CN109569248A - Remove tar and the device and its removal methods of collaboration denitration in coke oven flue gas - Google Patents
Remove tar and the device and its removal methods of collaboration denitration in coke oven flue gas Download PDFInfo
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- CN109569248A CN109569248A CN201811636382.1A CN201811636382A CN109569248A CN 109569248 A CN109569248 A CN 109569248A CN 201811636382 A CN201811636382 A CN 201811636382A CN 109569248 A CN109569248 A CN 109569248A
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- Prior art keywords
- flue gas
- electric precipitator
- ontology
- pollutant
- wash
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- 239000003546 flue gas Substances 0.000 title claims abstract description 205
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 194
- 239000000571 coke Substances 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 24
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 133
- 239000012716 precipitator Substances 0.000 claims abstract description 96
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 59
- 231100000719 pollutant Toxicity 0.000 claims abstract description 59
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 37
- 239000000443 aerosol Substances 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 13
- 230000015556 catabolic process Effects 0.000 claims abstract description 11
- 238000006731 degradation reaction Methods 0.000 claims abstract description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 7
- 239000000428 dust Substances 0.000 claims description 42
- 238000005406 washing Methods 0.000 claims description 42
- 239000003054 catalyst Substances 0.000 claims description 38
- 239000010419 fine particle Substances 0.000 claims description 26
- 239000005416 organic matter Substances 0.000 claims description 26
- 239000007921 spray Substances 0.000 claims description 26
- 229920002521 macromolecule Polymers 0.000 claims description 19
- 239000002245 particle Substances 0.000 claims description 13
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 12
- 150000003254 radicals Chemical class 0.000 claims description 10
- 230000005611 electricity Effects 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 3
- 239000012071 phase Substances 0.000 claims description 3
- 150000001732 carboxylic acid derivatives Chemical class 0.000 claims 4
- 239000011269 tar Substances 0.000 abstract description 36
- 239000000295 fuel oil Substances 0.000 abstract description 19
- 239000003517 fume Substances 0.000 abstract description 3
- 150000001735 carboxylic acids Chemical class 0.000 description 19
- 238000001816 cooling Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 239000000243 solution Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- 239000012530 fluid Substances 0.000 description 6
- 235000019504 cigarettes Nutrition 0.000 description 5
- 239000006196 drop Substances 0.000 description 4
- 239000000284 extract Substances 0.000 description 4
- -1 flue gas Compound Chemical class 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- WWILHZQYNPQALT-UHFFFAOYSA-N 2-methyl-2-morpholin-4-ylpropanal Chemical compound O=CC(C)(C)N1CCOCC1 WWILHZQYNPQALT-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 3
- 230000000903 blocking effect Effects 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000002386 leaching Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- XOCUXOWLYLLJLV-UHFFFAOYSA-N [O].[S] Chemical compound [O].[S] XOCUXOWLYLLJLV-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000003628 erosive effect Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000011859 microparticle Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000012855 volatile organic compound Substances 0.000 description 2
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 150000007933 aliphatic carboxylic acids Chemical group 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/02—Plant or installations having external electricity supply
- B03C3/04—Plant or installations having external electricity supply dry type
-
- 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
- B01D53/32—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 by electrical effects other than those provided for in group B01D61/00
- B01D53/323—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 by electrical effects other than those provided for in group B01D61/00 by electrostatic effects or by high-voltage electric fields
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
Abstract
The present invention relates to tar and the devices and its removal methods of collaboration denitration in fume treatment auxiliary technical field more particularly to a kind of removing coke oven flue gas.Tar and to cooperate with the device of denitration include that exhaust gas generator, the first electric precipitator, reducing agent add component, Benitration reactor, wash, the second electric precipitator and chimney in the removing coke oven flue gas.A kind of method for removing pollutant, applied in tar in above-mentioned removing coke oven flue gas and the device of collaboration denitration, comprising: the flue gas in exhaust gas generator is carried out the first processing by the first electric precipitator；Reducing agent adds component and adds reducing agent into flue gas；Nitrogen oxides in flue gas is catalysed and reduced into nitrogen by Benitration reactor；Pollutant in wash trapping removal flue gas；Second electric precipitator traps washed component treated the electrically charged combined pollutant in aerosol form in flue gas；Neat stress is discharged chimney.The present invention by flue gas tar heavy oil degradation and cooperation-removal combined pollutant.
Description
Technical field
The present invention relates to tar in fume treatment auxiliary technical field more particularly to a kind of removing coke oven flue gas and collaboration are de-
The device and its removal methods of nitre.
Background technique
Coke oven flue gas can be generated after coke-stove gas is burned, can contain macromolecule organic matter (weight in this coke oven flue gas
Tar), fine particle, NOXAnd SO2Equal combined pollutants, are expelled directly out, it will cause air pollutions, endanger ring if not handling
Border.
Coke ADSORPTION IN A FIXED BED method is mostly used to eliminate the tar heavy oil in coke oven flue gas on existing market greatly, and coke is fixed
Bed removal tar heavy oil low efficiency, plant maintenance heavy workload, system resistance drop are big, in addition, the cigarette after being handled in this manner
A certain amount of tar heavy oil is still carried in gas, be easy to cause catalyst blockage, reduces the service life of catalyst, and pollution and corruption
The pipeline etc. of erosion transmission flue gas.
Summary of the invention
It reduces catalyst to cause adherency to block catalyst in order to solve in flue gas in the related technology tar heavy oil and uses
The technical issues of service life, the embodiment of the invention provides tar in a kind of removing coke oven flue gas and cooperates with the device of denitration and its takes off
Except method, its object is to which the tar heavy oil in flue gas is degraded into low boiling point, water-soluble good small carboxylic acid molecules and derivative etc., from
And tar heavy oil is avoided not removed and occluding device from flue gas, increase the service life of catalyst.
In a first aspect, the present invention provides tar and the device of collaboration denitration in a kind of removing coke oven flue gas, including exhaust gas
Generator, the first electric precipitator, wash, the second electric precipitator and chimney, in which: further include that reducing agent adds component and takes off
Nitre reactor, the first electric precipitator include the first electric precipitator ontology, plasma power supply, the first discharge electrode and the first dust collector pole,
Exhaust gas generator, the first electric precipitator ontology, reducing agent add component, Benitration reactor, wash, the second electric precipitator and
Chimney is sequentially connected, and the first discharge electrode and the first dust collector pole are set to the first electric precipitator body interior, plasma power supply setting
In the outside of the first electric precipitator ontology, the first discharge electrode is connected with the cathode output end of plasma power supply, the first dust collector pole with
The cathode output end of plasma power supply is connected.
It is by the first electric precipitator that the macromolecule organic matter degradation in the flue gas in exhaust gas generator is low at carboxylic acid etc.
Molecular weight organics and by lower valency nitrogen oxides at high-valence state nitrogen oxides, consequently facilitating being taken off in wash
It removes, and keeps fine particulates charged in order to be removed, in addition, can be stifled to avoid its adherency by macromolecule organic matter degradation
The catalyst in Benitration reactor is filled in, the problem of catalyst activity reduces is avoided；Pass through plasma power supply cathode output end
To the first discharge electrode power, by flue gas oxygen and water be ionized into a large amount of living radicals, by the macromolecule in flue gas
Organic matter degradation and by lower valency nitrogen oxides, and keep fine particle charged, by plasma power supply cathode output end to
First dust collector pole power supply, to adsorb electrically charged fine particulates to remove it from flue gas；Pass through the second electric precipitator
Further trap washed component treated in flue gas in fine particulates existing for aerosol state, to ensure to discharge cigarette
Fine particulates content in gas is lower, so that neat stress be discharged by chimney.
It optionally, further include hot-blast stove, Benitration reactor includes Benitration reactor ontology, storage in Benitration reactor ontology
There is catalyst, Benitration reactor ontology is equipped with the second input terminal and second output terminal, the second input terminal and the first electric precipitator
It is connected by first pipe with hot-blast stove between first output end of ontology, second output terminal is connected with wash, and second is defeated
Enter end and is relatively higher than second output terminal.
It is installed with catalyst in Benitration reactor, the nitrogen oxides in the reducing agent and flue gas that add is made to pass through catalysis
Chemical reaction, to generate nitrogen and water, further, it is also possible to the escape amount of reducing agent be reduced, so that the reduction reaction sufficiently carries out；
In addition, flue-gas temperature is heated to the minimum of catalyst permission when in order to need and uses temperature by the setting to hot-blast stove
More than.
Optionally, wash includes washing ontology, circulated sprinkling portion and high efficiency demister, circulated sprinkling portion and is efficiently removed
Day with fog is set in turn in from the bottom up on washing ontology, and washing ontology is equipped with third input terminal and third output end, third are defeated
Enter end and be relatively lower than the setting of circulated sprinkling portion, third output end is relatively higher than high efficiency demister setting, third input terminal and second
Output end is connected, and third output end is connected with the second electric precipitator.
In washing ontology, lye is sprayed to flue gas by circulated sprinkling portion, by flue gas 90% or more high-valence state
The compositions such as the combined pollutants such as nitrogen oxides, organic acid, amine, oxysulfide, low molecule organic matter (VOCs) are absorbed and are removed, then
Secondary trapping will be carried out to it by high efficiency demister, in order to efficiently remove the combined pollutant in flue gas.
Optionally, wash further includes kinetic pump, and spraying layer is set to washing body interior, and kinetic pump is set to washing
The outside of ontology and be connected to setting with washing body interior, kinetic pump passes through the first pipeline and is connected with circulated sprinkling portion.
By the setting to kinetic pump, the solution extraction of body bottom portion can will be washed in order to kinetic pump to circulated sprinkling portion
Spray, consequently facilitating the lye to spray is recycled.
Optionally, the second electric precipitator gathers dust including the second electric precipitator ontology, the pulse power, the second discharge electrode, second
Pole and rinse-system, the pulse power are set to the second electric precipitator body exterior, and the second discharge electrode and the second dust collector pole are set to
Second electric precipitator body interior, the cathode output end and cathode output end of the pulse power are received with the second discharge electrode and second respectively
Dirt is extremely connected, and rinse-system is set to the second electric precipitator body interior and is located above the second dust collector pole.
By the setting to the second electric precipitator, efficiently to trap in flue gas in organic matter existing for aerosol form, thin
Microparticle and free water etc. to realize the minimum discharge of pollutant, while reducing the entrainment discharge amount of neat stress free water.
Second aspect, the present invention provides a kind of method for removing pollutant, which is characterized in that is applied to above-mentioned removing coke oven
It tar and is cooperateed in the device of denitration in flue gas, the method for removing pollutant includes: that macromolecule is generated in exhaust gas generator
Organic matter, fine particle, NOXAnd SO2Equal combined pollutants are simultaneously transported in the first electric precipitator；First electric precipitator pair
Flue gas carries out the first processing, so that dust fine particle is charged in order to remove in flue gas, and the macromolecule in flue gas is had
Machine object is degraded into the low-molecular-weight organic matters such as carboxylic acid and by lower valency nitrogen oxides at high-valence state nitrogen oxides；Reducing agent is thrown
Component is added to add reducing agent in through the first treated flue gas；Benitration reactor will add component through reducing agent treated cigarette
Nitrogen oxides in gas is catalysed and reduced into nitrogen；Through the first electric precipitator and Benitration reactor, treated for wash trapping
The low-molecular-weight organic matters such as the carboxylic acid in flue gas, high-valence state nitrogen oxides, oxysulfide and charged fine particulates；Second
Electric precipitator traps washed component treated the electrically charged combined pollutant in aerosol form in flue gas；Chimney will be through
Treated the neat stress discharge of second electric precipitator.
By above-mentioned method for removing pollutant, the tar heavy oil in flue gas, i.e. macromolecule organic matter can be degraded,
With the catalyst in anti-clogging Benitration reactor, the service life of catalyst is influenced；In addition, also by the lower valency nitrogen oxygen in flue gas
Compound is oxidized to high-valence state nitrogen oxides, consequently facilitating by wash by it absorbing and removing from flue gas, wash is also
Low molecular carboxylic acid type organic, high-valence state nitrogen oxides, oxysulfide, fine particle etc. in flue gas is dissolved and absorbed or washed
Removing, then by the second electric precipitator by flue gas due to wash washing generate the combined pollutant in aerosol form
It is removed in depth, so that the combined pollutant in flue gas is cleaned, avoids the exhaust emission atmosphere of pollutant in flue gas.
Optionally, the first processing includes: that plasma power supply is powered to the first discharge electrode；Streamer occurs for the first electric discharge pole surface
It discharges so as to fine solid particle charging particle and make O in flue gas in flue gas2、H2It is free that 0 equal flue gases molecular ionization generates high activity
Base；High mars free radical is by the lower valency nitrogen oxides in flue gas and by macromolecule organic matter degradation, the first dust collector pole
For adsorbing charged fine solid particle particle to remove it from flue gas.
By the first discharge electrode by flue gas oxygen and the flue gases molecular ionization such as water at free radical, then passing through free radical will
Macromolecule organic matter, that is, tar heavy oil in flue gas is degraded into the low-molecular-weight organic matters such as carboxylic acid, by lower valency nitrogen oxides
At high-valence state nitrogen oxides, removed in order to subsequent；In addition, the first discharge electrode makes fine particle charged, so that subtle
Particle is adsorbed to remove from flue gas.
Optionally, wash includes washing ontology, circulated sprinkling portion and high efficiency demister, and wash is trapped through first
Low-molecular-weight organic matters, high-valence state nitrogen oxides, the sulphur oxygen such as the carboxylic acid in electric precipitator and Benitration reactor treated flue gas
Compound and charged fine particulates include: flue gas from being input in washing ontology in Benitration reactor, and along washing ontology
It spreads from bottom to up；Circulated sprinkling portion sprays lye to flue gas, by macromoleculars such as high-valence state nitrogen oxides, carboxylic acids in flue gas
The combined pollutants washing absorption such as organic matter, oxysulfide enters in liquid phase, and flue gas is in aerosol form by spray generation
Combined pollutant is sent to high efficiency demister with flue gas；High efficiency demister trapping is thin in the flue gas after circulated sprinkling portion spray
Microparticle object and combined pollutant in aerosol form, it is removed from flue gas.
Flue gas is sprayed by circulated sprinkling portion, by the combined pollutant absorbing and removing in flue gas；By efficient
Demister carries out secondary trapping to combined pollutant, the combined pollutant in flue gas is removed clean.
Optionally, the second electric precipitator gathers dust including the second electric precipitator ontology, the pulse power, the second discharge electrode, second
Pole and rinse-system, the second electric precipitator trap washed component treated electrically charged the answering in aerosol form in flue gas
Closing pollutant includes: after flue gas inputs in the second electric precipitator ontology, and the pulse power is transmitted electricity to the second discharge electrode, so that flue gas
In fine particle it is charged, fine particle is enriched in second and is gathered dust pole surface, so that it be removed from flue gas；Rinse system
It unites and is rinsed to flue gas, the second discharge electrode and the second dust collector pole surface spraying solution, to dissolve answering in aerosol form in flue gas
It closes pollutant and keeps the second discharge electrode and the second dust collector pole surface cleaning.
By being set to the second electric precipitator ontology, the pulse power, the second discharge electrode, the second dust collector pole and rinse-system
It sets, convenient for further removing the fine particle in flue gas, and is trapped in flue gas by rinse-system in the compound of aerosol form
Pollutant is dissolved in it in liquid phase, to avoid pollution environment.
Optionally, reducing agent adds and is connected with hot-blast stove between component and Benitration reactor, and hot-blast stove will be added through reducing agent
Component treated flue gas to catalyst allows it is minimum using it is more than temperature or timing by flue gas to 350 DEG C with
On.
When flue-gas temperature is too low or catalyst is blocked, hot-blast stove minimum makes what flue gas to catalyst allowed
More than temperature, or flue gas is warming up to 350 DEG C or more so as to deposit or be adhered in catalyst surface and micro channel by timing
Ammonium hydrogen sulfate, carboxylic acid and its derivative decompose or distillation, restore the activity of catalyst.
It should be understood that the above general description and the following detailed description are merely exemplary, this can not be limited
Invention.
Detailed description of the invention
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for
For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings other
Attached drawing.
Fig. 1 is to remove tar in coke oven flue gas in an embodiment provided by the invention and the structure of the device of denitration is cooperateed with to show
It is intended to；
Fig. 2 is the structure that tar and the device of collaboration denitration in coke oven flue gas are removed in another embodiment provided by the invention
Schematic diagram；
Fig. 3 is the flow chart of method for removing pollutant provided by the invention.
In figure: 100, exhaust gas generator；110, air door is bypassed；200, the first electric precipitator；210, the first electric precipitator sheet
Body；211, first input end；212, the first output end；220, plasma power supply；230, the first discharge electrode；240, it first gathers dust
Pole；300, reducing agent adds component；400, hot-blast stove；500, Benitration reactor；510, Benitration reactor ontology；511, second is defeated
Enter end；512, second output terminal；520, cool down component；521, cooling heat exchanger；530, draw the integrated blower of increasing；540, circulating pump；
600, wash；610, ontology is washed；611, third input terminal；612, third output end；613, blender；620, circulation spray
Leaching portion；630, high efficiency demister；640, kinetic pump；700, the second electric precipitator；710, condenser；800, chimney；900, it heats up
Component；910, temperature rise heat exchanger.
Specific embodiment
The embodiment of the present invention is described below in detail, examples of the embodiments are shown in the accompanying drawings.Below with reference to
The embodiment of attached drawing description is exemplary, it is intended to is used to explain the present invention, and is not considered as limiting the invention.
Coke ADSORPTION IN A FIXED BED method is mostly used to eliminate the tar heavy oil in coke oven flue gas on existing market greatly, and coke is fixed
Bed removal tar heavy oil low efficiency, plant maintenance heavy workload, system resistance drop are big, in addition, the cigarette after being handled in this manner
A certain amount of tar heavy oil is still carried in gas, be easy to cause catalyst blockage, reduces the service life of catalyst, and pollution and corruption
The pipeline etc. of erosion transmission flue gas.
It reduces catalyst to cause adherency to block catalyst in order to solve in flue gas in the related technology tar heavy oil and uses
The technical issues of service life, the embodiment of the invention provides tar in a kind of removing coke oven flue gas and cooperates with the device of denitration and its takes off
Except method, its object is to which the tar heavy oil in flue gas is degraded into low boiling point, water-soluble good small carboxylic acid molecules and derivative etc., from
And tar heavy oil is avoided not removed and occluding device from flue gas, extend the service life of catalyst.Below with reference to-Fig. 2 pairs of Fig. 1
The structure of tar and the device of collaboration denitration is illustrated in the removing coke oven flue gas.
Tar and the device of collaboration denitration include the exhaust gas generator 100 being sequentially connected, are used in the removing coke oven flue gas
Keep the fine particle in flue gas charged and removes it and by the lower valency nitrogen oxides in flue gas and by macromolecule
First electric precipitator 200 of organic matter degradation, for adding reducing agent in through the first electric precipitator 200 treated flue gas
Reducing agent adds component 300, for adding being installed with for the flue gas progress denitration after component 300 adds reducing agent to through reducing agent
Benitration reactor 500, wash 600, the second electric precipitator 700 and the chimney 800 of catalyst.In the present embodiment, second
Electric precipitator 700 is wet electrical dust precipitator.
In specific implementation, the first electric precipitator 200 includes the first electric precipitator ontology 210, plasma power supply
220, the first discharge electrode 230 and the first dust collector pole 240, the first discharge electrode 230 and the first dust collector pole 240, are set to the first electricity and remove
Inside dirt device ontology 210, plasma power supply 220 is set to outside the first electric precipitator ontology 210, the first discharge electrode 230 with etc.
The cathode output end of ion power supply 220 is connected, and the first dust collector pole 240 is connected with the cathode output end of plasma power supply 220, exhaust gas
Generator 100 is connected with the first input end 211 of the first electric precipitator ontology 210, and reducing agent adds component 300 and removes with the first electricity
First output end 212 of dirt device ontology 210 is connected.
Plasma power supply 220 exports positive electricity to the first discharge electrode 230, the first discharge electrode 230 nearby generate streamer-discahrge with
By the macromolecular of oxygen and the flue gases molecular ionization such as water at the free radical with strong oxidizing property, in free radical and flue gas in flue gas
Amount organic matter and lower valency nitrogen oxides react, to generate low-molecular-weight organic matter and high-valence state nitrogen oxides, in addition, the
One discharge electrode 230 keeps fine particle charged, and the first dust collector pole 240 is connected with 220 cathode output end of plasma power supply, therefore lotus
The fine particle of electricity is enriched on the first dust collector pole 240, to achieve the effect that dedusting.
In the present embodiment, macromolecule organic matter is tar heavy oil, and low-molecular-weight organic matter is aliphatic carboxylic acid etc., lower valency
Nitrogen oxides can be nitric oxide, and high-valence state nitrogen oxides can be NO2、N2O4、N2O5Deng.
Optionally, Benitration reactor 500 includes Benitration reactor ontology 510, is stored with and urges in Benitration reactor ontology 510
Agent, Benitration reactor ontology 510 be equipped with the second input terminal 511 and second output terminal 512, reducing agent add component 300 with
Second input terminal 511 is connected, and second output terminal 512 is connected with wash 600, and it is defeated that the second input terminal 511 is relatively higher than second
Outlet 512.
In general, having added the flue gas of reducing agent by Benitration reactor 500 after flue gas inputs Benitration reactor 500
Interior catalyst so that in flue gas most nitrogen oxides and reducing agent occur reduction reaction generate harmless nitrogen and
Water, to prevent it from polluting air.
Flue-gas temperature is too low in order to prevent or catalyst surface and micro channel are attached blocking, the removing coke oven flue gas
Middle tar and the device for cooperateing with denitration further include hot-blast stove 400, and hot-blast stove 400 is set to reducing agent and adds component 300 and denitration
It is minimum using more than temperature to allow flue gas to catalyst between reactor 500, or flue gas is warming up to by timing
350 DEG C or more so that deposition or the ammonium hydrogen sulfate being adhered in catalyst surface and micro channel, carboxylic acid and its derivative decompose
Or distillation, restore the activity of catalyst.
Optionally, wash 600 includes washing ontology 610, circulated sprinkling portion 620 and high efficiency demister 630, circulation spray
Leaching portion 620 and high efficiency demister 630 are set in turn in from the bottom up on washing ontology 610, and it is defeated that washing ontology 610 is equipped with third
Enter end 611 and third output end 612, third input terminal 611 is relatively lower than the setting of circulated sprinkling portion 620,612 phase of third output end
It is arranged to high efficiency demister 630 is higher than, third input terminal 611 is connected with second output terminal 512, third output end 612 and second
Electric precipitator 700 is connected.In washing ontology 610, lye is sprayed to flue gas by circulated sprinkling portion 620, it will be in flue gas
Combined pollutants such as 90% or more high-valence state nitrogen oxides, organic acid, amine, oxysulfide, low molecule organic matter (VOCs) etc.
Composition is absorbed and is removed, then secondary trapping is carried out to it by high efficiency demister 630, compound in flue gas in order to efficiently remove
Pollutant.
Optionally, wash 600 further includes kinetic pump 640, kinetic pump 640 be set to the outside of washing ontology 610 and
Setting is connected to inside ontology 610 with washing, kinetic pump 640 is connected by the first pipeline with circulated sprinkling portion 620.In the present embodiment
In, in order to enable the combined pollutant in the flue gas that the lye being recycled is absorbed with it is uniformly mixed, consequently facilitating repeatedly making
With equipped with blender 613 in washing ontology 610, blender 613 is located on the side wall of washing ontology 610 and is located relatively at washing
The lower section of ontology 610.
It is diffused up after being entered in washing ontology 610 due to flue gas, in order to enable sufficiently flue gas is sprayed, therefore,
At least two layers of circulated sprinkling portion 620, and be divided between third input terminal 611 and high efficiency demister 630 up and down, and every layer of circulation
Spray portion 620 includes at least two for spraying the spray head of lye.
Furthermore, wash 600 further includes the fluid reservoir for storing the lye of spraying layer spray, fluid reservoir and dynamic
Power pump 640 is connected, and is equipped with leakage fluid dram below washing 610 bottom or side of ontology.Make when the lye in washing ontology 610 is recycled
With number it is more after, can by leakage fluid dram will wash ontology 610 in lye be discharged, then by kinetic pump 640 will be in fluid reservoir
Lye extract to circulated sprinkling portion 620 spray.
In the present embodiment, it is additionally provided with condenser between third output end 612 and the second electric precipitator 700, flue gas is from
It is interior to be suspended or dispersed in flue gas molecule containing the drop or fine particle that are generated due to spray after the output of three output ends 612
Combined pollutant cooling in aerosol form is changed into it by the combined pollutant in aerosol form formed, condenser
Liquid, so that it be made to separate with flue gas.
Second electric precipitator 700 includes the second electric precipitator ontology 710, the pulse power 720, the second discharge electrode 730, second
Dust collector pole 740 and rinse-system 750, the pulse power 720 are set to outside the second electric precipitator ontology 710, the second discharge electrode 730
It is set to inside the second electric precipitator ontology 710 with the second dust collector pole 740, the cathode output end and cathode of the pulse power 720 are defeated
Outlet is connected with the second discharge electrode 730 and the second dust collector pole 740 respectively, and rinse-system 750 is set to the second electric precipitator ontology
Inside 710 and it is located at 740 top of the second dust collector pole.
Optionally, it is successively arranged between Benitration reactor 500 and wash 600 for by the cooling component of flue gas cool-down
520 and draw the integrated blower 530 of increasing, the temperature rising module for flue gas to heat up is equipped between the second electric precipitator 700 and chimney 800
900。
In one possible implementation, cooling component 520 is cooling heat exchanger 521, and temperature rising module 900 is that heating is changed
Hot device 910, is connected with for will heat up heat exchanger 910 and cooling heat exchanger between temperature rise heat exchanger 910 and cooling heat exchanger 521
The circulating pump 540 that heat exchange coal medium circulation between 521 uses.
In the present embodiment, heat exchange coal medium draws the heat of flue gas to recycle flue gas cool-down in cooling heat exchanger 521
Pump 540 extracts the heat exchange coal medium after draw heat to the coal medium temperature that heat up to flue gas, exchanges heat at temperature rise heat exchanger 910
Decline, circulating pump 540 again will heat exchange coal medium extract at cooling heat exchanger 521 to flue gas cool-down.
Optionally, heat exchange coal medium is water.
In alternatively possible implementation, cooling component 520 is the waste heat boiler for Mist heat recovering, heating
Component 900 is flue gas heater.
In general, can also pass through bypass air door 110 and chimney 800 between exhaust gas generator 100 and the first electric precipitator 200
It is connected, is discharged in order to which the flue gas in exhaust gas generator 100 is directly passed through chimney 800.
In conclusion tar and the device of denitration is cooperateed in removing coke oven flue gas provided by the embodiments of the present application, by the
One electric precipitator by macromolecule organic matter degradation at low-molecular-weight organic matters such as carboxylic acids, to avoid macromolecule Organic Material Blocking
Catalyst surface or microporous pipeline are adhered to, and lower valency nitrogen oxides are washed at high-valence state nitrogen oxides in order to subsequent
It washs component to be removed, in addition, the first electric precipitator also makes fine particle charged to remove it；By wash by carboxylic acid
Equal low-molecular-weight organic matters, high-valence state nitrogen oxides, oxysulfide and fine particle etc. are absorbed to remove it from flue gas, then
The combined pollutant in aerosol form generated due to wash is removed by the second electric precipitator, finally by neat stress
Discharge, to avoid pollution air
Fig. 3 is the flow chart of method for removing pollutant provided by one embodiment of the present invention, which can
Include: to be applied to tar and the device of collaboration denitration, the method for removing pollutant in above-mentioned removing coke oven flue gas
Step 301, macromolecule organic matter, fine particle, NO are generated in exhaust gas generatorXAnd SO2Equal combined pollutants are simultaneously
It is transported in the first electric precipitator.
Step 302, the first electric precipitator to flue gas carry out first processing so that in flue gas dust fine particle it is charged so as to
In removal, and by the macromolecule organic matter degradation in flue gas at low-molecular-weight organic matters such as carboxylic acids and by lower valency nitrogen oxides
It is oxidized to high-valence state nitrogen oxides.
Optionally, the first processing includes: that plasma power supply 220 is powered to the first discharge electrode；First discharge electrode, 230 surface hair
Raw streamer-discahrge is so as to fine solid particle charging particle and make O in flue gas in flue gas2、H20 equal flue gases molecular ionization generates high activity
Free radical；High mars free radical is received by the lower valency nitrogen oxides in flue gas and by macromolecule organic matter degradation, first
Dirt pole 240 is for adsorbing charged fine solid particle particle to remove it from flue gas.
Step 303, reducing agent adds component and adds reducing agent in through the first treated flue gas.
After flue gas is exported from the first output end 212 of the first electric precipitator ontology 210, it is delivered to by second pipe de-
In nitre reactor 500.In this transmission process, reducing agent adds component 300 and is set to second pipe to be faced with the first output end 212
Close end, to add reducing agent in the flue gas into second pipe.
Step 304, Benitration reactor will add component treated the nitrogen oxides catalysis reduction in flue gas through reducing agent
It is nitrogen to remove it from flue gas.
In the present embodiment, reducing agent, which adds, is connected with hot-blast stove 400 between component 300 and Benitration reactor 500, specific next
It says, hot-blast stove 400 is set to second pipe side, and is located at reducing agent and adds component 300 and the input of Benitration reactor 500 second
Between end 512.When flue-gas temperature is too low or catalyst is blocked, hot-blast stove 400 allows flue gas to catalyst
It is minimum to be warming up to 350 DEG C or more using more than temperature or periodically by flue gas, so as to deposit or be adhered to catalyst surface and micropore
Ammonium hydrogen sulfate, carboxylic acid and its derivative in channel decompose or distillation, restores the activity of catalyst.
Optionally, Benitration reactor 500 includes Benitration reactor ontology 510, and Benitration reactor ontology 510 is equipped with second
Input terminal 511 and second output terminal 512 are installed with catalyst in Benitration reactor ontology 510, when flue gas passes through hot-blast stove 400
Entered in Benitration reactor ontology 510 after heating by the second input terminal 511, and via the catalysis of catalyst, so that in flue gas
High-valence state nitrogen oxides and reducing agent nitrogen and water are generated by the raw reduction reaction of catalytic reaction, and pass through the second output with flue gas
512 discharge Benitration reactor ontology 510 of end.
Step 305, wash trapping is through the carboxylic acid etc. in the first electric precipitator and Benitration reactor treated flue gas
Low-molecular-weight organic matter, high-valence state nitrogen oxides, oxysulfide and charged fine particulates.
Optionally, oxysulfide SO2Or SO3。
Wash includes washing ontology, circulated sprinkling portion and high efficiency demister, and wash is trapped through the first electric precipitation
Low-molecular-weight organic matters, high-valence state nitrogen oxides, the sulphur oxygen such as the carboxylic acid in device 200 and Benitration reactor 500 treated flue gas
Compound and charged fine particulates include: flue gas from being input in washing ontology 610 in Benitration reactor 500, and along washing
Ontology 610 is washed to spread from bottom to up；Circulated sprinkling portion 620 to flue gas spray lye, by flue gas high-valence state nitrogen oxides,
The combined pollutants washing absorption such as the low molecule organic matters such as carboxylic acid, oxysulfide enters in liquid phase, and flue gas is in by what spray generated
The combined pollutant of aerosol form is sent to high efficiency demister 630 with flue gas；High efficiency demister 630 is trapped through circulated sprinkling portion
The fine particulates in flue gas after 620 sprays and the combined pollutant in aerosol form, it is removed from flue gas.
Optionally, wash 600 further includes kinetic pump 640, after flue gas enters in washing ontology 610, circulated sprinkling
Portion 620 sprays lye, and to spray to flue gas, kinetic pump 640 will wash the solution extraction of 610 bottom of ontology to circulated sprinkling
Portion 620 sprays.When wash 610 bottom solution of ontology be recycled number it is more after, by be set to washing 610 bottom of ontology
Or solution is discharged the leakage fluid dram of side, and extracts lye to circulation out of storage lye reservoir by kinetic pump 640 and spray
Leaching portion 620 is sprayed to spray to flue gas.
In specific implementation, be successively arranged between Benitration reactor 500 and wash 600 cooling component 520 and
Draw the integrated blower 530 of increasing, temperature rising module 900 is equipped between the second electric precipitator 700 and chimney 800, method for removing pollutant is also
It include: that the component 520 that cools down will draw increasing through the exhaust-heat absorption in treated the flue gas of Benitration reactor 500 to reduce flue-gas temperature
Integrated blower 530 is by the fume extraction after cooling down and is delivered in wash 610；900 pairs of temperature rising module are removed through the second electricity
Treated that flue gas heats up for dirt device 700, and chimney 800 exports the flue gas after heating up to atmosphere.
Step 306, the second electric precipitator traps washed component treated electrically charged in aerosol form in flue gas
Combined pollutant.
In the present embodiment, when flue gas is after circulated sprinkling portion 620 sprays, drop or fine particle disperse and are suspended in cigarette
In gas molecule, the combined pollutant in aerosol form is formed, also contains the fine particle with charge in combined pollutant.?
It washs and condenser is set between the third output end 612 and the second electric precipitator 700 of ontology 610, by what is generated due to spray
It is transformed into liquid in the combined pollutant cooling of aerosol form, so that it is separated with flue gas.
Second electric precipitator 700 includes the second electric precipitator ontology 710, the pulse power 720, the second discharge electrode 730, second
Dust collector pole 740 and rinse-system 750, after flue gas inputs in the second electric precipitator ontology 710, the pulse power 720 is put to second
Electrode 730 is transmitted electricity, so that the fine particle in flue gas is charged, fine particle is enriched in 740 surface of the second dust collector pole, thus
It is removed from flue gas；Rinse-system 750 is rushed to the second discharge electrode 730,740 surface of the second dust collector pole and flue gas spray solution
It washes, to dissolve and absorb in flue gas in the combined pollutant of aerosol form and make the second discharge electrode 730 and the second dust collector pole 740
Surface keeps cleaning.
Step 307, chimney will be discharged through the second electric precipitator treated neat stress.
In conclusion method for removing pollutant provided by the embodiments of the present application, is dropped tar heavy oil by the first electric precipitator
Solution is the low-molecular-weight organic matters such as carboxylic acid to prevent tar heavy oil from adhering to blocking catalyst and micro channel, then will by wash
It is removed from flue gas, to prevent tar heavy oil from entering in atmosphere with flue gas emission, and then avoids pollution atmosphere；In addition, passing through the
One electric precipitator removes the fine particle in flue gas, and by lower valency nitrogen oxides at high-valence state nitrogen oxides, in order to
Wash is removed；It is gone by the combined pollutant in aerosol form that the second electric precipitator generates washed component
It removes, so that flue gas will not pollute after being discharged into atmosphere.
In the description of the present invention, it is to be understood that, term " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
The instructions such as " thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom" "inner", "outside"
Orientation or positional relationship is to be based on the orientation or positional relationship shown in the drawings, and is merely for convenience of the description present invention and simplification is retouched
It states, rather than the device or element of indication or suggestion meaning must have a particular orientation, be constructed and operated in a specific orientation,
Therefore it is not considered as limiting the invention.
In addition, term " first ", " second " are used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance
Or implicitly indicate the quantity of indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the present invention, the meaning of " plurality " is at least two, such as two, three
It is a etc., unless otherwise specifically defined.
In the present invention unless specifically defined or limited otherwise, term " installation ", " connected ", " connection ", " fixation " etc.
Term shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integral；It can be mechanical connect
It connects, is also possible to be electrically connected or can communicate each other；It can be directly connected, can also indirectly connected through an intermediary, it can be with
It is the interaction relationship of the connection or two elements inside two elements, unless otherwise restricted clearly.For this field
For those of ordinary skill, the specific meanings of the above terms in the present invention can be understood according to specific conditions.
Above is only a specific embodiment of the present invention, but technical characteristic of the invention is not limited thereto, Ren Heben
Within the field of the present invention, made changes or modifications all cover within the scope of the patent of the present invention the technical staff in field.
Claims (10)
1. tar and the device of collaboration denitration in a kind of removing coke oven flue gas, including exhaust gas generator, the first electric precipitator, washing
Component, the second electric precipitator and chimney, which is characterized in that it further include that reducing agent adds component and Benitration reactor, described first
Electric precipitator includes the first electric precipitator ontology, plasma power supply, the first discharge electrode and the first dust collector pole, and the exhaust gas occurs
Device, the first electric precipitator ontology, the reducing agent add component, the Benitration reactor, the wash, described
Two electric precipitators and the chimney are sequentially connected, and first discharge electrode and first dust collector pole are set to first electricity and remove
Dirt device body interior, the plasma power supply are set to the outside of the first electric precipitator ontology, first discharge electrode with
The cathode output end of the plasma power supply is connected, the cathode output end phase of first dust collector pole and the plasma power supply
Even.
2. tar and the device of collaboration denitration in removing coke oven flue gas according to claim 1, which is characterized in that further include
Hot-blast stove, the Benitration reactor include Benitration reactor ontology, are stored with catalyst in the Benitration reactor ontology, described
Benitration reactor ontology is equipped with the second input terminal and second output terminal, second input terminal and the first electric precipitator sheet
It is connected by first pipe with the hot-blast stove between first output end of body, the second output terminal and the wash phase
Even, second input terminal is relatively higher than the second output terminal.
3. tar and the device of collaboration denitration in removing coke oven flue gas according to claim 2, which is characterized in that described to wash
Washing component includes washing ontology, circulated sprinkling portion and high efficiency demister, and the circulated sprinkling portion and the high efficiency demister are under
It being up set in turn on the washing ontology, the washing ontology is equipped with third input terminal and third output end, and described the
Three input terminals are relatively lower than the circulated sprinkling portion setting, and the third output end is relatively higher than the high efficiency demister setting,
The third input terminal is connected with the second output terminal, and the third output end is connected with second electric precipitator.
4. tar and the device of collaboration denitration in removing coke oven flue gas according to claim 3, which is characterized in that described to wash
Washing component further includes kinetic pump, and the kinetic pump is set to the outside of the washing ontology and is connected to the washing body interior
Setting, the kinetic pump are connected by the first pipeline with the circulated sprinkling portion.
5. tar and cooperateing with the device of denitration in removing coke oven flue gas according to claim 1, which is characterized in that described the
Two electric precipitators include the second electric precipitator ontology, the pulse power, the second discharge electrode, the second dust collector pole and rinse-system, described
The pulse power is set to the second electric precipitator body exterior, and second discharge electrode and second dust collector pole are set to institute
The second electric precipitator body interior is stated, the cathode output end and cathode output end of the pulse power discharge with described second respectively
Pole is connected with second dust collector pole, and the rinse-system is set to the second electric precipitator body interior and is located at described the
Above two dust collector poles.
6. a kind of method for removing pollutant, which is characterized in that be applied to tar in removing coke oven flue gas as described in claim 1
And in the device of collaboration denitration, the method for removing pollutant includes:
Macromolecule organic matter, fine particle, NO are generated in the exhaust gas generatorXAnd SO2Equal combined pollutants are simultaneously conveyed
To in first electric precipitator；
First electric precipitator carries out the first processing to flue gas, so that dust fine particle is charged in order to remove in flue gas,
And by the macromolecule organic matter degradation in flue gas at the low-molecular-weight organic matters such as carboxylic acid and by lower valency nitrogen oxides at
High-valence state nitrogen oxides；
The reducing agent adds component and adds reducing agent in through the described first treated flue gas；
The nitrogen oxides catalysis for adding component through the reducing agent treated in flue gas is reduced to nitrogen by the Benitration reactor
Gas from flue gas to remove it；
Wash trapping is through the carboxylic acid etc. in first electric precipitator and the Benitration reactor treated flue gas
Low-molecular-weight organic matter, high-valence state nitrogen oxides, oxysulfide and charged fine particulates；
Second electric precipitator trapping is through electrically charged the answering in aerosol form in the wash treated flue gas
Close pollutant；
The chimney will be discharged through second electric precipitator treated neat stress.
7. a kind of method for removing pollutant according to claim 6, which is characterized in that it is described first processing include:
The plasma power supply is powered to first discharge electrode；
Streamer-discahrge occurs for the first electric discharge pole surface so as to fine solid particle charging particle and make O in flue gas in flue gas2、H20
Equal flue gases molecular ionization generates high mars free radical；
The high mars free radical is by the lower valency nitrogen oxides in the flue gas and by macromolecule organic matter degradation, institute
Dedusting pole is stated for adsorbing charged fine solid particle particle to remove it from flue gas.
8. a kind of method for removing pollutant according to claim 6, which is characterized in that the wash includes washing this
Body, circulated sprinkling portion and high efficiency demister, the wash trapping are handled through first electric precipitator and Benitration reactor
The low-molecular-weight organic matters such as the carboxylic acid in flue gas afterwards, high-valence state nitrogen oxides, oxysulfide and charged fine particulates
Include:
Flue gas is spread along the washing ontology from bottom to up from being input in the washing ontology in the Benitration reactor；
The circulated sprinkling portion sprays lye to flue gas, and the macromoleculars such as high-valence state nitrogen oxides, carboxylic acid in flue gas are organic
The combined pollutants washing absorption such as object, oxysulfide enters in liquid phase, and flue gas is by spray generation in the compound of aerosol form
Pollutant is sent to the high efficiency demister with flue gas；
The high efficiency demister traps the fine particulates in the flue gas after circulated sprinkling portion spray and is in aerosol shape
The combined pollutant of formula removes it from flue gas.
9. a kind of method for removing pollutant according to claim 6, which is characterized in that second electric precipitator includes the
Two electric precipitator ontologies, the pulse power, the second discharge electrode, the second dust collector pole and rinse-system, the second electric precipitator trapping
It include: when flue gas inputs institute through the electrically charged combined pollutant in aerosol form in the wash treated flue gas
After stating in the second electric precipitator ontology, the pulse power is transmitted electricity to second discharge electrode, so that the fine particle in flue gas
It is charged, fine particle is enriched in described second and is gathered dust pole surface, so that it be removed from flue gas；The rinse-system to
Flue gas, second discharge electrode and the second dust collector pole surface spraying solution rinse, to dissolve in flue gas in aerosol form
Combined pollutant and keep second discharge electrode and the second dust collector pole surface cleaning.
10. a kind of method for removing pollutant according to claim 6, which is characterized in that the reducing agent add component with
It is connected with hot-blast stove between the Benitration reactor, the hot-blast stove will add component through the reducing agent treated flue gas
Allow to catalyst minimum using more than temperature or periodically by flue gas to 350 DEG C or more.
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| CN201811636382.1A CN109569248A (en) | 2018-12-29 | 2018-12-29 | Remove tar and the device and its removal methods of collaboration denitration in coke oven flue gas |
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