CN201108808Y - Prepositioned cyclone pre-dedusting SCR smoke-gas denitration device - Google Patents
Prepositioned cyclone pre-dedusting SCR smoke-gas denitration device Download PDFInfo
- Publication number
- CN201108808Y CN201108808Y CNU2007201878150U CN200720187815U CN201108808Y CN 201108808 Y CN201108808 Y CN 201108808Y CN U2007201878150 U CNU2007201878150 U CN U2007201878150U CN 200720187815 U CN200720187815 U CN 200720187815U CN 201108808 Y CN201108808 Y CN 201108808Y
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- CN
- China
- Prior art keywords
- flue gas
- scr
- ammonia
- boiler
- scr reactor
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- Expired - Lifetime
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000003546 flue gas Substances 0.000 claims abstract description 73
- 239000000428 dust Substances 0.000 claims abstract description 51
- 230000003068 static Effects 0.000 claims abstract description 15
- 238000005507 spraying Methods 0.000 claims description 28
- 239000000463 material Substances 0.000 claims description 12
- 239000000779 smoke Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 8
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 5
- 239000010962 carbon steel Substances 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims description 4
- 238000009413 insulation Methods 0.000 claims description 3
- 238000003466 welding Methods 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 abstract description 35
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 16
- 238000002347 injection Methods 0.000 abstract description 4
- 239000007924 injection Substances 0.000 abstract description 4
- 238000011144 upstream manufacturing Methods 0.000 abstract description 4
- 238000005406 washing Methods 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 235000013339 cereals Nutrition 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 230000000414 obstructive Effects 0.000 description 3
- 239000004071 soot Substances 0.000 description 3
- BIGPRXCJEDHCLP-UHFFFAOYSA-N Ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- 241000209094 Oryza Species 0.000 description 2
- 235000007164 Oryza sativa Nutrition 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000000607 poisoning Effects 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 235000009566 rice Nutrition 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 241000272168 Laridae Species 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000000903 blocking Effects 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000003009 desulfurizing Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
Abstract
The utility model discloses a pre-cyclone pre-dust removal SCR flue gas denitration device. The upper part of the SCR reactor (3) is connected with a flue gas accessing pipe (8) introduced by a boiler (10), and the flue gas accessing pipe (8) is provided with a static mixer (2), the front end of which is provided with an ammonia injection grid (1); the lower part of the SCR reactor (3) is connected with an electrostatic dust collector (5), and an air preheater (4) is arranged between the electrostatic dust collector (5) and the SCR reactor (3); wherein, the flue gas accessing pipe (8) in the upstream of the ammonia injection grid (1) is provided with a high temperature resistant cyclone separator (6), and the nozzle of the ammonia injection grid (1) is towards the boiler (10). The pre-cyclone pre-dust removal SCR flue gas denitration device decreases the volume of the catalyst and the SCR reactor, reduces the supporting requirement, gets rid of the SCR bypass, reduces the SCR engineering cost, prolongs the service life of the catalyst and the washing cycle of an air pre-heater, and can not be provided with sootblowers or prolong the cycle of sootblowing.
Description
Technical field
The utility model belongs to equipment for denitrifying flue gas, specifically, is a kind of preposed whirlwind beforehand dust removal SCR equipment for denitrifying flue gas.
Background technology
Traditional equipment for denitrifying flue gas as shown in Figure 5, SCR reactor 3 tops connect the flue gas access tube 8 that boiler 10 is drawn, be provided with static mixer 2 in this flue gas access tube 8, these static mixer 2 fronts are provided with ammonia-spraying grid 1, described SCR reactor 3 bottoms are connected with electrostatic precipitator 5 by flue gas efferent duct 9, flue gas efferent duct 9 between electrostatic precipitator 5 and SCR reactor 3 is provided with air preheater 4, the described air input pipe 13 that enters boiler 10 links to each other with boiler 10 through described air preheater 4 by blower fan 11, and the nozzle of described ammonia-spraying grid 1 is towards SCR reactor 3.In the flue gas input pipe 8 between ammonia-spraying grid 1 and boiler 10; Be respectively equipped with baffle plate 12 in the flue gas efferent duct 9 between SCR reactor 3 and the air preheater 4.Being provided with pipeline in addition between boiler 10 and flue gas efferent duct 9 front ends communicates, also be provided with baffle plate 12 in this pipeline, as the SCR bypass, the nozzle of described ammonia-spraying grid 1 is towards identical with the flue gas direction, in the SCR reactor, the NOx in the flue gas is reduced into N with the ammonia that sprays in the flue gas in catalyst surface generation SCR (SCR) reaction
2And H
2O.Flue gas after being purified enters air preheater 4, electrostatic precipitator 5 and FGD desulfurizer more successively after smoke stack emission.
Because in the SCR reactor, exhaust gas dust concentration is higher, and contained flying dust easily causes catalyst abrasion and poisoning, shortens catalyst service life, increases operating cost; Bulky grain flying dust wherein (particularly puffed rice flying dust) causes catalyst to stop up especially easily, in order to reduce the probability that catalyst stops up, generally needs to select the large aperture catalyst, thereby can cause catalyst volume bigger, has increased SCR project investment cost; Must blowing out if catalyst just stops up, lose hugely, stop up the risk that causes blowing out for fear of catalyst, so in system's design, often need to be provided with SCR bypass 6, the cost of investment of the further increase of meeting SCR denitration like this; Higher owing to flying dust concentration in addition, the NH that denitration reaction leaks
3With SO
3And H
2O can generate ammonium hydrogen sulfate materials such as (ABS), and this material has bigger stickiness, can make dust at the air preheater surface aggregation, causes the contamination and the corrosion of air preheater, causes the obstruction of air preheater 4, so must improve the cleaning frequency of air preheater 4.
In addition, in conventional apparatus,, can cause denitrating catalyst heavy metal enrichment in electrostatic precipitator 5 dust of wearing and tearing, make that the heavy metal concentration of electrostatic precipitator flying dust is higher, influence the application of flying ash in electric power plant owing to the reasons such as wearing and tearing of denitrating catalyst.
Present trend is cancellation SCR bypass 6, and this can further increase flying dust undoubtedly and stop up the danger that causes shutdown, and traditional SCR device will be subjected to stern challenge more.
The utility model content
Technical problem to be solved in the utility model is to provide a kind of preposed whirlwind beforehand dust removal SCR equipment for denitrifying flue gas that can also reduce SCR reactor catalyst volume size and electrostatic precipitator size in cancellation SCR bypass.
The technical solution of the utility model is as follows: a kind of preposed whirlwind beforehand dust removal SCR equipment for denitrifying flue gas, comprise ammonia-spraying grid, the flue gas static mixer, the SCR reactor, air preheater, electrostatic precipitator, described SCR reactor one end connects the flue gas access tube that boiler is drawn, be provided with static mixer in this flue gas access tube, this static mixer front is provided with ammonia-spraying grid, the described SCR reactor other end is connected with deduster by the flue gas efferent duct, between electrostatic precipitator and SCR reactor, be provided with air preheater, its key is: the flue gas access tube of described ammonia-spraying grid upstream is provided with High-temperature resistant cyclone separator, and the nozzle of described ammonia-spraying grid is towards boiler.Increase a high temperature cyclone separator, bulky grain flying dust (especially puffed rice flying dust) is removed, can reduce of the obstruction of big particle diameter flying dust catalyst; Owing to removed the bulky grain flying dust, can select the less SCR denitrating catalyst in aperture simultaneously, reduce required catalyst volume; Because fly ash content descends significantly,, make the denitrating catalyst life-span prolong significantly so the wearing and tearing of catalyst and the probability of poisoning are reduced; Because the probability that flying dust causes catalyst to stop up is very low, there is no need to be provided with the SCR bypass again, can reduce the cost cost of SCR engineering, this also matches with the trend of present cancellation SCR bypass.In addition, because the significantly reduction of flying dust concentration, even the generation of ammonium hydrogen sulfate is arranged, because the minimizing of dust concentration, the probability that causes air preheater to stop up also declines to a great extent, and can prolong the cleaning frequency of air preheater.
Another advantage that the cyclone separator pre-dedusting device is set is because the flying dust great majority are cyclone separators before the SCR reactor removes, this part flying dust is not subjected to the influence of catalyst abrasion, can not make content wherein increase, and reduce owing to the dust concentration by catalyst in the flying dust of the electrostatic precipitator at rear portion, the wearing and tearing of catalyst descend, can make that also the content of beary metal in the dust descends to some extent, so the utility model can avoid the electrostatic precipitator content of beary metal that traditional SCR device causes to increase, have a strong impact on the situation (flying dust can be used as the raw material of producing cement etc.) of the application and the sale of flying dust.
The direction of ammonia-spraying grid ejection ammonia is opposite with the direction of flow of flue gas, and flue gas is more even with mixing of ammonia, and is more abundant with the catalyst reaction in the SCR reactor.
Because cyclone separator is between boiler and air preheater, flue-gas temperature is higher, dust concentration is higher, so the cyclone separator that adopts needs very strong heat resistant and wear resistant and decreases performance, what the present invention adopted is the heat resistant and wear resistant cyclone separator, the sidewall of the smoke inlet of described High-temperature resistant cyclone separator, straight tube, conically shaped, little ash bucket is an ordinary carbon steel, and be fixed with insulation material with bar for line in this side wall inner surfaces, be provided with the thin layer end plate in this bar for line outer end, outside end plate, be fixed with hexsteel, fill the heat-resistant, wear-resistant material between net; The described side wall inner surfaces welding hexsteel that inserts tube and ash discharging cylinder is filled the heat-resistant, wear-resistant material between net.Also be provided with the flue gas flow equalizing device of forming by staggered bank of tubes in the flue gas access tube between described boiler and ammonia-spraying grid.
Suitable cyclone separator is arranged in
Between air preheater and the economizer, under the flue-gas temperature condition with higher.Can reduce the wearing and tearing and the heat radiation of high temperature cyclone system, high temperature cyclone separator has the interface that contacts to adopt the heat resistant and wear resistant material as liner with dust with extraneous, has the parts that contact to adopt wearing piece inner with dust.In the cyclone separator bottom little ash bucket and ash-valve are set, the controlling level that ash-valve is looked ash bucket opens and closes automatically.The flying dust of collecting is directly given the user and is used.
Owing between economizer and SCR reactor, increased cyclone separator, make the flue gas level of disruption be greatly improved, in order to improve ammonia dispersed uniform degree in flue gas, the present invention is equipped with the flue gas flow equalizing device in the ammonia-spraying grid provided upstream, makes flue gas evenly better mix towards the ammonia of same direction with the ammonia-spraying grid ejection.This flue gas flow equalizing device adopts wrong row's bundle of parallel tubes, has advantages such as simple in structure, that current-sharing is effective and pressure drop is low.
Owing to removed most of flying dust through cyclone separator, when even the nozzle direction of spraying the ammonia nozzle is opposite with the flow of flue gas direction, can not stop up yet, if the direction of ammonia-spraying grid ejection ammonia is opposite with the direction of flow of flue gas, flue gas and ammonia to mix meeting more even, more abundant with the catalyst reaction in the SCR reactor, so the nozzle of the ammonia-spraying grid of denitrating system of the present invention is opposite with the flue gas direction.
The layout of the SCR system behind the cyclone separator is arranged similar substantially to traditional SCR reaction system, deflector, ammonia injection grid, static mixer, flying dust rectifier, catalyst, soot blower etc. need be set, behind the SCR reactor, pass through air preheater, electrostatic precipitator, FGD desulfurizer, air-introduced machine successively after smoke stack emission.
In the design of SCR reactor, because the reduction of fly ash content, can adopt the small-bore catalyst, because the small-bore specific surface area of catalyst is bigger, can be so that catalyst volume descends to some extent, can adopt less SCR reactor, SCR reactor load is less, and the requirement of supporting is reduced than traditional SCR reactor.In the design of inner part, because the stirring to flue gas of cyclone separator needs carefully to adjust by CFD simulation and physical flow model in the design of static mixer; Because the flying dust blocking probability is very low, the cycle that can not establish soot blower or will blow ash is provided with longlyer.The design of other inner parts (ammonia sprays grid, deflector and flying dust rectifier) is identical with traditional SCR reactor.
The air preheater of SCR reactor downstream is because fly ash content is lower, and the probability that the caking property flying dust stops up declines to a great extent, and the cycle that air preheater cleans significantly prolongs.
Electrostatic precipitator is owing to there has been the pre-dedusting of cyclone separator, and the load of dust descends, and can reduce the size of electrostatic precipitator and the number of electric field, reduces the investment of power plant to electrostatic precipitator.Owing to the decline of flying dust, can improve the quality of the flying dust of electrostatic precipitator simultaneously to catalyst abrasion.
The device of other that power-plant flue gas is handled is identical with the layout of the smoke processing system of traditional SCR process system as the design of FGD desulfurizer, air-introduced machine and chimney.
Also be provided with the flue gas flow equalizing device of forming by staggered bank of tubes 7 in the flue gas access tube between described boiler and ammonia-spraying grid.The flue gas of the isolated confusion of cyclone separator is passed through mixing tube, make flue gas evenly better mix towards the ammonia of same direction with the ammonia-spraying grid ejection.
Beneficial effect: the utility model can reduce the obstruction of big particle diameter flying dust to catalyst; Can select the less SCR denitrating catalyst in aperture for use, reduce required catalyst volume and SCR reactor, SCR reactor load is less, and the requirement of supporting is reduced than traditional SCR reactor, remove the SCR bypass simultaneously, can reduce the cost cost of SCR engineering greatly; The denitrating catalyst life-span prolongs significantly; The probability that air preheater stops up also declines to a great extent, and prolongs the cleaning frequency of air preheater, and the cycle that can not establish soot blower or will blow ash is provided with longlyer; Because the reduction of the flying dust of electrostatic precipitator load can reduce electric field level and quantity, reduces the investment to electrostatic precipitator.In addition, can also improve the quality and the utilization rate of electrostatic precipitator flying dust.
Description of drawings
Fig. 1 is a structural representation of the present utility model;
Fig. 2 is the structural representation of High-temperature resistant cyclone separator among Fig. 1;
Fig. 3 is smoke inlet among Fig. 2, straight tube, the little ash bucket sidewall of conically shaped stratiform structural representation;
Fig. 4 is middle tube and the ash discharging cylinder sidewall stratiform structural representation of inserting among Fig. 2;
Fig. 5 is the structural representation before improving.
The specific embodiment
The utility model is described in further detail below in conjunction with drawings and Examples:
As shown in Figure 1, the utility model preposed whirlwind beforehand dust removal SCR equipment for denitrifying flue gas, form by ammonia-spraying grid 1, flue gas static mixer 2, SCR reactor 3, air preheater 4, electrostatic precipitator 5 etc., described SCR reactor 3 tops connect the flue gas access tube 8 that boiler 10 is drawn, be provided with static mixer 2 in this flue gas access tube 8, these static mixer 2 fronts are provided with ammonia-spraying grid 1, described SCR reactor 3 bottoms are connected with electrostatic precipitator 5 by flue gas efferent duct 9, at electrostatic precipitator 5 and SCR reactor 3
Between be provided with air preheater 4, the flue gas access tube 8 of wherein said ammonia-spraying grid 1 upstream is provided with High-temperature resistant cyclone separator 6, the nozzle of described ammonia-spraying grid 1 is towards boiler 10.Also be provided with the flue gas flow equalizing device of forming by staggered bank of tubes 7 in the flue gas access tube 8 between described boiler 10 and ammonia-spraying grid 1.
As Fig. 2, Fig. 3, the described High-temperature resistant cyclone separator 6 of Fig. 4 comprises straight tube 6-1, aiutage 6-2, conically shaped 6-3, ash discharging cylinder 6-4 and end socket 6-12, described straight tube 6-1 top and bottom connect aiutage 6-2 and conically shaped 6-3 respectively, this aiutage 6-2 upper end nozzle is covered by end socket 6-12, this conically shaped 6-3 lower end communicates with ash discharging cylinder 6-4 through little ash bucket 6-11, be provided with the taper that communicates with aiutage 6-2 in the described straight tube 6-1 and insert tube 6-5, volute smoke inlet 6-14 and the tangential exhanst gas outlet 6-15 that extends are arranged respectively on described straight tube 6-1 and aiutage 6-2, described smoke inlet 6-14, straight tube 6-1, conically shaped 6-3, the sidewall 6-13 of little ash bucket 6-11 is an ordinary carbon steel, be fixed with insulation material 6-7 at this sidewall 6-13 inner surface with bar for line 6-6, be provided with thin layer end plate 6-8 in this bar for line 6-6 outer end, outside end plate 6-8, be fixed with hexsteel 6-9, fill heat-resistant, wear-resistant material 6-10 between net; The described ordinary carbon steel sidewall 6-13 inner surface welding hexsteel 6-9 that inserts tube 6-2 and ash discharging cylinder 6-4 fills heat-resistant, wear-resistant material 6-10 between net.
Operation principle: flue gas picks out from boiler 10, enters High-temperature resistant cyclone separator 6, and this High-temperature resistant cyclone separator 6 carries out separating of gas and solid particle dust with flue gas, and the solid particle dust gathers little ash bucket 6-11 downwards; Gas picks out from High-temperature resistant cyclone separator 6 tops, in flue gas access tube 8, in the process flue gas access tube 8 the flue gas flow equalizing device of being made up of staggered bank of tubes 7 is housed, evenly reverse ammonia with ammonia-spraying grid 1 ejection mixes, through static mixer 2 flue gas is evenly mixed with ammonia again, enter SCR reactor 3 and catalyst reaction, reacted flue gas carries out heat exchange through air preheater 4 and the air that enters boiler 10, the flue gas that reduces temperature enters electrostatic precipitator 5 dedustings again, and last desulfurization is discharged.
Claims (2)
1, a kind of preposed whirlwind beforehand dust removal SCR equipment for denitrifying flue gas, comprise ammonia-spraying grid (1), static mixer (2), SCR reactor (3), air preheater (4), electrostatic precipitator (5), described SCR reactor (3) top connects the flue gas access tube (8) that boiler (10) is drawn, be provided with static mixer (2) in this flue gas access tube (8), this static mixer (2) front is provided with ammonia-spraying grid (1), described SCR reactor (3) bottom is connected with electrostatic precipitator (5) by flue gas efferent duct (9), on the flue gas efferent duct (9) between electrostatic precipitator (5) and the SCR reactor (3), be provided with air preheater (4), the described air input pipe (13) that enters boiler (10) links to each other with boiler (10) through described air preheater (4) by blower fan (11), it is characterized in that: the flue gas access tube (8) of described ammonia-spraying grid (1) front is provided with High-temperature resistant cyclone separator (6), the nozzle of described ammonia-spraying grid (1) is towards boiler (10), described High-temperature resistant cyclone separator (6) comprises straight tube (6-1), aiutage (6-2), conically shaped (6-3), ash discharging cylinder (6-4) and end socket (6-12), described straight tube (6-1) top and bottom connect aiutage (6-2) and conically shaped (6-3) respectively, this aiutage (6-2) upper end nozzle is covered by end socket (6-12), this conically shaped (6-3) lower end communicates with ash discharging cylinder (6-4) through little ash bucket (6-11), be provided with the taper that communicates with aiutage (6-2) in the described straight tube (6-1) and insert tube (6-5), volute smoke inlet (6-14) and the tangential exhanst gas outlet (6-15) that extends are arranged respectively on described straight tube (6-1) and aiutage (6-2), described smoke inlet (6-14), straight tube (6-1), conically shaped (6-3), the sidewall (6-13) of little ash bucket (6-11) is an ordinary carbon steel, be fixed with insulation material (6-7) at this sidewall (6-13) inner surface with bar for line (6-6), be provided with thin layer end plate (6-8) in this bar for line (6-6) outer end, outside end plate (6-8), be fixed with hexsteel (6-9), fill heat-resistant, wear-resistant material (6-10) between net; Described ordinary carbon steel sidewall (6-13) the inner surface welding hexsteel (6-9) that inserts tube (6-2) and ash discharging cylinder (6-4) is filled heat-resistant, wear-resistant material (6-10) between net.
2, according to the described preposed whirlwind beforehand dust removal SCR equipment for denitrifying flue gas of claim 1, it is characterized in that: the flue gas flow equalizing device of being made up of staggered bank of tubes (7) is housed in the flue gas access tube (8) between described boiler (10) and ammonia-spraying grid (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201878150U CN201108808Y (en) | 2007-09-27 | 2007-09-27 | Prepositioned cyclone pre-dedusting SCR smoke-gas denitration device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201878150U CN201108808Y (en) | 2007-09-27 | 2007-09-27 | Prepositioned cyclone pre-dedusting SCR smoke-gas denitration device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201108808Y true CN201108808Y (en) | 2008-09-03 |
Family
ID=39893324
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007201878150U Expired - Lifetime CN201108808Y (en) | 2007-09-27 | 2007-09-27 | Prepositioned cyclone pre-dedusting SCR smoke-gas denitration device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201108808Y (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102068904A (en) * | 2010-12-10 | 2011-05-25 | 中电投远达环保工程有限公司 | SCR flue gas denitration technology and device by urea directly-spraying method |
| CN103962003A (en) * | 2013-01-25 | 2014-08-06 | 日立造船株式会社 | Method for removing ammonium salt of sulfuric acid of exhaust gas processing device, and exhaust gas processing device |
| CN106925108A (en) * | 2017-05-04 | 2017-07-07 | 无锡市东方环境工程设计研究所有限公司 | A kind of waste heat of coke-oven flue gas and desulphurization denitration dust pelletizing system |
| CN107626202A (en) * | 2017-11-06 | 2018-01-26 | 中国科学院过程工程研究所 | A kind of SCR denitration device, the method and its application of aluminium oxide calcining flue gas |
-
2007
- 2007-09-27 CN CNU2007201878150U patent/CN201108808Y/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102068904A (en) * | 2010-12-10 | 2011-05-25 | 中电投远达环保工程有限公司 | SCR flue gas denitration technology and device by urea directly-spraying method |
| CN102068904B (en) * | 2010-12-10 | 2013-10-02 | 中电投远达环保工程有限公司 | SCR flue gas denitration technology and device by urea directly-spraying method |
| CN103962003A (en) * | 2013-01-25 | 2014-08-06 | 日立造船株式会社 | Method for removing ammonium salt of sulfuric acid of exhaust gas processing device, and exhaust gas processing device |
| CN103962003B (en) * | 2013-01-25 | 2017-11-03 | 日立造船株式会社 | The ammonium salt of the sulfuric acid of waste gas treatment equipment removes method and waste gas treatment equipment |
| CN106925108A (en) * | 2017-05-04 | 2017-07-07 | 无锡市东方环境工程设计研究所有限公司 | A kind of waste heat of coke-oven flue gas and desulphurization denitration dust pelletizing system |
| CN107626202A (en) * | 2017-11-06 | 2018-01-26 | 中国科学院过程工程研究所 | A kind of SCR denitration device, the method and its application of aluminium oxide calcining flue gas |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20080903 |