CN102824824B - Amino wet combined desulfurization and denitration device and process - Google Patents
Amino wet combined desulfurization and denitration device and process Download PDFInfo
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- CN102824824B CN102824824B CN201210334034.5A CN201210334034A CN102824824B CN 102824824 B CN102824824 B CN 102824824B CN 201210334034 A CN201210334034 A CN 201210334034A CN 102824824 B CN102824824 B CN 102824824B
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Abstract
The invention discloses amino wet combined desulfurization and denitration device and a process. The device comprises a desulfurization tower with an inlet flue, a liquid ammonia storage tank, an ozone generator, and a booster fan on the inlet flue; and a defogging layer, a spraying layer and a tower kettle are orderly arranged inside the desulfurization tower from top to bottom. The device also comprises an oxidization slot communicated with the tower kettle, and an oxidization fan connected to the oxidization slot; the liquid ammonia storage tank is communicated to the tower kettle through one path of pipeline, and is communicated to the bottom part of the oxidization slot through another pipeline; the ozone generator is communicated to an air inlet of the booster fan through the pipeline; ozone is sprayed into smoke from the air inlet of the booster fan; nitric oxide in the smoke is oxidized into nitrogen dioxide; the smoke oxidized by ozone is conveyed to the desulfurization tower; liquid ammonia is sprayed to desulfurize and denitrate; the smoke is discharged after being defogged and dried; and circulating liquid by which sulfur dioxide and nitrogen dioxide are absorbed is oxidized outside the tower, and the liquid ammonia is conveyed to the oxidization slot to adjust the pH (Potential Of Hydrogen) value in the oxidization slot during the oxidization process.
Description
Technical field
The present invention relates to technical field of air pollution control, be specifically related to a kind of amino wet method combined desulfuring and denitrifying apparatus and technique, for sulfur dioxide in fire coal boiler fume and nitrogen oxide remove and by-product recovery utilizes.
Background technology
Ammonia-process desulfurization technique utilizes liquefied ammonia, ammoniacal liquor or urea to remove the SO in flue gas
2, generate the ammonium sulfate (NH of high-quality simultaneously
4)
2sO
4.Ammonia-process desulfurization technique is particularly suitable for large-scale thermal power machine group and chemical enterprise and burns the tail gas SO of cheap high-sulfur combustor
2remove, while the useless ammonia desulfurization of use, produce high-quality, highly purified ammonium sulfate, progressively become the mainstream technology of the recycling economy comprehensive utilization of mega project flue gas desulfurization.
Ammonia-process desulfurization technique has abundant raw material, and its maximum feature is SO
2resourcebility, can by pollutant SO
2recovery becomes high value-added product.Byproduct ammonium sulfate is a kind of nitrogenous fertilizer of function admirable, has good market prospects in China.
The sulfur dioxide of recovery, ammonia are all converted into chemical fertilizer by ammonia recovering method technology, do not produce any waste water, waste liquid and waste residue, do not have secondary pollution, be one truly by whole for pollutant resource, meet recycling economy require desulfur technology.
Ammonia process of desulfurization accessory substance is worth high, namely the running of ammonia recovering method desulfurizer is the production process of ammonium sulfate, often absorb 1 ton of liquefied ammonia and can remove 2 tons of sulfur dioxide, produce 4 tons of ammonium sulfate, conveniently 2000 yuan/ton, price liquefied ammonia, 700 yuan/ton, ammonium sulfate, then in flue gas, sulfur dioxide per ton embodies the value of about 400 yuan.Therefore relative motion expense is little, and sulfur content in coal amount is higher, and operating cost is lower.Enterprise can utilize cheap sulphur coal, significantly reduces fuel cost and desulfurization expense simultaneously, kills two birds with one stone.
Ammonia-process desulfurization technique has stronger advantage in the pollutant comprehensive regulation and resource, but hinders the development of ammonia-process desulfurization technique to a certain extent owing to there is the difficult problem such as the escaping of ammonia, oxidizing and crystallizing.Liquefied ammonia is volatile substances, there is certain the escaping of ammonia in detach procedure, and escape ammonia enters in air can cause secondary pollution to environment; In the oxidizing process of ammonium sulfite, the NH of excessive concentrations
4 +ion can have certain damping action to the oxidation of ammonium sulfite, causes system oxidation crystallization difficulty; Meanwhile, ammonia-process desulfurization technique is to the NO in flue gas
xremoval efficiency lower, to NO in boiler smoke
ximprovement need to set up separately a set of denitrification apparatus, if improve the denitration efficiency of ammonia-process desulfurization technique, realize simultaneous SO_2 and NO removal be ammonia-process desulfurization technique another need the difficult problem that solves.
Such as, application number be 200710052129.7 Chinese invention patent disclose a kind of wet ammonia flue gas cleaning technology and system thereof of simultaneous SO_2 and NO removal.This technique first makes the nitric oxide in flue gas carry out oxidation reaction and generates nitrogen dioxide, then make the sulfur dioxide in flue gas and nitrogen dioxide carry out reaction with ammoniacal liquor respectively and generate ammonium sulfite, ammonium nitrate and ammonium nilrite, ammonium sulfite wherein and ammonium nilrite generation oxidation reaction is made to generate byproduct of ammonium sulfate and ammonium nitrate again, demist is carried out to the flue gas after desulphurization denitration simultaneously, finally obtain clean flue gas.Its system comprises pre-dedusting device, hydrogen peroxide or the ozone injection apparatus and desulphurization denitration tower that connect successively, and desulphurization denitration tower bottom is connected with ammoniacal liquor device for supplying and air apparatus for feeding, and middle part is provided with the ammonia spray layer of injection capable of circulation, and top is provided with demister.
In this system, the more difficult control of its pH value can not take into account the desulfuration efficiency of flue gas and the oxidizing and crystallizing efficiency of ammonium sulfite, simultaneously, ammonia quantity delivered in this system in desulfurizing tower is carried out according to sulfur dioxide in flue gas content, and content of sulfur dioxide fluctuation range in flue gas is larger, be difficult to control, cause the pH value fluctuation range of whole slurries system comparatively large if fruit controls improper meeting, cause aerosol to produce in a large number, desulfuration efficiency is unstable.
Summary of the invention
The invention provides a kind of amino wet method method combined desulfurization and denitrification process that can improve ammonia-process desulfurization technique denitration efficiency, reduce the escaping of ammonia, remove aerosol, improve sulfite oxidation speed and increase ammonia sulfate crystal particle of knowing clearly.
A kind of amino wet method combined desulfuring and denitrifying apparatus, the booster fan comprising the desulfurizing tower of tape entry flue, liquid ammonia storage tank, ozone generator and be positioned on gas approach, demist layer, spraying layer and tower reactor is followed successively by from top to bottom in described desulfurizing tower, also comprise an oxidation trough be communicated with described tower reactor and the oxidation fan being connected to oxidation trough, described liquid ammonia storage tank is communicated to described tower reactor by pipeline one tunnel, another road is communicated to bottom described oxidation trough, described ozone generator by pipeline connection to the air intake vent place of described booster fan.
Ozone is passed into gas approach, utilizes ozone to be oxidized to the NO of indissoluble in flue gas very easily by the NO of liquid absorption
2, the flue gas after oxidation enters in desulfurizing tower and carries out spray desulphurization denitration; Complete the feeding of the circulation fluid after desulphurization denitration oxidation trough and carry out oxidizing and crystallizing; The ammonia sulfate crystal mixed serum completing oxidation in oxidation trough is further processed; Liquefied ammonia part supply in liquid ammonia storage tank is to desulfurizing tower as desulfurizing agent, and another part supply oxidizing groove is as the conditioning agent of oxidation trough pH value.The desulphurization denitration of flue gas separates with the oxidizing and crystallizing completing the circulation fluid after desulphurization denitration and carries out.
Described ozone generator is communicated to the air intake vent place of booster fan, namely ozone entrance is booster fan air intake vent place, booster fan air intake vent is negative pressure, can better prevent ozone from revealing, utilize the eddy current effect of booster fan impeller to be mixed completely with ozone by flue gas simultaneously, realize the complete oxidation NO of NO in flue gas
2, adopt booster fan air intake vent to add ozone and save flue gas blender, reduce the resistance of system.
Defeated ammonia pipeline in oxidation trough is arranged on bottom, adopt bottom ammonification, the pH value of the timely buffer oxide crystallizing layer of energy is (because slurries to be oxidized are mainly ammonium sulfite and ammonium bisulfite, hydrogen ion can be discharged after bisulfite is oxidized, the pH value of slurries is sharply declined, make oxide layer local ph too low, cause SO
2escape and reduce oxidation rate), ensure that the lasting high speed of whole oxidizing process is carried out.
As preferably, be provided with porous plate in described oxidation trough, porous plate is mainly used in the bubble that distributes, and makes oxidation wind bubble be uniformly distributed whole oxidation trough volume inner, plays stirring action simultaneously, accelerates gas-liquid turbulent extent, improves oxidation rate.By orifice plate gas distribution mode in oxidation trough, increase the contact of gas-liquid turbulent flow, improve the oxidation rate of ammonium sulfite, reduce the time of staying of ammonium sulfite in oxidation trough, reduce the volume of oxidation trough, save system operation cost and cost of investment.
More preferably, described oxidation trough is with the oxidation wind entrance be communicated with oxidation fan, and described porous plate is positioned at oxidation wind entrance top 0.5 ~ 0.8m place; The aperture of described porous plate is 3 ~ 5cm, and percent opening is 50 ~ 80%.
When porous plate percent opening is 50-80%, when aperture is 3-5cm, the stirring action played and slurries oxidation effectiveness best, percent opening refers to that the gross area of porous plate perforate accounts for the ratio of the porous plate gross area.
Porous plate is two-layer by being divided in oxidation trough, and lower floor is oxidizing and crystallizing layer, and the crystal grain that ammonia sulfate crystal forms 0.5-3mm is here suspended in bottom slurry, and discharges bottom oxidation trough; Top is clear layer, is ammonium sulfate, ammonium sulfite clear liquid, to the NO in flue gas
xthere is reduction, NO can be removed further
x.
Therefore, as preferably, described demist layer is made up of baffle flaggy and the sparge pipe be positioned at above baffle flaggy, and the quantity of described demist layer is two-layer, comprise bottom demist layer and top layer demist layer, the sparge pipe of described bottom demist layer is communicated with by the top of pipeline with described oxidation trough.
Sparge pipe clear layer above porous plate in oxidation trough being delivered to bottom demist layer as clear liquid flushing pump by corresponding conveying mechanism carries out degree of depth denitration to flue gas, removes the aerosol in flue gas, prevents the escape ammonia in flue gas.
More preferably, the nozzle on the sparge pipe of described demist layer is nozzle.
Bottom demist layer adopts nozzle, and the ammonium sulfite area of ejection is wide, great efforts, has and traps effect preferably, avoid the aerosol phenomenon of exiting flue gas to the escape ammonia in flue gas and dust; Top layer demist layer adopts nozzle, utilizes fresh water (FW) to rinse, prevents demister fouling and clogging.
Present invention also offers a kind of amino wet method combined process for desulfurization and denitration, comprising:
Ozone is sprayed in flue gas by the air intake vent of booster fan, be nitrogen dioxide by the nitrogen oxides in flue gas, flue gas after ozone oxidation is sent in desulfurizing tower, and sprayed into by liquefied ammonia in desulfurizing tower and absorb sulfur dioxide in flue gas and nitrogen dioxide, flue gas is got rid of after demist drying;
The circulation fluid absorbed after sulfur dioxide and nitrogen dioxide is introduced in oxidation trough, in oxidation trough, passes into oxidation wind, circulation fluid is oxidized to ammonia sulfate crystal slurries, after described ammonia sulfate crystal slurries process further, obtain ammonium sulfate finished product; In oxidation trough, the pH value in liquefied ammonia adjustment oxidation trough is sent in oxidizing process.
Ozone sprays in flue gas by the air intake vent of booster fan, and booster fan air intake vent is negative pressure, can better prevent ozone from revealing, and utilizes the eddy current effect of booster fan impeller to be mixed completely with ozone by flue gas simultaneously, and realizing NO complete oxidation in flue gas is NO
2.
Key reaction in desulfurizing tower is SO
2and NO
2react with ammonium sulfite solution and generate ammonium bisulfite and ammonium nitrate solution, ensure that the denitrification efficiency of desulfurizing tower must ensure that in desulfurizing tower, slurries have certain density sulfite ion, need continuous supply liquefied ammonia and ammonium bisulfite in desulfurizing tower to react the ammonium sulfite solution generating and have desulphurization denitration ability.
PH value in described desulfurizing tower is 5.8 ~ 6.2, and spraying layer liquid-gas ratio is 7-10L/m
3.In desulfurizing tower, slurry system is mainly ammonium sulfite-bisulfite ammono-system, and time slurry pH value too high (> 7), the ammonium salt solution in mixture system volatilizes ammonia; When pH value is too low, desulfuration efficiency is undesirable, when slurry system pH value at 5.8-6.2, liquid-gas ratio at 8-9L/m
3time, to the SO in flue gas
2and NO
2there is the trapping effect higher than 95%.
Ammonium bisulfite can generate ammonia sulfate crystal and sulfuric acid in oxidizing process simultaneously, whole oxidizing process can constantly make the pH value of oxidation trough slurries continue to reduce, the final oxidation rate affecting bisulfite, therefore, in oxidation trough, send into the pH value in liquefied ammonia adjustment oxidation trough in oxidizing process, keep the pH value of oxidation trough within the scope of 5.6-6.0.
Oxidation trough slurry reaction system is (NH when pH value of solution is less than 5.6
4)
2sO
3oxidation rate increase with the increase of pH; When pH is greater than 6.0, (NH
4)
2sO
3oxidation rate reduce with the increase of pH.Mainly because when pH value of solution is less than 6.0, in solution, there is part HSO in this
3 -, when pH is greater than 6.0, SO a large amount of in solution
3 2-, and HSO
3 -oxidation rate be greater than SO
3 2-oxidation rate.
Preferably, the quantity delivered of described ozone and the mol ratio of nitrogen oxides in effluent are 1: 1.High concentration SO in flue gas
2the oxygenation efficiency of NO can be promoted rapidly, the high concentration SO in inlet flue gas
2under existence condition, the conversion ratio of NO is more than 90%, therefore in setting ozone supply amount and flue gas, the ratio measured of NO is 1: 1.
Preferably, described ammonia sulfate crystal slurries are after cyclonic separation, and underflow is obtained finished product sulfuric acid ammonium after drying, and top stream sends desulfurizing tower inner top back to, carries out degree of depth denitration to flue gas.Be ammonium sulfate, ammonium sulfite clear liquid in the stream of top, to the NO in flue gas
xthere is reduction, NO can be removed further
x, therefore, top stream is sent desulfurizing tower top back to and is carried out degree of depth denitration to flue gas, and removes the escape ammonia in flue gas.
More preferably, the liquid-gas ratio that described top stream carries out degree of depth denitration to flue gas is 1-2L/m
3.
Beneficial effect of the present invention:
(1) oxidation of the purification of flue gas and ammonium sulfite and ammonium bisulfite separates and carries out by the present invention, adopt tower external oxidation, control the pH value of two reaction systems respectively, increase substantially desulfuration efficiency and ammonia sulfate crystal quality, the ammonia sulfate crystal that crystallization is produced has larger crystal particle diameter, be more convenient for being separated, thus improve the purity of ammonia sulfate crystal.
(2) ozone sprays in flue gas by the air intake vent of booster fan, can better prevent ozone from revealing, and utilizes the eddy current effect of booster fan impeller to be mixed completely with ozone by flue gas simultaneously, realizes the complete oxidation NO of NO in flue gas
2, improve the utilization rate of ozone; Adopt booster fan entrance to add ozone and save flue gas blender, reduce the resistance of system.
(3) in the oxidation trough of tower external oxidation, the liquefied ammonia of adjusted to ph is sent into by bottom oxidation trough, can the pH value of buffer oxide crystallizing layer in time, ensures that the lasting high speed of whole oxidizing process is carried out.
(4) adopt orifice plate gas distribution mode in oxidation trough, increase the contact of gas-liquid turbulent flow, improve the oxidation rate of ammonium sulfite, reduce between the stop of ammonium sulfite in oxidation trough, reduce the volume of oxidation trough, save system operation cost and cost of investment.
(5) supernatant liquor in oxidation trough or eddy flow shunting after top stream clear liquid degree of depth denitration is carried out to flue gas, prevent the escaping of ammonia.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Detailed description of the invention
As shown in Figure 1, a kind of amino wet method combined desulfuring and denitrifying apparatus, comprises desulfurizing tower 3, liquid ammonia storage tank 1, ozone generator 19, oxidation trough 10 and cyclone separator 15.
Desulfurizing tower 3 adopts spray column, in desulfurizing tower 3 by upper under be followed successively by demist layer 7, spraying layer 6 and tower reactor, be spray-absorption district between spraying layer 6 and tower reactor, the quantity of spraying layer 6 arranges three layers, arrange three circulating pumps 4 accordingly, every platform circulating pump 4 is communicated with the spraying layer of tower reactor and correspondence.
The quantity of demist layer 7 arranges two-layer, the one deck being positioned at below is bottom demist layer, the one deck being positioned at top is top layer demist layer, every layer of demist layer is by the sparge pipe composition above hydraulic barrier layer and hydraulic barrier layer, fine mist in the lower flue gas of hydraulic barrier layer gear, carries out demist drying to flue gas, and sparge pipe is to hydraulic barrier layer spray flushing liquor, sparge pipe is arranged some nozzles, the nozzle of bottom demist layer and the nozzle of top layer demist layer all adopt nozzle.
The spray-absorption district of desulfurizing tower 3 arranges smoke inlet, connects gas approach 5, gas approach 5 is arranged booster fan 18, and ozone generator 19 is communicated with the air intake vent place of booster fan 18 by ozone transfer pipeline.
Arrange between liquid ammonia storage tank 1 and desulfurizing tower 3 for ammonia pump 2, the entrance for ammonia pump 2 is communicated with liquid ammonia storage tank 1, and outlet point two-way, a road is communicated with the tower reactor of desulfurizing tower 3, and a road is communicated with the bottom of oxidation trough 10.
Oxidation trough 10 is communicated with by circulation fluid excavationg pump 9 with between tower reactor, the entrance of circulation fluid excavationg pump 9 is communicated with tower reactor, outlet is communicated with oxidation trough 10, the bottom of oxidation trough 10 is provided with oxidation wind pipe network, and oxidation wind entrance is set on oxidation trough 10 sidewall, the air-supply pipeline of oxidation fan 14 is communicated with oxidation wind pipe network by this oxidation wind entrance, by oxidation fan 14 to delivery of oxygen wind transmission in oxidation trough 10, the bottom of oxidation trough 10 is communicated to cyclone separator 15 by crystal solution excavationg pump 13, and the top of cyclone separator 15 flows through pipeline and is back in oxidation trough 10.
Arrange porous plate 11 in oxidation trough 10, porous plate 11 is positioned at 0.5 ~ 0.8m place of oxidation wind entrance top, and the aperture of porous plate 11 is 3 ~ 5cm, and percent opening is 50 ~ 80%.Porous plate 11 is two-layer by being divided in oxidation trough 10, the oxidation wind of the liquefied ammonia in liquid ammonia storage tank 1, the circulation fluid in tower reactor and oxidation fan 14 is all sent into below porous plate 11, the top stream of eddy flow current divider 15 sends into the top of porous plate 11, and the oxidation trough 10 being positioned at porous plate 11 upper section arranges the sparge pipe that pipeline is connected to bottom demist layer.
Technological process of the present invention is as follows:
Boiler smoke sends into desulfurizing tower through booster fan 18, the outlet of ozone generator 19 is positioned at booster fan 18 porch, under the effect of entrance negative pressure, ozone evenly enters in gas approach 5 NO be oxidized in raw flue gas, and in the quantity delivered of ozone and flue gas, NO content is 1: 1.High concentration SO in raw flue gas
2accelerate NO in flue gas to a great extent and be converted into NO
2speed, when flue gas moves to booster fan 18 inner chamber place, under the eddy current effect that mixed flue gas causes in the rotation of impeller, obtain abundant mixing, now NO obtains complete oxidation, and complete oxidation also to be entered in desulfurizing tower 3 through gas approach 5 by the raw flue gas that mixes and moves upward.
Desulfurizing agent liquefied ammonia is stored in liquid ammonia storage tank 1, liquefied ammonia is through delivering to bottom desulfurizing tower 3 for ammonia pump 2 points of two-way and bottom oxidation trough 10, circulation fluid in desulfurizing tower 3 is delivered to spraying layer 6 and is atomized into drop by circulating pump 4, slurry droplet through atomization moves downward under gravity, carries out sufficient absorption reaction generate ammonium sulfite, ammonium bisulfite, ammonium nilrite mixed serum falling into bottom desulfurizing tower with flue gas upwards.Flue gas after desulphurization denitration discharges chimney from desulfurizing tower outlet 8 after demist layer 7 demist.In desulfurizing tower, the pH value of flue gas and ammonium sulfite, ammonium bisulfite reaction system is 5.8-6.2, and spraying layer liquid-gas ratio is 7-10L/m
3.
Circulation fluid after desulphurization and denitration delivers to oxidation trough 10 by circulation fluid excavationg pump 9, the bisulfite that oxidation wind pipe network bottom the oxidized groove 10 of oxidation air that oxidation fan 14 exports is scattered in bubble oxidation slurries generates ammonia sulfate crystal precipitation and sulfuric acid, in oxidation trough 10, the pH value of slurries declines, regulate the liquefied ammonia flow entering oxidation trough 10, the pH value of controlled oxidization groove 10 is within the scope of 5.6-6.0.Arrange porous plate 11 in oxide layer, porous plate 11 percent opening is 50%-80%, and aperture is 3cm-5cm, and porous plate 11 exacerbates the turbulent extent of oxidation bubble and slurries, improves the oxidation rate of slurries sulfite hydrogen ammonium.
The ammonium sulfate at oxidation trough 10 top, ammonium sulfite, ammonium nitrate solution are delivered to the shower of bottom demist layer by clear liquid flushing pump, carry out deep desulfuration, denitration, deamination to the flue gas after desulphurization and denitration; The crystal mixed liquor of bottom is delivered to cyclone 15 through crystal solution excavationg pump 13 and is carried out cyclonic separation.Cyclone 15 underflow enters crystallizing and drying system 16 and obtains finished product sulfuric acid ammonium, ammonium nitrate, and top stream clear liquid returns in oxidation trough 10 and carries out precipitate and separate.Fresh water (FW) 17 delivers to the sparge pipe of top layer demist layer through pressurization, rinses, prevent fouling to demist layer 7.
Embodiment 1
Certain steam power plant, 3 130t/h boilers adopt this desulphurization and denitration technique, and desulfurizing tower liquid-gas ratio is 8L/m
3, desulfurizing tower pH value controls at 5.9-6.0, and oxidation trough pH value controls at 5.6-6.0, and ozone supply amount is 1: 1, and porous plate is positioned at 0.6m above oxidation air; Entrance SO
2concentration is 6324mg/m
3, NO concentration is 273mg/m
3, flue-gas temperature is 142 DEG C, outlet SO
2concentration is 38mg/m
3, NO concentration is 13mg/m
3, ammonium sulfate purity is 96.9%, and ammonia sulfate crystal particle size range is 1mm-3mm.
Embodiment 2
Certain power plant for self-supply, 1 335WM unit adopts this desulphurization and denitration technique, and desulfurizing tower liquid-gas ratio is 8, and desulfurizing tower pH value controls at 5.9-6.2, and oxidation trough pH value controls at 5.8-6.0, and ozone supply amount is 1: 1, and porous plate is positioned at 0.5m above oxidation air; Entrance SO
2concentration is 5428mg/m
3, NO concentration is 413mg/m
3, flue-gas temperature is 139 DEG C, outlet SO
2concentration is 27mg/m3, NO concentration is 17mg/m
3, ammonium sulfate purity is 97.3%, and ammonia sulfate crystal particle size range is 1mm-3mm.
Embodiment 3
Certain power plant, 5 75t/h boilers adopt this desulphurization and denitration technique, and desulfurizing tower liquid-gas ratio is 7, and desulfurizing tower pH value controls at 5.9-6.1, and oxidation trough pH value controls at 5.6-5.8, and ozone supply amount is 1: 1, and porous plate is positioned at 0.7m above oxidation air; Entrance SO
2concentration is 3861mg/m
3, NO concentration is 477mg/m
3, flue-gas temperature is 137 DEG C, outlet SO
2concentration is 18mg/m3, NO concentration is 21mg/m
3, ammonium sulfate purity is 96.1%, and ammonia sulfate crystal particle size range is 1mm-3mm.
Claims (2)
1. the wet method combined desulfuring and denitrifying apparatus of amino, comprise the desulfurizing tower (3) of tape entry flue (5), liquid ammonia storage tank (1), ozone generator (19) and the booster fan (18) be positioned on gas approach (5), described desulfurizing tower is followed successively by demist layer from top to bottom in (3), spraying layer and tower reactor, it is characterized in that, also comprise an oxidation trough be communicated with described tower reactor (10) and be connected to the oxidation fan (14) of oxidation trough (10), described liquid ammonia storage tank (1) is communicated to described tower reactor by pipeline one tunnel, another road is communicated to described oxidation trough (10) bottom, described ozone generator (19) by pipeline connection to the air intake vent place of described booster fan (18), porous plate (11) is provided with in described oxidation trough (10), described oxidation trough (10) is with the oxidation wind entrance be communicated with oxidation fan (14), and described porous plate (11) is positioned at oxidation wind entrance top 0.5 ~ 0.8m place, the aperture of described porous plate (11) is 3 ~ 5cm, and percent opening is 50 ~ 80%,
Described demist layer is made up of baffle flaggy and the sparge pipe be positioned at above baffle flaggy, the quantity of described demist layer is two-layer, comprise bottom demist layer and top layer demist layer, the sparge pipe of described bottom demist layer is communicated with by the top of pipeline with described oxidation trough (10);
Nozzle on the sparge pipe of described demist layer is nozzle.
2. an amino wet method combined process for desulfurization and denitration, is characterized in that, comprising:
Ozone is sprayed in flue gas by the air intake vent of booster fan, be nitrogen dioxide by the nitrogen oxides in flue gas, flue gas after ozone oxidation is sent in desulfurizing tower, and sprayed into by liquefied ammonia in desulfurizing tower and absorb sulfur dioxide in flue gas and nitrogen dioxide, flue gas is got rid of after demist drying;
The circulation fluid absorbed in desulfurizing tower after sulfur dioxide and nitrogen dioxide is introduced in oxidation trough, in oxidation trough, passes into oxidation wind, circulation fluid is oxidized to ammonia sulfate crystal slurries; In oxidation trough, the pH value in liquefied ammonia adjustment oxidation trough is sent in oxidizing process; PH value in described desulfurizing tower is 5.8 ~ 6.2, and the pH value in described oxidation trough is 5.6-6.0; The quantity delivered of described ozone and the mol ratio of nitrogen oxides in effluent are 1:1;
Described ammonia sulfate crystal slurries are after cyclonic separation, and underflow is obtained finished product sulfuric acid ammonium after drying, and top stream sends desulfurizing tower inner top back to, carries out degree of depth denitration to flue gas.
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| CN105169923B (en) * | 2015-07-21 | 2017-06-20 | 大唐华银电力股份有限公司金竹山火力发电分公司 | One kind improves limestone/lime gypsum wet flue gas desulfurizing technique |
| CN106076089B (en) * | 2016-08-16 | 2018-10-02 | 苏州仕净环保科技股份有限公司 | A kind of desulphurization denitration vent gas treatment tower |
| CN106823753A (en) * | 2017-03-30 | 2017-06-13 | 贵州诺威施生物工程有限公司 | Desulfurizing tower and desulfurization recovery system |
| CN108499335A (en) * | 2018-06-08 | 2018-09-07 | 大唐环境产业集团股份有限公司 | A kind of string tower desulphurization system for rinsing demister using recycling filtrate water |
| CN112675690A (en) * | 2020-12-11 | 2021-04-20 | 杭州蕴泽环境科技有限公司 | Low-water-consumption wet desulphurization system and method |
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| EP0223803A1 (en) * | 1985-05-25 | 1987-06-03 | Hölter, Heinz, Dipl.-Ing. | METHOD FOR SIMULTANEOUSLY REMOVING BY WASHING SO 2?, NO x? AND OPTIONALLY OTHER NOXIOUS SUBSTANCES CONTAINED IN FLUE GASES IN HEATING INSTALLATIONS SUPPLIED WITH FOSSILE FUELS |
| CN1647849A (en) * | 2004-12-17 | 2005-08-03 | 王明祥 | Smoke desulfurizing method by amino-thiamine method |
| CN100496676C (en) * | 2007-04-30 | 2009-06-10 | 武汉凯迪电力环保有限公司 | Wet ammonia flue gas cleaning technology simultaneously removing various pollutant and system thereof |
| CN202179925U (en) * | 2011-06-29 | 2012-04-04 | 北京国电清新环保技术股份有限公司 | Integrated purification device of desulfurization and denitrification flue gas |
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