CN101773770A - Method for removing waste gas pollutants of NOX and SO2 simultaneously - Google Patents

Method for removing waste gas pollutants of NOX and SO2 simultaneously Download PDF

Info

Publication number
CN101773770A
CN101773770A CN200910198957A CN200910198957A CN101773770A CN 101773770 A CN101773770 A CN 101773770A CN 200910198957 A CN200910198957 A CN 200910198957A CN 200910198957 A CN200910198957 A CN 200910198957A CN 101773770 A CN101773770 A CN 101773770A
Authority
CN
China
Prior art keywords
concentration
liquid
nta
waste gas
concentration range
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN200910198957A
Other languages
Chinese (zh)
Inventor
龙湘犁
董立
袁渭康
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
East China University of Science and Technology
Original Assignee
East China University of Science and Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by East China University of Science and Technology filed Critical East China University of Science and Technology
Priority to CN200910198957A priority Critical patent/CN101773770A/en
Publication of CN101773770A publication Critical patent/CN101773770A/en
Pending legal-status Critical Current

Links

Classifications

    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The invention relates to a method for controlling waste gas pollutants of NOX and SO2 simultaneously, in particular to a method for removing NO and SO2 in flue gas of a power plant simultaneously. The method uses absorption liquid consisting of Fe(II)-NTA and a desulfurizing agent to absorb NO and SO2 simultaneously, Fe(II)-NTA changes the NO from gas phase into liquid phase, the NO is reduced into harmless nitrogen in water solution under the catalysis of active carbon, simultaneously the Fe(III)-NTA produced by oxidization is reduced and regenerated into Fe(II)-NTA under the catalysis of active carbon, SO2 is dissolved in the absorption liquid and the produced sulfite radical is a reducing agent, thus realizing recycling of an absorbing agent of NO, also realizing that the absorption and reduction of NO and absorption and oxidization of SO2 are carried out simultaneously, and greatly reducing the control cost of nitric oxide and sulfur dioxide.

Description

A kind of NO that removes simultaneously xAnd SO 2The method of exhaust emission
Technical field
The present invention relates to a kind of NO that administers simultaneously XAnd SO 2The method of exhaust emission especially relates to NO and SO in the power-plant flue gas 2The time removal methods.
Background technology
China is to be the country of main energy sources with the coal.The discharging meeting of coal fired power generation produces bigger pollution to environment, has become a principal element of restriction power industry sustainable development.And the SO that coal combustion produces 2(1000-4000ppm) and NOx (300-800ppm), be that industrial waste gas pollutes the main root of (acid rain harm).And nitrogen oxide also can form photochemical pollution, produces greenhouse effects, damages the ozone layer, human body is had the intoxicating effect.The NO that was discharged in 2004 is 1,600 ten thousand tons, if do not take effective pollution control measures, the year two thousand twenty China nitrogen oxide emission will reach about 2,900 ten thousand tons, SO 2Discharge capacity will reach more than 4,350 ten thousand tons.In recent years, the air nitrous oxides concentration of some megapolis of China exceeds standard, and the environmental carrying capacity of nitrogen oxide is in saturation state substantially, some local even generation photochemical fog phenomenons.Along with China to SO 2The increase of the reinforcement of emission control and automobile quantity, NO xTo the contribution of the acid rain SO that will progressively forereach 2, in China's acid precipitation, nitrate anion and sulfate ion concentration ratio develop into 0.20: 1 in 2004, control SO by 0.15: 1 in 2000 2With the discharging of NO be extremely urgent.
NO xBe the general designation of nitrogen oxide, comprise N 2O, NO, N 2O 3, NO 2, N 2O 5Deng, the NO in the atmosphere more than 95% XBe NO, NO 2Only account for seldom amount, the NO in the flue gas XAlso NO more than 90%.Because the low concentration of NO chemical reactivity is low, it removes also just quite difficult technically.Developed multiple method of denitration through years of researches.What at present, industrial employing was more is catalytic reduction method.As patent US Pantent 4,221,768, Swedish Patent 8404840-4, USPantent 4,101,238, US Pantent 4,048,112 disclosed methods.
In the existing flue gas desulfur device in countries in the world, wet desulfurizing process accounts for 85%.Because extensively the ripe sulfur method of utilization is a wet method at present, therefore existing wet desulfurizing process is improved, desulphurization denitration is carried out simultaneously, have powerful competitiveness economically, also be the focus of desulphurization denitration Study on Technology exploitation simultaneously.The solubility of NO in the aqueous solution is very low, thus the wet method of NO remove have only two by way of, one be with solution in the complex salt complexing, NO is removed from waste gas; Another adopts the liquid phase oxidation agent to carry out oxidation exactly, and NO is oxidized to NO soluble in water 2
Japan Patent P1659565j (1976), P181759c (1976), P63100918, A2 (1988) remove NO when proposing XAnd SO 2Method adopt chloric acid, potassium permanganate, hydrogen peroxide, ozone etc. to make oxidant, the NO liquid phase oxidation is become NO soluble in water 2, but former thereby fail to promote and come because of cost height etc.The yellow phosphorus method that California, USA university Berkeley laboratory proposes (is seen document Nature, 1990,343 (11): 151-153), can remove the NO in the flue gas simultaneously XAnd SO 2, this method will consume a large amount of phosphor resources, and its toxicity is big, and operation is had relatively high expectations.
Adopt Fe (II)-EDTA (EDTA represents disodium ethylene diamine tetraacetate) to remove that NO has the high advantage of removal efficiency in the waste gas, (document sees reference: Bull.of the Chem.Soc.ofJpn. but because Fe (II)-EDTA easily is oxidized to Fe (III)-EDTA, 1968,41:2234-2239.Ind.Eng.Chem.Res., 1987,26:1468-1472.Inorg.Chem., 1990,29:1705-1711.Ind.Eng.Chem.Res., 1993,32:2580-2594.), and Fe (III)-EDTA can not complexing NO, and absorption efficiency is descended rapidly.People propose to regenerate with the biological reducing method, and (Fe (II) sees reference document: United States PatentUS5891408.Biotechnol.Prog., 2003,19:1323-1328.J Chem Technol Biotechnol, 2004,79:835-841.Biotechnology and Bio engineering, 2005,90:433-441.Environ Sci Technol, 2005,39:2616-2623.J of Chem Technol and Biotechnol, 2006,81:306-311.), but this method also is in the exploratory stage at present, also has many problems to need to solve.
Nitrilotriacetic acid/nitrilotriacetic acid/nitrogen base triacetic acid (NTA, English name: Nitrilotriacetic acid, molecular formula: N (CH 2COOH) 3, molecular weight: 191.14) with ferrous complex compound Fe (II)-NTA can with the NO complexing, NO polluted from waste gas, remove (Ind.Eng.Chem.Res., 1990,29:10-14) and EDTA compare, the nitrilotriacetic acid low price, molecular weight is little, has superiority economically.But with Fe (II)-EDTA is the same, Fe (II)-NTA also can be oxidized to Fe (III)-NTA, and Fe (III)-NTA can not complexing NO, and the removal efficiency of NO is descended.
Summary of the invention
The objective of the invention is to propose a kind of NO and SO of removing simultaneously 2The method of exhaust emission.
The technical issues that need to address of the present invention provide and a kind ofly remove NO and SO in the waste gas with Fe (II)-NTA solution 2Method, make NO and SO 2Absorption carry out simultaneously, and NO is reduced to harmless nitrogen, to overcome the above-mentioned defective that prior art exists, reduce the treatment cost of wet desulphurization denitration, improve the market competitiveness of wet desulphurization denitration technology.
Design of the present invention is such:
Utilization contains the absorption liquid while absorption of N O and the SO of Fe (II)-NTA and desulfurizing agent composition 2, Fe (II)-NTA changes NO over to liquid phase by gas phase, is reduced to harmless nitrogen again under activated carbon catalysis in the aqueous solution, and Fe (III)-NTA reducing/regenerating under activated carbon catalysis that simultaneous oxidation generates is Fe (II)-NTA, SO 2Being dissolved in the inferior sulfate radical that produces in the absorbent solution is reducing agent, and the basic principle of whole process is as follows:
Reaction as the formula (1) takes place in Fe (II)-NTA and NO, changes NO over to liquid phase by gas phase:
The pi-electron structure of activated carbon has the ability of transmitting electronics, can become the center of redox reaction, SO 2Be dissolved in the inferior sulfate radical that produces in the absorbent solution and can be used as reducing agent, under the catalysis of activated carbon, in the aqueous solution, NO is reduced to harmless N 2:
Fe (II)-NTA can be oxidized to Fe (III)-NTA by oxygen remaining in the waste gas, thereby loses the ability of complexed absorption NO.But activated carbon can impel Fe (III)-NTA to dissociate into Fe (III) and NTA (reaction (3)):
Fe (III) has stronger oxidability, and the inferior sulfate radical in the absorbent solution can be used as reducing agent, and Fe (III) reducing/regenerating is become Fe (II) (reaction (4)):
Fe (II) combines with NTA in solution again and generates Fe (II)-NTA (reaction (5)), and absorbent is regenerated, and absorption liquid removes the ability of NO can long term maintenance.
Fe(Ⅱ)+NTA→Fe(Ⅱ)-NTA (5)
Realize the technical scheme of the object of the invention:
The said method of the present invention in turn includes the following steps:
(1) exhaust emission is administered: in the reactor of routine, ferrous salt, nitrilotriacetic acid (NTA) and desulfurizing agent be dissolved in be used as absorption liquid in the aqueous solution, will contain NO and SO 2Waste gas feed, realize NO and SO 2Carry out when absorbing.
Described desulfurizing agent is ammonium sulfate, bivalent metal oxide, oxyhydroxide or carbonate etc., can be calcium oxide (lime), magnesia, Mg (OH) 2Or calcium carbonate (lime stone) etc.
The NO concentration range is in the described waste gas: 100~1000ppm; SO 2Concentration range be 500~5000ppm.
Usually can contain oxygen, O in the waste gas 2Concentration be 0~20%.
Operating pressure is a normal pressure, and temperature range is: 10~90 ℃, optimum value is: 30~60 ℃.
The pH scope of solution is generally: 1~9, and optimum value is: 3~7.
The concentration range of ferrous salt is: 0.008~0.2mol l -1, be preferably 0.04~0.08mol l -1
The concentration range of NTA is: 0.01~0.4mol l -1, be preferably 0.08~0.15mol l -1
The concentration of desulfurizing agent is 0~0.3mol l -1, be preferably 0.005~0.3mol l -1For example the concentration range of calcium oxide is: 0.005~0.3mol l -1, be recommended as 0.01~0.1mol l -1Magnesian concentration range is: 0.005~0.3mol l -1, be recommended as 0.01~0.1mol l -1The concentration range of calcium carbonate is: 0.005~0.3mol l -1, be recommended as 0.01~0.1mol l -1(NH 4) 2SO 4Concentration range be: 0.005~0.3mol l -1, be recommended as 0.03~0.2mol l -1
Common gas liquid ratio (volume flow ratio, M 3) be 10~300: 1, recommending gas liquid ratio is 200: 1.
Ferrous salt can be chosen any one kind of them from ferrous sulfate commonly used, frerrous chloride, ferrous nitrate, and preferably sulfuric acid is ferrous.
The present invention is to NO XAnd SO 2The reactor of Xi Shouing does not have special requirement simultaneously, NO XAnd SO 2Remove and can in common gas-liquid reactor such as packed tower, plate column or bubble tower etc., carry out.
(2) regeneration of reaction solution: step (1) reacted solution fed to make in the reactor of catalyst of activated carbon regenerate, this reactor is liquid-solid reactor commonly used, as fixed bed, slurry bed etc., activated carbon can be cocos active carbon commonly used, wood chip activated carbon, ature of coal activated carbon, asphalt based active carbon etc., regeneration temperature is 20~90 ℃, optimum temperature is 50~80 ℃, and regeneration pH is 1~9, and best pH is 3~7.Reaction solution can continue to use after the regeneration.
The basic process that the inventive method is implemented: above-mentioned absorption liquid is imported continuously by the top or the upper lateral part of gas-liquid reactor, and contains NO XAnd SO 2Waste gas from the bottom or the following side send into gas-liquid reactor continuously, in gas-liquid reactor, carry out NO XAnd SO 2Absorption reaction, reacted gas are constantly exported from the top or the upper lateral part of reactor, and absorption liquid flows out from the bottom or the following side of reactor, and importing contains in the liquid-solid reactor of activated carbon continuation use behind the process catalytic regeneration.
The present invention makees absorbent by adopting Fe-NTA solution, and activated carbon is made catalyst, sulphite is done the method that reducing agent regeneration NO absorbs active component Fe (II)-NTA, realizes recycling of NO absorbent, but also realizes NO absorption and reduction, SO 2Absorption and oxidation carry out simultaneously, nitrogen oxide and sulfur dioxide treatment cost are descended greatly.
Description of drawings
Fig. 1 is a kind of flow chart of the present invention.
Symbol description.
In the accompanying drawing: the 1-reactor, the 2-liquid-solid reactor, the 3-absorption liquid, 4-contains NO XAnd SO 2Waste gas, 5-activated carbon, 6-circulating slot.
The specific embodiment
The present invention is further elaborated below in conjunction with embodiment, but can not limit content of the present invention.
Embodiment 1
Absorption experiment is carried out in the packed tower of diameter 2cm, high 100cm, the gas-liquid two-phase adverse current, and empty tower gas velocity is 0.1m/s, liquid spraying density is 7m 3/ m 2.hr, absorption liquid 500ml.
In the absorption liquid: ferrous sulfate concentration is 0.02mol l -1, nitrilotriacetic acid concentration is 0.03mol l -1, the pH value is 6;
Gas flow is 300ml min -1, temperature is 50 ℃;
Gas feed consists of NO:600ppm, SO 2: 1500ppm, O 2: 5.2%, all the other are nitrogen.
Absorption liquid enters packed tower absorption of N O and SO by cat head 2, in tower bottom flow is gone into circulating slot, enter the fixed bed reactors that high 50cm, diameter 2cm be equipped with cocos active carbon from circulating slot again and carry out catalyst regeneration, reaction temperature be 70 ℃, liquid in regenerator with 35ml min -1Speed flow from lower to upper, the absorption liquid that leaves regenerator directly enters absorption of N O and SO in the packed tower 2Gas vent concentration is carried out on-line analysis by infrared spectrometer, per two minutes automatically sampling once reach when stablizing in operation, gas vent concentration is NO:50ppm, SO 2: 160ppm.The flow chart of logistics as shown in Figure 1.
Embodiment 2
Reactor and operating condition be with embodiment 1, but also have 0.03mol l in the absorption liquid -1Calcium oxide, reach when stablizing in operation, gas vent concentration is NO:50ppm, SO 2: 40ppm.
Embodiment 3
Reactor and operating condition be with embodiment 1, but also have 0.03mol l in the absorption liquid -1Magnesia, reach when stablizing in operation, gas vent concentration is NO:50ppm, SO 2: 40ppm.
Embodiment 4
Reactor and operating condition be with embodiment 1, but also have 0.03mol l in the absorption liquid -1Lime stone, reach when stablizing in operation, gas vent concentration is NO:50ppm, SO 2: 40ppm.
Embodiment 5
Reactor and operating condition be with embodiment 1, but also have 0.03mol l in the absorption liquid -1(NH 4) 2SO 4, reaching when stablizing in operation, gas vent concentration is NO:50ppm, SO 2: 40ppm.

Claims (10)

1. one kind removes SO in the waste gas simultaneously with Fe-NTA solution 2With the method for NO, it is characterized in that in the reactor of routine, when normal pressure and 10~90 ℃, feed absorption liquid and contain SO 2React the volume flow ratio M of gas-liquid with the waste gas of NO 3Be 10~300: 1;
Described absorption liquid is the aqueous solution that contains the pH 1~9 of ferrous salt, nitrilotriacetic acid and desulfurizing agent; Wherein, the concentration range of ferrous salt is 0.008~0.2mol l -1The nitrilotriacetic acid concentration range is 0.01~0.4mol l -1The concentration of desulfurizing agent is 0~0.3mol l -1
Described desulfurizing agent is ammonium sulfate, bivalent metal oxide, oxyhydroxide or carbonate.
2. the method for claim 1 is characterized in that described temperature range is 30~60 ℃, gas-liquid volume flow ratio M 3It is 200: 1.
3. the method for claim 1 is characterized in that the NO concentration range is 100~1000ppm in the described waste gas; SO 2Concentration range be 500~5000ppm; Containing concentration of oxygen in the waste gas is 0~20%.
4. the method for claim 1 is characterized in that the pH scope of described absorption liquid is: 3~7.
5. the method for claim 1, the concentration that it is characterized in that described molysite is 0.04~0.08mol l -1The concentration of described nitrilotriacetic acid is 0.08~0.15mol l -1The concentration of described desulfurizing agent is 0.005~0.3mol l -1
6. the method for claim 1 is characterized in that described bivalent metal oxide is calcium oxide, magnesia or calcium carbonate; The concentration range of described calcium oxide is 0.005~0.3mol l -1Described magnesian concentration range is 0.005~0.3moll -1The concentration range of described calcium carbonate is 0.005~0.3mol l -1
7. the method for claim 1 is characterized in that described ferrous salt is ferrous sulfate, frerrous chloride or ferrous nitrate.
8. the method for claim 1 is characterized in that described reaction back absorption liquid is to feed in the liquid-solid reactor of making catalyst of activated carbon to regenerate at 20~90 ℃ and pH at 1~9 o'clock.
9. the method for claim 1 is characterized in that described activated carbon is cocos active carbon, wood chip activated carbon or the ature of coal activated carbon of using always etc., and regeneration temperature is 50~80 ℃, and pH is 3~7.
10. as claim 1 and 8 described methods, it is characterized in that describedly importing in the liquid-solid reactor as claimed in claim 8 at the absorption liquid that from the reactor of routine, flows out.
CN200910198957A 2009-11-18 2009-11-18 Method for removing waste gas pollutants of NOX and SO2 simultaneously Pending CN101773770A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN200910198957A CN101773770A (en) 2009-11-18 2009-11-18 Method for removing waste gas pollutants of NOX and SO2 simultaneously

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN200910198957A CN101773770A (en) 2009-11-18 2009-11-18 Method for removing waste gas pollutants of NOX and SO2 simultaneously

Publications (1)

Publication Number Publication Date
CN101773770A true CN101773770A (en) 2010-07-14

Family

ID=42510436

Family Applications (1)

Application Number Title Priority Date Filing Date
CN200910198957A Pending CN101773770A (en) 2009-11-18 2009-11-18 Method for removing waste gas pollutants of NOX and SO2 simultaneously

Country Status (1)

Country Link
CN (1) CN101773770A (en)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102188882A (en) * 2011-04-12 2011-09-21 王晓晔 Integrated method for simultaneously realizing denitrification, desulfurization and heavy metal removal from flue gas, and special equipment suitable for the method
CN102476849A (en) * 2011-10-20 2012-05-30 常州亚环环保科技有限公司 Desulphurizing agent for removing sulphur compounds from wastewater and application method thereof
CN102989303A (en) * 2012-09-12 2013-03-27 河南绿典环保节能科技有限公司 Smoke wet-type oxidation integral desulfuration denitration and energy using method
CN103007725A (en) * 2012-09-12 2013-04-03 河南绿典环保节能科技有限公司 Wet-type oxidative denitration and energy utilization method of smoke
CN103230734A (en) * 2013-04-19 2013-08-07 上海交通大学 Method for combined removal of sulfur dioxide and nitrogen oxide in flue gas
CN103877831A (en) * 2014-04-03 2014-06-25 江汉大学 Integrated complex ferrous wet flue gas desulfurization and denitration method
CN105080317A (en) * 2014-05-05 2015-11-25 淮南市明月环保科技有限责任公司 Method for simultaneously reclaiming sulfur and nitrate
CN105214466A (en) * 2015-10-29 2016-01-06 北京市环境保护科学研究院 A kind of wet method coordinated desulfurization denitrating technique utilizing composite absorption liquid
CN110124451A (en) * 2019-05-13 2019-08-16 上海大学 SO in wet type substep removing flue gas2With the method for NO

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102188882A (en) * 2011-04-12 2011-09-21 王晓晔 Integrated method for simultaneously realizing denitrification, desulfurization and heavy metal removal from flue gas, and special equipment suitable for the method
CN102476849A (en) * 2011-10-20 2012-05-30 常州亚环环保科技有限公司 Desulphurizing agent for removing sulphur compounds from wastewater and application method thereof
CN102989303B (en) * 2012-09-12 2014-10-08 河南绿典环保节能科技有限公司 Smoke wet-type oxidation integral desulfuration denitration and energy using method
CN102989303A (en) * 2012-09-12 2013-03-27 河南绿典环保节能科技有限公司 Smoke wet-type oxidation integral desulfuration denitration and energy using method
CN103007725A (en) * 2012-09-12 2013-04-03 河南绿典环保节能科技有限公司 Wet-type oxidative denitration and energy utilization method of smoke
CN103007725B (en) * 2012-09-12 2015-03-18 河南绿典环保节能科技有限公司 Wet-type oxidative denitration and energy utilization method of smoke
CN103230734A (en) * 2013-04-19 2013-08-07 上海交通大学 Method for combined removal of sulfur dioxide and nitrogen oxide in flue gas
CN103230734B (en) * 2013-04-19 2016-03-02 上海交通大学 Combine the method removing sulfur dioxide in flue gas and nitrogen oxide
CN103877831A (en) * 2014-04-03 2014-06-25 江汉大学 Integrated complex ferrous wet flue gas desulfurization and denitration method
CN103877831B (en) * 2014-04-03 2016-07-06 江汉大学 A kind of method of complexation ferrous iron smoke-gas wet desulfurization denitrification integral
CN105080317A (en) * 2014-05-05 2015-11-25 淮南市明月环保科技有限责任公司 Method for simultaneously reclaiming sulfur and nitrate
CN105080317B (en) * 2014-05-05 2018-01-16 淮南市明月环保科技有限责任公司 Method that is a kind of while reclaiming sulphur and nitre
CN105214466A (en) * 2015-10-29 2016-01-06 北京市环境保护科学研究院 A kind of wet method coordinated desulfurization denitrating technique utilizing composite absorption liquid
CN110124451A (en) * 2019-05-13 2019-08-16 上海大学 SO in wet type substep removing flue gas2With the method for NO

Similar Documents

Publication Publication Date Title
CN101773770A (en) Method for removing waste gas pollutants of NOX and SO2 simultaneously
CN101711943B (en) Method for controlling pollutant waste gas containing NO through low-temperature liquid phase catalytic reduction
CN102350197B (en) Fume desulfurizing and denitrifying device based on magnesia and method
CN101306308B (en) Method for synchronously treating the combined pollution exhaust gas containing nitric oxide and sulfur dioxide
CN101274208B (en) Method for simultaneously removing sulfur dioxide and nitrogen oxide in exhaust air
CN101745305B (en) Method for removing various gaseous pollutants from smoke gas
CN101530729B (en) Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously
CN101352648A (en) Method for simultaneously treating sulfur dioxide and nitrogen oxide in exhaust air
CN102527205B (en) Method and system for simultaneously removing sulfur, niter and mercury from smoke based on catalytic oxidation
CN103463978B (en) Based on the device and method of catalytic oxidation of hydrogen peroxide flue gas and desulfurizing and denitrifying
CN104190220A (en) Device and method for denitrifying flue gas of coking furnace
CN105536886B (en) A kind of regeneration method of arsenic poisoning denitrating catalyst
CN101590369B (en) Mercury removal process based on lime-gypsum method desulphurization system and mercury removal absorption liquid
CN1544126A (en) Method for removing and reclaiming NO and SO2 in waste gas using ammonia solution
CN102527224A (en) Method and device for removing sulfur dioxide and nitrogen oxides from flue gas/ waste gas
CN103432877A (en) Integrated method for wet-process dust removal, desulfurization, denitrification demercuration, dearsenification of complexing ferroporphyrin smoke based on supergravity
CN102068893A (en) Process for simultaneously desulfurizing and denitrating coal combustion flue gas by wet method
CN107198963B (en) Efficient wet denitration method and device
CN102847418A (en) Additive for limestone-gypsum wet flue gas desulfurization and denitration process
CN102188889B (en) Device and method for combined removal of sulphur dioxide (SO2), nitrogen oxide (NOX) and mercury from fume
CN102698581A (en) Method for producing sodium sulfate and sodium nitrate by simultaneous desulfurization and denitrification by soda-citric acid cobalt (II)
CN101530730A (en) Method for simultaneously treating waste gas pollution of NOX and SO2
CN105233687A (en) Method for removing elemental mercury in coal-fired flue gas
CN102989302A (en) Smoke wet oxidation denitration method
CN102814112A (en) Method and device for desulfurizing and denitrating jointly

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20100714

C02 Deemed withdrawal of patent application after publication (patent law 2001)