CN116440698B - Dedusting and denitration equipment, and smoke and odor cooperative treatment system and method - Google Patents
Dedusting and denitration equipment, and smoke and odor cooperative treatment system and method Download PDFInfo
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- CN116440698B CN116440698B CN202310701152.3A CN202310701152A CN116440698B CN 116440698 B CN116440698 B CN 116440698B CN 202310701152 A CN202310701152 A CN 202310701152A CN 116440698 B CN116440698 B CN 116440698B
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- 239000000779 smoke Substances 0.000 title claims abstract description 94
- 238000011282 treatment Methods 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000000428 dust Substances 0.000 claims abstract description 138
- 230000003197 catalytic effect Effects 0.000 claims abstract description 105
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000003546 flue gas Substances 0.000 claims abstract description 100
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 55
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 23
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 19
- 230000008569 process Effects 0.000 claims abstract description 19
- 238000011221 initial treatment Methods 0.000 claims abstract description 4
- 230000002195 synergetic effect Effects 0.000 claims abstract description 4
- 239000003054 catalyst Substances 0.000 claims description 36
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 21
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 21
- 239000002918 waste heat Substances 0.000 claims description 16
- 239000007921 spray Substances 0.000 claims description 15
- 239000010815 organic waste Substances 0.000 claims description 13
- 238000003860 storage Methods 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 238000002485 combustion reaction Methods 0.000 claims description 10
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 9
- 238000001179 sorption measurement Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000012360 testing method Methods 0.000 claims description 7
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 4
- 238000005259 measurement Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 21
- 238000011084 recovery Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 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 abstract 1
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 21
- 239000002245 particle Substances 0.000 description 14
- 239000000460 chlorine Substances 0.000 description 11
- 239000000919 ceramic Substances 0.000 description 10
- 229910001385 heavy metal Inorganic materials 0.000 description 10
- 239000002956 ash Substances 0.000 description 9
- 239000010881 fly ash Substances 0.000 description 9
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 6
- 229910052801 chlorine Inorganic materials 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000004744 fabric Substances 0.000 description 5
- 230000008929 regeneration Effects 0.000 description 5
- 238000011069 regeneration method Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 239000003112 inhibitor Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 238000011278 co-treatment Methods 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 150000002739 metals Chemical class 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 238000004056 waste incineration Methods 0.000 description 3
- PZNSFCLAULLKQX-UHFFFAOYSA-N Boron nitride Chemical group N#B PZNSFCLAULLKQX-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000004075 alteration Effects 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 229910052793 cadmium Inorganic materials 0.000 description 2
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 239000002361 compost Substances 0.000 description 2
- 210000003608 fece Anatomy 0.000 description 2
- 239000010871 livestock manure Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- 239000011701 zinc Substances 0.000 description 2
- 229910052582 BN Inorganic materials 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000011276 addition treatment Methods 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 230000001877 deodorizing effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000005502 peroxidation Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
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- 238000012545 processing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000005507 spraying Methods 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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- 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
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/90—Odorous compounds not provided for in groups B01D2257/00 - B01D2257/708
-
- 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
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses a dedusting and denitration device, a smoke and odor cooperative treatment system and a method, wherein the device comprises the following components: the high-temperature dust removal tower comprises a shell, a cyclone dust removal unit and a filter cartridge dust removal unit which are communicated with each other and arranged in the shell; the cyclone dust removal unit is provided with an air inlet, the flue gas enters the cyclone dust removal unit from the air inlet for primary treatment, and the primarily treated flue gas is introduced into the filter cylinder dust removal unit which performs secondary treatment on the flue gas; the filter cylinder dust removal unit is provided with a smoke chamber, the smoke chamber is connected with one end of a smoke pipe, the other end of the smoke pipe is connected with a high-temperature denitration catalytic box, and the smoke after secondary treatment enters the high-temperature denitration catalytic box through the smoke pipe to be subjected to synergistic treatment with odor. The method effectively treats dioxin and nitrogen oxides generated by incineration of household garbage, cooperatively removes ammonia-containing odor, simplifies the treatment process, realizes reasonable recycling of wastes, and maximizes heat value recovery while achieving standard discharge of the flue gas.
Description
Technical Field
The invention belongs to the field of garbage treatment, and particularly relates to dust removal and denitration equipment, a smoke and odor cooperative treatment system and a smoke and odor cooperative treatment method.
Background
The existing household garbage and organic waste cooperative equipment mainly focuses on front waste heat utilization or cooperative incineration, and few references are made to the treatment of generated smoke/odor, and two systems of incineration smoke purification and odor deodorization in the traditional treatment relate to various equipment, and the occupied area is large, so that the novel comprehensive garbage treatment plant is not facilitated.
Wherein, a large amount of nitrogen oxides NO is generated in the garbage incineration process x The applicable temperature of the traditional denitration catalyst is 300-400 ℃, the loss of the heat value is overlarge when the traditional denitration catalyst is placed in front of a waste heat boiler, and the regeneration of dioxin is easy to cause; after the exhaust-heat boiler and the bag-type dust collector are arranged, the temperature of the flue gas is too low, and heat is required to be introduced again to achieve the catalytic effect.
The flue gas generated by the garbage incinerator contains various air pollutants, nitrogen oxides NO x Acid rain can be formed, an ozone layer is destroyed, a common flue gas treatment technology is a mode of cyclone dust removal, dry desulfurization, cloth bag dust removal and SCR denitration, and as the flue gas temperature after cloth bag dust removal does not accord with the catalysis condition of the SCR denitration catalyst, a denitration tower needs to be heated, the process flow is complex, more equipment and large occupied area are required.
The patent CN218608670U discloses a comprehensive treatment device for industrial silicon production waste gas pollution, which comprises a cyclone dust collector, a dry desulfurization mixing reactor, a cloth bag dust collector and an SCR middle-low temperature denitration reaction tower, wherein coarse particle dust is removed from waste gas through the cyclone dust collector, desulfurization is carried out through the dry desulfurization mixing reactor, then particles are removed through the cloth bag dust collection system, and the waste gas is discharged after reaching standards through detection of an on-line monitoring system after passing through the SCR middle-low temperature denitration reaction tower. The flue gas treatment process is optimized, and the cyclone dust collector, the cloth bag dust collector, the dry desulfurization and the medium-low temperature denitration are adopted to remove particles and fly ash in the flue gas, so that the medium-low temperature denitration catalyst can not be covered by adhesion and is not blocked, can stably operate for a long time, and the flue gas treatment effect is also ensured. According to the scheme, a two-stage dust removal process is adopted, large-particle-size particles in the flue gas are removed through cyclone dust removal, the small-particle fly ash smaller than 5 mu m is mainly intercepted in the follow-up dust removal process, the dust removal effect is better, the service life of equipment is prolonged, the equipment is complex, and the occupied area is large.
Patent CN115715927a shows a ceramic filter tube desulfurization, denitrification and dust removal integrated device, a plurality of shells, a catalyst ceramic fiber filter tube is installed inside; an air inlet pipe connected with the plurality of shells through pipelines and used for sending air into the shells; the air outlet flue is connected with the plurality of shells through pipelines and is used for conveying the flue gas in the shells; the preheating device is respectively connected with the air outlet flue and the shell through pipelines and is used for heating air conveyed by the air outlet flue and conveying the air into the shell; the pulse ash removing system is used for blowing and removing ash on the catalyst ceramic fiber filter tube. The ceramic filter cylinder is adopted, and the denitration catalyst is uniformly adhered to the internal ceramic fibers, so that denitration and dust removal integration is realized, the process flow is shortened, and the flue gas treatment efficiency is improved. According to the scheme, the ceramic filter cylinder is adopted for flue gas dust removal, the dust removal pressure is high, and the denitration efficiency is low due to the covering of fly ash on the catalyst.
Therefore, how to design the dust removal and denitration equipment to achieve the purposes of saving the flue gas denitration cost, simplifying the odor treatment process, recycling the odor components and the like is a problem to be solved by the technicians in the field.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a dust removal and denitration device, a smoke and odor cooperative treatment system and a dust removal and denitration method, which are used for effectively treating dioxin and nitrogen oxides generated by incineration of household garbage, simultaneously cooperatively removing ammonia-containing odor generated by organic wastes such as human and animal feces, kitchen garbage and the like in the storage and aerobic treatment processes, simplifying the treatment flow, realizing the reasonable utilization of resources of the wastes, and maximally realizing the heat value recovery on the basis of standard emission of the smoke.
In a first aspect, the present invention provides a dust removal and denitration apparatus, comprising: the high-temperature dust removal tower comprises a shell, a cyclone dust removal unit and a filter cartridge dust removal unit which are communicated with each other;
the cyclone dust removal unit is provided with an air inlet, the flue gas enters the cyclone dust removal unit from the air inlet for primary treatment, and the primarily treated flue gas is introduced into the filter cylinder dust removal unit which performs secondary treatment on the flue gas;
the filter cylinder dust removal unit is provided with a smoke chamber, the smoke chamber is connected with one end of a smoke pipe, the other end of the smoke pipe is connected with a high-temperature denitration catalytic box, and the smoke after secondary treatment enters the high-temperature denitration catalytic box through the smoke pipe to be subjected to synergistic treatment with odor.
Further, the high-temperature denitration catalytic box comprises a box body, a spray pipe and a catalytic module, wherein the spray pipe and the catalytic module are arranged in the box body, a denitration catalyst is filled in the catalytic module, ammonia water is sprayed to the catalytic module by the spray pipe, and flue gas subjected to secondary treatment is subjected to denitration through catalytic reduction between the catalytic module and the ammonia water.
Further, the catalytic module comprises at least one catalytic layer, and the spray pipe is arranged corresponding to the catalytic layers and is arranged in front of each catalytic layer; the denitration catalyst is in a honeycomb type pore structure.
Further, a baffle is arranged at the joint of the cyclone dust removal unit and the filter cylinder dust removal unit;
the cyclone dust removing unit comprises a cyclone sub-assembly comprising at least one cyclone, an air pipe and an ash storage hopper, wherein the air inlet is communicated with an inlet at the upper end of the cyclone, the ash storage hopper is arranged at an outlet at the lower end of the cyclone, the air pipe is correspondingly arranged with the cyclone and is positioned at the upper end of the cyclone, and the air pipe passes through the partition plate and is connected with the filter cylinder dust removing unit;
the cartridge dust removal unit comprises a cartridge assembly including at least one cartridge and a smoke chamber, the bottom of the cartridge is sealed, and the upper part of the cartridge is open and communicated with the smoke chamber.
Further, the processing air volume of the cyclone is 1000-1500 m 3 And/h, the airflow speed of an inlet at the upper end of the cyclone is 12-23 m/s.
Further, the relation between the number of cyclones and the performance parameters and the smoke amount is specifically expressed as follows:
；
wherein ,Qx Treating smoke volume for a single cyclone, wherein N is the number of the cyclones, phi is the diameter of the single cyclone, S x Inlet airflow velocity, Q, for cyclone inlet 0 For the flue gas quantity entering the cyclone dust removal unit, the unit is m 3 /h，v 0 For the flow rate of the flue gas entering the cyclone dust removal unit, the unit is m 3 /s。
Further, the relation between the number of filter cartridges and the performance parameters and the amount of the treated smoke is specifically expressed as follows:
；
wherein S is the filtering area of a single filter cartridge, D is the inner diameter of the filter cartridge, D is the outer diameter of the filter cartridge, h is the length of the filter cartridge, i.e. the length of the filter cartridge when horizontally placed, n is the number of the filter cartridges needed, v 1 Filtration rate for a single cartridge, Q 1 The amount of smoke entering the cartridge dust removal unit.
Further, the relationship between the size and the number of the catalytic layers and the amount of smoke is specifically expressed as:
；
wherein ,the space velocity of the flue gas passing through the catalytic layer in unit volume and unit time is h -1 ，/>For the volume of all catalytic layers, the unit is m 3 ，/>For the area flow rate of the flue gas through the catalytic layer, in m/s,/for>For the geometric surface area of the catalytic layers, it is assumed here that the geometric surface areas of the catalytic layers are identical in m 2 ，Q 2 For the amount of smoke entering the catalytic layer, the unit is m 3 /h，v 2 For the flow rate of the flue gas entering the catalytic layer, the unit is m 3 /s；
The relation between the flue gas parameters and the odor parameters is specifically expressed as:
；
wherein ,is the concentration of NO in the flue gas, & lt & gt>Is NO in flue gas 2 Concentration of->For denitration efficiency, the unit is%>Is the escape rate of ammonia, and the unit is ml/m 3 ，/>The amount of odor collected for the ith measurement is expressed in m 3 /h，The concentration of ammonia gas in the collected odor is measured for the ith time, and the unit is mg/m 3 T is the test interval time, the unit is h, T is the total time consumption of the aerobic treatment, the unit is h, and n is the total test times.
In a second aspect, the present invention also provides a smoke and odor cooperative treatment system, including: the incinerator, the waste heat boiler and the dedusting and denitration equipment are sequentially communicated.
In a third aspect, the present invention further provides a smoke and odor cooperative treatment method, which adopts the smoke and odor cooperative treatment system, and specifically includes the following steps:
introducing flue gas generated by the incinerator into a waste heat boiler to perform heat conversion;
the collected odor is subjected to ammonia enrichment through water adsorption, and the residual odor after enrichment is led into an air supply system to enter an incinerator to assist combustion in the incinerator and realize incineration treatment of residual organic waste gas synchronously;
the flue gas of the waste heat boiler enters a high-temperature dust removal tower for dust removal, and then enters a high-temperature denitration catalytic box through a flue pipe;
the enriched ammonia gas reacts with the flue gas through a high-temperature denitration catalytic box.
The invention provides equipment for dedusting and denitrating, and a smoke and odor cooperative treatment system and method, which at least comprise the following beneficial effects:
(1) The cyclone dust removal unit of the high-temperature dust removal tower in the dust removal and denitration device can be provided with the preliminary dust removal component according to the flue gas amount, and the filter cylinder dust removal unit at the top can also be adjusted in quantity according to the space occupation, so that the flexibility is high, the dust removal efficiency is high, and the application range is wide.
(2) According to the invention, the cyclone dust removal and filter cartridge dust removal units are arranged in the high-temperature dust removal tower, so that the particles with different particle diameters are removed in stages, and the dust removal effect with low cost, high efficiency and small occupied area under the high-temperature condition is realized.
(3) The high-temperature denitration catalytic box in the dedusting and denitration equipment provided by the invention takes ammonia water generated by the enrichment of odor ammonia as a reducing agent, and adopts a high Wen Tuoxiao catalyst to realize NO in flue gas x NH in odor 3 Co-treatment.
(4) The high-temperature dust removal tower is communicated with the high-temperature denitration catalytic box to carry out the cooperative treatment of the smoke and the odor, and the size of the catalytic module and the dosage of the catalyst can be adjusted according to the proportion of the smoke and the odor, so that the high-temperature dust removal tower is convenient to be accurately suitable for various scenes.
Drawings
Fig. 1 is a schematic view of the overall appearance of a dust removal and denitration device provided by the invention;
FIG. 2 is a schematic diagram of a cross-sectional structure of a dust removal and denitration device provided by the invention;
FIG. 3 is a schematic side view of the high temperature dust removal tower provided by the invention;
FIG. 4 is a schematic top view of a filter cartridge in the high temperature dust removal tower according to the present invention;
fig. 5 is a schematic flow chart of a smoke and odor cooperative treatment method provided by the invention.
Reference numerals illustrate:
1-a high-temperature dust removal tower; 11-an air inlet; 12-a housing; 13-cyclone; 131-cyclone sub-inlet; 14-wind pipes; 15-an ash storage hopper; 16-a filter cartridge; 17-smoke chamber; 18-a separator; 2-a high-temperature denitration catalytic box; 21-a box body; 22-spraying pipe; a 23-catalytic module; 3-smoke tube.
Detailed Description
In order to better understand the above technical solutions, the following detailed description will be given with reference to the accompanying drawings and specific embodiments. It will be apparent that the described embodiments are only some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The terminology used in the embodiments of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used in this application and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise, the "plurality" generally includes at least two.
It should also be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a product or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such product or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a commodity or device comprising such element.
When the household garbage is incinerated, the temperature of the flue gas at the outlet of the secondary combustion chamber of the incineration system is about 850 ℃, and the main pollution component of the flue gas is NO x 、SO x 、Cl 2 HCl, dioxins, heavy metals, fly ash, and the like. Wherein:
(1) For nitrogen oxides NO x Is treated by Selective Catalytic Reduction (SCR) denitration method, NO is catalyzed by a catalyst at a certain temperature x And ammonia to N 2 and H2 O. Nitrogen oxides NO in flue gas x Is mainly composed of NO and NO 2 Mainly, the specific reaction equation is as follows:
；
denitration catalyst is V 2 O 5 Is active component, tiO 2 Vanadium-titanium based catalyst as carrier by adjusting the ratio of active components, modifying and adding WO 3 、MnO 3 And the catalytic auxiliary agent can improve the catalytic activity of the vanadium-titanium-based catalyst at the high temperature of 400-550 ℃.
(2) The treatment for dioxin generally employs means for suppressing the generation. The generation of dioxin comprises high-temperature gas phase generation (500-850 ℃) and low Wen Yixiang generation (200-500 ℃). The GB18485-2014 'domestic waste incineration pollution control Standard' specifies that the incineration temperature is more than or equal to 850 ℃, the smoke residence time is more than or equal to 2s, and the purpose is to decompose dioxin generated at high temperature. Therefore, the current dioxin control is mainly to avoid low-temperature regeneration, and specific measures include chlorine removal to reduce chlorine-containing precursors of the dioxin, heavy metal removal to reduce the catalysis of the heavy metal on the dioxin, ash removal and dust removal to avoid regeneration of the dioxin on the surfaces of fly ash particles. The inhibitor component of dioxin mainly comprises (NH) 4 ) 2 SO 4 、CH 4 N 2 S, etc. is the main. Wherein the sulfur-containing species can form SO 2 With Cl 2 The reaction reduces chlorine sources, passivates catalytic metals such as Cu, fe and the like, and reacts with the metals to generate sulfate to cover active sites of fly ash, and the sulfonated precursor blocks the generation of dioxin; nitrogen group can passivate Cu, fe and other catalytic metals to generate NH 3 React with the volatilized chlorine to inhibit the generation of dioxin.
(3) The heavy metal treatment adopts an adsorption mode. The adsorbent is modified boron nitride, the boron nitride has larger specific surface area and high porosity, can realize the adsorption of heavy metals such as zinc, copper, cadmium, nickel and the like in a high-temperature section, can realize the removal of heavy metals in flue gas, and can also effectively limit the low-temperature regeneration of dioxin.
The above treatment of flue gas generated in the incineration of living garbage, while the odor mainly comes from organic wastes such as livestock and poultry manure, kitchen garbage and the like, and the organic wastes generate odor in the storage and disposal processes. Odor gasComprises NH as the main constituent 3 、H 2 S, organic waste gas VOC. Wherein the VOC is oxidatively decomposable at 800 ℃.
The invention provides a smoke and odor cooperative treatment system, which comprises: the incinerator, the waste heat boiler and the dedusting and denitration equipment are communicated in sequence. The incinerator comprises a first combustion chamber and a second combustion chamber, and the dedusting and denitration equipment comprises a high-temperature dedusting tower, a smoke pipe and a high-temperature denitration catalytic box which are sequentially communicated. The high-temperature denitration catalytic box is further provided with an alkali liquor quenching tower, an activated carbon adsorption box and a chimney which are sequentially communicated. The high-temperature dust removal tower comprises a cyclone dust removal unit and a filter cartridge dust removal unit.
The temperature inside the secondary combustion chamber in the incinerator is ensured to be above 850 ℃, and the residence time of the flue gas is at least 2s, so that dioxin generated due to high temperature is decomposed.
And then, the flue gas from the secondary combustion chamber enters a waste heat boiler to recover heat, and the outlet temperature is about 500 ℃.
After water adsorption, a large amount of ammonia gas is dissolved in water, and the formed ammonia water is used for subsequent flue gas catalytic denitration reaction.
Livestock manure and kitchen waste generate a large amount of odor in the storage and aerobic treatment processes, the odor contains ammonia, the fluctuation of the ammonia concentration of different decomposition stages of the aerobic compost is large, and the maximum ammonia concentration can reach 3000mg/m 3 The stack turning period is kept at 352-542 mg/m approximately 3 The concentration in the later period of decomposition is lower than 78-86 mg/m 3 . Because of the excellent absorption capacity of water to ammonia, the saturated concentration of ammonia water at normal temperature and normal pressure is 30-35%, and the concentration of ammonia water for Selective Catalytic Reduction (SCR) is about 20%, the stable ammonia water supply can be ensured by adjusting the water quantity to balance the absorption of ammonia water in different periods.
After the ammonia water is removed, the main components of the odor are organic waste gas VOC and O 2 . At the moment, ammonia-removing odor is led into a waste heat boiler, a small amount of steam of the waste heat boiler is utilized for preheating, the preheated waste heat enters a secondary combustion chamber, VOC is decomposed at the high temperature of the secondary combustion chamber, and O 2 As a supplementary gas, ensures the peroxidation of the flue gas.
The flue gas from the waste heat boiler is sprayed with dioxin inhibitor and heavy metal adsorbent powder, and then enters a high-temperature dust-removing tower together. In a high temperature dust removal tower. The cyclone dust removal units are uniformly mixed under the cyclone action, so that the inhibition and adsorption effects are achieved. SO generated by dioxin inhibitor under high temperature of sulfur base inside cyclone dust collection in high temperature dust collection stage 2 With Cl 2 Reaction (Cl) 2 +SO 2 +H 2 O2HCl+SO 3 ) Reduction of Cl 2 And (3) chloridizing the dioxin precursor, and reacting the alkaline component with the volatilized chlorine-containing substances to inhibit the formation of dioxin. The addition amount of the dioxin inhibitor is related to the addition treatment amount of the household garbage, and is generally 0.1-0.2% of the garbage. The heavy metal adsorbent can adsorb zinc, copper, cadmium, nickel and other heavy metals, and can be recovered or discharged from the bottom of the tower under the action of cyclone.
The cyclone dust removal stage realizes chlorine-containing substance removal, heavy metal adsorption and large-particle fly ash and powdery reagent removal in the flue gas, effectively inhibits regeneration of dioxin at 200-500 ℃, and small amount of dust smaller than 5 μm enters a filter cylinder dust removal unit at the upper part of the high-temperature dust removal tower along with the flue gas, so as to realize interception under the action of a filter cylinder component.
After two-stage dust removal by the cyclone dust removal unit and the filter cylinder dust removal unit, the flue gas enters a high-temperature denitration catalytic box, and NO in the flue gas x
Reacts with ammonia water enriched in odor under the catalysis of a catalyst in a catalytic module to generate N 2 and H2 O. The main reaction process is as follows:
；
thus, the co-treatment of the fume generated after the incineration of the household garbage and the odor generated by the organic waste is realized.
Then, the flue gas after denitration enters an alkali liquor quenching tower to be removed based on an acid-base neutralization principleSO in flue gas 2 Residual H 2 S and organic acid gas, and realizing flue gas cooling. The activated carbon tower has the use effects of adsorbing dioxin and deodorizing, is arranged at the tail end of flue gas treatment, can adsorb a small amount of residual pollutants, plays the role of double guarantee, and realizes the stable standard of flue gas.
Meanwhile, as shown in fig. 1 to 4, the present invention provides a dust removal and denitration apparatus, comprising: the high-temperature dust removal tower 1, the smoke pipe 3 and the high-temperature denitration catalytic box 2, wherein the high-temperature dust removal tower 1 comprises a shell 12, and a cyclone dust removal unit and a filter cartridge dust removal unit which are arranged inside the shell 12 and are communicated with each other;
the cyclone dust removal unit is provided with an air inlet 11, flue gas enters the cyclone dust removal unit from the air inlet 11 for primary treatment, and the primarily treated flue gas is introduced into the filter cylinder dust removal unit, and the filter cylinder dust removal unit carries out secondary treatment on the flue gas;
the filter cylinder dust removal unit is provided with a smoke chamber 17, the smoke chamber 17 is connected with one end of the smoke tube 3, the other end of the smoke tube 3 is connected with the high-temperature denitration catalytic box 2, and the smoke after secondary treatment enters the high-temperature denitration catalytic box 2 through the smoke tube 3 to be cooperatively treated with odor.
The high-temperature dust removal tower is communicated with the high-temperature denitration catalytic box to carry out the cooperative treatment of smoke and odor. The high-temperature dust removing tower in the dust removing and denitrating equipment is provided with cyclone dust removing and filter cylinder dust removing units, so that the particles with different particle diameters are removed in stages, and the dust removing effect with low cost, high efficiency and small occupied area under the high-temperature condition is realized; high-temperature denitration catalytic box in dedusting and denitration equipment takes ammonia water generated by enriching odor ammonia as a reducing agent, and selects high Wen Tuoxiao catalyst to realize NO in flue gas x NH in odor 3 Co-treatment.
A baffle 18 is arranged at the joint of the cyclone dust removal unit and the filter cartridge dust removal unit in the high-temperature dust removal tower 1; the cyclone dust removal unit comprises a cyclone sub-assembly comprising at least one cyclone 13 (as shown in fig. 4, the number of the cyclones can be set according to the amount of flue gas processed in different scenes, and the like, and is not particularly limited herein, the number of the cyclones is 3 in the embodiment), an air pipe 14 and an ash storage hopper 15, an air inlet 11 is communicated with an inlet at the upper end of the cyclone 13, an ash storage hopper 15 is arranged at an outlet at the lower end of the cyclone 13, the air pipe 14 is arranged corresponding to the cyclone 13 and is positioned at the upper end of the cyclone 13, and the air pipe 14 passes through a partition 18 to be connected with the filter cylinder dust removal unit.
In the cyclone dust removal unit, flue gas enters the high-temperature dust removal tower 1 from the air inlet 11, enters the cyclone 13 through the impeller structure of the cyclone inlet 131, air flow in the cyclone 13 carries out spiral movement, particles such as fly ash and smoke dust in the flue gas fall into the ash storage hopper 15 from the lower end of the cyclone 13, and after preliminary treatment of the cyclone, the flue gas is introduced into the filter cylinder dust removal unit from the air pipe 14 corresponding to the center of the upper end of the cyclone 13.
And the cyclone dust removal unit is used for removing particles such as fly ash, smoke dust and the like in the flue gas at a high temperature.
The cartridge dust removal unit includes a cartridge assembly (as shown in fig. 4, the number of cartridges may be set according to the amount of smoke to be treated in various situations, etc., and is not particularly limited herein, the number of cartridges is 12 in the present embodiment) and a smoke chamber 17, the bottom of the cartridge 16 is sealed, and the upper portion of the cartridge 16 is opened and communicates with the smoke chamber 17.
In the cartridge dust removing unit, the filter cartridge 16 inside the filter cartridge dust removing unit can be a ceramic filter cartridge, the filter cartridge 16 has a cylindrical structure, the bottom of the filter cartridge 16 is sealed and is only opened at the upper part, and the filter cartridge 16 is connected with the smoke chamber 17 through the upper part. The primarily treated flue gas enters the filter cartridge dust removal unit from the air pipe 14, the secondary treatment is completed by filtering the wall of the filter cartridge 16, the particle dust with small particle size (such as <5 μm) in the flue gas is removed, and the flue gas after the secondary treatment and filtering enters the smoke chamber 17 from the inside of the filter cartridge 16. The smoke chamber 17 is connected with one end of the smoke tube 3, the other end of the smoke tube 3 is connected with the high-temperature denitration catalytic box 2, and the smoke after secondary treatment enters the high-temperature denitration catalytic box 2 through the smoke tube 3 to be subjected to synergistic treatment with odor.
In cyclone dust removal units, the ability to perform a preliminary treatment on the flue gas is mainly determined by cyclone subassemblies, and the number of cyclones is related to the amount of flue gas. In the invention, the cyclone 13 adopts a ceramic cyclone with the diameter phi of 360mm, and the single cyclone processes the smoke quantity Q x 1000 to 1500 mm 3 Inlet airflow velocity of cyclone inlet 131S x Is 12 to 23 m/s.
The number of cyclones 13 and the relation between the performance parameter and the smoke amount are specifically expressed as follows:
；
wherein ,Qx Treating smoke volume for a single cyclone, wherein N is the number of the cyclones, phi is the diameter of the single cyclone, S x Inlet airflow velocity, Q, for cyclone inlet 0 For the flue gas quantity entering the cyclone dust removal unit, the unit is m 3 /h，v 0 For the flow rate of the flue gas entering the cyclone dust removal unit, the unit is m 3 /s。
In a cartridge dust removal unit, the ability to perform secondary treatment on flue gas is mainly determined by the cartridge assembly, and the number of cartridges is related to the amount of flue gas and the like. According to the invention, the filter cylinder 16 is a ceramic filter cylinder, the applicable temperature of the ceramic filter cylinder is 200-900 ℃, the porosity is not less than 80%, the inner diameter of the filter cylinder is 110-150 mm, the length of the filter cylinder is 2000-5000 mm, and the filtering speed is 1-3 m/min.
The number of cartridges 16 and the performance parameters versus the amount of treatment smoke are specifically expressed as:
；
wherein S is the filtering area of a single filter cartridge, D is the inner diameter of the filter cartridge, D is the outer diameter of the filter cartridge, h is the length of the filter cartridge, i.e. the length of the filter cartridge when horizontally placed, n is the number of the filter cartridges needed, v 1 Filtration rate for a single cartridge, Q 1 The amount of smoke entering the cartridge dust removal unit.
The high-temperature denitration catalytic box 2 comprises a box body 21, a spray pipe 22 and a catalytic module 23, wherein the spray pipe 22 and the catalytic module 23 are arranged in the box body 21, a denitration catalyst is filled in the catalytic module 23, ammonia water is sprayed to the catalytic module 23 by the spray pipe 22, and the flue gas subjected to secondary treatment is subjected to denitration by catalytic reduction with the ammonia water in the catalytic module 23.
The catalytic module 23 comprises at least one catalytic layer, and the spray pipe 22 is arranged corresponding to the catalytic layer and in front of each catalytic layer; the denitration catalyst is in a honeycomb type pore structure.
Namely, a layered catalytic module 23 is arranged in the high-temperature denitration catalytic box 2, and a spray pipe 22 is arranged at the front part of each layered catalytic module 23. Ammonia in the odor is adsorbed by water to form ammonia water, and the ammonia water is uniformly sprayed towards the catalytic module 23 through the spray pipe 22.
The catalytic module 23 is filled with a honeycomb denitration catalyst, and the kind of the catalyst is mainly related to the use temperature. The type of the catalyst can be determined according to the specific determination model of the use temperature, the flue gas granularity and the like. The flue gas after secondary treatment enters a high-temperature denitration catalytic box 2, and is subjected to selective catalytic reduction with ammonia water sprayed out of a spray pipe 22 under the catalysis of a denitration catalyst through a catalytic module 23, so that denitration is realized.
In the embodiment of the invention, the honeycomb denitration catalyst is placed in the massive catalytic layer, and the cross section of the denitration catalyst is 150mm.
Different types of denitration catalysts are selected at the front end and the rear end of the catalytic layer, and the applicable temperature of the denitration catalyst at the front end is 400-550 ℃. In the denitration process, ammonia water is required to be sprayed on the catalytic layer, so that the temperature of the rear end is slightly reduced, and the applicable temperature of denitration catalyst treatment selected by the catalytic layer of the rear end is 300-420 ℃ according to the actual temperature. The overall catalytic performance of the catalytic module 23 is improved by selecting different types of denitration catalysts at the front end and the rear end.
After determining the model of the denitration catalyst, the relation between the size and the number of the catalytic layers and the smoke amount is specifically expressed as follows:
；
wherein ,the space velocity of the flue gas passing through the catalytic layer in unit volume and unit time is h -1 ，/>For the volume of all catalytic layers, the unit is m 3 ，/>For the area flow rate of the flue gas through the catalytic layer, in m/s,/for>For the geometric surface area of the catalytic layers, it is assumed here that the geometric surface areas of the catalytic layers are identical in m 2 ，Q 2 For the amount of smoke entering the catalytic layer, the unit is m 3 /h，v 2 For the flow rate of the flue gas entering the catalytic layer, the unit is m 3 /s。
The waste incineration system discharges flue gas, and nitrogen oxides are NO and NO 2 Mainly, wherein the concentration of NO is（mg/m 3 ）、NO 2 Concentration of->（mg/m 3 ). With NO, NO 2 In the catalytic denitration, the amount of ammonia supplied from the lance 22 is equal to the amount of pure ammonia required +.>(kg/h) correlation.
The relation between the flue gas parameters and the odor parameters is specifically expressed as:
；
wherein ,Q2 For the amount of smoke entering the catalytic layer, the unit is m 3 /h，Is the concentration of NO in the flue gas, & lt & gt>Is NO in flue gas 2 Concentration of->For denitration efficiency, the unit is%>Is the escape rate of ammonia, and the unit is ml/m 3 ，/>The amount of odor collected for the ith measurement is expressed in m 3 /h，/>The concentration of ammonia gas in the collected odor is measured for the ith time, and the unit is mg/m 3 T is the test interval time, the unit is h, T is the total time consumption of the aerobic treatment, the unit is h, and n is the total test times.
The amount of ammonia supplied by the spray pipe 22 is related to the treatment process of front-end odor, the total time consumption in a set period is T (h), and the air quantity q (m) of the odor is measured every T (h) 3 /h), concentration of ammonia in malodor（mg/m 3 ) Ammonia gas produced per hour on average +.>(kg/h). At this time, enriched ammonia->Pure ammonia amount required to be satisfied in the catalytic module +.>。
For example, in one embodiment, the following test recordings are made of treated flue gas and malodor:
NO before treatment x The concentration average value is about 437 mg/m 3 The emission standard (GB 1885-2014) is 300 mg/m 3 (1 hour average), 250 mg/m 3 (24 hours mean) waste incineration plant will NO x The concentration is reduced to 175 mg/m 3 And discharging left and right. The molar ratio of ammonia nitrogen in SCR catalytic denitration is about 1.03-1.06.
The fluctuation of ammonia concentration in different decomposition stages of the aerobic compost is larger and reaches up to 3000mg/m 3 The stack turning period is kept at 352-542 mg/m approximately 3 The concentration in the later period of decomposition is lower than 78-86 mg/m 3 . The fluctuation value of the smoke gas/odor is large, and part of the data can be checked, for example, the air quantity of a kitchen aerobic process of a certain 10t/d is 12000 m 3 Per hour, the flue gas air volume of a certain 10t/d garbage pyrolysis process is about 1190 m 3 And (3) h, the organic waste aerobic process with the garbage incineration treatment capacity of 100-200 t/d and about 10t/d of a garbage treatment plant is usually cooperated, small-scale sludge and permeate treatment equipment is additionally arranged, external ammonia water is needed in the starting operation stage, and the cooperated treatment self-sufficiency can be realized after stable operation.
As shown in fig. 5, the invention further provides a smoke and odor cooperative treatment method, which adopts the smoke and odor cooperative treatment system, and specifically comprises the following steps:
introducing flue gas generated by the incinerator into a waste heat boiler to perform heat conversion;
the collected odor is subjected to ammonia enrichment through water adsorption, and the residual odor after enrichment is led into an air supply system to enter an incinerator to assist combustion in the incinerator and realize incineration treatment of residual organic waste gas synchronously;
the flue gas of the waste heat boiler enters a high-temperature dust removal tower for dust removal, and then enters a high-temperature denitration catalytic box through a flue pipe;
the enriched ammonia gas reacts with the flue gas through a high-temperature denitration catalytic box.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the invention. It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof.
Claims (6)
1. A smoke and odor cooperative treatment method is characterized in that the smoke and odor cooperative treatment system comprises: the incinerator, the waste heat boiler and the dedusting and denitration equipment are sequentially communicated;
the equipment for dedusting and denitrating comprises: the high-temperature dust removal tower (1), the smoke pipe (3) and the high-temperature denitration catalytic box (2), wherein the high-temperature dust removal tower (1) comprises a shell (12), and a cyclone dust removal unit and a filter cartridge dust removal unit which are communicated with each other and are arranged in the shell (12);
the cyclone dust removal unit is provided with an air inlet (11), flue gas generated by the incineration of the household garbage enters the cyclone dust removal unit from the air inlet (11) for primary treatment, and the primarily treated flue gas is introduced into the filter cartridge dust removal unit, and the filter cartridge dust removal unit carries out secondary treatment on the flue gas;
the filter cylinder dust removal unit is provided with a smoke chamber (17), the smoke chamber (17) is connected with one end of a smoke tube (3), the other end of the smoke tube (3) is connected with a high-temperature denitration catalytic box (2), and the smoke after secondary treatment enters the high-temperature denitration catalytic box (2) through the smoke tube to be subjected to synergistic treatment with odor, wherein the odor is generated in the storage and aerobic treatment processes of organic wastes;
the high-temperature denitration catalytic box (2) comprises a box body (21), a spray pipe (22) and a catalytic module (23) in the box body (21), a denitration catalyst is filled in the catalytic module (23), ammonia in odor is adsorbed by water to form ammonia water, the ammonia water is sprayed to the catalytic module (23) through the spray pipe (22), the flue gas after secondary treatment is subjected to denitration by catalytic reduction between the catalytic module (23) and the ammonia water, the catalytic module (23) comprises at least one layer of catalytic layer, the spray pipe (22) is arranged corresponding to the catalytic layer, different types are selected at the front part of each catalytic layer, the denitration catalyst at the front end and the rear end of the catalytic layer, the applicable temperature of the denitration catalyst treatment at the front end is 400-550 ℃, and the applicable temperature of the denitration catalyst treatment at the rear end is 300-420 ℃;
the relation between the size and the number of the catalytic layers and the amount of smoke is specifically expressed as follows:
；
wherein ,the space velocity of the flue gas passing through the catalytic layer in unit volume and unit time is h -1 ，/>For the volume of all catalytic layers, the unit is m 3 ，/>For the area flow rate of the flue gas through the catalytic layer, in m/s,/for>For the geometric surface area of the catalytic layers, it is assumed here that the geometric surface areas of the catalytic layers are identical in m 2 ，Q 2 For the amount of smoke entering the catalytic layer, the unit is m 3 /h，v 2 For the flow rate of the flue gas entering the catalytic layer, the unit is m 3 /s；
The relation between the flue gas parameters and the odor parameters is specifically expressed as:
；
wherein ,is the concentration of NO in the flue gas, & lt & gt>Is NO in flue gas 2 Concentration of->The denitration efficiency is shown in units of,is the escape rate of ammonia, and the unit is ml/m 3 ，/>The amount of odor collected for the ith measurement is expressed in m 3 /h，/>The concentration of ammonia gas in the collected odor is measured for the ith time, and the unit is mg/m 3 T is the test interval time, the unit is h, T is the total time consumption of the aerobic treatment, the unit is h, and n is the total test times;
the method specifically comprises the following steps:
introducing the flue gas generated by the household garbage in the incinerator into a waste heat boiler for heat conversion;
the collected organic waste is subjected to ammonia enrichment through water adsorption on odor generated in the storage and aerobic treatment process, and the residual odor after enrichment is collected into an air supply system to enter an incinerator to assist combustion in the incinerator and synchronously realize incineration treatment of the residual organic waste gas;
the flue gas of the waste heat boiler enters a high-temperature dust removal tower for dust removal, and then enters a high-temperature denitration catalytic box through a flue pipe;
the enriched ammonia gas reacts with the flue gas through a high-temperature denitration catalytic box.
2. The method for collaborative treatment of smoke and odor according to claim 1, wherein the denitration catalyst is a honeycomb-like pore structure.
3. A smoke and odor cooperative treatment method according to claim 1, characterized in that a partition (18) is arranged at the connection of the cyclone dust removal unit and the filter cartridge dust removal unit;
the cyclone dust removal unit comprises a cyclone sub-assembly comprising at least one cyclone (13), an air pipe (14) and an ash storage hopper (15), wherein the air inlet (11) is communicated with an inlet at the upper end of the cyclone (13), the ash storage hopper (15) is arranged at an outlet at the lower end of the cyclone (13), the air pipe (14) is arranged corresponding to the cyclone (13) and is positioned at the upper end of the cyclone (13), and the air pipe (14) penetrates through the partition plate (18) to be connected with the filter cylinder dust removal unit;
the cartridge dust removal unit comprises a cartridge assembly comprising at least one cartridge (16) and a smoke chamber (17), the bottom of the cartridge (16) is sealed, and the upper part of the cartridge (16) is open and communicated with the smoke chamber (17).
4. A smoke and odor cooperative treatment method according to claim 3, characterized in that the treated air volume of the cyclone (13) is 1000-1500 m 3 And/h, the air flow speed of the inlet at the upper end of the cyclone (13) is 12-23 m/s.
5. A smoke and odor cooperative treatment method according to claim 3, characterized in that the number of cyclones (13) and the relation between the performance parameter and the smoke amount are specifically expressed as:
；
wherein ,Qx Treating smoke volume for a single cyclone, wherein N is the number of the cyclones, phi is the diameter of the single cyclone, S x Inlet airflow velocity, Q, for cyclone inlet 0 For the flue gas quantity entering the cyclone dust removal unit, the unit is m 3 /h，v 0 For the flow rate of the flue gas entering the cyclone dust removal unit, the unit is m 3 /s。
6. A smoke and odor cooperative treatment method according to claim 3, characterized in that the number of filter cartridges (16) and the relation between the performance parameters and the amount of treated smoke are expressed in detail as:
；
wherein S is the filtering area of a single filter cartridge, D is the inner diameter of the filter cartridge, D is the outer diameter of the filter cartridge, h is the length of the filter cartridge, n is the number of filter cartridges needed, v 1 Filtration rate for a single cartridge, Q 1 The amount of smoke entering the cartridge dust removal unit.
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| CN104028088A (en) * | 2014-07-01 | 2014-09-10 | 南京大学 | Method for reducing NOx in smoke through ammonia source of household garbage |
| CN106705064A (en) * | 2016-12-20 | 2017-05-24 | 航天凯天环保科技股份有限公司 | Method for reducing dioxin in incineration gas of household garbage |
| CN107702108A (en) * | 2017-10-17 | 2018-02-16 | 北京高安屯垃圾焚烧有限公司 | Garbage burning boiler returns the method that spray garbage leachate reduces NOx emission |
| CN209549074U (en) * | 2019-01-26 | 2019-10-29 | 洛阳阿尔法新材料有限公司 | One kind being used for electric smelting Cr2O3The dust-extraction unit of the ultra-clean discharge of production |
| CN110030570A (en) * | 2019-05-27 | 2019-07-19 | 桂林航天工业学院 | Based on the integrated refuse burning system of the selective catalytic denitrification process plasma and method |
| CN214764491U (en) * | 2021-02-07 | 2021-11-19 | 江苏品德环保科技有限公司 | Purification device for waste incineration flue gas |
| CN113262630A (en) * | 2021-05-12 | 2021-08-17 | 上海环境卫生工程设计院有限公司 | Denitration equipment for solving problem of high ammonia escape in flue gas of waste incineration plant |
| CN219023761U (en) * | 2022-08-26 | 2023-05-16 | 城康材料技术有限公司 | Waste incineration flue gas treatment system |
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