CN105879608A - Technology for synchronously denitrating ferrous oxalate on basis of flue gas desulfurization by aid of ammonia processes - Google Patents

Technology for synchronously denitrating ferrous oxalate on basis of flue gas desulfurization by aid of ammonia processes Download PDF

Info

Publication number
CN105879608A
CN105879608A CN201610255821.9A CN201610255821A CN105879608A CN 105879608 A CN105879608 A CN 105879608A CN 201610255821 A CN201610255821 A CN 201610255821A CN 105879608 A CN105879608 A CN 105879608A
Authority
CN
China
Prior art keywords
tower
flue gas
concentration
absorption
circulating
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.)
Granted
Application number
CN201610255821.9A
Other languages
Chinese (zh)
Other versions
CN105879608B (en
Inventor
吴晓琴
刘成
吴高明
张春桃
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.)
Wuhan University of Science and Engineering WUSE
Wuhan University of Science and Technology WHUST
Original Assignee
Wuhan University of Science and Engineering WUSE
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 Wuhan University of Science and Engineering WUSE filed Critical Wuhan University of Science and Engineering WUSE
Priority to CN201610255821.9A priority Critical patent/CN105879608B/en
Publication of CN105879608A publication Critical patent/CN105879608A/en
Application granted granted Critical
Publication of CN105879608B publication Critical patent/CN105879608B/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • 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
    • B01D53/73—After-treatment of removed components
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • 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
    • B01D2258/025—Other waste gases from metallurgy plants

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Sustainable Development (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Treating Waste Gases (AREA)
  • Catalysts (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention discloses a technology for synchronously denitrating ferrous oxalate on the basis of flue gas desulfurization by the aid of ammonia processes. The technology includes allowing flue gas to flow into a concentration tower, carrying out contact reaction on the flue gas and concentrated liquid in the tower, delivering flue gas from the concentration tower into the middle of an absorption tower, allowing the flue gas to upwardly flow through a packing layer and a spray layer which are arranged on the upper portion of the absorption tower, carrying out reverse contact reaction on the flue gas and circulating absorption liquid and then exhausting the flue gas from flue gas outlets; leading out partial concentrated liquid from the bottom of the concentration tower, removing iron in the partial concentrated liquid by the aid of an iron removal system, then delivering the partial concentrated liquid into an ammonium sulfate crystallization system, enabling circulating absorption liquid sprayed out of the spray layer on the upper portion of the absorption tower to sequentially flow though the packing layer on the upper portion of the tower, carrying out reverse contact reaction on the circulating absorption liquid and the flue gas, enabling the circulating absorption liquid to flow into the bottom of the absorption tower, delivering the circulating absorption liquid to a photocatalytic regeneration reaction system, regenerating circulating absorption liquid, enabling the circulating absorption liquid to flow into a regeneration slurry tank, feeding ammonia water, oxalic acid and ferrous sulfate into the regeneration slurry tank, then delivering the ammonia water, the oxalic acid and the ferrous sulfate which are used as circulating absorption liquid into the spray layer on the upper portion of the absorption tower and spraying the circulating absorption liquid into the tower. The technology has the advantages of simplicity, low running cost and energy consumption, simplicity and convenience in control, good denitrating effects and high quality of byproducts.

Description

Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique
Technical field
The present invention relates to field of Environment Protection one flue gas multiple pollutant and work in coordination with Processing tecchnics, specifically It is that a kind of ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique.
Background technology
Smelting iron and steel industry sintering circuit is SO in addition to coal-burning power plant2With the main source of NOx, Account for the 98% and 50% of integrated complex's total emission volumn, after sintering flue gas multiple pollutant Collaborative Control Treatment technology is still that the key of pollution prevention.Sintering smoke characteristic is that exhaust gas volumn greatly and changes Greatly；Dust content is big；SO2Discharge capacity and change in concentration are bigger；Cigarette temperature is low and fluctuation is big, and one As 120～180 DEG C, low-temperature sintering technology can as little as about 80 DEG C；Complicated component；Oxygen-containing containing wet Amount is big, respectively 15～18% and 7～13%.Three kinds of main pollutant consistence scopes are: SO2: 400～5000mg/Nm3；NOx:200～600mg/Nm3；Flue dust: 2000～6000mg/Nm3。 The most also discharge HF, HCl, various metals (Cd, Cr, Cu, Ni, Hg, Pb, Ti, V, Zn, Mn etc.), gas chromatography (CH, PAHs, PCBs, PCDD/Fs etc.) And the CO of volumetric concentration nearly 1%.
The above sintering smoke characteristic is also its difficulty in treatment, causes denitration mature technology SCR Can not adapt to completely sinter flue gas with SNCR method.Complicated sintering flue gas may result in catalyst and loses Living, produce the problems such as the escaping of ammonia, independent SCR and SNCR system produces in iron and steel enterprise Producing higher production cost in flow process, built sintering system does not reserves enough desulphurization denitration spaces etc. Factor, immediate constraint both denitration technologies application at sintering industry.Additionally steel industry Industrial concentration is more and more higher, and newly-built sintering machine area is increasing, actual energy large-scale application Little in the mature technology of sintering fume treatment.According to atmosphere pollution prevention and control requirement, sinter flue gas Improvement multi-pollutant to be carried out Collaborative Control, therefore research and develop clean and effective, be suitable for, big flow Multi-pollutant is worked in coordination with the sintering smoke gas treatment technology of improvement and sintering smoke pollution prevention and control is had weight Want meaning.
In flue gas and desulfurizing and denitrifying field, sintering system is had and well adapts to by wet process Property, just point out that Wet technique simultaneous SO_2 and NO removal is best desulfurization as far back as nineteen ninety Makansi One of denitration technology, be a kind of have potential clean and effective, be suitable for, many pollutions of big flow Thing works in coordination with the sintering smoke gas treatment technology of improvement, is also study hotspot and the difficult point of this area.
The most domestic about 526 sets, 7.8 ten thousand m2Knot machine flue gas has built up desulphurization system, tentatively realizes Sintering flue gas SO2Control.But sintering device flue gas denitration engineering is considerably less in global range, only have Denitration engineering the most only have demonstration and explore purpose.
In the aspect to sintering flue gas multiple pollutant Collaborative Control, Taiyuan Iron & Steel Corp in 2010 Two 450m2Sintering machine uses active carbon desulfurization denitration technology, is domestic first sintering cigarette Desulfurization denitration engineering, but the regenerating active carbon after denitration rate only 33%, and desulphurization denitration and pair The aspects such as Product recycling there is also many problems.
In Absorption via Chemical Complexation, that most study is exactly FeIIEDTA method, is used for sintering Wet ammonia process desulfurizing, carries out ammoniacal liquor/Fe on this basisIIEDTA compounding realization sintering flue gas is same Step desulphurization denitration, is that a kind of flue gas multiple pollutant that sinters with application prospect works in coordination with the skill of improvement Art.But owing to flue gas dividing, easily by the Fe in absorbing liquid containing a certain amount of oxygenIIEDTA aoxidizes, Cause denitration efficiency to decline, even lose denitration ability.So far, existing desulphurization denitration Technique deposits problems with:
(1) flue gas ammoniacal liquor/FeIIEDTA compounds the complexing agent regeneration technology of synchronized desulfuring and denitrifying, adopts With iron chip filter, iron filings consumption is big, and in absorbing liquid, iron concentration is too high, has both added except iron Cost, has an effect on desulphurization denitration byproduct quality.
(2) when using electrolytic regeneration, equipment investment is big, and it is big that regeneration runs power consumption, and regeneration runs Cost is high, and the denitration efficiency after regeneration is relatively low, less than 50%.
(3) synchronize denitration complexing agent FeIIEDTA is expensive, and consumption is relatively big, synchronizes denitration fortune Row cost is high.
Summary of the invention
The invention aims to solve above-mentioned technical problem, it is provided that a kind of technique is simple, fortune Row low cost, energy consumption are low, control is easy, denitration effect is good, byproduct matter is measured based on cigarette The ferrous oxalate of the gas ammonia process of desulfurization synchronizes denitrating technique.
Technical scheme includes that flue gas enters concentration tower and concentrate haptoreaction in tower, goes out concentration tower Flue gas send into and pass upward through packing layer that tower top arranges and spraying layer in the middle part of absorption tower and follow Discharged by exhanst gas outlet after the reverse haptoreaction of ring absorbing liquid；The part drawn at the bottom of concentration tower tower is dense Contracting liquid, described is sprayed by top, absorption tower except sending into ammonium sulfate crystallization system after iron through iron removal system The circulating absorption solution of layer ejection sequentially passes through packing layer and the reverse haptoreaction of flue gas on tower top Enter again after being delivered to the regeneration of Photocatalytic Regeneration reaction system by circulating pump bottom rear entrance absorption tower Raw slurry tank, then in recycled pulp liquid bath, fill into conduct circulation after ammoniacal liquor, oxalic acid and ferrous sulfate Absorbing liquid is transmitted back to the spraying layer on top, absorption tower and sprays in tower.
The circulating absorption solution mesoxalic acid concentration controlled in absorption tower is 0.09～0.3mol/L, iron Ion+ferrous ion concentration is 0.015～0.05mol/L, and the pH value of circulating absorption solution is 5.0～5.5.
Concentrate bottom the absorbing liquid entering concentration tower drawn bottom described absorption tower and concentration tower The circulation ejection of concentration tower top is sent into after the concentrate mixing that liquid circulating pump is drawn.
Concentrating and precipitating first sent into by the concentrate entering iron removal system drawn bottom described concentration tower Pond is precipitated, and the suspension bottom concentrating and precipitating pond sends into described Photocatalytic Regeneration reaction system, on Iron removal system sent into by the clarified solution of section.
Described Photocatalytic Regeneration reaction system is the photo catalysis reactor being provided with light source.
Described iron removal system removes iron reactor for electrolysis.
The present invention adds oxalic acid and sulphur to circulating absorption solution in existing double tower ammonia desulfurizing process Acid is ferrous, and oxalic acid and the iron ion in absorbing liquid and ferrous ion react generation ferric oxalate and oxalic acid Ferrous.Ferric oxalate and ferrous oxalate are the salt that oxalate denominationby is formed with iron and ferrous ion.
In aqueous, under conditions of having oxygen, ferrous oxalate is easily oxidized to ferric oxalate.Oxalic acid Iron can form stable ferric oxalate complexes in aqueous, and these complex compounds have good light Chemism, has relatively active redox characteristic under ultraviolet light irradiates.Fe therein3+ It is reduced into Fe2+, oxalate is oxidized and generate H under photocatalysis2O2.Photo-reduction is raw The Fe become2+Again with H2O2React generation OH and Fe3+, Fe3+Again can be with oxalate denominationby Re-form ferric oxalate complexes.As the oxalate denominationby and the H that there is excess in solution2O2Time, To constantly produce hydroxy radical OH, produce the quantum yield of OH free radical up to about 1. OH free radical is the strongest 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 Utilize ferric oxalate can produce the characteristic of OH free radical under photocatalysis, by under absorption just The NO come is oxidized to nitrate anion to realize final removing, simultaneously by oxidized Fe3+It is reduced into Fe2+.Fe in absorbing liquid2+The rising of concentration, is conducive to absorbing the NO in flue gas.Above-mentioned reaction Process is complicated many courses of reaction, and research shows, adds oxalic acid reaction raw in absorbing liquid Become ferrous oxalate to combine illumination reaction, the removing of part nitrogen oxides can either be realized.
Photocatalytic Regeneration reaction system in the present invention is photo catalysis reactor, photo catalysis reactor May utilize nature light by day to react, in the case of natural lighting condition deficiency, can open Opening the light source carried and carry out light-catalyzed reaction, described light source is the cancellated many of arranged crosswise Layer light belt.Reacted absorbing liquid is being sent into after photo catalysis reactor, absorbing liquid mesoxalic acid iron network Compound issues third contact of a total solar or lunar eclipse chemical reaction at illumination condition, produces hydroxy radical OH, is aoxidized by NO Become nitrate anion to realize final removing, Fe3+It is reduced into Fe2+, Fe in solution3+Concentration fall Low, Fe2+Concentration raise, it is achieved that the regeneration of ferrous oxalate.
Further, the partial concentration liquid entering iron removal system drawn bottom described concentration tower is first Sending into concentrating and precipitating pond precipitation, after staticly settling, the suspension bottom concentrating and precipitating pond is sent into Described Photocatalytic Regeneration reaction system, iron removal system sent into by the clarified solution of epimere.Use to concentrate and sink Concentrate is concentrated layering by pond, shallow lake, and the suspension that bottom ferric oxalate content is high sends into Photocatalytic Regeneration Reaction system regenerates, and the clarified solution of epimere is then sent into iron removal system and carries out except iron, both can subtract The consumption of iron in few solution, can alleviate again the burden of iron removal system, improves imitating except iron of concentrate Rate, reduces the iron content in byproduct.
In recycled pulp liquid bath, the amount of filling into of ammoniacal liquor, complexing agent, oxalic acid and ferrous sulfate can be according to following Fe (II)+Fe (III) total concentration, oxalate denominationby concentration and solution ph in ring absorbing liquid Requirement fills into, in line with damaging, and the principle mended.
Beneficial effect:
(1) in flue gas ammoniacal liquor sulfur removal technology, add ferrous oxalate, utilize ferrous oxalate Complexing, it is achieved that synchronized desulfuring and denitrifying.
(2) due to ferric oxalate, the complexing of NO being weaker than ferrous oxalate, oxalic acid plays suppression Dioxygen oxidation Fe in flue gas2+Effect, it is ensured that the concentration of denitration complexing agent, improve with Step denitration effect.
(3) utilize concentrating and precipitating pond precipitation that concentrate carries out precipitated and separated, improve returning of iron Yield and the utilization rate of oxalic acid, reduce the burden of iron removal system, improves the quality of byproduct.
(4) market of oxalic acid is with low cost is easy to get, and reduces operating cost.Oxalic acid has simultaneously Stronger reproducibility, when electrolysis is except iron, advantageously reduces decomposition voltage, reduces fortune further Row cost.
Accompanying drawing explanation
Fig. 1 present invention process flow chart.
Fig. 2 is circulating absorption solution and the absorption oxidizing process schematic diagram of flue gas in the presence of oxalic acid.
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-washing Layer, 3-iron removal system, 4-Photocatalytic Regeneration reaction system, 5-recycled pulp liquid bath, 6-concentrate heavy Pond, shallow lake, 7-crystal system.
Detailed description of the invention
Process example:
See Fig. 1, in certain flue gas desulphurization system, exhaust gas volumn about 14～16Nm3/ h, SO2Concentration: 500～800mg/Nm3, NOx concentration (predominantly NO): 300～400mg/Nm3.Desulfurization uses Be double tower process.
Physical parameter and the relevant components of concentrate are as follows:
PH value: 5.0～5.5；
Ammonium sulfate concentrations: 20～45% (mass percent)；
Fe (II)+Fe (III) total concentration: 0.045～0.15mol/L；
Concentration of oxalic acid: 0.27～0.9mol/L；
Absorbing liquid temperature: 50-55 DEG C.
Flue gas enters concentration tower 1 top, flows from top to bottom.Flow process is taken out with by the bottom of tower The concentrate (containing ammoniacal liquor) that tower 1 circulating pump that go out, concentrated is sent to the ejection of concentration tower top is suitable Concurrent biochemical absorption of stream contact is reacted, and absorbs the sulfur dioxide in flue gas and nitrogen oxides.
Flue gas flow in the middle part of concentration tower 1 after through connection flue introduce absorption tower 2 middle part, inhale In receiving tower 2, flue gas flows to top of tower through packing layer 2.1 and spraying layer 2.2 from the bottom to top, Last scrubbed layer 2.3 washs heel row further toward chimney.
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 percent)；
Fe (II)+Fe (III) total concentration: 0.015～0.05mol/L；
Concentration of oxalic acid: 0.09～0.3mol/L；
Absorbing liquid temperature: 50 DEG C.
The flue gas risen reacts with the circulating absorption solution generation chemical absorbing from top to bottom sprayed out, Sulfur dioxide and nitrogen oxides in flue gas are absorbed；The oxygen carried due to flue gas is made With, there is also ferrous oxidising one-tenth ferric iron in side reaction i.e. circulating absorption solution simultaneously, oxidized The ferric iron generated reacts generation ferric oxalate further with the oxalate denominationby in circulating absorption solution Complex compound Fe (C2O4)+、WithDeng.Owing to ferric oxalate complexes is to nitrogen oxygen The complexing power of compound is more weak, along with the increase of the ferric amount of ferrous oxidising one-tenth, absorbing liquid Gradually lose denitration ability.
In order to absorbing liquid is regenerated, it is ensured that denitration effect, the feeding tower drawn from tower bottom The circulating absorption solution on top is introduced into Photocatalytic Regeneration reaction system before entering tower.In photocatalysis again In raw reaction system, circulating absorption solution carries out the main as follows 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 conditionWithMolten with water further Solve oxygen O2Reaction, ultimately forms H2O2。
2mol'sLight-catalyzed reaction, consumes the oxalate denominationby of 1mol, generates 1mol Hydroxy radical OH, the NO that oxidative absorption gets off, generate the Fe of 1mol simultaneously2+, real The regeneration of existing circulating absorption solution.
Absorbing liquid after regeneration enters recycled pulp liquid bath 5, refers to according to the physical property of absorbing liquid after regeneration Mark requires to supplement ammoniacal liquor, oxalic acid and the ferrous sulfate of loss in recycled pulp liquid bath 5, then by following Ring is pumped into the spraying layer 2.2 on top, absorption tower and sprays in tower.
The portion extracted out bottom 6-9L slurries and concentration tower 1 is drawn per hour bottom absorption tower 2 Concentrate is divided to be sprayed into by concentration tower 1 epimere, per hour by concentrating bottom concentration tower 1 after merging Tower slurries excavationg pump is discharged 2-3L slurries and is entered concentrating and precipitating pond 6, sedimentation time 30-40 Hour, supernatant enters iron removal system 3, and (i.e. electrolysis is except iron reactor, as number of patent application is 201520886784.2, invention entitled " a kind of oriented flow electrolysis unit ", it is also possible to for it It with electrolysis except the iron electrolysis reactor as principle), higher suspended of lower floor's ferrous oxalate content Liquid alternative part oxalic acid joins in circulating absorption solution and is sprayed into absorption tower 2 by spraying layer 2.2 In；Ammonium sulfate byproduct is produced except the concentrate after iron enters crystal system 7 through iron removal system 3.

Claims (6)

1. ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes a denitrating technique, including flue gas Entering concentration tower and concentrate haptoreaction in tower, the flue gas going out concentration tower is sent in the middle part of absorption tower The packing layer passing upward through the setting of top, absorption tower inversely contacts with circulating absorption solution with spraying layer Discharged by exhanst gas outlet after reaction；Extension concentrate at the bottom of concentration tower tower removes iron through iron removal system Rear feeding ammonium sulfate crystallization system, it is characterised in that described by the ejection of top, absorption tower spraying layer Circulating absorption solution sequentially pass through the packing layer on tower top and enter after the reverse haptoreaction of flue gas Recycled pulp liquid is entered after being delivered to the regeneration of Photocatalytic Regeneration reaction system by circulating pump bottom absorption tower Groove, then fill in recycled pulp liquid bath after ammoniacal liquor, oxalic acid and ferrous sulfate as circulating absorption solution The spraying layer being transmitted back to top, absorption tower sprays in tower.
2. ferrous oxalate based on flue gas ammonia method desulfurizing as claimed in claim 1 synchronizes denitration Technique, it is characterised in that control the circulating absorption solution mesoxalic acid concentration in absorption tower be 0.09～ 0.3mol/L, iron ion+ferrous ion total concentration is 0.015～0.05mol/L, cyclic absorption The pH value of liquid is 5.0～5.5.
3. ferrous oxalate based on flue gas ammonia method desulfurizing as claimed in claim 1 or 2 synchronizes Denitrating technique, it is characterised in that the absorbing liquid entering concentration tower drawn bottom described absorption tower The concentrate drawn with concentrate circulating pump bottom concentration tower is sent into concentration tower top after mixing and is followed Ring spray goes out.
4. the ferrous oxalate based on flue gas ammonia method desulfurizing as described in claim 1 or 3 synchronizes Denitrating technique, it is characterised in that the concentration entering iron removal system drawn bottom described concentration tower Liquid first sends into concentrating and precipitating pond precipitation, and the suspension bottom concentrating and precipitating pond sends into described photocatalysis Regenerative response system, iron removal system sent into by the clarified solution of epimere.
5. the ferrous oxalate based on flue gas ammonia method desulfurizing as described in claim 1 or 3 or 4 Synchronize denitrating technique, it is characterised in that described Photocatalytic Regeneration reaction system is to be provided with light source Photo catalysis reactor.
6. the ferrous oxalate based on flue gas ammonia method desulfurizing as described in claim 1 or 4 synchronizes Denitrating technique, it is characterised in that described iron removal system removes iron reactor for electrolysis.
CN201610255821.9A 2016-04-22 2016-04-22 Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique Expired - Fee Related CN105879608B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610255821.9A CN105879608B (en) 2016-04-22 2016-04-22 Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610255821.9A CN105879608B (en) 2016-04-22 2016-04-22 Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique

Publications (2)

Publication Number Publication Date
CN105879608A true CN105879608A (en) 2016-08-24
CN105879608B CN105879608B (en) 2018-11-02

Family

ID=56704473

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610255821.9A Expired - Fee Related CN105879608B (en) 2016-04-22 2016-04-22 Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique

Country Status (1)

Country Link
CN (1) CN105879608B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110090548A (en) * 2019-04-11 2019-08-06 昆明理工大学 A kind of method that copper ashes tailing cooperates with the wet desulphurization of zinc abstraction dedusting ash and recycles zinc sulfate

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5840651A (en) * 1993-11-19 1998-11-24 Mitsui Mining Co., Ltd. Process for the production of activated coke for simultaneous desulfurization and denitrification
CN104226095A (en) * 2014-07-30 2014-12-24 武汉悟拓科技有限公司 Synchronous denitration process based on wet ammonia process flue gas desulfurization
CN105413418A (en) * 2015-11-09 2016-03-23 武汉科技大学 Electrolytic regeneration based simultaneous desulfurization and denitrification reaction tower

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5840651A (en) * 1993-11-19 1998-11-24 Mitsui Mining Co., Ltd. Process for the production of activated coke for simultaneous desulfurization and denitrification
CN104226095A (en) * 2014-07-30 2014-12-24 武汉悟拓科技有限公司 Synchronous denitration process based on wet ammonia process flue gas desulfurization
CN105413418A (en) * 2015-11-09 2016-03-23 武汉科技大学 Electrolytic regeneration based simultaneous desulfurization and denitrification reaction tower

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
张婷等: "Fe(Ⅲ)草酸盐络合物的光化学性质及其应用", 《江西化工》 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110090548A (en) * 2019-04-11 2019-08-06 昆明理工大学 A kind of method that copper ashes tailing cooperates with the wet desulphurization of zinc abstraction dedusting ash and recycles zinc sulfate
CN110090548B (en) * 2019-04-11 2021-11-30 昆明理工大学 Method for wet desulphurization and zinc sulfate recovery of copper slag tailings and zinc smelting fly ash

Also Published As

Publication number Publication date
CN105879608B (en) 2018-11-02

Similar Documents

Publication Publication Date Title
CN102824844B (en) Desulfurization and denitrification agent, preparation method and application thereof
CN103706238B (en) System and method for removing SO2, NO and Hg in smoke on the basis of heterogeneous Fenton
CN104226095B (en) Based on the synchronous denitrating technique of flue gas wet ammonia process desulfurizing
CN105854560A (en) Flue gas desulfurization and denitration method
CN102836636B (en) Desulfurization denitration composition, preparation method and application thereof
CN103230734A (en) Method for combined removal of sulfur dioxide and nitrogen oxide in flue gas
CN105107340A (en) Desulfurization, denitrification and demercuration integration apparatus based on amino absorber and method therefor
CN112742190B (en) Complexing denitration process capable of recycling
CN105233687A (en) Method for removing elemental mercury in coal-fired flue gas
CN102824843B (en) Combined removal device and method for sulphur, mercury and nitrate in smoke
CN105833724B (en) Regenerated sintering flue gas synchronized desulfuring and denitrifying technique is coupled based on optical-electronic class fenton
CN103432879B (en) The method of the ferrous flue gas desulfurization and denitrification of hypergravity complexing
CN102836634B (en) Desulfurization denitration method
CN111330442B (en) Ammonia process catalysis combined desulfurization and denitrification method
CN104028103A (en) Method for catalyzing and oxidizing boiler smoke gas through chlorine dioxide and simultaneously desulfurizing and denitrating boiler smoke gas
CN105344215B (en) A kind of flue gas pollutant collaboration based on electrolysis removes technique
CN107485997A (en) A kind of flue gas multiple pollutant cooperation-removal system and method
CN105879608B (en) Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique
CN103432889B (en) The method of the ferrous denitrating flue gas of hypergravity complexing
CN104190227B (en) Synchronization denitrating system based on flue gas wet ammonia process desulfurizing
CN103432878B (en) The method of hypergravity complexing ferrous smoke-gas wet desulfurization denitration demercuration arsenic integration
CN105833725B (en) A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing
CN203648372U (en) System for combined removal of SO2, NO and Hg from smoke based on heterogeneous Fenton
CN105854558B (en) A kind of sintering flue gas synchronized desulfuring and denitrifying technique
CN113648812A (en) Integrated removal system and method for mercury and nitrate through photoelectric synergistic catalytic oxidation and wet-process absorption

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20181102

Termination date: 20210422