CN109569228A - The exhaust system and technique of flue gas of garbage furnace - Google Patents
The exhaust system and technique of flue gas of garbage furnace Download PDFInfo
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- CN109569228A CN109569228A CN201811600050.8A CN201811600050A CN109569228A CN 109569228 A CN109569228 A CN 109569228A CN 201811600050 A CN201811600050 A CN 201811600050A CN 109569228 A CN109569228 A CN 109569228A
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- flue gas
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 118
- 239000003546 flue gas Substances 0.000 title claims abstract description 118
- 238000000034 method Methods 0.000 title claims abstract description 73
- 239000010813 municipal solid waste Substances 0.000 title claims abstract description 40
- 230000008569 process Effects 0.000 claims abstract description 31
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000000843 powder Substances 0.000 claims abstract description 17
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 claims abstract description 13
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 11
- 231100000719 pollutant Toxicity 0.000 claims abstract description 11
- 150000001875 compounds Chemical class 0.000 claims abstract description 8
- 238000001179 sorption measurement Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 37
- 239000000428 dust Substances 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 22
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 19
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 238000000889 atomisation Methods 0.000 claims description 15
- 239000002245 particle Substances 0.000 claims description 15
- 239000000908 ammonium hydroxide Substances 0.000 claims description 14
- 238000002347 injection Methods 0.000 claims description 14
- 239000007924 injection Substances 0.000 claims description 14
- 238000005507 spraying Methods 0.000 claims description 14
- 229910052799 carbon Inorganic materials 0.000 claims description 13
- 238000005516 engineering process Methods 0.000 claims description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 10
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 10
- 239000000920 calcium hydroxide Substances 0.000 claims description 10
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 10
- 239000012670 alkaline solution Substances 0.000 claims description 9
- 239000002918 waste heat Substances 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 8
- 238000006386 neutralization reaction Methods 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 7
- 235000019504 cigarettes Nutrition 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 229910021529 ammonia Inorganic materials 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 4
- 230000004888 barrier function Effects 0.000 claims description 4
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 238000010410 dusting Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 230000007935 neutral effect Effects 0.000 claims description 3
- 238000006479 redox reaction Methods 0.000 claims description 3
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 239000000706 filtrate Substances 0.000 claims description 2
- 150000002500 ions Chemical class 0.000 claims 2
- 229960004424 carbon dioxide Drugs 0.000 claims 1
- 229910002090 carbon oxide Inorganic materials 0.000 claims 1
- 230000000149 penetrating effect Effects 0.000 claims 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 abstract description 12
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 12
- 229910052753 mercury Inorganic materials 0.000 abstract description 11
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 10
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 10
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 abstract description 10
- 229910000041 hydrogen chloride Inorganic materials 0.000 abstract description 10
- 239000013618 particulate matter Substances 0.000 abstract description 5
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 abstract description 2
- 229910000040 hydrogen fluoride Inorganic materials 0.000 abstract description 2
- 230000001360 synchronised effect Effects 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 4
- 235000011941 Tilia x europaea Nutrition 0.000 description 4
- 239000004571 lime Substances 0.000 description 4
- 238000011068 loading method Methods 0.000 description 4
- 238000004056 waste incineration Methods 0.000 description 4
- 239000002585 base Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OGBQILNBLMPPDP-UHFFFAOYSA-N 2,3,4,7,8-Pentachlorodibenzofuran Chemical compound O1C2=C(Cl)C(Cl)=C(Cl)C=C2C2=C1C=C(Cl)C(Cl)=C2 OGBQILNBLMPPDP-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N Nitrogen dioxide Chemical compound O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229940095054 ammoniac Drugs 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- PRORZGWHZXZQMV-UHFFFAOYSA-N azane;nitric acid Chemical compound N.O[N+]([O-])=O PRORZGWHZXZQMV-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000010882 bottom ash Substances 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- RCTYPNKXASFOBE-UHFFFAOYSA-M chloromercury Chemical compound [Hg]Cl RCTYPNKXASFOBE-UHFFFAOYSA-M 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000185 dioxinlike effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000005284 excitation Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 150000002240 furans Chemical class 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 125000000623 heterocyclic group Chemical group 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910001872 inorganic gas Inorganic materials 0.000 description 1
- 231100000567 intoxicating Toxicity 0.000 description 1
- 230000002673 intoxicating effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 229910000474 mercury oxide Inorganic materials 0.000 description 1
- UKWHYYKOEPRTIC-UHFFFAOYSA-N mercury(ii) oxide Chemical compound [Hg]=O UKWHYYKOEPRTIC-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/60—Combinations of devices covered by groups B01D46/00 and B01D47/00
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/06—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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
-
- 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
-
- 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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
-
- 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
-
- 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
- F22B1/1807—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines using the exhaust gases of combustion engines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/08—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being otherwise bent, e.g. in a serpentine or zig-zag
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
- B01D2258/0291—Flue gases from waste incineration plants
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Treating Waste Gases (AREA)
Abstract
This application discloses a kind of exhaust system of flue gas of garbage furnace and techniques, and the technique is the following steps are included: denitration；Semidry method removes sour gas and divalent mercuric compounds；Activated carbon adsorption and dry powder depickling；Dedusting；Flue gas heat exchange；Low temperature plasma decomposing pollutant；Wet process depickling.The present invention can be achieved the synchronous, efficient of multiple pollutant (including particulate matter, nitrogen oxides, oxysulfide, dioxin, hydrogen chloride, hydrogen fluoride, mercury and other heavy metals) and the ultra-low concentration discharge, it can be achieved that flue gas of refuse burning, NO be removed in depthX< 50mg/Nm3, SO2< 35mg/Nm3, dioxin TEQ < 0.01ng/Nm3, while the discharge index of HF, HCl, mercury and other heavy metals is greatly lowered.
Description
Technical field
The present invention relates to field of air pollution purification more particularly to the exhaust systems and work of a kind of flue gas of garbage furnace
Skill.
Background technique
With China's rapid development of economy, living standards of the people are improved rapidly, and urbanization process is continuously improved, all kinds of rubbish
The yield of rubbish is also sharply increasing." the big or middle municipal solid waste pollution ring in the whole nation in 2017 announced according to State Ministry of Environmental Protection
Border prevents and treats annual report " data show, it is 2016,18850.5 ten thousand tons of Municipal Domestic Garbage Output 214 big or middle, with annual 8-
10% growth rate increases.The method of domestic garbage disposal, predominantly garbage loading embeading and waste incineration.Garbage loading embeading is due to needing
A large amount of land resource is consumed, and effluent seepage contaminated soil and underground water, destroyed land resource easily occurs, causes serious two
Secondary pollution.Therefore in recent years, the treating capacity relative scale of garbage loading embeading is constantly reduced.Garbage incineration process and garbage loading embeading work
Skill and other treatment process compare, and have the advantages that rubbish wide adaptation range, capacity usage ratio are high, take up little area, waste incineration
The yield of process rubbish is also constantly increasing, and relative scale is continuously improved.Flourishing city, most of rubbish are opened at home
Begin to be handled using garbage incineration process.
Waste incineration also brings along new problem, China due to garbage classification carry out and bad, ash disposal after waste incineration
Slag should carry out, with a large amount of pollutant in flue gas, should especially being handled before discharging to atmosphere outside especially processing.Due to
The particularity of component of refuse, major pollutants in the flue gas that rubbish generates after burning are as follows: dust, SO2、HCl、NOX(PCDD/
PCDF etc.), heavy metal etc..Flue gas of refuse burning is by domestic traditional handicraft at present, it is difficult to achieve the purpose that deep treatment purifies.It is main
Want the reason is as follows that:
(1) denitration (NOXRemoval)
The application of domestic denitrating technique, predominantly SNCR (non-selective catalytic reduction), SCR (selective catalytic reduction
Method) and low-temperature SCR.SNCR is the traditional handicraft of flue gas of refuse burning denitration, is widely applied at present, technology maturation.SCR technique by
In the flue gas of refuse burning ingredient the characteristics of, catalyst poisoning is easily caused, and the more difficult matching of flue-gas temperature, technique are difficult to select.It is low
Warm SCR technique palpus desulfurization, dedusting and heating, equally exist the easy intoxicating phenomenon of catalyst, operating cost is high, technical maturity
Difference, it is difficult to promote and apply.Due to the denitration efficiency of SNCR, generally 50% or so, therefore denitration efficiency is not generally high, NOX's
There are technical problems for deep purifying.
(2) dioxin is removed
Dioxin is one of the most important index that flue gas of refuse burning is administered.Control technology is mainly Combustion System at present,
And spray into activated carbon powder before bag filter and adsorbed, the dioxin-like chemical that absorption is not yet decomposed and synthesized again,
Other removing control technique for applying are seldom.
(3) demercuration
A large amount of mercury exists in the form of element mercury in flue gas of refuse burning, is in gaseous state, mainly passes through activated carbon powder
Adsorption is carried out, other removing control technique for applying are equally seldom.
(4) desulfurization, removing HF, HCl
The deacidification of the common process of garbage power plant at present, mainly semidry method, dry method deacidification and wet process acid removal process are gone
It removes.There is the limitation of deacidification efficiency in semidry method deacidification, dry method deacidification and wet process acid removal process, lower discharge may be implemented and refer to
Mark, but be difficult to fully achieve the purpose of minimum discharge processing.
In conclusion domestic flue gas of refuse burning processing traditional at present, only may be implemented the emission control of low concentration,
But as what environment protection emission criterion required is gradually increased, emission control becomes more and more difficult, especially NOX, dioxin
With the control of mercury metal, it is difficult to reach the demand of minimum discharge.
Summary of the invention
The purpose of the present invention is to provide a kind of exhaust system of flue gas of garbage furnace and technique, which be can be realized
Deep purifying, while realizing the ultra-low concentration discharge of flue gas.
To solve this technical problem, the technical scheme is that
A kind of discharge technology of flue gas of garbage furnace, comprising the following steps:
Step A, denitration
Ammonia water spray is entered boiler internal and mixed with flue gas by SNCR denitration device；The NOx's in ammonia and flue gas in ammonium hydroxide
Equivalent proportion is 1.5 to 1.6；
Step B, semidry method removes sour gas and divalent mercuric compounds
It is passed through after the flue gas of step A is cooled down by waste heat boiler to semidry method rotary atomization device, semidry method rotation
Spraying device sprays alkaline solution drop；Sour gas and alkaline solution in flue gas occur neutralization reaction and form salt particle；Cigarette
Divalent mercuric compounds in gas are formed by curing dusting solid by the contact of alkaline solution particle；
Step C, activated carbon adsorption and dry powder depickling
It is passed through flue by the flue gas of step B, sprays active carbon into the flue gas of flue, active carbon is by two evils in flue gas
English and acid gas adsorption；Calcium hydroxide dry powder is sprayed into the flue gas of flue simultaneously, the sour gas in calcium hydroxide and flue gas is sent out
Raw acid-base neutralization reaction；
Step D, dedusting
It is passed through by the flue gas of step C to bag filter, bag filter utilizes the dust in filtrate trapping flue gas
Grain and active carbon and calcium hydroxide dry powder particle；
Step E, flue gas heat exchange
Into the low of gas-to-gas heat exchanger after the flue gas of step D is passed through to gas-to-gas heat exchanger and reacts with subsequent step G
The ultra-clean flue gas of temperature exchanges heat；
Step F, low temperature plasma decomposing pollutant
It is passed through by the flue gas of step E to low-temperature plasma reactor, low-temperature plasma reactor discharges so that in flue gas
Pollutant redox reaction or decomposition reaction occurs；
Step G, wet process depickling
It is passed through by the flue gas of step F to wet process extracting tower, gas liquid reaction, removing occurs with lye in wet process extracting tower
Sour gas and solid dust particle, obtain ultra-clean flue gas；The ultra-clean flue gas being discharged in step G is passed through to gas-to-gas heat exchanger,
Flue gas is discharged after gas-to-gas heat exchanger heats by chimney.
In one embodiment of the invention, the temperature of flue gas is 850 DEG C to 1100 DEG C at ammonia water spray in the step A.
In one embodiment of the invention, in the step F discharge type of low-temperature plasma reactor be corona discharge or
Person's dielectric barrier discharge.
In one embodiment of the invention, in the step F power supply crest voltage of low-temperature plasma reactor be 80KV extremely
120KV；The power supply pulsewidth of the low-temperature plasma reactor is 0.1 μ s to 1 μ s.
In one embodiment of the invention, when the flue gas of the step E discharge stops in step F low-temperature plasma reactor
Between be 1.8s to 2.5s.
In one embodiment of the invention, the flue gas of step D discharge flue gas stream in step E low-temperature plasma reactor
Speed is 0.8m/s to 2m/s.
In one embodiment of the invention, the flue gas of the step E discharge is in the mistake for entering step F low-temperature plasma reactor
Air-flow is 0.1 to 0.2 with respect to root-mean-square deviation in journey.
In one embodiment of the invention, the step G neutral and alkali solution atomization partial size is 30-50 μm, liquid-gas ratio 10-
18L/m3。
The present invention also provides a kind of exhaust systems of flue gas of garbage furnace, comprising: sequentially connected incinerator, waste heat pot
Furnace apparatus, semidry method rotary atomization device, bag-type dust collector, gas-to-gas heat exchanger, low-temperature plasma reactor and wet process are de-
Acid tower；SNCR denitration device is equipped in the incinerator；The semidry method rotary atomization device and the bag-type dust collector it
Between by flue be connected to, flue be equipped with active carbon flue mixed injection device and dry powder flue mixed injection device；The gas-
Gas heat exchanger has hot air intake, heat outlet, cold air import and cold air outlet, and hot air intake is filled by pipeline and bag-type dust
Connection is set, heat outlet is connect by pipeline with low-temperature plasma reactor, and cold air import is connected by pipeline and wet process extracting tower
It connects, cold air outlet connects chimney by pipeline.
In one embodiment of the invention, the out of stock device of SNCR includes twin spray gun, twin spray
Rifle is connected with ammonium hydroxide supply system, from ammonium hydroxide supply system to SNCR denitration device provisioning ammonium hydroxide；The semidry method rotating spraying
Device is using upper air fair current reaction tower；The discharge type of low-temperature plasma reactor is corona discharge or dielectric impedance
Electric discharge；Wet process extracting tower includes the lye layer set gradually from bottom to up, spraying layer and absorbs demisting layer, and the spraying layer passes through
Circulating pump connects lye layer, aspirates the lye in lye layer by circulating pump and then sprays downwards.
By using above-mentioned technical proposal, the beneficial effects of the present invention are: the present invention realizes flue gas by SNCR denitration
First denitration；Flue gas enters the first depickling of semidry method rotating spraying reaction unit progress after waste heat boiler cools down after SNCR reaction
With removal divalent mercuric compounds, semidry method rotating spraying reaction unit treated flue gas enters to be connected with bag filter
In flue, absorption and depickling, Zhi Houyan are carried out by active carbon flue mixed injection device and dry powder flue mixed injection device
Gas pass through bag filter dedusting, later flue gas by heat exchange after enter low-temperature plasma reactor carry out redox reaction or
Decomposition reaction, further denitration depickling and decomposes other pollutants, later by wet process extracting tower treated purifying smoke warp
It is discharged after gas-gas heater heating by chimney.It can be seen that the achievable multiple pollutant of the present invention (including particulate matter, nitrogen oxidation
Object, oxysulfide, dioxin, hydrogen chloride, hydrogen fluoride, mercury and other heavy metals) it is synchronous, efficiently be removed in depth, it can be achieved that rubbish
The ultra-low concentration discharge of rubbish incineration flue gas, NOX< 50mg/Nm3, SO2< 35mg/Nm3, dioxin TEQ < 0.01ng/Nm3, simultaneously
The discharge index of HF, HCl, mercury and other heavy metals is greatly lowered.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of embodiment of the exhaust system of flue gas of garbage furnace of the invention.
Each appended drawing reference in figure are as follows: 1, incinerator；2, SNCR denitration device；3, waste heat boiler device；4, semidry method rotates
Spraying device；5, active carbon flue mixed injection device；6, dry powder flue mixed injection device；7, bag-type dust collector；8, gas-
Gas heat exchanger；9, reaction of low temperature plasma device；10, wet process extracting tower；11, chimney.
Specific embodiment
In order to further explain the technical solution of the present invention, being explained in detail below by specific embodiment the present invention
It states.
It please refers to shown in Fig. 1, the present invention provides a kind of exhaust system of flue gas of garbage furnace, comprising: sequentially connected
It is incinerator 1, waste heat boiler device 3, semidry method rotary atomization device 4, bag-type dust collector 7, gas-to-gas heat exchanger (GGH) 8, low
Warm plasma reactor 9 and wet process extracting tower 10.
First denitration is carried out with the flue gas generated to incinerator 1 equipped with SNCR denitration device 2 in the incinerator 1.It is described
It is connected between semidry method rotary atomization device 4 and the bag-type dust collector 7 by flue, flue is mixed equipped with active carbon flue
Close injection apparatus 5 and dry powder flue mixed injection device 6.
The gas-to-gas heat exchanger 8 has hot air intake 81, heat outlet 82, cold air import 83 and cold air outlet 84, hot gas
Import 81 is connect by pipeline with bag-type dust collector 7, and heat outlet 82 is connect by pipeline with low-temperature plasma reactor 9,
Cold air import 83 is connect by pipeline with wet process extracting tower 10, and cold air outlet 84 connects chimney 11 by pipeline.
For the flue gas that incinerator 1 generates first through the first denitration of SNCR denitration device 2, the out of stock device 2 of SNCR includes double fluid
Body atomizing lance 21, the twin spray gun 21 are connected with ammonium hydroxide supply system 20, are taken off from ammonium hydroxide supply system 20 to SNCR
Nitre device 2 supplies ammonium hydroxide, and ammonium hydroxide is injected into the flue gas of the generation of incinerator 1 (cigarette at injection by twin spray gun 21
Temperature degree is between 850~1100 DEG C), it is sufficiently mixed after vaporization with flue gas, the NO in a large amount of ammonia and flue gas, NO2 are gone back
Original is at N2 (equivalent proportion of ammonia and NOx be 1.5~1.6), and with a certain amount of NH3Excessive unreacted.
Flue gas after preliminary denitration enters semidry method rotary atomization device 4, semidry method rotation spray after the cooling of waste heat boiler 3
For mist device 4 using upper air fair current reaction tower, lime white sprays into reaction tower after high-pressure rotary is atomized, flue gas from tower top into
Enter reaction tower, is mixed after being uniformly distributed with the lime white of high speed atomisation.Sour gas and lime in reaction tower, in flue gas
Reaction, by SO2, the acidic materials neutralization precipitation such as HCl, HF, generate inert solid matter CaCl2、CaF2、CaSO4, while stone
Flue gas, is cooled to the temperature of setting by the heat of vaporization in moisture absorption flue gas in mortar.Flue gas has enough anti-in tower
Between seasonable, moisture evaporating completely in lime white.Flue gas after reaction is flowed out from tower bottom, and wherein bulky grain solid exists because of inertial deposition
In tower bottom ash bucket, periodically it is discharged.The particulate solid that flue gas carries out is captured in subsequent handling bag-type dust collector 7 and goes
It removes.
Flue gas after semidry method rotary atomization device 4 reacts enters in flue, due to being provided with active carbon flue in flue
Mixed injection device 5 and dry powder flue mixed injection device 6, Powdered Activated Carbon and flue gas are realized uniformly mixed by strong turbulent flow
It closes, achievees the purpose that adsorb the pollutants such as heavy metal, dioxin and furans；It is dry that calcium hydroxide is sprayed into the flue gas of flue simultaneously
Acid-base neutralization reaction occurs for powder, sour gas of the calcium hydroxide in flue and in the filter bag surface and flue gas of bag-type dust collector 7.
Active carbon powder and calcium hydroxide dry powder are removed after absorbing pollutant by the capture of bag-type dust collector 7.
Solid-state salt particulate matter, the active carbon powder, niter generated in original dust particles and above-mentioned apparatus in flue gas
Grey dry powder etc. is removed together in bag filter 7.Bag filter 7 is the filtration using fabric to ash-laden gas
Body is filtered, and after dusty gas enters sack cleaner, particle is big, heavy dust, since the effect of gravity settles
Get off, fall into ash bucket, for the gas containing relatively fine dust when passing through filtrate, dust is purified flue gas by detention.
Enter low-temperature plasma after the cooling of gas-to-gas heat exchanger 8 by the flue gas of preliminary denitration, depickling, absorption and dedusting
Reactor 9.The discharge type of low-temperature plasma reactor 9 is corona discharge or dielectric barrier discharge, low-temperature plasma reaction
Device 9 includes discharge electrode and earthing pole, flue gas residence time 1.8-2.5s in low-temperature plasma reactor 9, the substance in flue gas
By the strong effect for the plasma pulse corona discharge that discharge electrode and earthing pole generate, excitation generates strong redox
Reaction.Reaction of nitrogen oxides is nitric acid ammonia particulate matter and part NO2、HNO3, part of nitrogen oxides can be reduced to N2；SO2
Gas can be sulfate of ammoniac by part reaction, realize partial removal purpose in low-temperature plasma reactor 9；Element mercury will be low
The free radical and other active particles that warm plasma reactor 9 generates are oxidized to mercury oxide, mercury chloride etc., are converted to by element mercury
Bivalent mercury is removed in subsequent wet process extracting tower 10；Other heavy metal substances can be sent out in low-temperature plasma reactor 9
The collective effect of raw corresponding oxidation reaction, 9 high energy electron of low-temperature plasma reactor and electric field force promotes other heavy metal objects
Matter is adsorbed by dust and droplet, is conducive to remove in subsequent wet extracting tower 10.Dioxin is produced in low-temperature plasma reactor 9
The reactions such as dechlorination, heterocycle fracture will occur under the action of raw free radical and other active particles, ultimately generate CO2、CO、
H2O, the inorganic gas small molecule such as HCl eliminates dioxin toxicity, realizes the purpose thoroughly removed.
Flue gas after low-temperature plasma reactor 9 acts on enters wet process extracting tower 10.Wet process extracting tower 10 include from down toward
On set gradually lye layer, spraying layer and absorb demisting layer, the spraying layer by circulating pump connection lye layer, pass through circulation
Pumping is inhaled the lye in lye layer and is then sprayed downwards.Flue gas enters from 10 lower part of wet process extracting tower, in lye layer and spraying layer
It is interior that gas liquid reaction occurs with lye, further remove sour gas and solid dust particle.10 apical sink of wet process extracting tower removes
Mist layer can reduce the water content in flue gas, except fog directly excludes, not mix with lower part lye, reduce sewage discharge.It is final net
Ultra-clean flue gas after change is drained into atmosphere after the heating of gas-to-gas heat exchanger 8 by chimney.
Outlet purifying smoke is 100-110 DEG C through 8 temperature after heating of gas-to-gas heat exchanger, it is no longer necessary to increase flue gas heating
Disappear white device, and the gas-to-gas heat exchanger 8 is rationally using treated the high-temperature flue gas of bag-type dust collector 7 to super before last discharge
Neat stress is heated, and has been reached reasonable using resource, has been reduced the purpose of energy consumption.Pollutant concentration in flue gas reaches super
Low concentration standard, wherein NOX< 50mg/Nm3, SO2< 35mg/Nm3, dioxin TEQ < 0.01ng/Nm3, it is greatly lowered simultaneously
The discharge index of HF, HCl, mercury and other heavy metals.
Embodiment provided by the invention is de- by low-temperature plasma reactor and SNCR as can be seen from the above description
The waste incinerator that nitre device, active carbon injection apparatus, bag-type dust collector, gas-to-gas heat exchanger and wet process extracting tower are combined
The exhaust system of flue gas can realize multiple pollutant (including particulate matter, nitrogen oxides, oxysulfide, dioxin, hydrogen chloride, fluorine
Change hydrogen, mercury and other heavy metals) collaboration, be efficiently removed in depth, entire process unit waste water yield is few, energy-saving and emission-reduction, most
The minimum discharge of flue gas of garbage furnace is realized eventually.
The present invention also provides a kind of discharge technologies of flue gas of garbage furnace, comprising the following steps:
Step A, denitration
Ammonia water spray is entered boiler internal and mixed with flue gas by SNCR denitration device；The NOx's in ammonia and flue gas in ammonium hydroxide
Equivalent proportion is 1.5 to 1.6；
Step B, semidry method removes sour gas and divalent mercuric compounds
It is passed through after the flue gas of step A is cooled down by waste heat boiler to semidry method rotary atomization device, semidry method rotation
Spraying device sprays alkaline solution drop；Sour gas and alkaline solution in flue gas occur neutralization reaction and form salt particle；Cigarette
Divalent mercuric compounds in gas are formed by curing dusting solid by the contact of alkaline solution particle；
Step C, activated carbon adsorption and dry powder depickling
It is passed through flue by the flue gas of step B, sprays active carbon into the flue gas of flue, active carbon is by two evils in flue gas
English and acid gas adsorption；Calcium hydroxide dry powder is sprayed into the flue gas of flue simultaneously, the sour gas in calcium hydroxide and flue gas is sent out
Raw acid-base neutralization reaction；
Step D, dedusting
It is passed through by the flue gas of step C to bag filter, bag filter utilizes the dust in filtrate trapping flue gas
Grain and active carbon and calcium hydroxide dry powder particle；
Step E, flue gas heat exchange
Into the low of gas-to-gas heat exchanger after the flue gas of step D is passed through to gas-to-gas heat exchanger and reacts with subsequent step G
The ultra-clean flue gas of temperature exchanges heat；
Step F, low temperature plasma decomposing pollutant
It is passed through by the flue gas of step E to low-temperature plasma reactor, low-temperature plasma reactor discharges so that in flue gas
Pollutant redox reaction or decomposition reaction occurs；
Step G, wet process depickling
It is passed through by the flue gas of step F to wet process extracting tower, gas liquid reaction, removing occurs with lye in wet process extracting tower
Sour gas and solid dust particle, obtain ultra-clean flue gas；The ultra-clean flue gas being discharged in step G is passed through to gas-to-gas heat exchanger,
Flue gas is discharged after gas-to-gas heat exchanger heats by chimney.
Further, the temperature of flue gas is 850 DEG C to 1100 DEG C at ammonia water spray in the step A.
Further, the discharge type of low-temperature plasma reactor is corona discharge or dielectric impedance in the step F
Electric discharge.
Further, the power supply crest voltage of low-temperature plasma reactor is 80KV to 120KV in the step F；It is described
The power supply pulsewidth of low-temperature plasma reactor is 0.1 μ s to 1 μ s.
Further, the flue gas of step E discharge residence time in step F low-temperature plasma reactor be 1.8s extremely
2.5s。
Further, the flue gas of step D discharge flue gas flow rate in step E low-temperature plasma reactor is 0.8m/s
To 2m/s.
Further, the flue gas of step E discharge air-flow phase during entering step F low-temperature plasma reactor
It is 0.1 to 0.2 to root-mean-square deviation.
Further, the step G neutral and alkali solution atomization partial size is 30-50 μm, liquid-gas ratio 10-18L/m3。
It should be appreciated that the technical concepts and features of above-described embodiment only to illustrate the invention, its object is to allow be familiar with this
The personage of item technology cans understand the content of the present invention and implement it accordingly, and it is not intended to limit the scope of the present invention.It is all
Equivalent change or modification made by Spirit Essence according to the present invention, should be covered by the protection scope of the present invention.
Claims (10)
1. a kind of discharge technology of flue gas of garbage furnace, which comprises the following steps:
Step A, denitration
Ammonia water spray is entered boiler internal and mixed with flue gas by SNCR denitration device；The equivalent of the NOx in ammonia and flue gas in ammonium hydroxide
Than being 1.5 to 1.6；
Step B, semidry method removes sour gas and divalent mercuric compounds
It is passed through after the flue gas of step A is cooled down by waste heat boiler to semidry method rotary atomization device, semidry method rotating spraying
Device sprays alkaline solution drop；Sour gas and alkaline solution in flue gas occur neutralization reaction and form salt particle；In flue gas
Divalent mercuric compounds by alkaline solution particle contact be formed by curing dusting solid；
Step C, activated carbon adsorption and dry powder depickling
Be passed through flue by the flue gas of step B, spray active carbon into the flue gas of flue, active carbon by flue gas dioxin and
Acid gas adsorption；Calcium hydroxide dry powder is sprayed into the flue gas of flue simultaneously, acid occurs for the sour gas in calcium hydroxide and flue gas
Alkali neutralization reaction；
Step D, dedusting
Be passed through by the flue gas of step C to bag filter, bag filter using the dust particles in filtrate trapping flue gas with
And active carbon and calcium hydroxide dry powder particle；
Step E, flue gas heat exchange
It is super into the low temperature of gas-to-gas heat exchanger after the flue gas of step D is passed through to gas-to-gas heat exchanger and reacts with subsequent step G
Neat stress exchanges heat；
Step F, low temperature plasma decomposing pollutant
It is passed through by the flue gas of step E to low-temperature plasma reactor, low-temperature plasma reactor discharges so that dirt in flue gas
It contaminates object and redox reaction or decomposition reaction occurs；
Step G, wet process depickling
It is passed through by the flue gas of step F to wet process extracting tower, gas liquid reaction occurs with lye in wet process extracting tower, removing is acid
Gas and solid dust particle, obtain ultra-clean flue gas；The ultra-clean flue gas being discharged in step G is passed through to gas-to-gas heat exchanger, flue gas
It is discharged after gas-to-gas heat exchanger heats by chimney.
2. the discharge technology of flue gas of garbage furnace as described in claim 1, which is characterized in that ammonium hydroxide sprays in the step A
The temperature for penetrating place's flue gas is 850 DEG C to 1100 DEG C.
3. the discharge technology of flue gas of garbage furnace as described in claim 1, which is characterized in that low temperature etc. in the step F
The discharge type of ion reactor is corona discharge or dielectric barrier discharge.
4. the discharge technology of flue gas of garbage furnace as described in claim 1, which is characterized in that low temperature etc. in the step F
The power supply crest voltage of ion reactor is 80KV to 120KV；The power supply pulsewidth of the low-temperature plasma reactor be 0.1 μ s extremely
1μs。
5. the discharge technology of flue gas of garbage furnace as described in claim 1, which is characterized in that the cigarette of the step E discharge
Gas residence time in step F low-temperature plasma reactor is 1.8s to 2.5s.
6. the discharge technology of flue gas of garbage furnace as claimed in claim 5, which is characterized in that the cigarette of the step D discharge
Gas flue gas flow rate in step E low-temperature plasma reactor is 0.8m/s to 2m/s.
7. the discharge technology of flue gas of garbage furnace as described in claim 1, which is characterized in that the cigarette of the step E discharge
The opposite root-mean-square deviation of gas air-flow during entering step F low-temperature plasma reactor is 0.1 to 0.2.
8. the discharge technology of flue gas of garbage furnace as described in claim 1, which is characterized in that the step G neutral and alkali is molten
Liquid atomizing particle size is 30-50 μm, liquid-gas ratio 10-18L/m3。
9. a kind of exhaust system of flue gas of garbage furnace characterized by comprising sequentially connected incinerator, waste heat boiler
Device, semidry method rotary atomization device, bag-type dust collector, gas-to-gas heat exchanger, low-temperature plasma reactor and wet process depickling
Tower；SNCR denitration device is equipped in the incinerator；Between the semidry method rotary atomization device and the bag-type dust collector
It is connected to by flue, flue is equipped with active carbon flue mixed injection device and dry powder flue mixed injection device；The gas-gas
Heat exchanger has hot air intake, heat outlet, cold air import and cold air outlet, and hot air intake passes through pipeline and bag-type dust collector
Connection, heat outlet are connect by pipeline with low-temperature plasma reactor, and cold air import is connect by pipeline with wet process extracting tower,
Cold air outlet connects chimney by pipeline.
10. the exhaust system of flue gas of garbage furnace as claimed in claim 9, which is characterized in that the out of stock device of SNCR
Including twin spray gun, which is connected with ammonium hydroxide supply system, takes off from ammonium hydroxide supply system to SNCR
Nitre device provisioning ammonium hydroxide；The semidry method rotary atomization device is using upper air fair current reaction tower；Low-temperature plasma reaction
The discharge type of device is corona discharge or dielectric barrier discharge；Wet process extracting tower includes the lye set gradually from bottom to up
Layer, spraying layer and absorption demisting layer, the spraying layer connect lye layer by circulating pump, are aspirated in lye layer by circulating pump
Then lye sprays downwards.
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