent is quick lime or calcium hydroxide.
5. the trapping inhalable particulate flue gas purifying method that is used for as claimed in claim 2, it is characterized in that in step 2) in, described flue gas behind preliminary desulphurization reaction enters ciculation fluidized reaction coalescence district by the venturi accelerating region the speed of flue gas in ciculation fluidized reaction coalescence district is 4～9m/s.
6. the trapping inhalable particulate flue gas purifying method that is used for as claimed in claim 5 is characterized in that in step 2) in, flue gas is 33～65m/s in the speed of venturi accelerating region.
7. the trapping inhalable particulate flue gas purifying method that is used for as claimed in claim 2 is characterized in that in step 2) in, the described water that is used for conditioned reaction temperature and coalescence particle is sprayed into the expander section of venturi accelerating region separately by water injector.
8. the trapping inhalable particulate flue gas purifying method that is used for as claimed in claim 2 is characterized in that in step 2) in, described water injector is an atomizing water spraying device.
9. the trapping inhalable particulate flue gas purifying method that is used for as claimed in claim 2 is characterized in that in step 3), and the required bed pressure drop of described ciculation fluidized reaction and coalescence is 1000～1500Pa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910112432A CN101648112A (en) | 2009-08-26 | 2009-08-26 | Flue gas purifying device and flue gas purifying method for trapping inhalable particulate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910112432A CN101648112A (en) | 2009-08-26 | 2009-08-26 | Flue gas purifying device and flue gas purifying method for trapping inhalable particulate |
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| Publication Number | Publication Date |
|---|---|
| CN101648112A true CN101648112A (en) | 2010-02-17 |
Family
ID=41670505
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910112432A Pending CN101648112A (en) | 2009-08-26 | 2009-08-26 | Flue gas purifying device and flue gas purifying method for trapping inhalable particulate |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102961928A (en) * | 2012-11-01 | 2013-03-13 | 科林环保装备股份有限公司 | Bag dust collector for controlling PM2.5 fine particle |
| CN103857459A (en) * | 2011-08-17 | 2014-06-11 | 哈拉尔德·萨奥尔 | Method and device for cleaning waste gas by means of a fluidized bed reactor |
| CN108043192A (en) * | 2018-01-26 | 2018-05-18 | 福建龙净环保股份有限公司 | Pollutant removing system after a kind of stove |
| CN111036006A (en) * | 2019-12-24 | 2020-04-21 | 上海海事大学 | Sound wave enhanced ship waste gas desulfurization and particulate matter removal device |
| CN112191061A (en) * | 2020-08-27 | 2021-01-08 | 中冶南方都市环保工程技术股份有限公司 | Coke oven flue gas treatment system and method |
| CN114558423A (en) * | 2022-04-08 | 2022-05-31 | 陕西理工大学 | A kind of asphalt flue gas coke powder jet adsorption purification device |
| CN115138192A (en) * | 2022-07-11 | 2022-10-04 | 成都卓越四方环境科技有限公司 | Device and process for removing dust, sulfur and nitrogen in cooperation with flue gas of submerged arc furnace |
-
2009
- 2009-08-26 CN CN200910112432A patent/CN101648112A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103857459A (en) * | 2011-08-17 | 2014-06-11 | 哈拉尔德·萨奥尔 | Method and device for cleaning waste gas by means of a fluidized bed reactor |
| CN103857459B (en) * | 2011-08-17 | 2017-03-22 | 哈拉尔德·萨奥尔 | Method and device for cleaning exhaust gases by means of a fluidized bed reactor |
| EP2744589B1 (en) * | 2011-08-17 | 2019-01-23 | Harald Sauer | Method and device for cleaning exhaust gases by way of fluidized bed reactors |
| CN102961928A (en) * | 2012-11-01 | 2013-03-13 | 科林环保装备股份有限公司 | Bag dust collector for controlling PM2.5 fine particle |
| CN108043192A (en) * | 2018-01-26 | 2018-05-18 | 福建龙净环保股份有限公司 | Pollutant removing system after a kind of stove |
| CN108043192B (en) * | 2018-01-26 | 2023-10-24 | 福建龙净环保股份有限公司 | System for removing pollutants from furnace |
| CN111036006A (en) * | 2019-12-24 | 2020-04-21 | 上海海事大学 | Sound wave enhanced ship waste gas desulfurization and particulate matter removal device |
| CN111036006B (en) * | 2019-12-24 | 2021-08-03 | 上海海事大学 | A device for desulfurization and particulate matter removal of ship exhaust gas enhanced by sound waves |
| CN112191061A (en) * | 2020-08-27 | 2021-01-08 | 中冶南方都市环保工程技术股份有限公司 | Coke oven flue gas treatment system and method |
| CN112191061B (en) * | 2020-08-27 | 2025-01-14 | 中冶南方都市环保工程技术股份有限公司 | A coke oven flue gas treatment system and method |
| CN114558423A (en) * | 2022-04-08 | 2022-05-31 | 陕西理工大学 | A kind of asphalt flue gas coke powder jet adsorption purification device |
| CN115138192A (en) * | 2022-07-11 | 2022-10-04 | 成都卓越四方环境科技有限公司 | Device and process for removing dust, sulfur and nitrogen in cooperation with flue gas of submerged arc furnace |
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Application publication date: 20100217 |