CN101530729B - Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously - Google Patents

Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously Download PDF

Info

Publication number
CN101530729B
CN101530729B CN2009100472463A CN200910047246A CN101530729B CN 101530729 B CN101530729 B CN 101530729B CN 2009100472463 A CN2009100472463 A CN 2009100472463A CN 200910047246 A CN200910047246 A CN 200910047246A CN 101530729 B CN101530729 B CN 101530729B
Authority
CN
China
Prior art keywords
absorption
tower
layer
sulfur dioxide
absorption liquid
Prior art date
Application number
CN2009100472463A
Other languages
Chinese (zh)
Other versions
CN101530729A (en
Inventor
龙湘犁
朱海嵩
毛彦鹏
陈瑜
袁渭康
Original Assignee
华东理工大学
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 华东理工大学 filed Critical 华东理工大学
Priority to CN2009100472463A priority Critical patent/CN101530729B/en
Publication of CN101530729A publication Critical patent/CN101530729A/en
Application granted granted Critical
Publication of CN101530729B publication Critical patent/CN101530729B/en

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 provides an absorption tower for recovering sulfur dioxide from flue gas to realize simultaneous implementation of oxidation and absorption; the absorption tower comprises a tower body, an absorption liquid distribution device is arranged at the upper part in the tower body and below a defoaming layer and is connected with an absorption liquid inlet on the tower body, an absorption layer of sulfur dioxide and nitrogen oxide which is arranged below the absorption liquid distribution device, a tower plate which is arranged below the absorption layer of sulfur dioxide and nitrogen oxide, a flue gas distributor which is arranged below the tower plate, an absorption liquid regeneration layer which is arranged below the flue gas distributor, a cycle absorption liquid outlet which is arranged below the gas distributor and above the absorption liquid regeneration layer, an absorption liquid cycle storage tank which is arranged below the absorption liquid regeneration layer, an ammonium sulfate and ammonium nitrate grout outlet which is arranged below the absorption liquid cycle storage tank and a downcomer which is arranged between the tower plate and the absorption liquid cycle storage tank. The tower body is characterized in that a gas outlet is arranged at the top part of the tower; and the defoaming layer is arranged in the tower and below a purified flue gas outlet and is internally provided with a defoaming part.

Description

A kind ofly administer NO and SO<sub in the waste gas simultaneously〉2</sub multifunctional absorption tower

Technical field

The present invention relates to a kind of remove and reclaim NO and SO in the waste gas 2Technology and device, be specifically related to remove and reclaim NO and SO in the waste gas with alkaline solution 2Technology and device.

Background technology

The pollution of acid rain and the harm that causes thereof have become one of environmental problem of paying close attention to countries in the world.SO 2With NOx be two kinds of dusty gas that discharge capacity is maximum, harmfulness is maximum.Nitrogen oxide also can form photochemical pollution, produces greenhouse effects, damages the ozone layer, human body is had the intoxicating effect.The nitrogen oxide that China was discharged in 2000 is 1,200 ten thousand tons, if do not take effective pollution control measures, the year two thousand twenty 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, the environmental carrying capacity of nitrogen oxide is in saturation state substantially, some local even generation photochemical fog phenomenons, in China's acid precipitation, nitrate anion and sulfate ion concentration ratio develop into 0.20: 1 in 2004 by 0.15: 1 in 2000, the acid rain that shows Future in China pollute may with by sulfuric acid type to the compound development of sulfuric acid/nitric acid, control SO 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 NO respond is relatively poor, therefore, it removes also just quite difficult technically.Developed multiple method of denitration through years of researches.At present, what industrial employing was more is catalytic reduction method, as patent US Patent 4,221,768, SwedishPatent 8404840-4, US Patent 4,101,238, US Patent 4,048,112 disclosed methods, but this method reaction needs to consume a large amount of reducing agents, and the NO in the flue gas can not recycle.

Japan Patent P1659565j (1976), P181759c (1976), P63100918, A2 (1988) remove NO when proposing XAnd SO 2Oxidant that method adopts, as chloric acid, potassium permanganate, hydrogen peroxide, ozone etc., liquid phase oxidation NO XDeng because cost height etc. is former thereby fail to promote and come.Another kind method adopts yellow phosphorus (to see document Nature, 1990,343 (11): 151-153), can remove the NO in the flue gas simultaneously XAnd SO 2, but belong to the method for abandoning entirely.This method will consume a large amount of phosphor resources, and its toxicity is big, and operation is had relatively high expectations.

The early 1970s people propose to adopt Fe (II)-EDTA (EDTA represents ethylenediamine tetra-acetic acid, use usually disodium ethylene diamine tetraacetate and ferrous salt formulated) to remove NO in the waste gas, and the reaction equation of Fe (II)-EDTA and NO is as follows:

(document sees reference: Bull.of the Chem.Soc.of Jpn. 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, so the industrialization that delays of this method.

Chinese patent CN101306308 discloses and has a kind ofly removed NO and SO in the waste gas with Fe (II)-EDTA solution 2Method, its principle is such:

Utilization contains the absorption liquid while absorption of N O and the SO of Fe (II)-EDTA and desulfurizing agent composition 2Fe (III)-EDTA that Fe (II)-EDTA oxidation generates can not complexing NO, but under the effect of activated-carbon catalyst, Fe (III)-EDTA can be dissociated into ferric ion Fe (III) and EDTA (seeing formula (2)), Fe (III) has stronger oxidability, can be with SO 2Be dissolved in the inferior sulfate radical that produces in the absorbent solution and be oxidized to sulfate radical (seeing formula (3)), itself be reduced to ferrous ion Fe (II), Fe (II) combines with EDTA in solution again and generates Fe (II)-EDTA (reaction (4)), absorbent is regenerated, and the ability that absorption liquid removes NO can keep for a long time.

Fe(II)+EDTA→Fe(II)-EDTA (4)

Said process can be realized NO and SO 2Remove simultaneously and carry out, absorption liquid can recycle, and is with low cost, no secondary wastewater pollutes and produces, and has stronger economy, technical advantage.

Summary of the invention

The technical problem that this patent quasi-solution is determined is that a kind of energy of design realizes removing simultaneously NO and SO in the waste gas 2The absorption tower, make technological process more succinct, reduce the construction cost and the operating cost of desulphurization denitration.

Technical scheme of the present invention:

The absorption tower is cylindrical or square vertical tower body; This absorption tower structure is as follows:

Be arranged on the purification exhanst gas outlet of top of tower;

Be arranged on the tower internal upper part, purify the foam-removing layer below the exhanst gas outlet, droplets entrained is separated through foam-removing layer in the flue gas, and the band foam amount that makes flue gas is less than 100mg Nm -3Foam-removing layer is the structured packing of lower resistance, and as mellapak packing or wire packing, the recommendation mass transfer area is 50~500m 2/ m 3, optimum value is 150~250m 2/ m 3, the material of plate ripple arranged packing is polypropylene or fiberglass, and the height of mass transfer elements layer is 0.1~3m, and optimum value is 0.2~2m.

Be arranged on the absorption liquid distribution apparatus tower body internal upper part, foam-removing layer below, that enter the mouth and be connected with absorption liquid on being arranged on tower body, the absorption liquid distribution apparatus can be any pattern, as long as be evenly distributed, preferred nozzle, or antipriming pipe, or groove type distributor, material adopts polypropylene or fiberglass.

Be arranged on the sulfur dioxide and the nox adsorption layer of absorption liquid distribution apparatus below, be the core texture on absorption tower, require that mass transfer area is big, resistance is low, corrosion-resistant.The mass transfer elements layer can be selected plate ripple arranged packing, grid packing or sieve plate for use, and plate ripple arranged packing or grid packing mass transfer area are 100~500m 2/ m 3, optimum value is 150~250m 2/ m 3, the height of mass transfer elements layer is 0.5~7m, optimum value is 1~5m; The percent opening of sieve plate is 8-32%, and the aperture is 12-25mm, and sieve plate is the 2-6 piece, is suitably the 3-5 piece.The material of absorbed layer is polypropylene or fiberglass.

Be arranged on the column plate of described sulfur dioxide and nox adsorption layer below, this column plate can be float valve type column plate, blister-type column plate and the screen hole type column plate of using always, and material is anti-corrosion materials such as polypropylene or fiberglass.

Be arranged on the flue gas distributor that is connected with smoke inlet of column plate below.

Be arranged on the regeneration of absorption solution layer of flue gas distributor below, this regeneration of absorption solution layer is the fixed bed that is filled with Pd/carbon catalyst, comprises the activated carbon by preparations such as coconut husk, wood chip and atures of coal.

Be arranged on a circulating absorption solution outlet of flue gas distributor below, regeneration of absorption solution layer top.

Be arranged on the absorption liquid circulating storage groove of regeneration of absorption solution layer below.An evacuation port is arranged on the tower body of this absorption liquid circulating storage groove bottom; And be connected by downspout between above-mentioned column plate and the absorption liquid circulating storage groove.

Adopt said apparatus to realize that the while desulphurization denitration comprises the steps: from flue gas

Put into following absorption liquid at sulfur dioxide and nox adsorption layer: the aqueous solution of soluble ferrite and disodium ethylene diamine tetraacetate preparation or contain the soluble ferrite of lime stone slurry, lime solution, magnesia, ammonium sulfate, sodium sulfite and the aqueous solution of disodium ethylene diamine tetraacetate preparation; Wherein: based on the reactant liquor cumulative volume, Fe-disodium ethylene diamine tetraacetate concentration is 0.005~0.2mol/l solution, and the pH value is 1~9.The concentration expressed in percentage by weight that contains calcium oxide concentration 0.005~0.3mol/l, magnesium oxide concentration 0.005~0.3mol/l, calcium carbonate concentration 0.005~0.3mol/l, ammonium sulfate in the aqueous solution of described soluble ferrite and disodium ethylene diamine tetraacetate preparation is that 1-40% or sodium sulfite concentration expressed in percentage by weight are 1-20%.

Containing sulfur dioxide concentration is that 700-4000ppm, nitrous oxides concentration are that 200-800ppm, temperature are 110-180 ℃ boiler smoke, enter in the tower after directly being cooled to 50~100 ℃ by the logical people Ta Nei of smoke inlet or through reheater, distribute the back adverse current upwards by flue gas distributor, at first the column plate through the top contacts cooling with absorption liquid, enter sulfur dioxide and nox adsorption district then, contact NO and SO with the absorption liquid of absorption liquid distribution apparatus ejection 2This zone that is absorbed in realize simultaneously, enter foam-removing layer with flue gas then, remove behind the droplet in the flue gas and enter in the atmosphere by purifying exhanst gas outlet.

Absorbed the absorption liquid of sulfur dioxide and nitrogen oxide at sulfur dioxide and nox adsorption layer, go downstream and enter the column plate of below with after the flue gas of high temperature contacts, enter the circulating slot of bottom, absorption tower through the downspout of column plate, and then from lower to upper by the catalyst in the regeneration of absorption solution layer, the absorption liquid after the regeneration is exported through being pumped into the absorption liquid distribution apparatus on top, absorption tower by the circulating absorption solution that is positioned at the regeneration zone top.

Fully contact in order to ensure gas-liquid two-phase, the sprinkle density of absorption liquid is at 3-60m 2/ m 3Hr -1Between, preferred 5-20m 3m -2Hr -1Between, the volume flow ratio of flue gas and absorption liquid is 20-200.

In order to ensure the NO assimilation effect, the pH scope of solution is generally: 1~9, and optimum value is: 4~7; The concentration range of ferrous salt is: 0.005~0.1mol/l is preferably 0.02~0.06mol/l; The concentration range of EDTA is: 0.06~0.11mol/l is preferably 0.02~0.07mol/l.

The concentration of desulfurizing agent is 0~0.3mol/l.Be preferably 0.005~0.3mol/l.For example the concentration range of calcium oxide is: 0.005~0.3mol/l is recommended as 0.01~0.1mol/l; Magnesian concentration range is: 0.005~0.3mol/l is recommended as 0.01~0.1mol/l; The concentration range of calcium carbonate is: 0.005~0.3mol/l is recommended as 0.01~0.1mol/l.Or the concentration expressed in percentage by weight of ammonium sulfate is 1-40%, or the sodium sulfite percentage concentration is 1-20%.

In order to ensure the regeneration effect of absorption liquid, C catalyst is housed in the regenerator, comprise activated carbon by preparations such as coconut husk, wood chip and atures of coal.

This desulphurization denitration tower is the equipment with multifunction structure, and seven function: SO are specifically arranged 2Absorption, inferior sulfate radical oxidation, nox adsorption, NO reduction, regeneration of absorption solution, flue gas ash removal, flue gas remove foam (mist), and the technical standard that can reach is as follows:

SO 2Absorb (or deviating from) efficient: 〉=95-99%,

The nitrogen oxide extrusion rate: 〉=90%,

Cleaning of off-gas contain foam (mist) content≤100mg/Nm 3

Dust removing effects: 〉=70-95%,

Description of drawings

Fig. 1 is a kind of flow chart of the present invention.

Symbol description.

1. purification exhanst gas outlet, 2. absorption liquid import, 3. gas approach, 4. pump, 5. circulating absorption solution outlet, 6. evacuation port, 7. absorption liquid circulating slot, 8. regeneration of absorption solution layer, 9. tower downspout, 10. gas distributor, 11. column plate, 12. absorbed layers, 13. absorption liquid distribution apparatus, 14. foam-removing layers.

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

One flow is 100Nm 3/ hr flue gas enters the absorption tower, and amount of nitrogen oxides is 400ppm in the flue gas, SO 2Content is 800ppm, and dustiness is 90mg/Nm 3, temperature is 130 ℃.

As shown in Figure 1, the diameter 0.5m on absorption tower, absorbed layer (12) adopts 100m in the high 5m, tower 2/ m 3Plate ripple arranged packing highly is 2m; Foam-removing layer (14) is 150m for mass transfer area 2/ m 3The polypropylene board ripple packing, highly be 0.5m; Column plate (11) is the blister-type column plate, and the aperture is that 80mm, spacing are 300mm.Regeneration of absorption solution floor height 1m, interior dress 20-40 purpose cocos active carbon.

Flue gas enters the absorption tower from the smoke inlet (3) on absorption tower, from lower to upper by column plate (10), behind absorbed layer (12) and the foam-removing layer (14), enters atmosphere by purifying exhanst gas outlet (1) through gas distributor.After leaving the absorption tower, SO in the tail gas 2Content is 8ppm, and amount of nitrogen oxides is 15ppm, and foam (mist) content is 40mg/Nm 3

Liquid sprays into absorbed layer from top to down by liquid distribution trough (13), at absorbed layer absorbing NOx and SO 2After enter the column plate (11) of tower bottom, by the absorption liquid circulating slot (7) at the bottom of entering tower from downspout (9) after the inlet flue gas preheating through column plate, pass through the regeneration of absorption solution layer (8) in the tower more from bottom to top, send back in the absorption tower by pump (4) from absorption liquid loop exit (5) at last.Absorption liquid flow 0.8m 3/ hr, the pH value is 5.5-6.2, and ammonium sulfate content is 8-14% (weight), and ferrous sulfate concentration is 0.02mol/l, and EDTA concentration is 0.02mol/l.

Embodiment 2

The coal-burning boiler of a 270T/h, flue gas flow are 300,000 Nm 3/ hr, amount of nitrogen oxides are 480ppm, SO 2Content is 1500ppm, and dustiness is 90mg/Nm 3, flue-gas temperature is 130 ℃.Absorption tower diameter 7m, high 15m.After leaving the absorption tower, SO in the tail gas 2Content is 15ppm, and amount of nitrogen oxides is 40ppm, and foam (mist) content is 80mg/NH 3

As accompanying drawing 1, the absorbed layer in the absorption tower adopts 100m 2/ m 3Plate ripple arranged packing highly is 6m.Absorption liquid flow 200m 3/ hr, the pH value is 7.2-8.1, and ferrous sulfate concentration is 0.02mol/l, and EDTA concentration is 0.02mol1 -1, calcium oxide concentration is 0.022mol/l.Regeneration of absorption solution floor height 1.5m, interior dress 20-40 purpose ature of coal activated carbon.

Foam-removing layer is that mass transfer area is 150m 2/ m 3The polypropylene board ripple packing, highly be 0.5m.

Column plate is the screen hole type column plate, and the aperture is that 15mm, percent opening are 9%.

Embodiment 3

The coal-burning boiler of a 670T/h, flue gas flow are 850,000 Nm 3/ hr, amount of nitrogen oxides are 540ppm, SO 2Content is 2100ppm, and dustiness is 190mg/Nm 3, flue-gas temperature is 170 ℃.Absorption tower diameter 9m, high 17m.After leaving the absorption tower, SO in the tail gas 2Content is 30ppm, and amount of nitrogen oxides is 50ppm, and foam (mist) content is 70mg/Nm 3

In the absorption tower:

Absorbed layer adopts 150m 2/ m 3Plate ripple arranged packing highly is 7m.Absorption liquid flow 320m 3/ hr, the pH value is 7.8-8.2, and magnesium oxide concentration is 0.03mol/l, and ferrous sulfate concentration is 0.03mol/l, and EDTA concentration is 0.04mol/l.

Regeneration of absorption solution floor height 2m, interior dress 20-40 purpose ature of coal activated carbon.

Foam-removing layer is that mass transfer area is 150m 2/ m 3The polypropylene board ripple packing, highly be 1m.

Column plate is the screen hole type column plate, and the aperture is that 20mm, percent opening are 10%.

Claims (8)

1. absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously is characterized in that described absorption tower is made of following the setting:
An outlet that purifies flue gas is arranged at the tower body top;
Below the outlet of tower inside, purification flue gas, a foam-removing layer is arranged, be provided with the foam removal parts in the foam-removing layer;
An absorption liquid distribution apparatus that is connected with absorption liquid inlet on the tower body is arranged below the foam-removing layer in tower body;
Sulfur dioxide and nox adsorption layer are arranged below described absorption liquid distribution apparatus;
A column plate is arranged below described sulfur dioxide and nox adsorption layer;
A flue gas distributor that is connected with smoke inlet is arranged below column plate;
A regeneration of absorption solution layer is arranged below flue gas distributor;
In a circulating absorption solution outlet below the flue gas distributor, above the regeneration of absorption solution layer;
An absorption liquid circulating storage groove is arranged below the regeneration of absorption solution layer; An evacuation port is arranged on the tower body of this absorption liquid circulating storage groove bottom; And be connected by downspout between above-mentioned column plate and the absorption liquid circulating storage groove.
2. the absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously according to claim 1 is characterised in that described foam-removing layer is the plate ripple arranged packing or the wire packing of lower resistance, and the height of layer is 0.1~3m, and mass transfer area is 50~500m 2/ m 3The material of described plate ripple arranged packing is polypropylene or fiberglass.
3. the absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously according to claim 1 is characterized in that described absorption liquid distribution apparatus is a nozzle, or antipriming pipe, or groove type distributor.
4. the absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously according to claim 1 is characterized in that described sulfur dioxide and nox adsorption layer select plate ripple arranged packing, grid packing or sieve plate for use; Plate ripple arranged packing or grid packing mass transfer area are 100~500m 2/ m 3, the height of mass transfer elements layer is 0.5~7m; The percent opening of sieve plate is 8-32%, and the aperture is 12-25mm, and sieve plate is the 2-6 piece, and the material of absorbed layer is polypropylene or fiberglass.
5. the absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously according to claim 1 is characterized in that described column plate is float valve type column plate, blister-type column plate and the screen hole type column plate of using always; Material is polypropylene or fiberglass.
6. the absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously according to claim 1 is characterized in that described regeneration of absorption solution layer, is the fixed bed that is filled with activated carbon catalyst.
7. the absorption tower that removes sulfur dioxide and nitrogen oxide from waste gas simultaneously as claimed in claim 1 is characterized in that described sulfur dioxide and nox adsorption layer put into following absorption liquid: the aqueous solution of soluble ferrite and disodium ethylene diamine tetraacetate preparation or contain the soluble ferrite of lime stone slurry, lime solution, magnesia, ammonium sulfate, sodium sulfite and the aqueous solution of disodium ethylene diamine tetraacetate preparation; Wherein: based on the reactant liquor cumulative volume, Fe-disodium ethylene diamine tetraacetate concentration is 0.005~0.2mol/l solution, and the pH value is 1~9.
8. the absorption tower that from waste gas, removes sulfur dioxide and nitrogen oxide simultaneously as claimed in claim 7, it is characterized in that the concentration expressed in percentage by weight that contains calcium oxide concentration 0.005~0.3mol/l, magnesium oxide concentration 0.005~0.3mol/l, calcium carbonate concentration 0.005~0.3mol/l, ammonium sulfate in the aqueous solution of described soluble ferrite and disodium ethylene diamine tetraacetate preparation is that 1-40% or sodium sulfite concentration expressed in percentage by weight are 1-20%.
CN2009100472463A 2009-03-09 2009-03-09 Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously CN101530729B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2009100472463A CN101530729B (en) 2009-03-09 2009-03-09 Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2009100472463A CN101530729B (en) 2009-03-09 2009-03-09 Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously

Publications (2)

Publication Number Publication Date
CN101530729A CN101530729A (en) 2009-09-16
CN101530729B true CN101530729B (en) 2011-06-29

Family

ID=41101717

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2009100472463A CN101530729B (en) 2009-03-09 2009-03-09 Multifunctional absorption tower for controlling NO and SO2 in waste gas simultaneously

Country Status (1)

Country Link
CN (1) CN101530729B (en)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101837237B (en) * 2009-12-29 2012-11-14 中国恩菲工程技术有限公司 Flue gas desulphurization system
CN101837236B (en) * 2009-12-29 2013-02-27 中国恩菲工程技术有限公司 Flue gas desulfurization method
CN102008879A (en) * 2010-10-14 2011-04-13 中化化肥有限公司 Desulfurizing tower
CN102188882B (en) * 2011-04-12 2013-06-12 北京国电清新环保技术股份有限公司 Integrated method for simultaneously realizing denitrification, desulfurization and heavy metal removal from flue gas, and special equipment
CN102728204A (en) * 2012-07-20 2012-10-17 华东理工大学 Absorption tower for treating NO and SO2 in waste gas simultaneously
CN103623661B (en) * 2012-08-20 2015-11-25 中国石油化工集团公司 A kind of column for smoke purification
CN103071368A (en) * 2012-12-10 2013-05-01 贵州长绿科技有限公司 Oxynitride-containing exhaust gas washing device
CN103239977A (en) * 2013-05-14 2013-08-14 成都信息工程学院 Denitration method for cuprammouium complex by complexing absorption
PL2851115T3 (en) 2013-09-20 2016-10-31 A scrubber tower of a flue gas purification device
CN104226095B (en) * 2014-07-30 2016-06-01 武汉悟拓科技有限公司 Based on the synchronous denitrating technique of flue gas wet ammonia process desulfurizing
CN105935542A (en) * 2016-06-10 2016-09-14 江苏蓝天水净化工程有限公司 Chlorine absorption device
CN105903329B (en) * 2016-06-14 2018-06-29 广东万引科技发展有限公司 A kind of flue gas desulfurization and denitration technique
CN106823693B (en) * 2017-03-28 2019-08-27 中北大学 A kind of deep desulfuration absorbent for smoke-gas wet desulfurization
CN109126424A (en) * 2018-09-07 2019-01-04 南通航泰船舶机械有限公司 A kind of ship desulfurization and denitrification integral process

Also Published As

Publication number Publication date
CN101530729A (en) 2009-09-16

Similar Documents

Publication Publication Date Title
CN104857835B (en) Flue gas integrated treatment unit and method
CN102824844B (en) Desulfurization and denitrification agent, preparation method and application thereof
CN104226095B (en) Based on the synchronous denitrating technique of flue gas wet ammonia process desulfurizing
CN103223292B (en) Ammonia process flue gas treatment method for acidic tail gas and device
CN101745305B (en) Method for removing various gaseous pollutants from smoke gas
CN101422691B (en) Multi-pollutant removing technique and device of fuel coal smoke
CN101352647B (en) Simultaneous desulfuration and denitration technique by wet flue gas method
CN103301749B (en) The method of flue gas and desulfurizing and denitrifying
JP6171096B2 (en) Semi-dry simultaneous desulfurization / denitration / demercury equipment and method using circulating fluidized bed
CN101879404B (en) Recycled flue gas desulfurization and denitration method
CN100496676C (en) Wet ammonia flue gas cleaning technology simultaneously removing various pollutant and system thereof
CN106659971A (en) Method and apparatus for removing contaminants from exhaust gases
CN101254394B (en) Sintering device flue gas multiple pollutant removing process and system thereof
CN102580496B (en) Liquid-phase oxidation multistage absorbed flue gas desulfurization and denitrification technology and device
CN103706238B (en) System and method for removing SO2, NO and Hg in smoke on the basis of heterogeneous Fenton
CN100496672C (en) Wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction and system thereof
CN100488601C (en) Flue gas desulfurization method by using magnesium compound and ammonia for circulated regeneration
CN102512952B (en) Fluidized bed-based flue gas combined desulfurization and denitration process
CN102527205B (en) Method and system for simultaneously removing sulfur, niter and mercury from smoke based on catalytic oxidation
CN102247750B (en) Method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process
CN103657368B (en) A kind of simultaneous SO_2 and NO removal demercuration dry-method fume gas purification method and device
CN102755823B (en) Method for desulfurizing high-sulphur boiler flue gas to prepare high-purity ammonium bisulfite
CN100391579C (en) Method for desulfurizing waste gas and reutilizing sulfur source
KR102036816B1 (en) Method and apparatus for effectively removing sulfur oxides and dust in gas by ammonia-based process
CN101279185B (en) Gas phase oxidation-liquid phase reduction method for absorbing and removing nitrous oxides in exhaust air

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model