CN105833725B - A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing - Google Patents
A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing Download PDFInfo
- Publication number
- CN105833725B CN105833725B CN201610255823.8A CN201610255823A CN105833725B CN 105833725 B CN105833725 B CN 105833725B CN 201610255823 A CN201610255823 A CN 201610255823A CN 105833725 B CN105833725 B CN 105833725B
- Authority
- CN
- China
- Prior art keywords
- tower
- flue gas
- layer
- complexing agent
- concentration
- 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.)
- Active
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
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
- B01D53/74—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
Abstract
The invention discloses a kind of synchronization denitration complexing agent regeneration technologies based on flue gas ammonia method desulfurizing, concentration tower and concentrate haptoreaction in tower are sent into after being pressurized including flue gas, the flue gas for going out concentration tower is sent into absorption tower, the flue gas enters absorption tower by the smoke inlet in the middle part of absorption tower, is discharged after at least one layer of photochemical reaction layer, packing layer and the spraying layer of the setting of tower top and the reverse haptoreaction of circulating absorption solution by exhanst gas outlet successively；The circulating absorption solution sprayed by absorption tower top spraying layer enters absorb the bottom of the tower after packing layer, photochemical reaction layer and the reverse haptoreaction of flue gas successively, enter recycled pulp liquid bath after being pumped to the regeneration of Photocatalytic Regeneration reaction system by cycle again, then fill into ammonium hydroxide, complexing agent, oxalic acid and ferrous sulfate as circulating absorption solution in slurry tank is regenerated and be transmitted back in the spraying layer penetrating tower on absorption tower top.Present invention process is simple, operating cost is low, low energy consumption, control is easy, denitration effect is good, byproduct is high-quality.
Description
Technical field
The present invention relates to a kind of flue gas ammonia process synchronized desulfuring and denitrifying techniques of field of environment protection, specifically a kind of to be based on cigarette
The synchronization denitration complexing agent regeneration technology of the gas ammonia process of desulfurization.
Background technology
China's flue gas desulfurization and denitrification technology is started late, but with the appearance of tightened up environmental protection measure, flue gas desulfurization
Denitration is imperative.Flue gas and desulfurizing and denitrifying technological development has been included in " 863 " Major Research Plan by the Ministry of Science and Technology.
In recent years, China was more active to the research of desulfurization and denitrification integral technology, although most new processes are also in development in laboratory
With the pilot scale stage, but some technical matters have obtained larger improvement.Simultaneous SO_2 and NO removal technology can be in same set of system
Interior realization desulfurization and denitration, have the characteristics that：1. equipment is simplified, floor space is small.Traditional joint flue gas desulfurization and denitrification work
Skill is usually De-NO_x such as selective catalytic reduction (SCR) or selective non-catalytic reduction before deduster
(SNCR), so as to fulfill combined desulfurization and denitration.Not only equipment is more for this classification administration way, but also takes up a large area, not as good as
The equipment for realizing desulfurization and denitration simultaneously in same set of system is simplified.2. capital expenditure is few, production cost is low.Flue gas simultaneous desulfurization
Denitration technology can realize desulfurization and denitration in same set of system, and a large amount of capital expenditures are needed unlike traditional handicraft, reduce
Production run cost.3. high degree of automation, management is convenient.Due to realizing the integration of desulphurization denitration in same set of system,
It is brought conveniently to equipment management.To adapt to the demand of present and following Air Pollution Control, the new skill of simultaneous SO_2 and NO removal is developed
Art, new equipment are increasingly becoming one of the developing direction in Air Pollution Control field.
Traditional Wet Flue Gas Desulfurization Technique can remove SO：Up to more than 90%, then with SCR dry processes combine, two kinds of techniques because
Worked independently using different technologies, there are scale of investment it is big, of high cost the problem of.It is found that early in Sada in 1986 and partner
Some metal complexes, such as Fe (II) EDTA can rapidly be reacted with NO, can promote the absorption of nitride.These are wet type FGD+
The design of metal complex technique has prepared condition.Wet type FGD+ metal complex techniques are that ferrous iron is added in nonacidic solutions
Ion forms the amino hydroxy acid ferrous chelate compounds such as Fe (II) EDTA.NO can be in combination into ferrous nitrosyl complex, so as to add
The fast absorption rate of NO, while ferrous nitrosyl complex can be with the SO that is dissolved in solution2Reaction generation N2, a series of N, Sization
Close object etc..But Fe (II) EDTA cleaning solutions can be inactivated gradually, cause regeneration of absorption solution complicated, which is also in experiment rank
Section.In this regard, some researchers by the NO in the renewable ferrous cysteine Solution for Simultaneous Removal gas of experiment discussion and
SO2, removal efficiency when finding 20min is respectively 82.3% and 94.4%.Ferrous cysteine complexometry can not only remove NO and
SO2, and cystine can be reduced into cysteine and reaction cycle is enable to carry out, and show certain application potential.
Iron system and cobalt system complex compound are preferable to the complexing of NO.Although Fe (II) EDTA and ferrous cysteine are at the same time
Certain application potential is shown, but since EDTA and cysteine are expensive in terms of desulphurization denitration, to desulfurization simultaneously
Denitration brings larger cost pressure.So seek the highly efficient regeneration of complexing agent, the conversion of NO, release complexing agent in the liquid phase,
It is the key that realize simultaneous SO_2 and NO removal that effective process cycle is stablized in foundation.
Invention content
Present invention offer one kind is simple for process, operating cost is low, low energy consumption, control is easy, denitration effect is good, by-product quality
A kind of measured synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing, solves revival in the prior art
The low problem of rate.
Technical solution is sent into concentration tower and concentrate haptoreaction in tower after including flue gas supercharging, and the flue gas for going out concentration tower is sent
Enter absorption tower with being discharged after the reverse haptoreaction of circulating absorption solution that tower top spraying layer sprays by absorption tower top；Concentration tower
Concentrate after the partial reaction that bottom of towe is drawn is through iron removal system except ammonium sulfate crystallization system is sent into after iron, the flue gas is by absorbing
Smoke inlet in the middle part of tower enters absorption tower, successively by tower top setting at least one layer of photochemical reaction layer, packing layer and
Spraying layer after the reverse haptoreaction of circulating absorption solution by exhanst gas outlet with being discharged；It is described to be followed by what absorption tower top spraying layer sprayed
Ring absorbing liquid enters absorb the bottom of the tower after packing layer, photochemical reaction layer and the reverse haptoreaction of flue gas successively, then by following
After ring is pumped to the regeneration of Photocatalytic Regeneration reaction system, then ammonium hydroxide, complexing agent, oxalic acid and sulfuric acid Asia are filled into slurry tank is regenerated
The spraying layer for being transmitted back to absorption tower top after iron as circulating absorption solution is sprayed into tower.
Control spray into the circulating absorption solution in absorption tower Fe (II) EDTA+Fe (III) total concentration for 0.015~
0.05mol/L, a concentration of 0.09~0.3mol/L of oxalate denominationby, the pH value of circulating absorption solution is 5.0~5.5.
What the absorbing liquid into concentration tower that the absorb the bottom of the tower is drawn was drawn with concentration tower bottom concentrate circulating pump
Concentration tower top cycle is sent into after concentrate mixing to spray.
The concentrate into iron removal system that the concentration tower bottom is drawn first is sent into concentrating and precipitating pond precipitation, concentrating and precipitating
The suspension in bottom of pond portion is sent into the Photocatalytic Regeneration reaction system, and the clarified solution of epimere is sent into iron removal system.
The photochemical reaction layer is made of the light bar of multilayer network structure, and the light bar is connect through binding post with power supply.
The voidage of the light bar of the reticular structure is 0.6-0.9.
The light bar of adjacent two layers reticular structure in the photochemical reaction layer of absorption tower epimere is controlled alternately to shine.
The Photocatalytic Regeneration reaction system is the photo catalysis reactor equipped with light source.
The iron removal system is electrolysis except iron reactor.
The present invention is in the double tower synchronized desulfuring and denitrifying technique of existing compounding ammonia-Fe (II) EDTA complexing agents to cyclic absorption
Liquid adds in oxalic acid, and oxalic acid can react generation ferric oxalate and ferrous oxalate with the iron ion in absorbing liquid and ferrous ion.Ferric oxalate
It is the salt that oxalate denominationby is formed with iron and ferrous ion with ferrous oxalate.
In aqueous solution, ferrous oxalate is easily oxidized to ferric oxalate under conditions of having oxygen.Ferric oxalate in aqueous solution may be used
Stable ferric oxalate complexes are formed, these complex compounds have good photochemical activity, have under ultraviolet light relatively living
The redox characteristic of jump, Fe therein3+It is reduced into Fe2+, oxalate aoxidized under photocatalysis and generates H2O2.Light
Restore the Fe of generation2+Again with H2O2It reacts and generates OH and Fe3+, Fe3+Ferric oxalate can be re-formed with oxalate denominationby again
Complex compound.When the oxalate denominationby and H that there is excess in solution2O2When, hydroxy radical OH will be constantly generated, generates OH certainly
By the quantum yield of base up to 1 or so.OH free radicals are very strong oxidants, and energy rapid oxidation is absorbed what is got offWith
NO.Oxalate denominationby is then constantly consumed with the progress of reaction, ultimately produces carbon dioxide.Inventor is exactly to be existed using ferric oxalate
The characteristic of OH free radicals can be generated under photocatalysis, the NO absorbed is oxidized to nitrate anion to realize final removing,
The Fe that will be aoxidized simultaneously3+It is reduced into Fe2+.Fe in absorbing liquid2+The raising of concentration is conducive to the generation of Fe (II) EDTA, realizes
The regeneration of complexing agent.Above-mentioned reaction process is a complicated more reaction process, research shows that, oxalic acid is added in circulating absorption solution
Reaction generation ferrous oxalate combination illumination reaction, can either realize the removing of part nitrogen oxides, moreover it is possible to substitute iron chip filter realization
The regeneration of complexing agent Fe (II) EDTA, in present invention process, when ferrous oxalate and Fe (II) EDTA complexing agents be not simultaneously in use,
Traditional iron chip filter can be only substituted, the usage amount of Fe (II) EDTA complexing agents can also be reduced, effectively reduces the operation of system
Cost.
Based on above-mentioned principle, in order to improve denitration efficiency and circulating absorption solution regeneration efficiency, inventor is on absorption tower top
The lower section of original packing layer is provided with photochemical reaction layer, and illumination condition is manufactured in tower, and effect has three：A flue gases by down toward
During upper process photochemical reaction layer, chemical absorbing occurs with the circulating absorption solution for from top to bottom flowing through this layer and reacts, in flue gas
Sulfur dioxide and nitrogen oxides are absorbed, while also there are side reactions：Complexes absorption Fe (II) EDTA in absorbing liquid,Be Fe (III) EDTA by the dioxygen oxidation in flue gas,B, since photochemical reaction layer is with more
The light bar of layer reticular structure, provides effective illumination condition, contains in absorbing liquidUnder photocatalysis,
It chemically reacts, 2 moleculesUltimately generate the Fe of 1 molecule2+With 1 hydroxy radical OH, generation
Hydroxy radical OH, in further oxidative absorption liquidAnd NO；The nitrogen oxides absorbed is aoxidized, and is aoxidized
Fe3+It is reduced, there is synchronizing regeneration effect；C, the light bar of multilayer network structure are similar to filling-material structure, are conducive to cyclic absorption
Liquid being evenly distributed with and uniformly mixing, and extend flue gas and circulating absorption solution gas-liquid contact time in this with flue gas, is conducive to gas
The update at liquid interface, circulating absorption solution are regenerated with flue gas while reacting, and further improve removal effect.
In order to ensure regeneration effect, the preferably voidage of the light bar of reticular structure is 0.6-0.9, and crossing conference leads to gas-liquid
The specific surface area of contact is too small, causes tower effect low, too small gas phase drag to be caused to increase, and preferably by controlling adjacent two layers
The mode that the light bar of reticular structure alternately shines can make absorbing liquid be substantially carried out regenerative response in a luminous floor light bar area,
Then absorbing reaction is substantially carried out in non-luminous floor light bar area, ensures the efficient progress of each reaction, final realize efficiently takes off
The purpose of sulphur denitration.Experiment shows using alternately luminous control mode than full-luminous control mode reaction efficiency higher, and
It is more energy saving.
Photocatalytic Regeneration reaction system in the present invention is photo catalysis reactor, and photo catalysis reactor is on daytime using certainly
Right light is reacted, insufficient in natural lighting condition, can be opened included light source and be carried out light-catalyzed reaction, the light
Multilayer optical band of the source for the reticular structure of arranged crosswise.Absorbing liquid after reaction is after photo catalysis reactor is sent into, cyclic absorption
Liquid mesoxalic acid iron complex issues raw Photochemical redox reaction, Fe in illumination condition3+It is reduced into Fe2+, while generation has
The NO absorbed is oxidized to nitrate anion to realize final removing by the hydroxy radical OH of strong oxidizing property.Fe3+It is reduced into Fe2 +, Fe in solution2+Concentration raising, broken Fe3+With the complexation equilibrium of EDTA, Fe (III) EDTA concentration reduces, Fe (II)
EDTA concentration increases, and realizes the regeneration of Fe (II) EDTA, and the iron chip filter of traditional iron filings tower is replaced using photo catalysis reactor,
It reduces except iron cost, avoids that iron filings consumption is big, the dense generation from excessively high problem of iron ion in absorbing liquid, improve byproduct
Quality.
Further, the partial concentration liquid for being sent to iron removal system that the concentration tower bottom is drawn first is sent into concentrating and precipitating pond
Precipitation, after staticly settling, the suspension in concentrating and precipitating bottom of pond portion is sent into the Photocatalytic Regeneration reaction system, the clarification of epimere
Liquid is sent into iron removal system.Concentrate is concentrated using concentrating and precipitating pond and is layered, oxalic acid iron content high suspension in bottom is as grass
Acid is filled by Photocatalytic Regeneration reaction system in circulating absorption solution, and the clarified solution of epimere is then sent into iron removal system and is carried out except iron,
Not only the consumption of iron in solution can have been reduced, but also the burden of iron removal system can be mitigated, has improved the de-ironing efficiency of concentrate, has reduced byproduct
In iron content.
The amount of filling into that ammonium hydroxide in slurry tank, complexing agent, oxalic acid and ferrous sulfate are regenerated in the present invention can be according to cyclic absorption
The requirement of ammonium sulfate concentrations in liquid, Fe (II) EDTA+Fe (III) concentration, oxalate denominationby concentration and solution ph is filled into,
In line with damaging, the principle mended.
Advantageous effect：
(1) oxalic acid is added in flue gas ammonium hydroxide and Fe (II) EDTA compounding synchronized desulfuring and denitrifying techniques, since oxalic acid is
A kind of stronger reducing agent, oxalic acid play the dioxygen oxidation Fe inhibited in flue gas2+Effect, ensure that absorbing liquid have it is more highly concentrated
Fe (II) EDTA of degree, is conducive to denitration；Be easy to get since the market of oxalic acid is of low cost, have it is energy-saving, reduce operation into
Sheet while the usage amount and loss amount that EDTA in complexing agent can be reduced.
(2) photochemical reaction layer is set on absorption tower top, the circulating absorption solution for making inversely to contact with flue gas is in photochemistry
Side ABSORPTION EDGE regenerates in conversion zone, improves the denitration efficiency to flue gas；It is further complete using alternately luminous control mode ratio
Luminous control mode reaction efficiency higher, and it is more energy saving, also improve the service life of light bar.
(3) it is precipitated using concentrating and precipitating pond and precipitated and separated is carried out to concentrate, improve the rate of recovery of iron, reduce iron removal system
Burden, improve the quality of byproduct.
(4) the suspension oxalic acid concentration of iron in concentrating and precipitating bottom of pond portion is high, into Photocatalytic Regeneration reaction system, improves again
Come into force fruit and denitration efficiency.
(5) oxidation conversion can be carried out to the NO absorbed using the method for the present invention, denitration complexing agent is restored again
Raw, denitration efficiency is up to more than 50%.Present invention process is simple, easily operated, good reliability.
Description of the drawings
Fig. 1 present invention process flow charts.
Fig. 2 is the absorption oxidation process schematic diagram of circulating absorption solution and 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 towers, 2- absorption towers, 2.1- packing layers, 2.2- spraying layers, 2.3- scrubber layers, 2.4- photochemistry are anti-
Answer layer, 3- iron removal systems, 4- Photocatalytic Regenerations reaction system, 5- regeneration slurry tank, 6- concentrating and precipitatings pond, 7- crystal systems.
Specific embodiment
Embodiment：
Referring to Fig. 1, in certain flue gas desulphurization system, exhaust gas volumn about 14~16Nm3/ h, SO2Concentration：800~1200mg/Nm3,
NOx concentration (predominantly NO)：300~400mg/Nm3.Desulfurization is using double tower process.Flue gas enters concentration tower 1 after supercharging
Top is flowed from top to bottom.It is sprayed in flow process with being sent at the top of concentration tower by bottom of towe extraction, concentrated 1 circulating pump of tower
The concurrent biochemical absorbing reaction of concentrate (contain ammonium hydroxide) co-current contact, absorb the sulfur dioxide and nitrogen oxides in flue gas, together
When most of particle in flue gas is washed.
The physical parameter and relevant components of concentrate are as follows：
PH value：5.0~5.5；
Ammonium sulfate concentrations：20~45% (mass percents)；
EDTA-Fe (II)+EDTA-Fe (III) concentration：0.045~0.15mol/L；
Concentration of oxalic acid：0.27~0.9mol/L；
Absorbing liquid temperature：50-55 DEG C.
Flue gas flows to the middle part through connection flue introducing absorption tower 2 behind 1 middle part of concentration tower, and flue gas is under in absorption tower 2
Supreme at least one layer of photochemical reaction layer 2.4 (being two layers in the present embodiment), packing layer 2.1 and the spraying layer 2.2 of passing through is to tower top
Portion is flowed, and last washed layer 2.3 further washs heel row toward chimney.
The physical parameter and relevant components of circulating absorption solution are as follows：
PH value：5.0~5.5；
Ammonium sulfate concentrations：5~15% (mass percents)；
EDTA-Fe (II)+EDTA-Fe (III) total concentration：0.015~0.05mol/L；
Concentration of oxalic acid：0.09~0.3mol/L；
Absorbing liquid temperature：50℃.
In photochemical reaction layer 2.4 with the circulating absorption solution from top to bottom sprayed out chemical absorbing occurs for the flue gas of rising
It reacts (reaction process principle is referring to Fig. 2), the sulfur dioxide and nitrogen oxides in flue gas are absorbed；It is carried due to flue gas
Oxygen acts on, at the same also there are Fe (II), Fe (II) EDTA in side reaction, that is, circulating absorption solution andBy cigarette
Dioxygen oxidation in gas for Fe (III), Fe (III) EDTA andIt is wherein further by the Fe (III) of oxidation generation
Generation ferric oxalate complexes Fe (C are reacted with the oxalate denominationby in circulating absorption solution2O4)+、With
Deng；Since 2.4 pairs of circulating absorption solution of photochemical reaction layer have regeneration effect, by nitrogen oxides that absorption is got off and aoxidized
Fe (III) EDTA is reduced therewith, has synchronizing regeneration effect (reaction process principle is referring to Fig. 3).
Circulating absorption solution carries out the main as follows of light-catalyzed reaction：
In the solution of the saturation of the air, under acid conditionWithFurther with oxygen in water O2Reaction, finally
Form H2O2。
Fe2++H2O2→Fe3+OH-+·OH (4)
2mol'sThe Fe of 1mol is generated after light-catalyzed reaction2+, the oxalate denominationby of 1mol is consumed, is carried simultaneously
For the NO that the further oxidative absorptions of hydroxy radical OH of 1mol get off, due to consuming oxalic acid root, Fe2+Generation broken Fe
(III) the complexation equilibrium concentration of EDTA, generation Fe (II) EDTA, i.e. Fe (II) EDTA are regenerated.
The photochemical reaction layer 2.4 is made of the light bar of multilayer network structure, is connect through binding post with power supply, the net
The voidage of shape structure is controlled in 0.6-0.9.Adjacent two layers in the photochemical reaction layer 2.4 on preferred 2 top of absorption tower during operation
The light bar of reticular structure alternately shines.
In absorption tower lower part, absorbing liquid from the circulation fluid absorbing liquid of tower lower part is drawn by recycled pulp liquid pump and enters photocatalysis
Regenerative response system 4 (to be equipped with the photo catalysis reactor of light source), can be by sunlight, and auxiliary light irradiates, cyclic absorption
In liquidCarry out light-catalyzed reaction：2mol'sThe Fe of 1mol is generated after light-catalyzed reaction2+, consumption
The oxalate denominationby of 1mol, while the hydroxy radical OH, the NO that further oxidative absorption gets off of 1mol are provided.Due to consumption grass
Acid group and Fe3+, Fe in solution2+Concentration raising, broken Fe3+With the complexation equilibrium of EDTA, Fe (III) EDTA concentration drop
Low, Fe (II) EDTA concentration increases, and realizes the regeneration of complexing agent Fe (II) EDTA.
Per hour from 2 bottom of absorption tower draw 6-9L slurries merge with the partial concentration liquid that 1 bottom of concentration tower is extracted out after by
1 epimere of concentration tower sprays into, and drawing 2-3L slurries from 1 bottom of concentration tower per hour enters concentrating and precipitating pond 6, sedimentation time 30-
40 hours, supernatant enters iron removal system 4, and (i.e. electrolysis was except iron reactor, such as number of patent application are 201520886784.2, invent
Entitled " a kind of oriented flow electrolysis unit ", or other electrolysis reactors to be electrolysed except iron as principle), lower floor's oxalic acid
The higher suspension of iron content is transmitted back to Photocatalytic Regeneration reaction system 4.
Regeneration slurry tank 5 is sent by the slurries of 4 Base top contact of Photocatalytic Regeneration reaction system, is mended into regeneration slurry tank 5
Enter the ammonium hydroxide, complexing agent (Fe (II) EDTA), oxalic acid of consumption to meet the related property parameter request of circulating absorption solution, finally send
Enter spraying layer 2.2 to spray into absorption tower 2；Through iron removal system 3 ammonium sulfate by-product is produced except the concentrate after iron enters crystal system 7
Product contain EDTA in remaining solution, can loopback Photocatalytic Regeneration reaction system 4.
The ammonia process of desulfurization, Fe (II) EDTA complexing existing popular responses such as denitration and regenerative response involved in present invention process,
Its principle is not described in detail here compared with technology.Through NOx removal efficiency 50% in the above method treated flue gas with
On, SO2More than 90% removal efficiency.
Claims (7)
1. a kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing, be sent into after being pressurized including flue gas concentration tower with
Concentrate haptoreaction in tower, flue gas feeding absorption tower and the circulating absorption solution sprayed from tower top spraying layer for going out concentration tower are inverse
By being discharged at the top of absorption tower after haptoreaction；Concentrate after the reaction of concentration tower bottom of towe extension is through iron removal system except after iron
It is sent into ammonium sulfate crystallization system, which is characterized in that the flue gas enters absorption tower by the smoke inlet in the middle part of absorption tower, passes through successively
Cross tower top setting at least one layer of photochemical reaction layer, packing layer and spraying layer and the reverse haptoreaction of circulating absorption solution after by
Exhanst gas outlet is discharged；The circulating absorption solution sprayed by absorption tower top spraying layer is successively by packing layer, photochemical reaction
Layer with the reverse haptoreaction of flue gas after enter absorb the bottom of the tower, then by cycle be pumped to Photocatalytic Regeneration reaction system regeneration it is laggard
Enter and regenerate slurry tank, then ammonium hydroxide, complexing agent, oxalic acid and ferrous sulfate are filled into as circulating absorption solution loopback in slurry tank is regenerated
Spraying layer to absorption tower top is sprayed into tower；The photochemical reaction layer is made of the light bar of multilayer network structure, the lamp
Band is connect through binding post with power supply；Control the light bar alternating of adjacent two layers reticular structure in the photochemical reaction layer of absorption tower epimere
It shines.
2. a kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing as described in claim 1, feature exist
In it is 0.015~0.05mol/L that control, which sprays into Fe (II) EDTA+Fe (III) total concentration in the circulating absorption solution in absorption tower, careless
A concentration of 0.09~0.3mol/L of acid ion, the pH value of circulating absorption solution is 5.0~5.5.
3. a kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing as claimed in claim 1 or 2, feature
It is, the concentration that the absorbing liquid into concentration tower that the absorb the bottom of the tower is drawn is drawn with concentration tower bottom concentrate circulating pump
Concentration tower top cycle is sent into after liquid mixing to spray.
4. a kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing as described in claim 1, feature exist
In the concentrate into iron removal system that the concentration tower bottom is drawn first is sent into concentrating and precipitating pond precipitation, concentrating and precipitating bottom of pond
The suspension in portion is sent into the Photocatalytic Regeneration reaction system, and the clarified solution of epimere is sent into iron removal system.
5. a kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing as described in claim 1, feature exist
In the voidage of the light bar of the reticular structure is 0.6-0.9.
6. the synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing as described in claim 1 or 3 or 4, feature
It is, the Photocatalytic Regeneration reaction system is the photo catalysis reactor equipped with light source.
7. a kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing as described in claim 1, feature exist
In the iron removal system is electrolysis except iron reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610255823.8A CN105833725B (en) | 2016-04-22 | 2016-04-22 | A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610255823.8A CN105833725B (en) | 2016-04-22 | 2016-04-22 | A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105833725A CN105833725A (en) | 2016-08-10 |
| CN105833725B true CN105833725B (en) | 2018-07-06 |
Family
ID=56590185
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610255823.8A Active CN105833725B (en) | 2016-04-22 | 2016-04-22 | A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105833725B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112742190B (en) * | 2020-12-11 | 2022-08-05 | 攀钢集团攀枝花钢铁研究院有限公司 | Complexing denitration process capable of recycling |
| CN112717694B (en) * | 2020-12-11 | 2022-08-05 | 攀钢集团攀枝花钢铁研究院有限公司 | Regeneration method of ineffective complexing denitration agent |
Citations (3)
| 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 |
| CN102247748A (en) * | 2011-06-30 | 2011-11-23 | 湖北省宏源药业有限公司 | Treatment method and treatment system of tail gas from glyoxylic acid production by nitric acid oxidation of glyoxal |
| 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 |
-
2016
- 2016-04-22 CN CN201610255823.8A patent/CN105833725B/en active Active
Patent Citations (3)
| 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 |
| CN102247748A (en) * | 2011-06-30 | 2011-11-23 | 湖北省宏源药业有限公司 | Treatment method and treatment system of tail gas from glyoxylic acid production by nitric acid oxidation of glyoxal |
| 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 |
Non-Patent Citations (2)
| Title |
|---|
| Fe(Ⅲ)草酸盐络合物的光化学性质及其应用;张婷等;《江西化工》;20081231;第26-29页 * |
| 化学吸收-生物还原法处理烟气主氮氧化物—Fe(Ⅱ)Cit的吸收及其生物还原特性研究;姜锦林;《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》;20080915;第27页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105833725A (en) | 2016-08-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104226095B (en) | Based on the synchronous denitrating technique of flue gas wet ammonia process desulfurizing | |
| CN106621796B (en) | Method and device for simultaneously removing carbonyl sulfide and carbon disulfide | |
| CN105854560A (en) | Flue gas desulfurization and denitration method | |
| CN201333376Y (en) | Flue gas desulfurization and denitration purifying device | |
| JP2016515936A (en) | Absorption medium, method for producing absorption medium, and method and apparatus for separating hydrogen sulfide from acid gas | |
| CN102658021A (en) | Advanced technology and device for integrating oxidation catalysis, desulfurization and denitrification | |
| CN104524935B (en) | Single tower type double-cycle spray composite absorption device and method | |
| CN205653162U (en) | System for sulphuric acid is prepared to sulphur waste liquid that contains that utilizes coal gas wet oxidation process to produce | |
| CN105833725B (en) | A kind of synchronization denitration complexing agent regeneration technology based on flue gas ammonia method desulfurizing | |
| CN104096462A (en) | Novel technology for yellow phosphorus tail gas purification | |
| CN105833724B (en) | Regenerated sintering flue gas synchronized desulfuring and denitrifying technique is coupled based on optical-electronic class fenton | |
| CN105032173A (en) | Device and process of ammonia-soda-process combined desulfurization and denitrification | |
| CN111330442B (en) | Ammonia process catalysis combined desulfurization and denitrification method | |
| CN105502302A (en) | Method and system for preparing smelting flue gas into sulphur | |
| CN105268294A (en) | Double-tower double-circulation wet oxidation and catalysis combined removal system and method | |
| CN109529578A (en) | The process unit and process of hydrogen sulfide and sulfur dioxide liquid phase reactor desulfurization | |
| CN104190227B (en) | Synchronization denitrating system based on flue gas wet ammonia process desulfurizing | |
| CN104028103A (en) | Method for catalyzing and oxidizing boiler smoke gas through chlorine dioxide and simultaneously desulfurizing and denitrating boiler smoke gas | |
| CN110252090A (en) | A method of sodium sulfite sulfur removal technology absorptive capacity and utilization rate are improved using triethanolamine | |
| CN202700350U (en) | Device for desulfurizing flue gas by using sodium-calcium dual alkali method | |
| CN106379916B (en) | Desulphurizing activated coke parses smoke recycling and utilizes method | |
| CN105879608B (en) | Ferrous oxalate based on flue gas ammonia method desulfurizing synchronizes denitrating technique | |
| CN105854558B (en) | A kind of sintering flue gas synchronized desulfuring and denitrifying technique | |
| CN105771651B (en) | Flue gas ammonia process synchronized desulfuring and denitrifying technique based on Fenton-like effect | |
| CN105879607B (en) | A kind of flue gas ferrous oxalate denitrating technique of Photocatalytic Regeneration |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20171107 Address after: 430083, Hubei Wuhan Qingshan District Factory No. 2 Gate joint stock company organs Applicant after: Wuhan iron and Steel Company Limited Applicant after: Wuhan University of Science and Technology Address before: 430083 Qingshan District, Hubei, Wuhan Applicant before: WUHAN IRON AND STEEL CORPORATION Applicant before: Wuhan University of Science and Technology |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |