CN203253338U - Flue gas desulphurization and denitration integrated device - Google Patents
Flue gas desulphurization and denitration integrated device Download PDFInfo
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- CN203253338U CN203253338U CN2013201504976U CN201320150497U CN203253338U CN 203253338 U CN203253338 U CN 203253338U CN 2013201504976 U CN2013201504976 U CN 2013201504976U CN 201320150497 U CN201320150497 U CN 201320150497U CN 203253338 U CN203253338 U CN 203253338U
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Abstract
The utility model discloses a flue gas desulphurization and denitration integrated device. The device comprises a desulfurizer, a denitrator, a demister, a doctor solution intermediate tank, a denitration solution intermediate tank, a doctor solution oxidation tank, a denitration solution oxygen supplementation tank, an ammonium sulfate solution concentrator, an ammonium sulfate mother solution crystallization tank, an ammonium sulfate crystallization centrifugal machine, an ammonium sulfate drier and a self-suction injector. According to the device, a wet process is adopted to remove sulfur dioxide and nitrogen oxides from flue gas at the same time in the same process system, no sulfur-containing or ammonia nitrogen-containing waste liquid is discharged outside during the whole process. The device realizes integration of desulphurization and denitration, is miniaturized, and discharges no waste liquid during the whole technological process.
Description
Technical field
The utility model relates to fire coal, the living flue gas of oil burning boiler burning, and the desulphurization denitration process field of the catalytic cracked regenerated flue gas of oil plant, the sulfuric acid tail gas process field of gas washing in SA production, chemical fertilizer production vent gas treatment etc. contains the exhaust-gas treatment field of sulfur dioxide, nitrogen oxide component.Be specifically related to a kind of flue gas desulfurization and denitrification integrated apparatus.
Background technology
Along with the fast development of China's economy, the increase of industrial pollution source and corresponding legislations of environmental protection are more and more stricter.Promote simultaneously the progress of environmental improvement science and technology, produced large quantities of environomental pollution source improvement technology.Wherein the relevant flue gas technology that removes sulfur dioxide, nitrogen oxide has been developed a variety of techniques, but these technical functionality characteristics only nearly all are for single kind of component.Technology removing aspect the sulfur dioxide of flue gases has ammonia process, lime-gypsum method, and two alkaline process, the soda method is such as sodium-hydroxide method or magnesium hydroxide method etc.The technology of denitration aspect has dry method, the selective catalytic reduction method of dry method main technique (SCR), and SNCR method (SNCR), and SCR-SNCR mixes reducing process.The common feature of dry method is as reducing agent with ammonia.Difference is that the SCR method is to mix by catalytic bed, wherein nitrogen oxide (NO+NO with ammonia under 350～390 ℃ of flue-gas temperatures
2) become nitrogen and aqueous vapor with ammonia by the oxygen components redox in the flue gas.Reaction equation is:
4NH
3+ 4NO+O
2==4N
2+ 6H
2O, or
4NH
3?+3NO?+O
2?==?6N
2?+?6H
2O，
And the SNCR method be in the catalyst-free flue-gas temperature under 900～1250 ℃ condition, spray into reducing agent ammonia or urea, redox reaction occurs under the flue gas oxygen content effect, nitrogen oxide is reduced to nitrogen and aqueous vapor.Reaction equation is:
4NO?+NH
3?+O
2?==N
2?+?H
2O，
SCR-SNCR mixing method is to utilize the reducing agent of anterior SNCR method escape as the reducing agent of rear portion SNCR method.Twice denitration operation denitration efficiency reaches the highest, finally can reach more than 80%.
Except the dry method denitration, also have energetic plasma oxidizing process, absorption method, wet method etc.The problems such as SCR method denitration efficiency is relatively high, and commercial Application is more extensive, but has construction investment and operating cost height, and catalyst is easy inactivation because of dust-laden, and the escapement ratio of ammonia is wayward.SNCR method commercial Application is also more extensive, without catalyst, adopts ammonia or urea as the reducing agent of nitrogen oxide, requires NH
3/ NOx mol ratio is not less than 2～2.3, and denitration efficiency just can reach 30～50%, at high temperature reacts, and also has the escapement ratio problem of ammonia, and ammonia react has the generation of side reaction product NOx under the high temperature, causes the secondary pollution source.
Although energetic plasma oxidizing process denitration efficiency effect is high, energy consumption is higher, and cost of equipment is relatively more expensive, and operating cost is high, the disadvantages affect such as maintenance of equipment expense height its in industrial application.
Absorption method technique is fairly simple, but the adsorbent consumption is large, and the adsorption plant capacity is also very large, the complicated difficulty of adsorbent reactivation, and the equipment operating resistance is large, and the denitration that therefore is not suitable for large-scale flue gas is processed.
The wet denitration technology also has a variety of processes, and alkali absorption method is arranged, sour absorption process, oxidation absorption process, Reducing and absorption method, Absorption via Chemical Complexation, microbial method etc.
Alkali absorption method is the method with alkaline solution absorbing NOxes such as potassium, sodium, magnesium, ammoniums.But NO dissolubility in the aqueous solution is very low, and alkali lye can only absorb the NO that is dissolved in the water
2, so alkali absorption method can only to be applicable to NOx content higher, or do not contain NO or the very low gas of NO content.Therefore it is very low alkali absorption method to be used for denitrating flue gas efficient.
The acid absorption process is to utilize acid solution to absorb NO+NO
2, nitrogen oxide is easy to be dissolved in the acid solution, can also generate nitrous acid sulfuric acid with strong sulfuric acid response, but can not generate nitrous acid sulfuric acid with the dilute sulfuric acid reaction.Need the concentrated sulfuric acid owing to absorb, therefore be not suitable for industrial-scale production.
The oxidation absorption process is to utilize oxidant that NO is oxidized to NO
2Or NOx, oxidant commonly used has ozone, hydrogen peroxide, and hydrogen peroxide, sodium chlorite, clorox, potassium permanganate, nitric acid etc. are oxidized to NOx with NO first, then change into nitrate anion and generate nitrate.The oxidation absorption process can be oxidized to NOx with NO effectively, but accessory substance is nitrate, and chlorate etc. are harmful to water quality environment.In addition, the oxidant consumption expense is higher, gives birth to section's cost height, and accessory substance is corrosive to equipment.Therefore limitation is deposited in the application of oxidation absorption process.
The Reducing and absorption method is to utilize gas phase or liquid phase catalytic oxidation effect that NO partial oxygen in the flue gas is changed into NO
2Or NOx, then NO
2Or NOx and NO reaction generation N
2O
4Or N
2O
3Be reduced at last N
2And water.Reducing agent commonly used has sulphite, thiosulfate, the aqueous solution of the compounds such as urea.
Absorption via Chemical Complexation is to utilize the liquid complexing absorbent directly the NO of indissoluble to be transferred to liquid phase with complex form from gas phase, improves NO in the solubility of liquid phase.The NO reduction generates simple substance nitrogen in the complex compound when adding reducing agent in liquid phase, generates salt and be fixed up when in the solution alkali compounds being arranged.The complexed absorption law technology is in the research and development stage at present, and still industrialization is realized at the end, the realization desulfurization and denitrification integral and reach higher efficient but this method can combine reduction with oxidizing process, so Absorption via Chemical Complexation is a kind of very promising technology.
Various denitration technologies more than comprehensive remove the dry method denitration technology and have realized that large scale industry is outside the pale of civilization, and still the end is extensive for the at present application of liquid phase denitration technology, and main cause is except denitration efficiency is not so good as dry method SCR method height, and function singleness is confined to denitration.And the oxidant that adopts, the absorbent price comparisons such as reducing agent are expensive, and the low difficulty that reclaims of product concentration in solution, stay in the solution ambient water quality is produced secondary pollution.But wet method liquid phase denitrating technique plant construction expense is lower, and operating cost is also low than dry method, and operating condition is also looser.Therefore, the research of the exploitation of wet method liquid phase denitration technology and desulfurization and denitrification integral technology is very valuable and problem technical prospect.
The utility model content
Goal of the invention: for the deficiencies in the prior art, the purpose of this utility model provides a kind of flue gas desulfurization and denitrification integrated apparatus, flue gas is removed sulfur dioxide and remove nitrogen oxide (NO+NOx) and be integrated in the system, adopt wet type liquid desulfuration denitrating technique, desulfurization and denitration associating, discharging any waste liquor not, not outer waste air reaches zero-emission.
Technical scheme: in order to realize the foregoing invention purpose, the technical solution adopted in the utility model is as follows:
A kind of flue gas desulfurization and denitrification integral method: in same process system, adopt wet processing simultaneously flue gas to be removed sulfur dioxide (SO
2) and remove nitrogen oxide (NO+NOx); The ammonia fertilizer method is adopted in desulfurization, and the nertralizer of ammoniacal liquor while as the accessory substance nitric acid of sulphur dioxide desulfurizing agent and denitrating technique generation uses; Oxidation-reduction method is adopted in denitration, makes nitrogen oxide (NO+NO with desulfurizing byproduct sulfurous acid ammonium salt or ammonium bisulfite
2) be reducing agent, and add urea as reducing agent, to contain quinone-hydroxy compounds as catalyst, be blown into air to the denitration circulation fluid, for the oxidation reaction of nitric oxide (NO) provides dissolved oxygen and oxidant; Denitration reaction by-product ammonium salt imports doctor solution and reclaims nitrogenous ammonium salt; Reclaim ammonia nitrogen chemistry fertilizer ammonium sulfate and ammonium nitrate, and full technical process is not discharged sulfur-bearing or is contained the ammonia nitrogen waste liquid outside system.
Ammonium sulfite or sulphur hydracid ammonium and air are adopted in described nitric oxide production oxidation, and ammonium sulfite or ammonium hydrogen sulfate are from ammonia fertilizer method desulphurization circulating liquid, and air is filled into the dissolved oxygen that then generates with the hydrogen peroxide form under catalyst action by oxygen complementation device.
Described catalyst is a kind of soluble compound that contains quinone-hydroxyl, can change into the quinone based compound, photosensitive article thing from hydroxy compounds under the oxygen effect, and dissolved oxygen and water can be changed into peroxide water.
The whereabouts of denitration reaction rich solution is to be blended into to participate in generating nitrogenous nitrogenous fertilizer in the doctor solution.
Described desulfurization reactor and Benitration reactor equipment adopt the hypergravity bed, and two hypergravity beds can independently divide and are arranged, also can be superimposed on same axis.
A kind of flue gas desulfurization and denitrification integrated apparatus comprises devulcanizer, denitrator, demister, doctor solution medial launder, denitration liquid medial launder, doctor solution oxidation trough, denitration liquid oxygenating groove, ammonium sulfate inspissator, ammonium sulfate liquor crystallization tank, ammonium sulfate crystallization centrifuge, ammonium sulfate drier and self-adsorption ejector; Described devulcanizer communicates with denitrator by flue gas pipeline; Described denitrator communicates with demister by pipeline; Described devulcanizer communicates with the doctor solution medial launder by the solution circulation pipeline, establishes circulating pump at the solution circulation pipeline; Described doctor solution medial launder communicates with the doctor solution oxidation trough, and described doctor solution oxidation trough communicates with flue gas pipeline; Described doctor solution oxidation trough communicates with ammonium sulfate inspissator, ammonium sulfate liquor crystallization tank, ammonium sulfate crystallization centrifuge and ammonium sulfate drier successively by pipeline; Being equipped with return line at described ammonium sulfate liquor crystallization tank and ammonium sulfate crystallization centrifuge communicates with the doctor solution medial launder; Described denitrator communicates with the denitration liquid medial launder by pipeline; Described denitration liquid medial launder communicates with self-adsorption ejector and denitration liquid oxygenating groove successively by pipeline; Described denitration liquid oxygenating groove communicates with denitrator by pipeline; Described denitration liquid medial launder communicates with the doctor solution medial launder by pipeline; Described demister communicates with the denitration liquid medial launder by pipeline.
The integrated method of flue gas desulfurization and denitrification of the present utility model, flue gas to be removed sulfur dioxide and removes nitrogen oxide (NO+NOx) be integrated in the system, adopt wet type liquid desulfuration denitrating technique, sulfur dioxide remove employing ammoniacal liquor-ammonium salt process, it is reducing agent that removal of nitrogen oxide adopts urea, with the compound that contains quinone-hydroxyl as for electric reduction catalyst, catalyst can be tannin extract or naphthoquinone sulfonic acid salt, be blown into the dissolved oxygen content that air improves solution to solution, mix sulfur removing pregnant solution to denitration solution, increase denitration solution and contain NH
4HSO
3, (NH
4)
2SO
3Or SO
2Etc. the reproducibility compound, the denitration rich solution is entered the remaining urea of recovery and ammonium nitrate in the desulfuration solution, final nitrogen pool and the output that increases chemical fertilizer, sulfur removing pregnant solution oxidized waste air returns oxidation and the dissolubility that flue gas increases the favourable raising of Oxygen Amount in Flue Gas NO, not discharging any waste liquor is united in desulfurization and denitration, not outer waste air reaches zero-emission.
The flue gas desulfurization and denitrification principle is as follows:
(1) desulfurization unit main chemical reactions
The dissolving of ammonia in desulfuration solution:
NH
3?+NH
4HSO
3?==（NH
4）
2SO
3，
NH
3?+NH
4HSO
4?==（NH
4）
2SO
4，
Doctor solution ammoniacal liquor and ammonium salt solution sulfur dioxide absorption:
NH
3·H
2O?+SO
2?==NH
4HSO
3，
（NH
4）
2SO
3?+H
2O?+?SO
2?==2NH
4HSO
3，
（NH
4）
2SO
4?+?SO
2?+?H
2O?==?2?NH
4HSO
3，
Urea and nitric acid reclaim and change into ammonium salt:
HNO
3?+?NH
3?=NH
4NO
3，
2（NH
2）
2CO?+?4H
2O?+4?SO
2?+?O
2?==?4NH
4SO
3?+?2CO，
Sulfite oxidation becomes ammonium sulfate:
（NH
4）
2SO
3?+?O
2?==（NH
4）
2SO
4，
NH
4HSO
3?+?O
2?==NH
4HSO
4，
NH
4HSO
4?+NH
3?=（NH
4）
2SO
4，
(2) denitration unit main chemical reactions:
The reduction-state catalyst absorbs the reaction of oxygen generation oxidation regeneration, and generates active oxygen:
Reduction-state (RQ-OH)+0.5O
2==oxidation state (RQ=O)+H
20
2,
Oxidized catalyst oxygen supply oxidation NO:
The adding of catalyst improves the dissolving of air oxygen amount in denitration liquid, promotes oxidation and the dissolving of NO.
Oxidation state (RQ=O)+NO+H
2O==reduction-state (RQ-OH)+NO
2,
Active oxygen is to the NO oxidation:
NO?+?H
2O
2?==NO
2?+?H
2O，
2NO
2?+H
2O?=?HNO
2?+?HNO
3，
2NO
2?==N
2O
2，
NO?+?NO
2?==N
2O
3，
N
2O
3?+H
2O?==2HNO
2，
N
2O
2?+H
2O?==HNO
2?+?HNO
3，
The reduction reaction of reproducibility compound:
The reducing agent that the ammonium sulfite that generates in denitration adding reducing agent urea and the doctor solution or ammonium bisulfite have oxidation susceptibility to nitrogen oxide, nitrogen oxide is reduced to nitrogen, carbon dioxide, and generate ammonium salt.Extract part solution and be blended into the denitration circulation fluid from circulation desulfurization liquid, its purpose is exactly for replenishing and increase denitrification reducing agent, the reduction reaction efficient of nitrogen oxide being improved.
（NH
2）
2CO?+?HNO
2?==2N
2?+CO
2?+?3H
20，
4（NH
4）
2SO
3?+?2NO
2?==4（NH
4）
2SO
4?+?N
2，
2（NH
4）
2SO
3?+2NO?==?2（NH
4）
2SO
4?+?N
2，
4NH
4HSO
3?+?2NO
2?==?4NH
4HSO
4?+?N
2，
2NH
4HSO
3?+?2NO?==?2NH
4HSO
4?+?N
2。
Oxidation reaction in the oxygenating groove:
2HNO
2?+?O
2?==?2HNO
3，
HNO
3?+?NH
3?==NH
4NO
3，
2NH
4HSO
3?+?O
2?==?2NH
4HSO
4，
2（NH4）
2SO
3?+?O
2?==?2（NH
4）
2SO
4。
Beneficial effect: compared with prior art, advantage of the present utility model comprises: 1) adopt to contain quinone-hydroxy compounds as oxidation reduction catalyst, improve meltage and the nitric oxide production oxygenation efficiency of air oxygen in denitration solution; 2) utilize the sulfurous acid ammonium salt in the desulfuration solution to improve nitrogen oxide (NO+NO as the reducing agent of denitration
2) reduction efficiency; 3) the denitration rich solution is added desulfurization and follows liquid and reclaim nitric acid, ammonium nitrate and remaining urea in the denitration waste liquid, and so that technical process efflux without waste liquid; 4) desulfurization and denitrification integral is integrated into the technical process that removes two differential responses conditions of sulfur dioxide and nitrogen oxide in one individual system, connects each other and non-interference; 5) the desulfurization and denitrification reaction device adopts hypergravity bed surrogate response tower, implement device miniaturization.
Description of drawings
Fig. 1 is the structural representation of flue gas desulfurization and denitrification integrated apparatus.
The specific embodiment
Below in conjunction with specific embodiment the utility model is further described.
A kind of flue gas desulfurization and denitrification integrated apparatus; as shown in Figure 1; flue gas A removes the solid particle ash content through sack cleaner in advance, and temperature carries out entering flue gas desulfurization device 1 about a heat exchange to 100 ℃ when 150 ℃ of left and right sides, and devulcanizer 1 adopts hypergravity bed or tower absorbing device.Add ammoniacal liquor D to doctor solution medial launder 4,, with pump doctor solution C circulation is pressed into devulcanizer 1 sulfur dioxide absorption gas and generates ammonium bisulfite or ammonium sulfite as desulfuration solution with ammonium salt solution.Flow into doctor solution medial launder 4 from devulcanizer 1 behind the desulfuration solution washing smoke absorption sulfur dioxide.After replenishing ammoniacal liquor D, doctor solution medial launder 4 desulphurization circulating liquid send devulcanizer 1 washing flue gas back to through circulating pump again.When doctor solution ammonium salt-containing concentration during at 350～450g/L, the extension rich solution is delivered to doctor solution oxidation trough 6 behind the pump of circulating pump, air blast is blown into air F to doctor solution oxidation trough 6 simultaneously, at the oxidized ammonium sulfate normal salt that changes into of the sour ammonium acid salt in doctor solution oxidation trough 6 interior Asias.Oxidizing reaction temperature is controlled at 60～80 ℃, to improve conversion rate of oxidation.The oxidation solution P of doctor solution oxidation trough 6 pumps with pump and is concentrated into ammonium sulfate concentrations to ammonium sulfate inspissator 8 usefulness low-pressure heating vapour X heating evaporations and reaches more than 50%.Concentrate being delivered to ammonium sulfate liquor crystallization tank 9 usefulness cooling water W cooling makes the mother liquor crystallization and grows up in crystallization tank again.At last crystalline mother solution is sent into ammonium sulfate crystallization centrifuge 10 isolation of crystalline and filtrate, filtrate L and Jie Jing Cao Full flow out together foldback doctor solution medial launder 4 of rare crystalline mother solution Z.The ammonia sulfate crystal that centrifugation goes out send ammonium sulfate drier 11 usefulness low-pressure steam X thermal dehydrations dry, obtains commodity ammonium sulfate products S.
In addition, the doctor solution M that extracts the last oxidation of part out behind circulating pump delivers to the additional denitrification reducing agent of denitration solution system.
Send into again denitrator 2 through the flue gas after the devulcanizer 1 desulfurization processing, adopt denitration circulation fluid washing smoke absorption nitrogen oxide (NO+NOx).The denitration circulation fluid consists of oxidation, dissolving and the reduction reaction of finishing the flue gas oxynitrides by components such as catalyst, denitrification reducing agent urea and sulfurous acid ammonium salts.Flue gas after the denitration leaves and enters demister 3 behind the denitrator 2 and remove the liquid foam of carrying secretly, discharges at last system.Rich solution after denitration absorbs flows into denitration liquid medial launder 5, takes out force feed through recycle liquid pump again and enters the dissolved oxygen content that self-adsorption ejector 12 air amount F and denitration liquid are blended in denitration liquid oxygenating groove 7 oxidation regeneration catalyst and increase denitration liquid.Then pump denitration liquid I to denitrator 2 continuous washing flue gases with the denitration liquid circulating pump from denitration liquid oxygenating groove 7.Tell simultaneously part denitration liquid N behind the pump and be returned to doctor solution medial launder 4 to reclaim the ammonia nitrogen resource.The off-air that denitration liquid oxygenating groove 7 is discharged imports demister 3 front flues and flue gas converges the system that together discharges.Denitrating catalyst K and reducing agent U add denitration liquid medial launder 5.
Desulphurization reaction operation control solution (NH
4)
2SO
3/ NH
4HSO
3About concentration ratio 2:1, pH value keeps solution to the absorbability of sulfur dioxide about 6～8.Desulfurization absorption operation temperature is controlled in 70～90 ℃ of scopes.Oxidizing reaction temperature is controlled in 65～75 ℃ of scopes, the speed that keeps oxidation to answer.Total ammonia concentration in the solution is in 350～450g/L scope.
The denitration reaction operating temperature is controlled in 70～85 ℃ of scopes, and pH value is in 5.5～6.5 scopes.Urea concentration is about 15～20% in the solution.Catalyst concn is in 20～60mg/L scope.
This flue gas desulfurization and denitrification integral method is simultaneously flue gas to be removed sulfur dioxide (SO in a process system
2) and remove nitrogen oxide (NO+NOx).Adopt wet processing, ammonia fertilizer method technique is adopted in desulfurization, with ammoniacal liquor as sulphur dioxide desulfurizing agent, the nertralizer of the accessory substance nitric acid that produces as denitrating technique.Oxidation-reduction method technique is adopted in denitration, makes nitrogen oxide (NO+NO with desulfurizing byproduct sulfurous acid ammonium salt or ammonium bisulfite
2) be reducing agent, and add urea as reducing agent.To contain quinone-hydroxy compounds as catalyst, be blown into air to the denitration circulation fluid, for the oxidation reaction of nitric oxide (NO) provides dissolved oxygen and oxidant.Denitration reaction by-product ammonium salt imports doctor solution and reclaims nitrogenous ammonium salt.Full technical process is not discharged sulfur-bearing or is contained the ammonia nitrogen waste liquid outside system.Reclaim ammonia nitrogen chemistry fertilizer ammonium sulfate and ammonium nitrate.Oxidation-reduction method is adopted in denitration.Add urea as the reducing agent of nitrogen oxide, ammonium sulfite or sulphur hydracid ammonium and air are adopted in nitric oxide production oxidation, ammonium sulfite or ammonium hydrogen sulfate are from ammonia fertilizer method desulphurization circulating liquid, and air is filled into the dissolved oxygen that then generates with the hydrogen peroxide form under catalyst action by oxygen complementation device.In addition, together enter denitrification apparatus behind the solution oxygen complementation device and behind the residue of the off-air behind the sulfite oxidation device oxygen remittance flue gas.The required oxygen of oxidation of nitric oxide reaction is by the catalytic action of the catalyst that adds denitration solution, this catalyst is a kind of soluble compound that contains quinone-hydroxyl, this catalyst can change into the quinone based compound, photosensitive article thing from hydroxy compounds under the oxygen effect, and dissolved oxygen and water can be changed into peroxide water.Peroxide water has oxidisability to nitric oxide, and this quinone based compound, photosensitive article thing can transmit charge energy and have reproducibility.The whereabouts of denitration reaction rich solution is to be blended into to participate in generating nitrogenous nitrogenous fertilizer in the doctor solution.Therefore the ammonium nitrate waste liquid final sum desulfurization waste liquor that contains of denitrating technique process generation converges production nitrogenous fertilizer.Desulfurization reactor and Benitration reactor equipment adopt the hypergravity bed.Two reactors can independently divide and are arranged, also can be superimposed on same axis.
Claims (1)
1. a flue gas desulfurization and denitrification integrated apparatus is characterized in that: comprise devulcanizer (1), denitrator (2), demister (3), doctor solution medial launder (4), denitration liquid medial launder (5), doctor solution oxidation trough (6), denitration liquid oxygenating groove (7), ammonium sulfate inspissator (8), ammonium sulfate liquor crystallization tank (9), ammonium sulfate crystallization centrifuge (10), ammonium sulfate drier (11) and self-adsorption ejector (12); Described devulcanizer (1) communicates with denitrator (2) by flue gas pipeline; Described denitrator (2) communicates with demister (3) by pipeline; Described devulcanizer (1) communicates with doctor solution medial launder (4) by the solution circulation pipeline, establishes circulating pump at the solution circulation pipeline; Described doctor solution medial launder (4) communicates with doctor solution oxidation trough (6), and described doctor solution oxidation trough (6) communicates with flue gas pipeline; Described doctor solution oxidation trough (6) communicates with ammonium sulfate inspissator (8), ammonium sulfate liquor crystallization tank (9), ammonium sulfate crystallization centrifuge (10) and ammonium sulfate drier (11) successively by pipeline; Being equipped with return line at described ammonium sulfate liquor crystallization tank (9) and ammonium sulfate crystallization centrifuge (10) communicates with doctor solution medial launder (4); Described denitrator (2) communicates with denitration liquid medial launder (5) by pipeline; Described denitration liquid medial launder (5) communicates with self-adsorption ejector (12) and denitration liquid oxygenating groove (7) successively by pipeline; Described denitration liquid oxygenating groove (7) communicates with denitrator (2) by pipeline; Described denitration liquid medial launder (5) communicates with doctor solution medial launder (4) by pipeline; Described demister (3) communicates with denitration liquid medial launder (5) by pipeline.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874282A (en) * | 2015-05-12 | 2015-09-02 | 江苏揽山环境科技有限公司 | Flue gas desulfurization system |
| CN105582798A (en) * | 2016-03-09 | 2016-05-18 | 周紫阳 | Waste gas treatment device |
| CN108619875A (en) * | 2018-07-04 | 2018-10-09 | 广西科技大学鹿山学院 | Sintering flue gas plasma/urea method simultaneous SO_2 and NO removal technique and its system |
| CN109260918A (en) * | 2017-07-18 | 2019-01-25 | 吕朝妮 | A kind of flue gas desulfurization and denitrification integral method and its dedicated unit |
-
2013
- 2013-03-29 CN CN2013201504976U patent/CN203253338U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874282A (en) * | 2015-05-12 | 2015-09-02 | 江苏揽山环境科技有限公司 | Flue gas desulfurization system |
| CN104874282B (en) * | 2015-05-12 | 2017-12-12 | 江苏揽山环境科技股份有限公司 | A kind of flue gas desulphurization system |
| CN105582798A (en) * | 2016-03-09 | 2016-05-18 | 周紫阳 | Waste gas treatment device |
| CN109260918A (en) * | 2017-07-18 | 2019-01-25 | 吕朝妮 | A kind of flue gas desulfurization and denitrification integral method and its dedicated unit |
| CN108619875A (en) * | 2018-07-04 | 2018-10-09 | 广西科技大学鹿山学院 | Sintering flue gas plasma/urea method simultaneous SO_2 and NO removal technique and its system |
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