CN103170229A - An integrated desulfurization and denitrification system for industrial kilns - Google Patents
An integrated desulfurization and denitrification system for industrial kilns Download PDFInfo
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- CN103170229A CN103170229A CN2013100655653A CN201310065565A CN103170229A CN 103170229 A CN103170229 A CN 103170229A CN 2013100655653 A CN2013100655653 A CN 2013100655653A CN 201310065565 A CN201310065565 A CN 201310065565A CN 103170229 A CN103170229 A CN 103170229A
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- flue gas
- denitrification
- denitration reaction
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 17
- 230000023556 desulfurization Effects 0.000 title claims abstract description 16
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000003546 flue gas Substances 0.000 claims abstract description 40
- 230000003647 oxidation Effects 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 34
- 239000007921 spray Substances 0.000 claims abstract description 23
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 20
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 20
- 238000002360 preparation method Methods 0.000 claims abstract description 13
- 239000000428 dust Substances 0.000 claims abstract description 10
- 239000002918 waste heat Substances 0.000 claims abstract description 10
- 238000003860 storage Methods 0.000 claims abstract description 8
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000000889 atomisation Methods 0.000 claims abstract description 5
- 238000006386 neutralization reaction Methods 0.000 claims abstract 11
- 238000000926 separation method Methods 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims 1
- 230000008676 import Effects 0.000 abstract description 23
- 238000000034 method Methods 0.000 description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 12
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 11
- 238000005507 spraying Methods 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 239000004568 cement Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 229910002089 NOx Inorganic materials 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 230000001473 noxious effect Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea group Chemical group NC(=O)N XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Treating Waste Gases (AREA)
Abstract
A desulfurization and denitrification integrated system for an industrial kiln mainly comprises: be equipped with the spray gun that SNCR denitration reductant sprayed atomization device on the industrial kiln, this spray gun links to each other with SNCR denitration reductant preparation facilities, and this SNCR denitration reductant preparation facilities links to each other with the reductant import on the oxidation neutralization denitration reaction tower, and this oxidation neutralization denitration reaction tower import links to each other with the dust remover export. The inlet of the dust remover is connected with a waste heat flue gas outlet of an industrial kiln, the outlet of the oxidation neutralization denitration reaction tower is connected with a chimney, the lower part of the oxidation neutralization denitration reaction tower is provided with an ammonium salt pool, the bottom of the oxidation neutralization denitration reaction tower is provided with an ammonium salt outlet, the oxidation neutralization denitration reaction tower is also provided with an ozone inlet which is connected with the outlet of an ozone generating device, and the inlet of the ozone generating device is connected with the outlet of a liquid oxygen storage tank. The system is optimized, so that a simple, efficient and environment-friendly desulfurization and denitrification integrated system is realized, and the investment and the operation cost are saved.
Description
Technical field
The present invention relates to a kind of Industrial Stoves desulfurization and denitrification integral system.
Background technology
The fuel such as coal are all the main consume fuel of Industrial Stoves all the time, and SO in coal-fired flue-gas
2, NO
XThe primary pollution source of atmosphere.In recent years, and along with carrying out of country " 12 " planning and going deep into of environmental protection work, nitrogen oxide is listed in the binding indicator system, requires total emission volumn to cut down 10%, and flue gas desulfurization and denitrification has also entered the important schedule that atmosphere is administered.Present most widely used denitrating flue gas skill is SCR technology and SNCR technology, and SCR technology denitration efficiency can reach more than 95%, but because investment is large, system complex, the reasons such as operating cost height, and inapplicable and Industrial Stoves.Although and that the SNCR denitration technology is invested is low, operating cost is few, and system is simple, and the scope of application is wide, and its denitration efficiency is very low, can not satisfy the discharge standard that country formulates.Have at present patent with SCR and SNCR denitration technology in conjunction with denitration, in this technology, still there are some drawbacks in the SCR denitration technology, because be applied in the industrial furnace smoke denitration, contain alkaline matter in flue gas, cause catalyst poisoning, reaction efficiency reduces, and needs frequently more catalyst changeout, the price of catalyst is very high, has greatly increased operating cost.SCR ammonia oxidation reaction tower inside a lot of tower trays that distributing, be covered with catalyst on tower tray in addition, causes flue gas resistance to increase, and kiln tail blower fan power consumption strengthens.So the gas denitrifying technology that non-secondary pollution, resource consumption are few, operating cost is low that research and development are fit to China's national situation is of great significance the NOX pollution problem tool that solves China.
China national Department of Intellectual Property disclosed that a kind of to be called in " a kind of cement kiln flue-gas denitration process and denitrification apparatus " publication number be 102512925A on June 27th, 2012, its desulfuration efficiency is high, but be applied on the cement kiln tail denitrating flue gas, contain alkaline matter in kiln exit gas, cause catalyst poisoning, reaction efficiency reduces, and needs frequently more catalyst changeout, the price of catalyst is very high, has greatly increased operating cost.
" a kind of SNCR denitrating system " publication number 102658022A that China national Department of Intellectual Property announces.Its system exists the escape of ammonia to increase, and the NOX percent reduction is reduced.NH
3Be high volatile volatile and noxious material, the escape of ammonia can cause new environmental pollution.
Summary of the invention
The object of the present invention is to provide a kind of without the escaping of ammonia and can improve a kind of Industrial Stoves desulfurization and denitrification integral system of Industrial Stoves production material quality.The present invention is mainly: with SNCR(SNCR reaction) organically combine with the denitration method in denitration method and oxidation.
To achieve these goals, the present invention adopts following technical scheme:
its Industrial Stoves are provided with the spray gun of SNCR denitrification reducing agent spraying atomizing device, this spray gun is connected with the reducing agent preparation facilities of SNCR denitration, this reducing agent preparation facilities also with in oxidation is connected with an import on the denitration reaction tower, also be connected with the deduster outlet with the import of denitration reaction tower flue gas in this oxidation, this deduster import can directly be connected with the waste heat flue gas outlet of Industrial Stoves, also can be connected with the waste heat flue gas outlet of Industrial Stoves by waste heat boiler, in described oxidation, outlet is connected with chimney with the denitration reaction tower flue gas, in this oxidation and denitration reaction tower bottom is provided with the ammonium salt pond, its bottom is provided with the ammonium salt outlet, this ammonium salt outlet can be connected with the ammonium salt liquid-solid separation device.Also be provided with the ozone import in above-mentioned oxidation He on the denitration reaction tower, it is connected with the ozone generating-device outlet, and this ozone generating-device import is connected with the outlet of liquid oxygen storage tank.The spray gun of above-mentioned SNCR denitrification reducing agent spraying atomizing device is evenly arranged along the vertical cross-section surrounding that flue gas in kiln passes through, this spray gun can flue gas passes through in kiln a vertical cross-section arrange, also can arrange at a plurality of vertical cross-sections, spray gun quantity is n, 1≤n≤20.Above-mentioned reducing agent is urea or ammoniacal liquor.
The course of work of the present invention is roughly as follows:
High-temperature flue gas is discharged from the afterbody of Industrial Stoves, the a large amount of nitrogen oxide and the sulfur dioxide that wherein burn and produce, at first adopt SNCR denitration method, when 850 ~ 1250 ℃ of industrial furnace smoke temperature ranges, spray in right amount by air-atomized reducing agent, make that in flue gas, a part of NOx is reduced to harmless N
2And H
2O is deviate from.the NOx that does not remove and remaining reducing agent are along with flue gas enters the kiln afterbody, at the flue gas afterbody, waste heat boiler is set and carries out exchange heat, flue-gas temperature is down to 120 ℃ of left and right and is entered deduster, adopt in oxidation between deduster and chimney and carry out desulfurization and denitration with the denitration method, namely allow the high concentration oxygen in liquid oxygen storage tank produce ozone through ozone generating-device, be ejected in oxidation with in the denitration reaction tower nitric oxide Quick Oxidation in flue gas is become nitrogen dioxide, simultaneously the sulfur dioxide Quick Oxidation in flue gas is become sulfur trioxide, the SNCR denitrification reducing agent be ejected in oxidation through the jet atomization device simultaneously and the denitration reaction tower in, so gaseous ammonia, the nitrogen oxide of vaporous water and gaseous state and oxysulfide be the synthetic ammonium salt of reaction rapidly, ammonium salt and oarse-grained dust granules are deposited in the ammonium salt pond by the crystallization pump and are pumped into during the ammonium salt liquid-solid separation device separates, and final products are nitrogenous fertilizer, clean flue gas enters chimney through air-introduced machine.
The present invention compared with prior art has following advantage:
1, due to in the oxidation of SNCR denitration method and the denitration method organically combine, at first take full advantage of the hot conditions in Industrial Stoves, spray into appropriate reducing agent at Industrial Stoves, remove a part of NOx in flue gas, reduce the live load of ammonia oxidation, make in follow-up oxidation to reduce with denitration method reaction tower scale, especially reduce the consumption of oxidant, reduced operating cost, its denitrification efficiency all can reach more than 90%;
2, efficiency of dust collection can reach more than 90%, and kiln exit gas pm emission dust concentration is much smaller than 50mg/Nm3.Industry kiln stove tail dust pelletizing system adopts electric precipitation substantially, the up-to-date regulation flue gas particle of national standard dust concentration 50mg/Nm3, and electric precipitation can not meet requirement, must change a bag dedusting into, has greatly increased power consumption and operation expense but change bag dedusting into.As adopting the present invention technology, electric precipitation can meet the demands, and does not need to carry out kiln tail dedusting electricity and changes the bag transformation.Adopt this invention technology can obviously reduce equipment investment by calculating.
3, the byproduct of desulphurization denitration acquisition is that ammonium nitrate and ammonium sulfate can be used as chemical fertilizer, can take full advantage of the reducing agent that consumes, and saves operating cost.
Description of drawings
Fig. 1 is the inventive example 1 flow process simplified schematic diagram.
Fig. 2 is that the spray gun of SNCR denitrification reducing agent spraying atomizing device in the inventive example 1 is arranged simplified schematic diagram.
Fig. 3 is the inventive example 2 flow process simplified schematic diagram.
Fig. 4 is the inventive example 3 flow process simplified schematic diagram.
Attached number in the figure explanation
In 1-oxidation and the denitration reaction tower, 2-ammonium salt pond, 3-ammonium salt liquid-solid separation device, 4-ozone generating-device, the spray gun of 5-SNCR denitrification reducing agent spraying atomizing device, 6-liquid oxygen storage tank, 7-dore furnace, 8-rotary kiln, 9-rotary kiln end, 10-kiln tail Pyatyi preheater, 11-waste heat boiler, 12-deduster, 13-chimney, 14-SNCR denitrification reducing agent preparation facilities, 15-glass furnace, 16-ceramic kiln.
The specific embodiment
Below in conjunction with drawings and Examples, the present invention is described in further detail:
In the flow process simplified schematic diagram of shown in Figure 1 cement kiln desulfurization and denitrification integral system, the cement rotary kiln tail is established dore furnace.This dore furnace is connected with the thermal medium entrance of cement slurry preheater, this preheater is plural serial stage, afterbody preheater hot media outlet is connected with the deduster import, between is established waste heat boiler, be connected with denitration method reaction tower gas approach in the outlet of this deduster and oxidation, be connected with chimney with denitration method reaction tower exhanst gas outlet in this oxidation, establish air-introduced machine between the two.In this oxidation and denitration method reaction tower bottom is provided with the ammonium salt pond, its bottom is provided with the ammonium salt outlet, be provided with the reducing agent import with the denitration reaction tower in this oxidation, it is connected with an outlet of SNCR denitrification reducing agent preparation facilities, another outlet of this reducing agent preparation facilities also be located at dore furnace on the spray gun entrance of 6 SNCR denitrification reducing agent spraying atomizing devices be connected.The layout sketch of the spray gun of the SNCR denitrification reducing agent spraying atomizing device on dore furnace is seen Fig. 2.Also be provided with the ozone import in above-mentioned oxidation He on the denitration reaction tower, it is connected with the ozone generating-device outlet, and this ozone generating-device import is connected with the outlet of liquid oxygen storage tank.
In the flow process simplified schematic diagram of shown in Figure 3 glass furnace desulfurization and denitrification integral system, the outlet of glass furnace body tail flue gas is connected with the exhaust-heat boiler flue gas import, the exhaust-heat boiler flue gas outlet is connected with the deduster import, in the outlet of this deduster and oxidation, import is connected with the denitration reaction tower flue gas, in this oxidation, outlet is connected with chimney with the denitration reaction tower flue gas, establishes air-introduced machine between the two.In this oxidation and denitration reaction tower bottom is provided with the ammonium salt pond, its its bottom is provided with the ammonium salt outlet, be provided with the reducing agent import with the denitration reaction tower in this oxidation, it is connected with an outlet of SNCR denitrification reducing agent preparation facilities, another outlet of this reducing agent preparation facilities also be located at glass furnace on the spray gun entrance of SNCR denitrification reducing agent spraying atomizing device be connected.Also be provided with the ozone import in oxidation He on the denitration reaction tower, it is connected with the ozone generating-device outlet, and this ozone generating-device import is connected with the outlet of liquid oxygen storage tank.
In the flow process simplified schematic diagram of shown in Figure 4 furnace desulfurization and denitrification integral system, the outlet of furnace body tail flue gas is connected with the exhaust-heat boiler flue gas import, the exhaust-heat boiler flue gas outlet is connected with the deduster import, in the outlet of this deduster and oxidation, import is connected with the denitration reaction tower flue gas, in this oxidation, outlet is connected with chimney with the denitration reaction tower flue gas, establishes air-introduced machine between the two.In this oxidation and denitration reaction tower bottom is provided with the ammonium salt pond, its bottom is provided with the ammonium salt outlet, be provided with the reducing agent import with the denitration reaction tower in oxidation, it is connected with an outlet of reducing agent preparation facilities, another outlet of this reducing agent preparation facilities also be located at ceramic kiln on the spray gun entrance of SNCR denitrification reducing agent spraying atomizing device be connected.Also be provided with the ozone import in oxidation He on the denitration reaction tower, it is connected with the ozone generating-device outlet, and this ozone generating-device import is connected with the outlet of liquid oxygen storage tank.
Claims (5)
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100655653A CN103170229A (en) | 2013-03-01 | 2013-03-01 | An integrated desulfurization and denitrification system for industrial kilns |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100655653A CN103170229A (en) | 2013-03-01 | 2013-03-01 | An integrated desulfurization and denitrification system for industrial kilns |
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| Publication Number | Publication Date |
|---|---|
| CN103170229A true CN103170229A (en) | 2013-06-26 |
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|---|---|---|---|
| CN2013100655653A Pending CN103170229A (en) | 2013-03-01 | 2013-03-01 | An integrated desulfurization and denitrification system for industrial kilns |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103341306A (en) * | 2013-07-24 | 2013-10-09 | 上海交通大学 | Lean ammonia SNCR (Selective Non-Catalytic Reduction) and oxidation absorption combined denitration and demercuration method |
| CN103406006A (en) * | 2013-08-30 | 2013-11-27 | 安徽省元琛环保科技有限公司 | SCR (Selective Catalytic Reduction) denitration device for NOx control of rotary cement kiln |
| CN103977695A (en) * | 2014-06-05 | 2014-08-13 | 株洲三特环保节能股份有限公司 | Method and system for removing nitric oxide from flue gas in cement kiln |
| CN105561754A (en) * | 2016-02-18 | 2016-05-11 | 山东巨亚环保科技股份有限公司 | Boiler denitration device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489129A (en) * | 2011-12-14 | 2012-06-13 | 山东中玻节能环保发展有限公司 | Industrial flue gas purification, desulfurization and denitrification integrated device and working method thereof |
| CN102661667A (en) * | 2012-05-31 | 2012-09-12 | 河南中材环保有限公司 | System and method for denitration, residual heat utilization and dedusting of cement kiln |
| CN202725014U (en) * | 2012-06-26 | 2013-02-13 | 肖开标 | Energy-saving denitration device for cement dry kiln |
| CN203264548U (en) * | 2013-03-01 | 2013-11-06 | 大连易世达新能源发展股份有限公司 | An integrated desulfurization and denitrification system for industrial kilns |
-
2013
- 2013-03-01 CN CN2013100655653A patent/CN103170229A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489129A (en) * | 2011-12-14 | 2012-06-13 | 山东中玻节能环保发展有限公司 | Industrial flue gas purification, desulfurization and denitrification integrated device and working method thereof |
| CN102661667A (en) * | 2012-05-31 | 2012-09-12 | 河南中材环保有限公司 | System and method for denitration, residual heat utilization and dedusting of cement kiln |
| CN202725014U (en) * | 2012-06-26 | 2013-02-13 | 肖开标 | Energy-saving denitration device for cement dry kiln |
| CN203264548U (en) * | 2013-03-01 | 2013-11-06 | 大连易世达新能源发展股份有限公司 | An integrated desulfurization and denitrification system for industrial kilns |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103341306A (en) * | 2013-07-24 | 2013-10-09 | 上海交通大学 | Lean ammonia SNCR (Selective Non-Catalytic Reduction) and oxidation absorption combined denitration and demercuration method |
| CN103341306B (en) * | 2013-07-24 | 2015-12-09 | 上海交通大学 | A kind of method of poor ammonia SNCR reduction and oxidative absorption combined denitration demercuration |
| CN103406006A (en) * | 2013-08-30 | 2013-11-27 | 安徽省元琛环保科技有限公司 | SCR (Selective Catalytic Reduction) denitration device for NOx control of rotary cement kiln |
| CN103977695A (en) * | 2014-06-05 | 2014-08-13 | 株洲三特环保节能股份有限公司 | Method and system for removing nitric oxide from flue gas in cement kiln |
| CN105561754A (en) * | 2016-02-18 | 2016-05-11 | 山东巨亚环保科技股份有限公司 | Boiler denitration device |
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Application publication date: 20130626 |