CN105771651A - Synchronous flue gas desulfurization and denitrification process with ammonia method based on Fenton-like effect - Google Patents

Synchronous flue gas desulfurization and denitrification process with ammonia method based on Fenton-like effect Download PDF

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CN105771651A
CN105771651A CN201610255087.6A CN201610255087A CN105771651A CN 105771651 A CN105771651 A CN 105771651A CN 201610255087 A CN201610255087 A CN 201610255087A CN 105771651 A CN105771651 A CN 105771651A
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tower
flue gas
absorption
absorption tower
concentration
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CN105771651B (en
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吴高明
刘成
吴晓琴
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Wuhan University of Science and Engineering WUSE
Wuhan Iron and Steel Co Ltd
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Wuhan University of Science and Engineering WUSE
Wuhan Iron and Steel Corp
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B01D53/965—Regeneration, reactivation or recycling of reactants including an electrochemical process step
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/80—Organic bases or salts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/80—Type of catalytic reaction
    • B01D2255/802—Photocatalytic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

Abstract

The invention discloses a synchronous flue gas desulfurization and denitrification process with an ammonia method based on a Fenton-like effect. The synchronous flue gas desulfurization and denitrification process comprises the following steps: flue gas is fed into a concentration tower after pressurization and is subjected to contact reaction with concentrated liquid in the tower; the flue gas getting out of the concentration tower is fed into an absorption tower, is subjected to reverse contact reaction with circulation absorption liquid sprayed out from a spraying layer at the upper part of the tower, and then is discharged from the top of the absorption tower; part of concentrated liquid after reaction is led out from the tower bottom of the concentration tower, is subjected to iron removal through an iron removal system, and then is fed into an ammonium sulfate crystallization system; the flue gas enters the absorption tower from a flue gas inlet in the middle of the absorption tower, sequentially passes through at least one photochemical reaction layer, a filler layer and the spraying layer arranged at the upper part of the tower, is subjected to reverse contact reaction with the circulation absorption liquid, and then is discharged from the flue gas outlet; the circulation absorption liquid at the bottom of the absorption tower is supplemented with aqueous ammonia, a complexing agent Fe (II) EDTA, oxalic acid and ferrous sulfate and then is used as the circulation absorption liquid for being sent back to an injection tower on the spraying layer at the upper part of the absorption tower. The synchronous flue gas desulphurization and denitrification process provided by the invention is simple, low in operation cost, low in energy consumption, easy to control, good in denitrification effect and good in byproduct quality.

Description

Flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect
Technical field
The present invention relates to the gas cleaning of field of Environment Protection, specifically a kind of flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect.
Background technology
Existing flue gas synchronized desulfuring and denitrifying method is divided into five big classes according to technical process: solid phase adsorption/regeneration synchronized desulfuring and denitrifying technology, gas-solid catalysis synchronized desulfuring and denitrifying technology, sorbent injection synchronized desulfuring and denitrifying technology, high energy electron active oxidation synchronized desulfuring and denitrifying technology, wet flue gas synchronized desulfuring and denitrifying technology.
What flue gas was implemented wet method synchronized desulfuring and denitrifying most study is Fe (II) the EDTA method in Absorption via Chemical Complexation.From 20 century 70s, Japan and some scholars of the U.S. have begun to Fe (II) EDTA method is carried out substantial amounts of research, it is believed that NO is had good complexation effect by Fe (II) EDTA, and denitration efficiency is high.But, Fe (II) EDTA self is also easy in by flue gas entrained O in the process of complexation NO2Aoxidized, formed NO Fe (III) EDTA without absorbing activity.Yin Qide etc. propose " Fe2+Intercalating agent complexation-iron powder reducing-acid absorbs absorption method " remove the new technology of NO in flue gas.Experiments show that, NO removal efficiency can increase along with iron powder consumption and reactor mixing speed and increase, and iron powder particle diameter is more big, and assimilation effect is more poor.At iron powder 0.8g, iron powder particle diameter is less than 0.077mm, and stir speed (S.S.) is 900r min-1, when oxygen content is 5%, obtain more than 90% NO removal efficiency.LiWang etc. adopt Fe (II) EDTA/Na2SO3Make reducing agent and absorb NO and SO simultaneously2, and Fe (II) EDTA is regenerated.Research shows there is SO2Time NO absorption rate improve 1.59 times.
For the wet ammonia process desulfurizing that sintering adopts, carry out composite realization of ammonia-Fe (II) EDTA on this basis and sinter flue gas synchronized desulfuring and denitrifying, be that a kind of flue gas multiple pollutant that sinters with application prospect works in coordination with the technology of improvement.But owing to flue gas dividing containing a certain amount of oxygen, Fe (II) the EDTA oxidation that easily will absorb in liquid, cause that denitration efficiency declines, even lose denitration ability.
Summary of the invention
The present invention provides that a kind of technique is simple, operating cost is low, energy consumption is low, control is easy, denitration effect is good, the measured flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect of side-product matter.
Technical scheme sends into concentration tower and concentrated solution haptoreaction in tower after including flue gas supercharging, the flue gas going out concentration tower is sent into absorption tower and discharged by top, absorption tower after the reverse haptoreaction of circulating absorption solution of tower top spraying layer ejection；Concentrated solution after the partial reaction drawn at the bottom of concentration tower tower sends into ammonium sulfate crystallization system after iron removal system deironing, described flue gas is entered absorption tower by the smoke inlet in the middle part of absorption tower, is discharged by exhanst gas outlet after sequentially passing through at least one of which photochemical reaction layer of tower top setting, packing layer and spraying layer and the reverse haptoreaction of circulating absorption solution；The described circulating absorption solution by the ejection of top, absorption tower spraying layer enters the photochemical reaction layer of bottom, absorption tower and carries out photochemical reaction regeneration after sequentially passing through packing layer, photochemical reaction layer and the reverse haptoreaction of flue gas, the circulating absorption solution bottom absorption tower is transmitted back to the spraying layer on top, absorption tower as circulating absorption solution after filling into ammonia, chelating agent Fe (II) EDTA, oxalic acid and ferrous sulfate and sprays in tower.
Controlling Fe (II) EDTA+Fe (III) EDTA total concentration in the circulating absorption solution spraying in absorption tower is 0.015～0.05mol/L, and oxalate denominationby concentration is 0.09～0.3mol/L, and the pH value of circulating absorption solution is 5.0～5.5.
The liquid that absorbs entering concentration tower drawn bottom described absorption tower sends into the circulation ejection of concentration tower top with the concentrated solution of concentrated solution circulating pump extraction bottom concentration tower after mixing.
The concentrated solution entering iron removal system drawn bottom described concentration tower first sends into concentrating and precipitating pond precipitation, and after staticly settling, the suspension bottom concentrating and precipitating pond returns in absorption tower, and iron removal system sent into by the clear liquor of epimere.
Described photochemical reaction layer is made up of the cancellated light bar of multilamellar, and described light bar is connected with power supply through binding post.
The voidage of described cancellated light bar is 0.6-0.9.
Control the cancellated light bar of adjacent two layers alternately luminescence in the photochemical reaction layer of absorption tower epimere.
Described iron removal system is electrolysis deironing reactor.
The upper surface of the photochemical reaction layer of described absorption tower hypomere is concordant with liquid level at the bottom of tower.
The present invention adds oxalic acid to circulating absorption solution in the double tower synchronized desulfuring and denitrifying technique of existing composite ammonia-Fe (II) EDTA chelating agent, and oxalic acid can react generation ferric oxalate and Ferrox. with the iron ion absorbed in liquid and ferrous ion.Ferric oxalate and Ferrox. are the salt that oxalate denominationby is formed with ferrum and ferrous ion.
The structural formula of ferric oxalate is as follows: the structural formula of Ferrox. is as follows:
In aqueous, when having oxygen, Ferrox. is easily oxidized to ferric oxalate.Ferric oxalate can form stable ferric oxalate complexes in aqueous, and these complex have good photochemical activity, has relatively active redox characteristic, Fe therein under irradiation under ultraviolet ray3+It is reduced into Fe2+, oxalate is oxidized and generate H under photocatalysis2O2.The Fe that photo-reduction generates2+Again with H2O2Fenton reaction is occurred to produce OH and Fe3+, Fe3+Ferric oxalate complexes can be again formed again with oxalate denominationby.When solution exists excessive oxalate denominationby and H2O2Time, will constantly produce hydroxy radical OH, produce the quantum yield of OH free radical up to about 1.OH free radical is very strong oxidant, can be absorbed by rapid oxidationAnd NO.Oxalate denominationby is then constantly consumed with the carrying out of reaction, ultimately produces carbon dioxide.Inventor utilizes ferric oxalate Fenton-like characteristic in aqueous just, in conjunction with photochemical reaction, the NO absorbed is oxidized to nitrate anion to realize final elimination, simultaneously by oxidized Fe3+It is reduced into Fe2+, absorb Fe in liquid2+The rising of concentration, is conducive to the generation of Fe (II) EDTA, it is achieved the regeneration of chelating agent.Above-mentioned course of reaction is complicated many courses of reaction, research shows, absorb and liquid adds oxalic acid generation Ferrox. in conjunction with illumination reaction, the elimination of part nitrogen oxides can either be realized, iron chip filter can also be substituted and realize the regeneration of chelating agent Fe (II) EDTA, in present invention process, when Ferrox. and Fe (II) EDTA use simultaneously, it is possible not only to substitute traditional iron chip filter, that can also reduce Fe (II) EDTA makes consumption, and efficiency reduces the operating cost of system.
Based on above-mentioned principle, in order to improve denitration efficiency and circulating absorption solution regeneration efficiency, inventor has been arranged below photochemical reaction layer the original packing layer in top, absorption tower, illumination condition is manufactured in tower, its effect has three: a flue gas from the bottom to top through photochemical reaction layer, react with the circulating absorption solution generation chemical absorbing from top to bottom flowing through this layer, sulfur dioxide and nitrogen oxides in flue gas are absorbed, and there is also side reaction simultaneously: absorb complexes absorption Fe (II) EDTA in liquid,By the dioxygen oxidation in flue gas be Fe (III) EDTA,B, owing to photochemical reaction layer has the cancellated light bar of multilamellar, it is provided that effective illumination condition, contains in absorption liquidUnder photocatalysis, there is chemical reaction, 2 moleculesUltimately generate the Fe of 1 molecule2+With 1 hydroxy radical OH, in the further oxidative absorption liquid of hydroxy radical OH of generationAnd NO；The nitrogen oxides absorbed is oxidized, oxidized Fe3 +It is reduced, there is synchronizing regeneration effect；nullc，The cancellated light bar of multilamellar is similar to filling-material structure，Be conducive to the uniform and Homogeneous phase mixing of circulating absorption solution and flue gas，And extend flue gas and the circulating absorption solution gas-liquid contact time at this，Be conducive to the renewal of gas-liquid interface，Circulating absorption solution and flue gas react while regenerating，Further increase removal effect，In order to ensure regeneration effect，The voidage of preferred cancellated light bar is 0.6-0.9，Cross conference and cause that the specific surface area of gas-to-liquid contact is too small，Cause that tower effect is low，Too small meeting causes that gas phase drag increases，And the mode alternately luminous preferably by controlling the cancellated light bar of adjacent two layers，Absorption liquid can be made to be substantially carried out regenerative response in a luminous floor light bar district，Then it is substantially carried out absorption reaction in a non-luminous floor light bar district，Ensure efficiently carrying out of each reaction，Finally realize the purpose of high-efficiency desulfurization denitration.Experiments show that, adopt alternately luminous control mode higher than full-luminous control mode reaction efficiency and more energy-conservation.
Further, inventor is also also provided with photochemical reaction layer at bottom, absorption tower liquid level with lower part, to with smoke reaction after circulating absorption solution carry out further photochemical reaction regeneration, NO not oxidized in circulating absorption solution is oxidized further at this layer, further chelating agent is regenerated simultaneously.The upper surface of photochemical reaction layer is concordant with liquid level, is conducive to the abundant regeneration of Fe (III) EDTA, improves the cyclic absorption liquid measure of regeneration, also can avoid tower bottom simultaneously and perturb liquid at high speed turbulence that pump the causes impact wear to light bar.
Further, the partial concentration liquid entering iron removal system drawn bottom described concentration tower first sends into concentrating and precipitating pond precipitation, and after staticly settling, the suspension bottom concentrating and precipitating pond returns in absorption tower, and iron removal system sent into by the clear liquor of epimere.Adopt concentrating and precipitating pond by concentrated solution concentration layering, the suspension that bottom ferric oxalate content is high is sent in the circulating absorption solution on top, absorption tower as oxalic acid, the clear liquor of epimere is then sent into iron removal system and is carried out deironing, both the consumption of ferrum in solution can have been reduced, the burden of iron removal system can be alleviated again, improve the de-ironing efficiency of concentrated solution, reduce the iron content in side-product.
In the present invention, the amount of the ammonia, chelating agent, oxalic acid and the ferrous sulfate that fill into circulating absorption solution can fill into according to the requirement of ammonium sulfate concentrations, Fe (II) EDTA+Fe (III) EDTA total concentration, oxalate denominationby concentration and solution ph in circulating absorption solution, in line with damaging, and the principle mended.
Beneficial effect:
(1) adding oxalic acid in the composite synchronized desulfuring and denitrifying technique of flue gas ammonia and EDTA, owing to oxalic acid is a kind of stronger reducing agent, oxalic acid plays the dioxygen oxidation Fe suppressed in flue gas2+Effect, it is ensured that circulating absorption solution has Fe (II) EDTA of higher concentration, is conducive to denitration；Be easy to get owing to the market of oxalic acid is with low cost, have energy-saving and cost-reducing, reduce operating cost, simultaneously can reduce EDTA in chelating agent make consumption and loss amount.
(2) photochemical reaction layer is set on top, absorption tower, makes the circulating absorption solution that contact reverse with flue gas ABSORPTION EDGE regeneration in limit in photochemical reaction layer, improve the denitration efficiency to flue gas；Further adopt alternately luminous control mode higher than full-luminous control mode reaction efficiency and more energy-conservation, also improve the service life of light bar.
(3) it is also provided with photochemical reaction layer at absorption tower hypomere, oxidized further with NO not oxidized in the circulating absorption solution after smoke reaction, the chelating agent not being reproduced is regenerated further simultaneously.
(4) utilize concentrating and precipitating pond that concentrated solution carries out precipitated and separated, improve the response rate of ferrum, reduce the burden of iron removal system, improve the quality of side-product.
(5) adopting the inventive method that the NO absorbed can carry out oxidation to convert, denitration chelating agent carries out reducing/regenerating, desulfuration efficiency is up to more than 90%, and denitration efficiency is up to more than 50%, hence it is evident that be better than existing desulfurizing and denitrifying process.Present invention process is simple, easily operated, good reliability.
Accompanying drawing explanation
Fig. 1 present invention process flow chart.
Fig. 2 is the absorption oxidizing process schematic diagram that oxalic acid exists lower circulating absorption solution and flue gas.
Fig. 3 is the regenerative response Principle of Process figure of circulating absorption solution under illumination condition.
Wherein, 1-concentration tower, 2-absorption tower, 2.1-packing layer, 2.2-spraying layer, 2.3-scrubber layer, 2.4-photochemical reaction layer, 3-iron removal system, 4-crystal system, 5-concentrating and precipitating pond.
Detailed description of the invention
Embodiment:
Physical parameter and the relevant components of concentrated solution are as follows:
PH value: 5.0～5.5；
Ammonium sulfate concentrations: 20～45% (mass percents)；
Fe (II) EDTA+Fe (III) EDTA total concentration: 0.045～0.15mol/L；
Concentration of oxalic acid: 0.27～0.9mol/L；
Absorb liquid temp: 50-55 DEG C.
Physical parameter and the relevant components of circulating absorption solution are as follows:
PH value: 5.0～5.5；
Ammonium sulfate concentrations: 5～15% (mass percents)；
The total total concentration of Fe (II) EDTA+Fe (III) EDTA: 0.015～0.05mol/L；
Concentration of oxalic acid: 0.09～0.3mol/L；
Absorb liquid temp: 50 DEG C.
Referring to Fig. 1, in certain flue gas desulphurization system, exhaust gas volumn is 14～16Nm about3/ h, SO2Concentration: 800～1200mg/Nm3, NOx concentration (is mainly NO): 300～400mg/Nm3.What desulfurization adopted is double tower process.Enter concentration tower 1 top after flue gas is intensified, flow from top to bottom.With the concurrent biochemical absorption reaction of concentrated solution (containing ammonia) co-current contact being sent to the ejection of concentration tower top by tower 1 circulating pump that extract out at the bottom of tower, concentrated in flow process, absorb the sulfur dioxide in flue gas and nitrogen oxides, the most of granule in flue gas is washed simultaneously.
Flue gas stream in the middle part of concentration tower 1 after through connection flue introduce absorption tower 2 middle part, in absorption tower 2, flue gas flows to top of tower through at least one of which photochemical reaction layer 2.4 (being two-layer in the present embodiment), packing layer 2.1 and spraying layer 2.2 from the bottom to top, and last scrubbed layer 2.3 washs heel row further toward chimney.
The flue gas risen reacts (course of reaction principle is referring to Fig. 2) with the circulating absorption solution generation chemical absorbing from top to bottom sprayed out in photochemical reaction layer 2.4, and sulfur dioxide and nitrogen oxides in flue gas are absorbed；Due to the oxygen effect that flue gas carries, there is also simultaneously the Fe (II) in side reaction and circulating absorption solution, Fe (II) EDTA andBy the dioxygen oxidation in flue gas be Fe (III), Fe (III) EDTA andWherein the Fe (III) of oxidized generation reacts generation ferric oxalate complexes Fe (C further with the oxalate denominationby in circulating absorption solution2O4)+、WithDeng；Owing to circulating absorption solution is had regeneration effect by photochemical reaction layer 2.4, the nitrogen oxides and oxidized Fe (III) EDTA that are absorbed are reduced therewith, have synchronizing regeneration effect.
Circulating absorption solution carries out main following (course of reaction principle is referring to Fig. 3) of light-catalyzed reaction:
2 F e ( C 2 O 4 ) 3 3 - + h ν → 2 F e ( C 2 O 4 ) 2 2 - + C 2 O 4 2 - + 2 CO 2 - - - ( 1 )
In the solution of the saturation of the air, under acid conditionWithFurther with oxygen in water O2Reaction, ultimately forms H2O2。
Fe2++H2O2→Fe3+OH-+·OH(4)
2mol'sThe Fe of 1mol is generated after light-catalyzed reaction2+, consume the oxalate denominationby of 1mol, the hydroxy radical OH of 1mol, the NO that oxidative absorption gets off be provided simultaneously, owing to consuming oxalic acid root, Fe2+Generation broken the complexation equilibrium concentration of Fe (III) EDTA, generate Fe (II) EDTA, namely Fe (II) EDTA is regenerated.
Described photochemical reaction layer 2.4 is made up of the cancellated light bar of multilamellar, is connected with power supply through binding post, and described cancellated voidage controls at 0.6-0.9.The cancellated light bar of adjacent two layers alternately luminescence in the photochemical reaction layer 2.4 on top, preferred absorption tower 2 during operation.
With one layer of photochemical reaction layer 2.4 that the circulating absorption solution after smoke reaction flows down through bottom, absorption tower 2, carry out photochemical regeneration reaction further (also known as light-catalyzed reaction, course of reaction principle is referring to Fig. 2), improving the regeneration rate of circulating absorption solution, the upper surface of the photochemical reaction layer 2.4 of described absorption tower 2 hypomere is concordant with liquid level at the bottom of tower；The circulating absorption solution regenerated bottom absorption tower 2 sends into tower top through circulation, spraying layer 2.2 spray in tower.According to the concentration change situation of each component of circulating absorption solution, the chelating agent of consumption, oxalic acid, ammonia and ferrous sulfate can be filled in circulating absorption solution.
Draw bottom absorption tower 2 per hour after 6-9L serosity merges with the partial concentration liquid extracted out bottom concentration tower 1 and sprayed into by concentration tower 1 epimere, bottom concentration tower 1, discharged 2-3L serosity by concentration tower serosity excavationg pump per hour and enter concentrating and precipitating pond 5, 30-40 hour sedimentation time, supernatant enters iron removal system 3 (i.e. electrolysis deironing reactor, if number of patent application is 201520886784.2, denomination of invention is " a kind of oriented flow electrolysis unit ", can also be other electrolysis reactor being principle with electrolysis deironing), the alternative part oxalic acid of suspension that lower floor's ferric oxalate content is higher joins in circulating absorption solution and is sprayed in absorption tower 2 by spraying layer 2.2；
Concentrated solution after iron removal system deironing enters crystal system 4 and produces ammonium sulfate side-product, containing more Fe (III) EDTA in remaining solution after producing side-product, alternative part chelating agent is added in circulating absorption solution and sprays into regeneration in the tower of absorption tower 2.
Relating to the existing popular responses such as the ammonia process of desulfurization, Fe (II) EDTA complexation denitration and regenerative response in present invention process, its principle, compared with technology, is not described in detail here.NOx removal efficiency more than 50% in flue gas after said method processes, SO2Removal efficiency more than 90%.

Claims (9)

1. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect, including sending into concentration tower and concentrated solution haptoreaction in tower after flue gas supercharging, the flue gas going out concentration tower is sent into absorption tower and is discharged by top, absorption tower after the reverse haptoreaction of circulating absorption solution of tower top spraying layer ejection；The reacted concentrated solution of extension at the bottom of concentration tower tower sends into ammonium sulfate crystallization system after iron removal system deironing, it is characterized in that, described flue gas is entered absorption tower by the smoke inlet in the middle part of absorption tower, is discharged by exhanst gas outlet after sequentially passing through at least one of which photochemical reaction layer of tower top setting, packing layer and spraying layer and the reverse haptoreaction of circulating absorption solution；The described circulating absorption solution by the ejection of top, absorption tower spraying layer enters the photochemical reaction layer of bottom, absorption tower and carries out photochemical reaction regeneration after sequentially passing through packing layer, photochemical reaction layer and the reverse haptoreaction of flue gas, the circulating absorption solution bottom absorption tower is transmitted back to the spraying layer on top, absorption tower as circulating absorption solution after filling into ammonia, chelating agent Fe (II) EDTA, oxalic acid and ferrous sulfate and sprays in tower.
2. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as claimed in claim 1, it is characterized in that, controlling Fe (II) EDTA+Fe (III) EDTA total concentration in the circulating absorption solution spraying in absorption tower is 0.015～0.05mol/L, oxalate denominationby concentration is 0.09～0.3mol/L, and the pH value of circulating absorption solution is 5.0～5.5.
3. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as claimed in claim 1 or 2, it is characterized in that, the liquid that absorbs entering concentration tower drawn bottom described absorption tower sends into the circulation ejection of concentration tower top with the concentrated solution of concentrated solution circulating pump extraction bottom concentration tower after mixing.
4. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as claimed in claim 1, it is characterized in that, the concentrated solution entering iron removal system drawn bottom described concentration tower first sends into concentrating and precipitating pond precipitation, suspension bottom concentrating and precipitating pond returns in absorption tower, and iron removal system sent into by the clear liquor of epimere.
5. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as claimed in claim 1 or 2, it is characterised in that described photochemical reaction layer is made up of the cancellated light bar of multilamellar, and described light bar is connected with power supply through binding post.
6. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as claimed in claim 5, it is characterised in that the voidage of described cancellated light bar is 0.6-0.9.
7. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as described in claim 5 or 6, it is characterised in that control the cancellated light bar of adjacent two layers alternately luminescence in the photochemical reaction layer of absorption tower epimere.
8. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as claimed in claim 1, it is characterised in that described iron removal system is electrolysis deironing reactor.
9. the flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect as described in claim 1 or 5, it is characterised in that the upper surface of the photochemical reaction layer of described absorption tower hypomere is concordant with liquid level at the bottom of tower.
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