CN108339384A - A kind of coke oven flue gas desulfurization denitration method - Google Patents
A kind of coke oven flue gas desulfurization denitration method Download PDFInfo
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- CN108339384A CN108339384A CN201711445754.8A CN201711445754A CN108339384A CN 108339384 A CN108339384 A CN 108339384A CN 201711445754 A CN201711445754 A CN 201711445754A CN 108339384 A CN108339384 A CN 108339384A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
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- B01D2258/0283—Flue gases
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Abstract
The present invention relates to Air Pollution Control fields, provide a kind of coke oven flue gas desulfurization denitration method, include the following steps：Coke oven flue gas is passed through in hot-blast stove and promotes its temperature to 250 310 DEG C by S1；S2, then the coke oven flue gas for improving temperature is passed through in SCR reactors and is reacted in catalyst surface and ammonia；The coke oven flue gas for being stripped of nitrogen oxides is passed through heat pipe waste heat boiler, exchanged heat in heat pipe waste heat boiler by S3, is reduced coke oven flue gas temperature and is generated steam for plant area's use；The coke oven flue gas for reducing temperature is passed through desulfurizing tower, reacted with ammonium hydroxide in desulfurizing tower by S4；Mixed solution is passed through oxidation tank, is aoxidized in oxidation tank by S5, can be ammonium sulfate by the sulfite oxidation in mixed solution, and be passed through desulfurizing tower again, wherein the oxidation tank is located at outside the desulfurizing tower.The oxidation tank of the present invention is set to outside desulfurizing tower, on the one hand can effectively be controlled the escaping of ammonia rate, on the other hand oxidation process can be made more thorough.
Description
Technical field
The present invention relates to Air Pollution Control field, specially a kind of coke oven flue gas desulfurization denitration method.
Background technology
A variety of pollutant components are usually contained in industrial smoke, such as sulfur dioxide, nitrogen oxides, dust and are attached on dust
The substances such as heavy metal, bioxin, moisture can also carry part soluble inorganic salt in flue gas.Existing smoke processing system master
If being handled for Single Pollution object, for such complicated flue gas characteristic, smoke processing system is also sufficiently complex, exists
The shortcomings that being difficult to timely respond to load variations.
Limestone-gypsum method or ammonia-ammonium sulfate method are commonly used in removing for sulfur dioxide in engineering, but both systems are all
It is difficult to handle nitrogen oxides, and there are serious exiting flue gas the phenomenon that containing alkali droplet, secondary pollution is caused to environment.It is right
In the removing of nitrogen oxides, traditional method mainly selective catalytic reduction method and selective non-catalytic reduction method, although effect
The problems such as rate is higher, but there are NH_3 leakage, escapes.
Invention content
The purpose of the present invention is to provide a kind of coke oven flue gas desulfurization denitration methods, can at least solve in the prior art
Segmental defect.
To achieve the above object, the embodiment of the present invention provides the following technical solutions：A kind of coke oven flue gas desulfurization denitration method,
Include the following steps：
Coke oven flue gas is passed through in hot-blast stove and promotes its temperature to 250-310 DEG C by S1；
S2, then the coke oven flue gas for improving temperature is passed through in SCR reactors and is reacted in catalyst surface and ammonia,
To remove the nitrogen oxides in coke oven flue gas；
The coke oven flue gas for being stripped of nitrogen oxides is passed through heat pipe waste heat boiler by S3, in heat pipe waste heat boiler into
Row heat exchange reduces coke oven flue gas temperature and generates steam for plant area's use；
The coke oven flue gas for reducing temperature is passed through desulfurizing tower, reacted with ammonium hydroxide in desulfurizing tower, to remove coke by S4
Sulfur dioxide in kiln gas, and form the mixed solution of ammonium sulfite, ammonium hydroxide and ammonium sulfate；
The mixed solution is passed through oxidation tank, is aoxidized in oxidation tank by S5, can be by the ammonium sulfite in mixed solution
It is oxidized to ammonium sulfate, and is passed through desulfurizing tower again, wherein the oxidation tank is located at outside the desulfurizing tower.
Further, ammonia is provided to the SCR reactors simultaneously using ammonia water tank, ammonium hydroxide is provided to the desulfurizing tower；Its
In, when providing ammonia to the SCR reactors, the ammonium hydroxide in ammonia water tank is first passed through ammonium hydroxide evaporator, ammonia is obtained and leads to again
Enter the SCR reactors, when providing ammonium hydroxide to desulfurizing tower, can the ammonium hydroxide in ammonia water tank be directly passed through the oxidation tank, then
It is passed through in desulfurizing tower by the oxidation tank.
Further, when ammonia is passed through the SCR reactors, ammonium hydroxide when being passed through oxidation tank and ammonium hydroxide be passed through it is equal when desulfurizing tower
Using liquid pump pressurized treatments.
Further, the desulfurizing tower is separated by concentrating part and oxidative absorption part using blast cap demarcation strip, concentrated
Part is located at the lower section of the desulfurizing tower, and oxidative absorption part is located at the top of the desulfurizing tower；Reaction in the S4 steps
It is happened at oxidative absorption part, the concentrating part after obtaining ammonium sulfate back to desulfurizing tower is aoxidized in the S5 steps and is evaporated
Concentration.
Further, the slurries reacted in oxidation tank are re-fed by desulfurizing tower circulation desulfurization using circulation technology, specifically
Ground uses circulating line, the connectivity part of circulating line and desulfurizing tower to be located at the oxidized portion between oxidation tank and desulfurizing tower.
Further, the slurries obtained below desulfurizing tower are returned again to by desulfurizing tower using concentration technology, specifically, if dense
Pipe, two ports of the concentration pipeline and the connectivity part of the desulfurizing tower are respectively positioned on the concentrating part.
Further, the coke oven flue gas for eliminating nitrogen oxides and sulfur dioxide first passes through wet type electricity before desulfurizing tower is discharged and removes
Dirt device is by other harmful substances and moisture removal in coke oven flue gas.
Further, it when desulfurizing tower is discharged in the ammonium sulfate of generation, first passes through ash filter and filters out and be blended in sulphur
Impurity in sour ammonium.
Further, it will be collected into ammonium sulfate surge tank by the filtered ammonium sulfate of ash filter, to carry
Supply plant area's ammonium sulfate preparation system.
Further, in oxidation tank during oxidative ammonium and during desulfurizing tower handles sulfur dioxide
It is all made of blender agitating solution, uniformly to mix.
Compared with prior art, the beneficial effects of the invention are as follows：
1, SCR reactors are first passed through and catalyst bed removes denitrification, are then gone again by desulfurizing tower and oxidation tank
Except sulfur dioxide, oxidation tank is set to outside desulfurizing tower, on the one hand can effectively control the escaping of ammonia rate, on the other hand can make oxidation process
More thoroughly.
2, can be by waste heat recovery by heat pipe waste heat boiler, and lead to plant area's steam pipe network, it is net to save coke oven flue gas
The operating cost of change.
3, using circulation technology, it is ensured that the removal rate of higher sulfur dioxide.
4, using concentration technology, the ammonium sulfate of larger concentration can be obtained.
5, other harmful substances and moisture in cigarette can be eliminated by setting wet electrical dust precipitator so that finally be arranged by outlet flue
The flue gas gone out is nontoxic and drying can be used.
6, the impurity being blended in ammonium sulfate can be filtered out by setting ash filter so that the quality of the ammonium sulfate of acquisition is more
It is good.
7, setting ammonium sulfate surge tank can be convenient for collecting ammonium sulfate；
8, it can ensure that the solution in oxidation tank and desulfurizing tower keeps uniformly mixed state by blender.
Description of the drawings
Fig. 1 is a kind of step flow chart of coke oven flue gas desulfurization denitration method provided in an embodiment of the present invention；
Fig. 2 is a kind of structural schematic diagram of coke oven flue gas desulfurization denitration method provided in an embodiment of the present invention；
In reference numeral：1- smoke-intake pipes；2- denitrification apparatus；20- hot-blast stoves；21-SCR reactors；22- catalyst beds；
3- desulfurizers；30- desulfurizing towers；31- oxidation tanks；310- first sprays line；311- second sprays line；312- thirds spray line；
313- outlet flues；314- first goes out liquid portion；315- second goes out liquid portion；316- first pipes；317- second pipes；More than 4- heat pipe-types
Heat boiler；5- plant areas steam pipe network；6- ammonia feedways；60- ammonia water tanks；61- ammonium hydroxide evaporators；7- blast cap demarcation strips；80-
Wet electrical dust precipitator；81- ash filters；82- ammonium sulfate surge tanks；83- plant areas ammonium sulfate preparation system；The first liquid pumps of 90-；
The second liquid pumps of 91-；92- third liquid pumps；The 4th liquid pumps of 93-；The 5th liquid pumps of 94-；The 6th liquid pumps of 95-；The 7th liquid pumps of 96-；97- is stirred
Mix device；98- water inlet lines.
Specific implementation mode
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation describes, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts all other
Embodiment shall fall within the protection scope of the present invention.
It please refers to Fig.1 and Fig. 2, the embodiment of the present invention provides a kind of coke oven flue gas desulfurization denitration method, include the following steps：
Coke oven flue gas is passed through in hot-blast stove and promotes its temperature to 250-310 DEG C by S1；S2, then the coke oven flue gas that temperature will be improved
It is passed through in SCR reactors and reacts in catalyst surface and ammonia, to remove the nitrogen oxides in coke oven flue gas；S3 will take off
In addition to the coke oven flue gas of nitrogen oxides is passed through heat pipe waste heat boiler, exchanges heat in heat pipe waste heat boiler, reduce coke
Kiln gas temperature and generate steam for plant area use；The coke oven flue gas for reducing temperature is passed through desulfurizing tower, in desulfurizing tower by S4
It reacts with ammonium hydroxide, to remove the sulfur dioxide in coke oven flue gas, and forms the mixing of ammonium sulfite, ammonium hydroxide and ammonium sulfate
Solution；The mixed solution is passed through oxidation tank, is aoxidized in oxidation tank by S5, can be by the ammonium sulfite oxygen in mixed solution
Ammonium sulfate is turned to, and is passed through desulfurizing tower again, wherein the oxidation tank is located at outside the desulfurizing tower.The active temperature of catalyst
To belong to middle low temperature at 250~310 DEG C, with by hot-blast stove rise Lai Temperature Matching, can be saved about compared with high temperature denitrating technique
50% thermal energy, 300 DEG C or so of the flue gas come out with SCR reactors using heat pipe waste heat boiler are exchanged heat, and are generated
0.8MPa steam is incorporated to plant area's steam pipe network, and can meet the work temperature in desulfurizing tower by flue gas cool-down to 150-170 DEG C
Degree, and the operating cost of cock-oven gas purifying is saved, desulfurizing tower can allow in ammonia spray to coke oven flue gas, form sulfurous acid
The mixed solution of ammonium, ammonium sulfate and ammonium hydroxide, obtained ammonium sulfite enter in oxidation tank, can in oxidation tank further oxygen
Change forms ammonium sulfate, this tower external oxidation method can effectively control the escaping of ammonia rate.On the one hand this method may be used compared with existing method
Effectively control the escaping of ammonia rate, on the other hand can make oxidation process more thorough, eliminate the same of nitrogen oxides and sulfur dioxide
When ammonium sulfate is also obtained, can be used for industrial production ammonium sulfate.
It is specific embodiment below：
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, being carried simultaneously to the SCR reactors using ammonia water tank
For ammonia, ammonium hydroxide is provided to the desulfurizing tower；Wherein, when providing ammonia to the SCR reactors, first by the ammonia in ammonia water tank
Water is passed through ammonium hydroxide evaporator, obtains ammonia and is passed through the SCR reactors again, can be directly by ammonia when providing ammonium hydroxide to desulfurizing tower
Ammonium hydroxide in water pot is passed through the oxidation tank, then is passed through in desulfurizing tower by the oxidation tank.It by this method can be by same
A ammonia water tank provides ammonium hydroxide and ammonia simultaneously, saves cost of manufacture.
Said program is advanced optimized, when ammonia is passed through the SCR reactors, ammonium hydroxide is when being passed through oxidation tank and ammonium hydroxide is logical
Liquid pump pressurized treatments are all made of when entering desulfurizing tower.The placement constraint of pipeline can be overcome using liquid pump.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, the desulfurizing tower is separated into using blast cap demarcation strip
For concentrating part and oxidative absorption part, concentrating part is located at the lower section of the desulfurizing tower, and oxidative absorption part is located at described de-
The top of sulphur tower；Reaction in the S4 steps is happened at oxidative absorption part, is aoxidized in the S5 steps after obtaining ammonium sulfate
Concentrating part back to desulfurizing tower is evaporated concentration.Concentrating part is used to purify, and obtains the ammonium sulfate of higher concentration,
Oxidative absorption part is used to dispose the sulfur dioxide in coke oven flue gas.
Said program is advanced optimized, the slurries reacted in oxidation tank, which are re-fed into desulfurizing tower, using circulation technology follows
Ring desulfurization specifically uses circulating line, the connectivity part of circulating line and desulfurizing tower to be located at institute between oxidation tank and desulfurizing tower
State oxidized portion.Circulation technology can ensure the removal rate of higher sulfur dioxide.
As the prioritization scheme of the embodiment of the present invention, the slurries obtained below desulfurizing tower are again returned to using concentration technology
To desulfurizing tower, specifically, if concentration pipeline, two ports of the concentration pipeline and the connectivity part of the desulfurizing tower are respectively positioned on institute
State concentrating part.The ammonium sulfate of larger concentration can be obtained in concentration technology.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, eliminating the coke oven cigarette of nitrogen oxides and sulfur dioxide
Gas first passes through wet electrical dust precipitator by other harmful substances and moisture removal in coke oven flue gas before desulfurizing tower is discharged.So that
The flue gas being finally discharged by outlet flue is nontoxic and drying can be used.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, when desulfurizing tower is discharged in the ammonium sulfate of generation,
It first passes through ash filter and filters out the impurity being blended in ammonium sulfate, can make the better quality of the ammonium sulfate obtained.
Said program is advanced optimized, referring to Fig. 2, will be collected by the filtered ammonium sulfate of ash filter
In ammonium sulfate surge tank, in order to provide plant area's ammonium sulfate preparation system is given.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, in oxidation tank during oxidative ammonium with
And it is all made of blender agitating solution during desulfurizing tower handles sulfur dioxide, uniformly to mix.
The embodiment of the present invention also provides a kind of coke oven flue gas system for desulfuration and denitration, referring to Fig. 2, this system include into
Smoke pipe 1 is used for the denitrification apparatus 2 of denitration, is used for the desulfurizer 3 of desulfurization, and for the denitrification apparatus 2 and described de-
Ammonia feedway 6 of the sulphur device 3 for ammonia.Wherein smoke-intake pipe 1 enters this system for coke oven flue gas, and denitrification apparatus 2 includes connection
Hot-blast stove 20, SCR (selective catalytic reduction) reactor 21 and catalyst bed 22, hot-blast stove 20 can be by the cigarettes of entrance
Gas is warming up to 250~310 DEG C, and catalyst bed 22 uses honeycombed catalyst, and active temperature is belonged at 250~310 DEG C
Middle low temperature, with by hot-blast stove 20 rise Lai Temperature Matching, compared with the thermal energy that high temperature denitrating technique can save about 50%, flue gas into
Enter smoke-intake pipe 1, is then heated up later to the ammonia that in SCR reactors 21, at the same time ammonia feedway 6 generates by hot-blast stove 20
Also it can be passed through in SCR reactors 21, the nitrogen oxides in flue gas can be removed through catalyst reaction.Then the flue gas is passed through
There is spray space to desulfurizing tower 30, in desulfurizing tower 30, can allow in the ammonia spray to flue gas that ammonia feedway 6 provides, shape
At the mixed solution of ammonium sulfite, ammonium sulfate and ammonium hydroxide, this is the prior art.The spray space is equipped with the in the vertical direction
One sprinkling line 310, second sprays line 311 and third sprays line 312, and multiple spray heads are all provided on each sprinkling line, it is preferred that
As shown in Fig. 2, horizontal blast cap demarcation strip 7 is set between first layer sprinkling line and second layer sprinkling line, the one of the blast cap demarcation strip 7
End goes out liquid portion 314 with first and connect, it can realize blocking flue gas and slurries are converged to the first purpose for going out liquid portion 314.Stream
The ammonium sulfite gone out enters in oxidation tank 31, and further oxidation forms ammonium sulfate in oxidation tank 31.Oxidation tank 31 is connected with
Oxidation fan, to accelerated oxidation rate.SCR reactors 21 are installed on flue gas collating unit, are used for rectification.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, this system further includes that can connect with plant area steam pipe network 5
Logical heat pipe waste heat boiler 4, the catalyst bed 22 are connected to the heat pipe waste heat boiler 4, the heat pipe-type waste heat
Boiler 4 is connected to the oxidation tank 31.300 DEG C or so of the flue gas come out using heat pipe waste heat boiler 4 and SCR reactors 21
It exchanges heat, generates 0.8MPa steam and be incorporated to plant area's steam pipe network 5, and desulfurization can be met by flue gas cool-down to 150-170 DEG C
Operating temperature in tower 30, and save the operating cost of cock-oven gas purifying.Heat pipe waste heat boiler 4 is connected with water inlet line
98, water can be thus supplemented into boiler.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, above-mentioned ammonia feedway 6 include ammonia water tank 60 and
Ammonium hydroxide evaporator 61,60 side of the ammonia water tank are connected to the oxidation tank 31,60 other side of the ammonia water tank and the ammonium hydroxide
Evaporator 61 is connected to, and the ammonium hydroxide evaporator 61 is connected to the SCR reactors 21.Ammonium hydroxide is stored in ammonia water tank 60, it has
Two outlet ends, one end are connected to by pipeline with oxidation tank 31, and the other end is connected to by pipeline with ammonium hydroxide evaporator 61, ammonium hydroxide warp
It crosses ammonium hydroxide evaporator 61 and becomes being passed through SCR reactors 21 again after ammonia and reacted.Preferably, the pipeline difference being connected at two
If the first liquid pump 90 and the second liquid pump 91, can overcome the placement constraint of pipeline.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, desulfurizing tower 30 is installed on first pipe 316, the first pipe
316 one end of road is connected to the desulfurizing tower 30, and connectivity part is located at the top of the blast cap demarcation strip 7, the first pipe 316
The other end is connected to the oxidation tank 31；The first pipe 316 is installed on third liquid pump 92.First pipe 316 with it is above-mentioned
First sprinkling line 310 is connected to, and is equipped with third liquid pump 92, can the slurries reacted in oxidation tank 31 be re-fed into desulfurizing tower 30
Circulation desulfurization can make finally obtained ammonium sulfate quality higher.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, desulfurizing tower 30 is installed on second pipe 317, described
The both ends of two pipelines 317 are connected to the desulfurizing tower 30, and two connectivity parts are respectively positioned on 7 lower section of the blast cap demarcation strip；Institute
It states second pipe 317 and is installed on the 4th liquid pump 93.Second pipe 317 is connected to above-mentioned third sprinkling line 312, is equipped with the 4th liquid
Pump 93, the slurries that can obtain 30 lower section of desulfurizing tower return again to desulfurizing tower 30, make slurries and high temperature cigarette by spraying space
Gas abundant mass transfer heat exchange, flue gas cool-down while, evaporate a large amount of moisture, and ammonium sulfate is made to achieve the purpose that concentration.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, desulfurizing tower 30 is installed on third pipeline, the third pipe
Road one end is connected to oxidation tank 31, and the other end is connected to the second above-mentioned sprinkling line 311, is equipped with the 6th liquid pump 95, can will be filled
The slurries divided after oxidation are supplemented to desulfurizing tower 30, promote concentrating degree.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, being installed at the outlet flue 313 in desulfurizing tower 30
There is wet electrical dust precipitator 80.Other harmful substances and the moisture in cigarette can be eliminated so that be finally discharged by outlet flue 313
Flue gas is nontoxic and drying can be used.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, this system further includes ash filter 81, it is described de-
30 lower part of sulphur tower has goes out liquid portion 315 for ammonium sulfate flows out second, and described second goes out liquid portion 315 filters with the lime-ash
Device 81 is connected to, and the 5th liquid pump 94 is equipped between ash filter 81 and the flow path of the desulfurizing tower 30.If ash filter 81
The impurity being blended in ammonium sulfate can be filtered out so that the better quality of the ammonium sulfate of acquisition.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, this system further includes that can prepare to be with plant area's ammonium sulfate
The ammonium sulfate surge tank 82 of 83 connection of system, the ammonium sulfate surge tank 82 are connected to the ash filter 81.If ammonium sulfate is slow
Rushing tank 82 can be convenient for collecting ammonium sulfate, and ammonium sulfate is then pushed to plant area's ammonium sulfate system by the 7th liquid pump 96
Ammonium sulfate is prepared in standby system 83.
As the prioritization scheme of the embodiment of the present invention, referring to Fig. 2, being equipped in desulfurizing tower 30 and ammonium sulfate surge tank 82
Blender 97, for stirring evenly solution.
It although an embodiment of the present invention has been shown and described, for the ordinary skill in the art, can be with
Understanding without departing from the principles and spirit of the present invention can carry out these embodiments a variety of variations, modification, replace
And modification, the scope of the present invention is defined by the appended.
Claims (10)
1. a kind of coke oven flue gas desulfurization denitration method, which is characterized in that include the following steps：
Coke oven flue gas is passed through in hot-blast stove and promotes its temperature to 250-310 DEG C by S1；
S2, then the coke oven flue gas for improving temperature is passed through in SCR reactors and is reacted in catalyst surface and ammonia, with de-
Except the nitrogen oxides in coke oven flue gas；
The coke oven flue gas for being stripped of nitrogen oxides is passed through heat pipe waste heat boiler, is changed in heat pipe waste heat boiler by S3
Heat reduces coke oven flue gas temperature and generates steam for plant area's use；
The coke oven flue gas for reducing temperature is passed through desulfurizing tower, reacted with ammonium hydroxide in desulfurizing tower by S4, to remove coke oven cigarette
Sulfur dioxide in gas, and form the mixed solution of ammonium sulfite, ammonium hydroxide and ammonium sulfate；
The mixed solution is passed through oxidation tank, is aoxidized in oxidation tank by S5, can be by the sulfite oxidation in mixed solution
For ammonium sulfate, and it is passed through desulfurizing tower again, wherein the oxidation tank is located at outside the desulfurizing tower.
2. a kind of coke oven flue gas desulfurization denitration method as described in claim 1, it is characterised in that：Institute is given simultaneously using ammonia water tank
It states SCR reactors and ammonia is provided, ammonium hydroxide is provided to the desulfurizing tower；Wherein, when providing ammonia to the SCR reactors, first
Ammonium hydroxide in ammonia water tank is passed through ammonium hydroxide evaporator, ammonia is obtained and is passed through the SCR reactors again, ammonium hydroxide is being provided to desulfurizing tower
When, can the ammonium hydroxide in ammonia water tank be directly passed through the oxidation tank, then be passed through in desulfurizing tower by the oxidation tank.
3. a kind of coke oven flue gas desulfurization denitration method as claimed in claim 2, it is characterised in that：It is anti-that ammonia is passed through the SCR
It answers when device, be all made of liquid pump pressurized treatments when ammonium hydroxide is passed through oxidation tank and when ammonium hydroxide is passed through desulfurizing tower.
4. a kind of coke oven flue gas desulfurization denitration method as described in claim 1, it is characterised in that：Using blast cap demarcation strip by institute
It states desulfurizing tower and is separated into concentrating part and oxidative absorption part, concentrating part is located at the lower section of the desulfurizing tower, oxidative absorption
Part is located at the top of the desulfurizing tower；Reaction in the S4 steps is happened at oxidative absorption part, oxygen in the S5 steps
Change the concentrating part after obtaining ammonium sulfate back to desulfurizing tower and is evaporated concentration.
5. a kind of coke oven flue gas desulfurization denitration method as claimed in claim 4, it is characterised in that：It will be aoxidized using circulation technology
The slurries reacted in tank are re-fed into desulfurizing tower circulation desulfurization, specifically, circulation pipe are used between oxidation tank and desulfurizing tower
The connectivity part of road, circulating line and desulfurizing tower is located at the oxidized portion.
6. a kind of coke oven flue gas desulfurization denitration method as claimed in claim 4, it is characterised in that：Using concentration technology by desulfurization
The slurries obtained below tower return again to desulfurizing tower, specifically, if concentration pipeline, two ports of the concentration pipeline and institute
The connectivity part for stating desulfurizing tower is respectively positioned on the concentrating part.
7. a kind of coke oven flue gas desulfurization denitration method as described in claim 1, it is characterised in that：Eliminate nitrogen oxides and two
The coke oven flue gas of sulfur oxide first passed through before desulfurizing tower is discharged wet electrical dust precipitator by other harmful substances in coke oven flue gas with
And moisture removal.
8. a kind of coke oven flue gas desulfurization denitration method as described in claim 1, it is characterised in that：By the ammonium sulfate of generation
When desulfurizing tower is discharged, first passes through ash filter and filter out the impurity being blended in ammonium sulfate.
9. a kind of coke oven flue gas desulfurization denitration method as claimed in claim 8, it is characterised in that：Ash filter mistake will be passed through
Ammonium sulfate after filter is collected into ammonium sulfate surge tank, in order to provide plant area's ammonium sulfate preparation system is given.
10. a kind of coke oven flue gas desulfurization denitration method as described in claim 1, it is characterised in that：It is aoxidized in oxidation tank sub-
It is all made of blender agitating solution during ammonium sulfate and during desulfurizing tower handles sulfur dioxide, uniformly to mix
It closes.
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