CN103816778A - Synergic removal method for multiphase contaminant in sintering flue gas - Google Patents
Synergic removal method for multiphase contaminant in sintering flue gas Download PDFInfo
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- CN103816778A CN103816778A CN201410039452.0A CN201410039452A CN103816778A CN 103816778 A CN103816778 A CN 103816778A CN 201410039452 A CN201410039452 A CN 201410039452A CN 103816778 A CN103816778 A CN 103816778A
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Abstract
The invention relates to a synergic removal method for a multiphase contaminant in sintering flue gas. The method comprises the following steps: performing primary dust removal on the sintering flue gas, pressurizing the dust removed sintering flue gas, and partially oxidizing the gas; performing catalytic oxidation on the oxidized flue gas to generate nitric acid and sulfuric acid, neutralizing nitric acid and sulfuric acid with ammonia water to generate ammonium sulfate and ammonium nitrate, and conveying a mixed solution of ammonium sulfate and ammonium nitrate to an ammonium sulfate evaporative crystallization system; demisting the flue gas subjected to catalytic oxidation, performing chemical agglomeration and secondary dust removal and purification on the gas, and discharging the purified flue gas. The method not only can treat the multiphase contaminant in the sintering flue gas, but also can obtain the high-quality byproducts.
Description
Technical field
The present invention relates to field of environment protection, be specifically related to the heterogeneous pollutant cooperation-removal of a kind of sinter fume method.
Background technology
In sinter fume, contain multiple pollutant component, as gas phase has sulfur dioxide, nitrogen oxide etc., solid phase has dust and is attached on the materials such as the heavy metal, bioxin on dust, and in flue gas, moisture also can carry part soluble inorganic salt.Sinter fume also has exhaust gas volumn and flue gas characteristic with mineral and the violent characteristic of production load variations.Existing smoke processing system is mainly to process for Single Pollution thing, and for the flue gas characteristic of complexity like this, smoke processing system is also very complicated, is difficult to the shortcoming that timely load-responsive changes.
For removing of sulfur dioxide, conventional limestone-gypsum method or ammonia-ammonium sulfate method in engineering, but these two kinds of systems all cannot be processed nitrogen oxide, and in solution after treatment, contain dust and other impurity, accessory substance quality is had to impact.The FeII(EDCA that sulfur dioxide and nitrogen oxide remove simultaneously) method or other catalytic eliminating systems, also exist in solution after treatment and contain dust and other impurity, to the influential problem of accessory substance quality.And all there is the problem of carrying large quantity of moisture and accessory substance in flue gas in said system, so not only reduce the output of accessory substance, and increased fresh water (FW) consumption, the more important thing is and also easily cause secondary pollution.Therefore, we are in the urgent need to a kind of method of processing the heterogeneous pollutant of sinter fume, to improve the quality of accessory substance.
Summary of the invention
Technical problem to be solved by this invention is to provide the heterogeneous pollutant cooperation-removal of a kind of sinter fume method, and the method can not only be processed the heterogeneous pollutant of sinter fume, and can obtain the accessory substance of high-quality.
The technical solution adopted in the present invention is: the heterogeneous pollutant cooperation-removal of a kind of sinter fume method, and described method is: sinter fume is carried out after one-time dedusting to supercharging partial oxidation; Flue gas after oxidation carries out catalytic oxidation and generates nitric acid and sulfuric acid, and nitric acid and sulfuric acid and ammonia neutralization generate ammonium sulfate and ammonium nitrate, and the mixed solution of ammonium sulfate and ammonium nitrate is sent into sulphur ammonium ammonium nitrate evaporation and crystallization system; Flue gas after catalytic oxidation after demist, carries out chemical agglomeration and final dusting purifies, and discharges.
Press such scheme, the concrete steps of described method are:
1), sinter fume is passed into disposable dust remover and carry out one-time dedusting, remove the solid-phase contaminants of adhering on dust in sinter fume and dust, flue gas after one-time dedusting through booster fan in pipeline after supercharging, oxidant in oxidant generator sprays into pipeline, be nitrogen dioxide by the oxidation of nitric oxide in flue gas, sulfur dioxide is not oxidized;
2), the flue gas after oxidation enters absorption tower, with form absorbent solution counter current contacting by ammoniacal liquor and catalyst, sulfur dioxide, nitrogen dioxide under catalyst action with oxidation fan in the oxygen reaction that passes into, generate nitric acid and sulfuric acid, nitric acid and sulfuric acid and ammonia neutralization generation ammonium sulfate and ammonium nitrate;
3), reach after finite concentration when ammonium sulfate and the ammonium nitrate on absorption tower, separate through three phase separator, ammonium sulfate and salpeter solution are sent into sulphur ammonium ammonium nitrate evaporation and crystallization system, make ammonium sulfate and ammonium nitrate;
4), through step 2) process flue gas after the demist section on absorption tower, enter reunion chamber with the agglomerator spraying into, make aerosol and drop coacervating large particle in flue gas, bulky grain drop is part sedimentation in reunion chamber, and residue bulky grain drop is removed through secondary filter; Flue gas after purification is discharged by chimney.
Further scheme is, in step 3), when ammonium sulfate and the ammonium nitrate on absorption tower reach after finite concentration, separate through three phase separator, catalyst is sent in blending tank after ammoniacal liquor mixes in blending tank through catalyst force (forcing) pump, sent in absorption tower through the upper entrance on absorption tower.
Further scheme is, step 2) in, the mass ratio 0.3-3:1 of the ammoniacal liquor in blending tank and catalyst.
Further scheme is, in step 1), solid-phase contaminants is heavy metal and bioxin; Oxidant in step 1) is for adopting high-concentration oxygen or ozone.
Further scheme is, step 2) in, described catalyst is organic polymer catalyst.
Further scheme is, step 2) in, described absorbent solution recycles in absorption tower by circulating pump.
Further scheme is, in step 3), after the ammonium sulfate on absorption tower and ammonium nitrate reach molality and are 1.25-1.45mol/Kg, separate through three phase separator, ammonium sulfate and salpeter solution are sent into sulphur ammonium ammonium nitrate evaporation and crystallization system through solution surge tank and solution transfer pump, make ammonium sulfate and ammonium nitrate.
Further scheme is, in step 4), the fouling in the demist section on absorption tower is sprayed into and cleans through technique water pump by the water of technique water tank.
Further scheme is, in step 4), described agglomerator dissolves, mixes, keeps in the agglomerator dissolving tank of belt stirrer, carries through agglomerator delivery pump, under the compressed-air actuated effect providing at air compressor, spray into pipeline, and mix from demist section flue gas out.
Further scheme is, described agglomerator is organic polymer catalyst, sprays in pipeline with solution form.
Further scheme is, in step 4), described reunion chamber is divided into two regions, and top is divided into air-flow by district, and bottom is divided into grit decanting zone; Air-flow is rectangular channel by district, and passage below is connected with grit decanting zone, and grit decanting zone is the dirt bucket of two funnel-shaped structures, and two dirt buckets arrange along airflow direction, in described dirt bucket, is vertically provided with baffle plate.
Sinter fume is removed and at dust, heavy metal and this temperature in flue gas, is the solid-state bioxin on solid phase particles that is attached to after disposable dust remover dedusting, after flue gas ash removal, enter pipeline, after booster fan supercharging, mix with the oxidant in oxidant generator, nitric oxide in flue gas is oxidized to nitrogen dioxide, and sulfur dioxide does not change; Flue gas enters behind absorption tower and absorbent solution counter current contacting subsequently, the catalyst trap that sulfur dioxide in flue gas and nitrogen dioxide are absorbed in solution enters in solution, and under the effect of catalyst with oxidation fan in the oxygen generation oxidation reaction that passes into, generate sulfuric acid and nitric acid, sulfuric acid and nitric acid, by the ammonia neutralization in solution, generate ammonium sulfate and ammonium nitrate; Absorbent solution circulates in absorption tower by circulating pump; When ammonium sulfate in absorbent solution and ammonium nitrate concn are when higher, absorption liquid part enters three phase separator, lime-ash sinks to three phase separator bottom, and fall into slag bucket, after static layering, be positioned at after the ammonium sulfate of lower floor and ammonium nitrate mixed liquor enter solution surge tank and enter sulphur ammonium ammonium nitrate evaporation and crystallization system by solution transfer pump; The catalyst that is positioned at upper strata enters blending tank by catalyst force (forcing) pump, and ammoniacal liquor enters blending tank through ammoniacal liquor measuring pump from ammonia water tank, and the two adds in absorption tower after mixing; Demist section is equipped with in top, absorption tower, removes the moisture in flue gas, and demist section is rinsed by technique water tank and the feedwater of technique water pump; Agglomerator is carried by agglomerator delivery pump, and spray into pipeline under compressed air effect, compressed air is provided by air compressor, agglomerator with absorb after contain aerocolloidal flue gas and mix, mixed flue gas enters reunion chamber, speed reduces rapidly, the particle of different-grain diameter is collision mutually in reunion chamber, forms bulky grain, and preliminary sedimentation, the particle of sedimentation is not removed subsequently in secondary filter, and the flue gas after purification is discharged by chimney.
In oxidant generator, be high-concentration oxygen, ozone or hydrogen peroxide; Disposable dust remover and secondary filter are dry dust removal system, and efficiency of dust collection is more than 98%; In blending tank, the mass ratio of ammoniacal liquor and catalyst is 0.3-3:1; Three phase separator can precipitate the bubble in lime-ash, the elimination solution in absorbent solution, ammonium sulfate, ammonium nitrate mixed liquor and catalyst in separate absorbent solution.
The present invention is directed to existing sinter fume treatment process and devices in system complexity, being difficult to timely load-responsive changes, accessory substance contains impurity, secondary pollution, and the economy causing due to a large amount of consumption of fresh water (FW) and accessory substance loss etc. reduces problem, being provided with cleaner efficiently removes dust, subsequently flue gas oxidation is sent into absorption tower, under the effect of catalyst, carry out chemical absorbing, flue gas after absorption carries moisture and solubility accessory substance, under the effect of molecule agglomerator, the drop coacervating large particle of accessory substance will be contained in flue gas, and in the indoor reunion sedimentation of reunion of special construction, finally by emptying the flue gas after purifying, after absorption liquid separating catalyst, enter by-product production flow process.
Beneficial effect of the present invention is: 1, disposable dust remover is set, removes the heavy metallic oxide that adheres on dust in sinter fume and dust with pollutants such as bioxin, improve degree of purity and the output of accessory substance.2, oxidant generator is set the nitric oxide in flue gas is oxidized, improve the clearance of nitrogen oxide.3, use catalyst to improve sulfur dioxide and nitric oxide production seizure effect, improve the treatment effect of vapor phase contaminants, and reduce the escaping of ammonia.4, reduce aerocolloidal discharge by reunion chamber is set, improve the aerosol phenomenon of traditional sulfur removal technology, thereby improve heterogeneous pollutant removal.5, reduce fresh water (FW) consumption, save operating cost, improve accessory substance quality and economic benefit etc.6, native system flexibility is strong, good to flue gas load adaptability, non-secondary pollution.
Accompanying drawing explanation
Fig. 1 is the structural representation of one embodiment of the present of invention.
Fig. 2 is the structural representation of reunion chamber.
In figure: 1, disposable dust remover, 2, booster fan, 3, oxidant generator, 4, oxidation fan, 5, absorption tower, 61, the first circulating pump, 62, the second circulating pump, 7, three phase separator, 8, slag bucket, 9, catalyst force (forcing) pump, 10, blending tank, 11, ammonia water tank, 12, ammoniacal liquor measuring pump, 13, solution surge tank, 14, solution transfer pump, 15, sulphur ammonium ammonium nitrate evaporation and crystallization system, 16, technique water tank, 17, technique water pump, 18, air compressor, 19, agglomerator dissolving tank, 20, agglomerator delivery pump, 21, reunion chamber, 22, secondary filter, 23, chimney, 24, reunion chamber inlet, 25, air-flow passes through district, 26, the outlet of reunion chamber, 27, baffle plate, 28, grit decanting zone.
The specific embodiment
Further illustrate embodiments of the invention below in conjunction with accompanying drawing.
The heterogeneous pollutant cooperation-removal of a kind of sinter fume method, described method is: sinter fume is carried out after one-time dedusting to supercharging partial oxidation; Flue gas after oxidation carries out catalytic oxidation and generates nitric acid and sulfuric acid, and nitric acid and sulfuric acid and ammonia neutralization generate ammonium sulfate and ammonium nitrate, and the mixed solution of ammonium sulfate and ammonium nitrate is sent into sulphur ammonium ammonium nitrate evaporation and crystallization system; Flue gas after catalytic oxidation after demist, carries out chemical agglomeration and final dusting purifies, and discharges.
Referring to Fig. 1 and Fig. 2, concrete steps are:
1), sinter fume is passed into disposable dust remover 1 and carry out one-time dedusting, removing what on dust in sinter fume and dust, adhere to is the pollutants such as heavy metal and bioxin, flue gas after one-time dedusting through booster fan 2 in pipeline after supercharging, high-concentration oxygen or ozone that oxidant generator is 3 li spray into pipeline, be nitrogen dioxide by the oxidation of nitric oxide in flue gas, sulfur dioxide is not oxidized;
2), the flue gas after oxidation enters absorption tower 5, with form absorbent solution counter current contacting by ammoniacal liquor and catalyst, sulfur dioxide, nitrogen dioxide under catalyst action with oxidation fan 4 in the oxygen reaction that passes into, generate nitric acid and sulfuric acid, nitric acid and sulfuric acid and ammonia neutralization generate ammonium sulfate and ammonium nitrate;
3), after the ammonium sulfate on absorption tower 5 and ammonium nitrate reach molality and are 1.25-1.45mol/Kg, separate through three phase separator 7, ammonium sulfate and salpeter solution are sent in sulphur ammonium ammonium nitrate evaporation and crystallization system 15 through solution surge tank 13 and solution transfer pump 14, made ammonium sulfate and ammonium nitrate; Catalyst is sent in blending tank 10 after in blending tank 10, ammoniacal liquor mixes, in the upper entrance on absorption tower 5 is sent into absorption tower 5 through catalyst force (forcing) pump 9; The mass ratio 2:1 of the ammoniacal liquor in blending tank 10 and catalyst.
4), through step 2) process flue gas after the demist section on absorption tower 5, enter reunion chamber 21 with the agglomerator spraying into, make aerosol and drop coacervating large particle in flue gas, bulky grain drop is part sedimentation in reunion chamber 21, and residue bulky grain drop is removed through secondary filter 22; Flue gas after purification is discharged by chimney 23.In this step, described agglomerator dissolves, mixes in the agglomerator dissolving tank 19 of belt stirrer, temporary, carry through agglomerator delivery pump 20, under the compressed-air actuated effect providing at air compressor 18, spray into pipeline, and mix from demist section flue gas out.
In step 2) and step 3) in, described catalyst is organic polymer catalyst.In step 3), the ammoniacal liquor in blending tank 10 is provided through ammoniacal liquor measuring pump 12 by ammonia water tank 11.
In step 2) in, absorbent solution recycles in absorption tower 5 by the first circulating pump 61 and the second circulating pump 62.In step 4), the fouling in the demist section on absorption tower 5 is sprayed into and cleans through technique water pump 17 by the water of technique water tank 16.In step 4), described agglomerator is organic polymer catalyst, sprays in pipeline with solution form; In step 4), described reunion chamber 21 is divided into two regions, and top is divided into air-flow by district 25, and bottom is divided into grit decanting zone 28; Air-flow is respectively arranged with reunion chamber inlet 24 and reunion chamber outlet 26 by the both sides in district 25; Air-flow is rectangular channel by district 25, and passage below is connected with grit decanting zone 28, and grit decanting zone 28 is the dirt bucket of two funnel-shaped structures, and two dirt buckets are arranged along airflow direction; In each dirt bucket, be vertically provided with baffle plate 27.
The heterogeneous pollutant cooperation-removal of this method sinter fume used system, this system comprises disposable dust remover 1, described disposable dust remover 1 is connected with first entrance on absorption tower 5 by booster fan 2, first outlet on absorption tower 5 is connected with the first entrance of three phase separator 7, three phase separator 7 first outlet successively with solution surge tank 13, solution transfer pump 14 and sulphur ammonium ammonium nitrate evaporation and crystallization system 15 are connected, the second entrance of three phase separator 7 successively with catalyst force (forcing) pump 9, blending tank 10, ammoniacal liquor measuring pump 12, ammonia water tank 11 is connected, the first outlet of three phase separator 7 is connected with slag bucket 8, second entrance on described absorption tower 5 is connected with blending tank 10, second outlet on described absorption tower 5 is connected with reunion chamber 21, secondary filter 22, chimney 23 successively, second outlet on described absorption tower 5 is connected with agglomerator dissolving tank 19 by agglomerator delivery pump 20, between second outlet on described absorption tower 5 and agglomerator delivery pump 20, is provided with air compressor 18, between booster fan 2 and absorption tower 5, be provided with oxidant generator 3, the 3rd entrance on absorption tower 5 is connected with oxidation fan 4, the 4th entrance on absorption tower 5 is connected with technique water tank 16 by technique water pump 17, described absorption tower 5 is connected with the first circulating pump 61 and the second circulating pump 62 respectively.
In the present embodiment, more than first entrance on absorption tower 5 is positioned at absorption tower 5 liquid levels, the 3rd entrance on absorption tower 5 is positioned at the lower left quarter on absorption tower 5, the 4th entrance on absorption tower 5 is positioned at absorption tower 5 upper right quarters, first outlet on absorption tower 5 is positioned at the right lower quadrant on absorption tower 5, and the first outlet of three phase separator 7 is positioned at three phase separator 7 bottoms.
In the present embodiment, catalyst force (forcing) pump 9, ammonia water tank 11, ammoniacal liquor measuring pump 12, blending tank 10 forms absorbent solution preparation system, three phase separator 7, slag bucket 8, solution surge tank 13, solution transfer pump 14 and sulphur ammonium ammonium nitrate evaporation and crystallization system 15 form sulphur ammonium ammonium nitrate preparation system, air compressor 18, agglomerator dissolving tank 19, agglomerator delivery pump 20 and reunion chamber 21 form aerosol reunion system, absorption tower 5, oxidation fan 4, circulating pump 61/62, technique water tank 16 and technique water pump 17 form smoke absorption system, booster fan 2, chimney 23 and connect the pipeline composition air supplying and exhausting system of each equipment.
Sinter fume is removed and at dust, heavy metal and this temperature in flue gas, is the solid-state bioxin on solid phase particles that is attached to after disposable dust remover 1 dedusting, in pipeline, pass through booster fan 2 superchargings, oxygen or the ozone of flue gas after supercharging in oxidant generator 3 mixes, nitric oxide in flue gas is oxidized to nitrogen dioxide, and sulfur dioxide is not oxidized; Flue gas mixes with absorbent solution adverse current after entering absorption tower 5 subsequently, and the catalyst reaction in the sulfur dioxide in flue gas and nitrogen dioxide and absorbent solution, by transferring in flue gas in solution; Oxidation fan 4 passes into oxygen, and under the effect of oxygen and catalyst, sulfur dioxide and nitrogen dioxide generation oxidation reaction, generate sulfuric acid and nitric acid, and sulfuric acid and nitric acid is absorbed the ammonia neutralization in solution, generates ammonium sulfate and ammonium nitrate; The mixed solution that contains ammonium sulfate, ammonium nitrate, ammoniacal liquor and catalyst circulates by the first circulating pump 61 and the second circulating pump 62 in absorption tower 5, constantly catches sulfur dioxide and nitrogen dioxide final ammonium sulfate and the ammonium nitrate of generating; Until the concentration of ammonium sulfate and ammonium nitrate reaches a certain value in absorption tower 5, conventionally adopt mixed solution density as basis for estimation, in the time that mixed liquor density reaches 1.25-1.45, mixed solution is passed in three phase separator 7, a small amount of lime-ash is separated and fall into slag bucket 8, the solution of ammonium sulfate and ammonium nitrate enters solution surge tank 13, and is delivered to sulphur ammonium ammonium nitrate evaporation and crystallization system 15 by solution transfer pump 14; Catalyst enters blending tank 10 by catalyst force (forcing) pump 9, and simultaneously ammoniacal liquor enters blending tank 10 by ammonia water tank 11 by ammoniacal liquor measuring pump 12, and ammoniacal liquor and catalyst enter absorption tower 5 after mixing blending tank 10 is interior; Flue gas after purifying is interior on absorption tower 5 is discharged from absorption tower 5 through demist section, and the fouling in demist section sprays into cleaning by the water of technique water tank 16 through technique water pump 17; In flue gas after demist, contain droplet, and carry ammonium sulfate and ammonium nitrate, form aerosol, therefore the compressed air providing by air compressor 18 in pipeline is injected to agglomerator in flue gas, with the drop generation aggregation in flue gas, generate bulky grain, bulky grain drop is part sedimentation in reunion chamber 21, remaining bulky grain drop carries out sedimentation in secondary filter 22, and the flue gas after purification is discharged by chimney 23; Agglomerator, in the interior dissolving of agglomerator dissolving tank 19 temporary, is carried by agglomerator delivery pump 20.
In the present embodiment, in step 2) and step 3) in, described catalyst is sulfoxide compound; In step 4), described agglomerator is dimethyl cellulose.
Claims (10)
1. the heterogeneous pollutant cooperation-removal of a sinter fume method, is characterized in that: described method is: sinter fume is carried out after one-time dedusting to supercharging partial oxidation; Flue gas after oxidation carries out catalytic oxidation and generates nitric acid and sulfuric acid, and nitric acid and sulfuric acid and ammonia neutralization generate ammonium sulfate and ammonium nitrate, and the mixed solution of ammonium sulfate and ammonium nitrate is sent into sulphur ammonium ammonium nitrate evaporation and crystallization system; Flue gas after catalytic oxidation after demist, carries out chemical agglomeration and final dusting purifies, and discharges.
2. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 1 method, is characterized in that: the concrete steps of described method are:
1), sinter fume is passed into disposable dust remover and carry out one-time dedusting, remove the solid-phase contaminants of adhering on dust in sinter fume and dust, flue gas after one-time dedusting through booster fan in pipeline after supercharging, oxidant in oxidant generator sprays into pipeline, be nitrogen dioxide by the oxidation of nitric oxide in flue gas, sulfur dioxide is not oxidized;
2), the flue gas after oxidation enters absorption tower, with form absorbent solution counter current contacting by ammoniacal liquor and catalyst, sulfur dioxide, nitrogen dioxide under catalyst action with oxidation fan in the oxygen reaction that passes into, generate nitric acid and sulfuric acid, nitric acid and sulfuric acid and ammonia neutralization generation ammonium sulfate and ammonium nitrate;
3), reach after finite concentration when ammonium sulfate and the ammonium nitrate on absorption tower, separate through three phase separator, ammonium sulfate and salpeter solution are sent into sulphur ammonium ammonium nitrate evaporation and crystallization system, make ammonium sulfate and ammonium nitrate;
4), through step 2) process flue gas after the demist section on absorption tower, enter reunion chamber with the agglomerator spraying into, make aerosol and drop coacervating large particle in flue gas, bulky grain drop is part sedimentation in reunion chamber, and residue bulky grain drop is removed through secondary filter; Flue gas after purification is discharged by chimney.
3. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, it is characterized in that: in step 3), when ammonium sulfate and the ammonium nitrate on absorption tower reach after finite concentration, separate through three phase separator, catalyst is sent in blending tank after ammoniacal liquor mixes in blending tank through catalyst force (forcing) pump, sent in absorption tower through the upper entrance on absorption tower; The mass ratio 0.3-3:1 of the ammoniacal liquor in blending tank and catalyst.
4. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, is characterized in that: in step 1), solid-phase contaminants is heavy metal and bioxin; Oxidant in step 1) is for adopting high-concentration oxygen, ozone or hydrogen peroxide.
5. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, is characterized in that: step 2) in, described catalyst is: organic polymer catalyst; Step 2) in, described absorbent solution recycles in absorption tower by circulating pump.
6. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, it is characterized in that: in step 3), after the ammonium sulfate on absorption tower and ammonium nitrate reach molality and are 1.25-1.45mol/Kg, separate through three phase separator, ammonium sulfate and salpeter solution are sent into sulphur ammonium ammonium nitrate evaporation and crystallization system through solution surge tank and solution transfer pump, make ammonium sulfate and ammonium nitrate.
7. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, is characterized in that: in step 4), the fouling in the demist section on absorption tower is sprayed into and cleans through technique water pump by the water of technique water tank.
8. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, it is characterized in that: in step 4), described agglomerator dissolves, mixes, keeps in the agglomerator dissolving tank of belt stirrer, carry through agglomerator delivery pump, under the compressed-air actuated effect providing at air compressor, spray into pipeline, and mix from demist section flue gas out.
9. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 8 method, is characterized in that: described agglomerator is organic polymer catalyst, sprays in pipeline with solution form.
10. the heterogeneous pollutant cooperation-removal of sinter fume as claimed in claim 2 method, is characterized in that: in step 4), described reunion chamber is divided into two regions, and top is divided into air-flow by district, and bottom is divided into grit decanting zone; Air-flow is rectangular channel by district, and passage below is connected with grit decanting zone, and grit decanting zone is the dirt bucket of two funnel-shaped structures, and two dirt buckets are arranged along airflow direction; In each dirt bucket, be vertically provided with baffle plate.
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Application publication date: 20140528 |