CN110553269A - High and low calorific value hazardous waste collaborative incineration melting harmless treatment system and application - Google Patents
High and low calorific value hazardous waste collaborative incineration melting harmless treatment system and application Download PDFInfo
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- CN110553269A CN110553269A CN201910746782.6A CN201910746782A CN110553269A CN 110553269 A CN110553269 A CN 110553269A CN 201910746782 A CN201910746782 A CN 201910746782A CN 110553269 A CN110553269 A CN 110553269A
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- 238000002844 melting Methods 0.000 title claims abstract description 74
- 230000008018 melting Effects 0.000 title claims abstract description 74
- 239000002920 hazardous waste Substances 0.000 title claims abstract description 36
- 239000000725 suspension Substances 0.000 claims abstract description 171
- 239000002699 waste material Substances 0.000 claims abstract description 114
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 68
- 239000003546 flue gas Substances 0.000 claims abstract description 68
- 239000007789 gas Substances 0.000 claims abstract description 16
- 239000002253 acid Substances 0.000 claims abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 56
- 238000005243 fluidization Methods 0.000 claims description 32
- 238000002156 mixing Methods 0.000 claims description 32
- 238000001816 cooling Methods 0.000 claims description 28
- 239000000428 dust Substances 0.000 claims description 28
- 239000000463 material Substances 0.000 claims description 22
- 239000004744 fabric Substances 0.000 claims description 20
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 18
- 239000004202 carbamide Substances 0.000 claims description 18
- 239000002893 slag Substances 0.000 claims description 16
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 8
- 238000004380 ashing Methods 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 claims description 5
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 238000003795 desorption Methods 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000005453 pelletization Methods 0.000 claims description 4
- 239000012855 volatile organic compound Substances 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 238000010891 electric arc Methods 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 239000003345 natural gas Substances 0.000 claims description 3
- 239000010802 sludge Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 239000002910 solid waste Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 239000003960 organic solvent Substances 0.000 description 4
- 238000009272 plasma gasification Methods 0.000 description 4
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- 230000009467 reduction Effects 0.000 description 3
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- 239000000779 smoke Substances 0.000 description 3
- 238000004056 waste incineration Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 239000003818 cinder Substances 0.000 description 2
- 238000009713 electroplating Methods 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
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- 239000002480 mineral oil Substances 0.000 description 2
- 235000010446 mineral oil Nutrition 0.000 description 2
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- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
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- 230000008676 import Effects 0.000 description 1
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- 230000004048 modification Effects 0.000 description 1
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- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
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- 230000001988 toxicity Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000013585 weight reducing agent Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/442—Waste feed arrangements
- F23G5/444—Waste feed arrangements for solid waste
-
- 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
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
- F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
-
- 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
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/10—Intercepting solids by filters
- F23J2217/104—High temperature resistant (ceramic) type
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
the invention relates to a high and low calorific value hazardous waste collaborative incineration and melting harmless treatment system which comprises an incineration and melting furnace and a multi-stage suspension preheating collaborative deacidification system which are connected, wherein the incineration and melting furnace can carry out incineration and melting harmless treatment on hazardous waste, and the multi-stage suspension preheating collaborative deacidification system can preheat low calorific value hazardous waste and remove acid gas in flue gas in a collaborative mode. The system realizes that on one hand, the high-temperature flue gas generated by burning the high-calorific-value dangerous waste is utilized to fully preheat the low-calorific-value dangerous waste, and the melting operation cost of the low-calorific-value dangerous waste is reduced; on the other hand, the low-calorific-value dangerous waste is mixed with the high-calorific-value dangerous waste in the incineration and incineration chamber, so that the furnace temperature is effectively controlled, the treatment capacity of the high-calorific-value dangerous waste is improved, and the aims of incineration, melting, harmlessness and resource utilization of the high-calorific-value dangerous waste and the low-calorific-value dangerous waste are finally fulfilled.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and particularly relates to a harmless treatment system for collaborative incineration and melting of high and low calorific value dangerous wastes and application thereof.
Background
With the increasing exhaustion of resources and the increasing requirement of environmental protection, a large number of traditional waste treatment technologies cannot meet the requirement of pollution treatment, wherein the hazardous waste with the greatest environmental hazard can be divided into: low calorific value hazardous waste and high calorific value hazardous waste. The low-heat value dangerous waste has the characteristics of low heat value, high water content, high leaching toxicity and the like, and mainly comprises surface treatment waste, metal surface treatment sludge, electroplating sludge, acid pickling sludge, metal smelting leaching slag, incineration residue and the like; the high-calorific-value dangerous waste has the characteristics of high calorific value, high volatility, easiness in combustion and the like, and mainly comprises pesticide waste, organic solvent waste, waste mineral oil, rectification residue, organic resin waste, waste halogenated organic solvent, water treatment sludge and the like. At present, the high-calorific-value dangerous waste is mainly treated by the traditional incineration treatment process; and because the low-calorific-value dangerous waste is not suitable for the traditional incineration treatment process waste, only a stable solidification landfill treatment technology with high potential safety hazard and a melting solidification treatment technology with high cost can be selected. The low-cost effective disposal and resource utilization of high and low calorific value dangerous wastes become the focus of social wide attention and the difficult problems which need to be solved urgently.
Through searching, the following patent publications related to the patent application of the invention are found:
1. the utility model provides a continuous overflow row sediment plasma melting furnace and application (CN109469910A), the melting furnace includes furnace body, plasma torch heating system and molten bath, the furnace body top is equipped with the material import, and furnace is made to this furnace internal coaxiality, the molten bath includes molten bath body, continuous overflow row cinder notch and intermittent type row clean mouth, plasma torch heating system includes plasma torch generator and generator protection heat insulating sleeve, and generator protection heat insulating sleeve closely suit is on plasma torch generator's surface, and plasma torch generator sets up along furnace body circumferencial direction equipartition interval, and at least one plasma torch generator sets up in the top or both sides that are close to continuous overflow row cinder notch. The melting furnace realizes high-efficiency and rapid melting and continuous overflow deslagging of the low-calorific-value hazardous waste plasma melting furnace, and finally achieves the purposes of large processing capacity, high thermal efficiency, low labor consumption, high automation degree, low operation risk and low equipment investment of low-calorific-value hazardous waste plasma melting equipment.
2. a plasma gasification melting furnace and a method (CN108395906A) for harmless treatment of dangerous solid waste by using the same, the plasma gasification melting furnace comprises: a housing including a first end and a second end opposite to each other; a feed inlet and a syngas outlet at the first end; a slag discharge port at the second end; and a plurality of gas supply holes and a plurality of plasma torches disposed on the housing between the first end and the second end. The invention also provides a method for performing harmless treatment on dangerous solid waste by using the plasma gasification melting furnace. The invention aims to provide a plasma gasification melting furnace, which utilizes a plasma torch to generate a high-temperature energy source under a negative-pressure oxygen-deficient environment, so that organic components in dangerous solid wastes entering the furnace are cracked and gasified and are converted into crude synthesis gas, inorganic components are melted to form harmless vitreous residues, the volume reduction, weight reduction and primary harmless treatment of the dangerous solid wastes are realized, and the solid wastes can be thoroughly harmless and have no secondary pollution by matching with other systems.
by contrast, the present patent application is substantially different from the above patent publications.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a high-calorific-value and low-calorific-value dangerous waste collaborative incineration and melting harmless treatment system and application thereof, the system solves the problems that the high-calorific-value dangerous waste is limited by the furnace temperature and has low treatment capacity, and the low-calorific-value dangerous waste is insufficiently preheated and melted and has high operation cost, and on one hand, the high-temperature smoke generated by incineration of the high-calorific-value dangerous waste is utilized to fully preheat the low-calorific-value dangerous waste, so that the melting operation cost is reduced; on the other hand, the low-calorific-value dangerous waste is mixed with the high-calorific-value dangerous waste in the incineration and incineration chamber, so that the furnace temperature is effectively controlled, the treatment capacity of the high-calorific-value dangerous waste is improved, and the aims of incineration, melting, harmlessness and resource utilization of the high-calorific-value dangerous waste and the low-calorific-value dangerous waste are finally fulfilled.
The technical problem to be solved by the invention is realized by adopting the following technical scheme:
the utility model provides a high, low heat value hazardous waste burns melting innocent treatment system in coordination, the system preheats in coordination deacidification system including the burning melting furnace and the multistage suspension that are connected to set up, burning melting furnace can burn melting innocent treatment with hazardous waste, multistage suspension preheats in coordination deacidification system and can preheat the acid gas in low heat value hazardous waste and the in coordination desorption flue gas.
Moreover, the incineration melting furnace comprises a high-temperature melting pool, an incineration preheating chamber, a slag discharging system, an incineration preheating chamber material conveying device, a reciprocating material pushing device, a high-calorific-value dangerous waste charging opening C and an upper outlet, wherein the incineration preheating chamber is obliquely arranged downwards along the horizontal direction, one end of the incineration preheating chamber arranged above is communicated with the upper outlet, the incineration preheating chamber arranged below the upper outlet is communicated with the high-calorific-value dangerous waste charging opening C, the high-calorific-value dangerous waste charging opening C is connected with the incineration preheating chamber through the reciprocating, the bottom of the high-temperature molten pool is provided with an outlet which is connected with a slag discharge system.
moreover, the material conveying device of the ashing preheating chamber is a high-temperature grate, a chain or a rotary furnace type incineration conveying facility; the heating equipment of the high-temperature molten pool is high-temperature plasma, high-temperature electric arc or natural gas pure oxygen combustion.
The multistage suspension preheating and deacidification cooperative system comprises a first suspension preheater, a second suspension preheater, a third suspension preheater, a fourth suspension preheater and a fifth suspension preheater, wherein the first suspension preheater, the second suspension preheater, the third suspension preheater, the fourth suspension preheater and the fifth suspension preheater are all arranged in the vertical direction, the top parts of the first suspension preheater, the second suspension preheater, the third suspension preheater, the fourth suspension preheater and the fifth suspension preheater are communicated with one another and provided with an inlet and an upper outlet, the inlet and the upper outlet are arranged at intervals, and the bottom parts of the first suspension preheater, the;
An outlet at the upper part of the incineration ashing preheating chamber is connected with an inlet of a first suspension preheater, a first urea feeding port is arranged at the inlet of the first suspension preheater, and urea can be sprayed into the flue gas of the first suspension preheater through the first urea feeding port to carry out SNCR (selective non-catalytic reduction) denitration; the lower outlet of the suspension preheater I is connected with the middle high-temperature area of the incineration ashing preheating chamber;
An outlet at the upper part of the first suspension preheater is connected with an inlet of a second suspension preheater, a second urea feeding port is arranged at the inlet of the second suspension preheater, and urea can be sprayed into the flue gas of the second suspension preheater through the second urea feeding port to carry out SNCR (selective non-catalytic reduction) denitration; the lower outlet of the suspension preheater II is connected with the inlet of the suspension preheater I;
An outlet at the upper part of the second suspension preheater is connected with an inlet of the third suspension preheater, and an outlet at the lower part of the third suspension preheater is connected with an inlet of the second suspension preheater;
An outlet at the upper part of the suspension preheater III is connected with an inlet of the suspension preheater IV, a feed back feeding point B is arranged at the inlet of the suspension preheater IV, and an outlet at the lower part of the suspension preheater IV is connected with an inlet of the suspension preheater III;
the upper outlet of the suspension preheater IV is connected with the inlet of the suspension preheater V, a low-heat-value dangerous waste feeding point A is arranged at the inlet of the suspension preheater V, low-heat-value dangerous waste containing CaO can be added into the outlet pipeline of the suspension preheater IV through the low-heat-value dangerous waste feeding point A, and the lower outlet of the suspension preheater V is connected with the inlet of the suspension preheater IV through a material returning feeding point B.
Moreover, the system also comprises an NH 3 + air jet mixing system, an SCR denitration reactor system, a Venturi fluidization deacidification cooperative cooling system, an active carbon jet mixing system and a cloth bag dust removal system which are sequentially connected, wherein the NH 3 + air jet mixing system is connected with the outlet of the multi-stage suspension preheating cooperative deacidification system, the outlet of the Venturi fluidization deacidification cooperative cooling system is also connected with the multi-stage suspension preheating cooperative deacidification system, and the outlet of the cloth bag dust removal system is also connected with the charging hole of the incineration melting furnace;
NH 3 + air sprays the hybrid system and can mix NH 3, air and flue gas even, SCR denitration reactor system can the selective catalytic desorption NOx in the flue gas, acid gas in the flue gas can be got rid of to venturi fluidization deacidification is cooling system in coordination to through deacidification agent evaporation heat absorption with flue gas temperature drop to required temperature, active carbon sprays the hybrid system and can mix active carbon and flue gas even, dust and active carbon particle in the sack dust pelletizing system can get rid of the flue gas.
And the upper outlet of the suspension preheater five is connected with the inlet of the NH 3 + air injection mixing system.
The SCR denitration reactor system comprises a flue gas inlet at the top and a lower outlet at the bottom, an NH 3 + air injection mixing system is arranged at the flue gas inlet of the SCR denitration reactor system, and a three-layer denitration catalyst is placed in the SCR denitration reactor system and used for selectively catalyzing NOx in flue gas to generate N 2 and H 2 O;
The Venturi fluidization deacidification cooperative cooling system comprises a lower inlet, an upper outlet and a bottom outlet, the lower outlet of the SCR denitration reactor system is connected with the lower inlet of the Venturi fluidization deacidification cooperative cooling system, and one or more of Ca (OH) 2 solution, Na 2 CO 3 solution and NaOH solution can be sprayed into the upper part of the Venturi fluidization deacidification cooperative cooling system;
The material at the bottom of the Venturi fluidization deacidification and cooling system is connected with a feed back feeding point B of the suspension preheater IV through a bottom outlet and a feed back conveying pipeline 8;
The upper outlet of the Venturi fluidization deacidification and cooling system is connected with the inlet of an activated carbon jet mixing system, activated carbon particles can be sprayed into the inlet of the cloth bag dust removal system by the activated carbon jet mixing system, the activated carbon and the flue gas are fully mixed through turbulent flow mixing, and the activated carbon jet mixing system is used for adsorbing trace dioxin and volatile organic compounds in the flue gas; and the bottom outlet of the cloth bag dust removal system is connected with a high-heat value dangerous waste charging opening C through a feed back conveying pipeline.
and a first outer discharge port is arranged on a pipeline between the outlet of the Venturi fluidization deacidification and temperature reduction system and the multistage suspension preheating and deacidification system, and a second outer discharge port is arranged on a pipeline between the outlet of the cloth bag dust removal system and the incineration melting furnace.
The application of the high and low calorific value hazardous waste collaborative incineration melting harmless treatment system in the aspect of incineration melting harmless treatment of respectively feeding and preprocessing hazardous wastes with different calorific values.
the invention has the advantages and positive effects that:
1. The system solves the problems that the high-calorific-value dangerous waste is limited by the furnace temperature and has low treatment capacity, and the low-calorific-value dangerous waste is insufficiently preheated and melted and has high operation cost, and realizes that the low-calorific-value dangerous waste is sufficiently preheated by using high-temperature flue gas generated by burning the high-calorific-value dangerous waste and the melting operation cost of the low-calorific-value dangerous waste is reduced; on the other hand, the low-calorific-value dangerous waste is mixed with the high-calorific-value dangerous waste in the incineration and incineration chamber, so that the furnace temperature is effectively controlled, the treatment capacity of the high-calorific-value dangerous waste is improved, and the aims of incineration, melting, harmlessness and resource utilization of the high-calorific-value dangerous waste and the low-calorific-value dangerous waste are finally fulfilled.
2. The system is provided with a low-calorific-value dangerous waste feeding point A, a return feeding point B and a high-calorific-value dangerous waste feeding point C in a separate feeding mode, high-calorific-value dangerous waste is effectively treated while the low-calorific-value dangerous waste is preheated by fully utilizing high-temperature flue gas, the treatment capacity of the high-calorific-value dangerous waste is increased by utilizing the mixing of the low-calorific-value dangerous waste, and finally the high-calorific-value dangerous waste incineration residue, the low-calorific-value dangerous waste, the return fly ash and the like are subjected to molten glass harmless treatment and resource utilization.
3. The system of the invention adopts a mode of connecting the multistage suspension preheaters in series, thereby realizing the full preheating of the low-calorific-value dangerous waste by the high-temperature flue gas and saving the melting operation cost of the low-calorific-value dangerous waste to the maximum extent.
4. according to the system, low-heat value dangerous waste containing CaO is added into the outlet pipeline of the suspension preheater IV through the feeding point A at the top of the multistage suspension preheater, so that the low-heat value dangerous waste can be preheated in the multistage suspension preheater, and meanwhile, the CaO in the material can effectively contact with the acid gas in the flue gas, so that the acid gas in the flue gas is fully removed, and compared with a wet deacidification process for tail gas, the system is more water-saving and energy-saving.
5. according to the tail gas purification system, the SNCR denitration system, the multistage suspension preheating collaborative deacidification system, the SCR denitration system, the Venturi fluidization deacidification collaborative cooling system, the activated carbon adsorption system, the cloth bag dust removal system and other process systems are adopted, so that the NOx emission concentration in the tail gas is lower than 50mg/Nm 3 2 and is lower than 100mg/Nm 3, and the dioxin emission concentration is lower than 0.01ng-TEQ/m 3.
6. The system is particularly suitable for incineration melting harmless treatment of respectively feeding pretreatment of dangerous wastes with different heat values, such as: high calorific value hazardous waste: pesticide waste, organic solvent waste, waste mineral oil, rectification residue, organic resin waste, waste halogenated organic solvent, water treatment sludge and the like, and low-calorific-value dangerous waste: surface treatment waste, metal surface treatment sludge, electroplating sludge, acid washing sludge, metal smelting leaching slag, incineration residue and the like, and belongs to the technical field of harmless and resource utilization of solid waste.
7. the system solves the problems of high-temperature melting of low-calorific-value dangerous waste, high tail gas purification operation cost and low incineration treatment capacity of high-calorific-value dangerous waste in the incineration, melting and harmless treatment process of the dangerous waste, and is used for collaborative incineration, melting and harmless treatment of high-calorific-value dangerous waste and low-calorific-value dangerous waste.
8. The high-calorific-value dangerous waste has high calorific value and is limited by the temperature of the incinerator, and the treatment capacity is low; the low-calorific-value dangerous waste directly enters a high-temperature molten pool from the original water-containing state at room temperature, and is heated to a molten state, so that a large amount of energy is consumed, and the operation cost is high. Therefore, how to combine the advantages of the high-calorific-value and low-calorific-value dangerous wastes to form a low-calorific-value dangerous waste mixed with a high-calorific-value dangerous waste to increase the treatment capacity of the low-calorific-value dangerous waste is urgently needed, and meanwhile, the high-temperature smoke generated by the high-calorific-value dangerous waste fully preheats the low-calorific-value dangerous waste so as to reduce the melting operation cost of the low-calorific-value dangerous waste. In order to solve the problems, the invention provides a harmless treatment system for the collaborative incineration and melting of high and low calorific value dangerous wastes. On one hand, the high-temperature melting and solidification realizes the thorough oxidative decomposition of dioxin in low-heat value dangerous waste, and heavy metals and calcium silicon inorganic matters are solidified into non-toxic and harmless glass state water-quenched slag through quenching after high-temperature melting. On the other hand, incineration residues generated after incineration and incineration of the high-calorific-value dangerous waste directly enter a high-temperature molten pool at the tail part, the incineration residues are further melted in the high-temperature molten pool and then are solidified into non-toxic and harmless glass state water-quenched slag, and the generated high-temperature flue gas can fully preheat the low-calorific-value dangerous waste, so that the melting operation cost of the low-calorific-value dangerous waste is further reduced.
drawings
FIG. 1 is a schematic diagram of the structural connection of the system of the present invention.
Detailed Description
The present invention will be further described with reference to specific examples, which are intended to be illustrative, not limiting and are not intended to limit the scope of the invention.
structures not specifically described in detail herein are to be understood as conventional in the art.
The utility model provides a high, low heat value hazardous waste is burning melting innocent treatment system in coordination, as shown in figure 1, the system preheats in coordination deacidification system 2 including the burning melting furnace 1 and the multistage suspension that are connected to set up, burning melting furnace can burn melting innocent treatment with hazardous waste, multistage suspension is preheated in coordination deacidification system and can preheat low heat value hazardous waste, reduce melting cost and in coordination deacidification gas in the flue gas.
in this embodiment, the incineration melting furnace includes a high-temperature melting bath 101, an incineration preheating chamber 102, a slag discharge system 103, an incineration preheating chamber material conveying device 104, a reciprocating material pushing device 105, a high-calorific-value dangerous waste feeding port C and an upper outlet 106, the incineration preheating chamber is arranged obliquely downwards along the horizontal direction, one end of the incineration preheating chamber arranged above is communicated with the upper outlet, the incineration preheating chamber close to the upper outlet is communicated with the high-calorific-value dangerous waste feeding port C, the high-calorific-value dangerous waste feeding port C is arranged below the upper outlet, the high-calorific-value dangerous waste feeding port C is connected with the incineration preheating, the bottom of the high-temperature molten pool is provided with an outlet which is connected with a slag discharge system.
Preferably, the material conveying device of the ashing preheating chamber can be a high-temperature grate, a chain or a rotary furnace type incineration conveying facility; the heating device of the high-temperature molten pool can be high-temperature plasma, high-temperature electric arc or natural gas pure oxygen combustion.
In this embodiment, the multistage suspension preheating and deacidification cooperative system includes a first suspension preheater 200, a second suspension preheater 203, a third suspension preheater 204, a fourth suspension preheater 205 and a fifth suspension preheater 206, wherein the first suspension preheater, the second suspension preheater, the third suspension preheater, the fourth suspension preheater and the fifth suspension preheater are all arranged along a vertical direction, the top portions of the first suspension preheater, the second suspension preheater, the third suspension preheater, the fourth suspension preheater and the fifth suspension preheater are communicated with each other and provided with an inlet and an upper outlet, the inlet and the upper outlet are arranged at intervals, and the bottom portions of the first suspension preheater, the first suspension preheater and;
The upper outlet of the incineration preheating chamber is connected with the inlet of the suspension preheater I, the temperature of high-temperature flue gas generated by incineration and incineration of high-calorific-value dangerous waste in the incineration preheating chamber is about 1100 ℃, and the high-temperature flue gas enters the suspension preheater I; a first urea feeding port 201 is arranged at an inlet of the first suspension preheater, and urea can be sprayed into the flue gas of the first suspension preheater through the first urea feeding port to carry out SNCR denitration; the upper outlet flue gas temperature of the first suspension preheater was about 950 ℃. The temperature of a lower low-calorific-value dangerous waste outlet of a suspension preheater I is about 750 ℃, a lower material outlet of the suspension preheater I is connected with a middle high-temperature region of an incineration and incineration preheating chamber, the material is further preheated to 900 ℃ by smoke generated by incineration of high-calorific-value dangerous waste in the incineration and incineration preheating chamber and then enters a high-temperature molten pool together with incineration residues of the high-calorific-value dangerous waste, and the material is completely melted in the high-temperature molten pool at 1500 ℃ and then enters a bottom slag tapping system to be non-toxic and harmless water-quenched glassy slag which is used as a paving building material for recycling;
An outlet at the upper part of the first suspension preheater is connected with an inlet of the second suspension preheater, a second urea feeding port 202 is arranged at the inlet of the second suspension preheater, and urea can be sprayed into the flue gas of the second suspension preheater through the second urea feeding port to carry out SNCR (selective non-catalytic reduction) denitration; and the temperature of the flue gas at the upper outlet of the second suspension separator is about 800 ℃. The outlet temperature of the low-calorific-value hazardous waste at the lower part of the suspension preheater II is about 600 ℃, and the outlet at the lower part of the suspension preheater II is connected with the inlet of the suspension preheater I;
And an outlet at the upper part of the second suspension preheater is connected with an inlet of the third suspension preheater, and the flue gas temperature at an outlet at the upper part of the third suspension separator is about 650 ℃. The outlet temperature of the low-calorific-value hazardous waste at the lower part of the suspension preheater III is about 450 ℃, and the outlet at the lower part of the suspension preheater III is connected with the inlet of the suspension preheater II;
And an outlet at the upper part of the suspension preheater III is connected with an inlet of the suspension preheater IV, and the flue gas temperature at an outlet at the upper part of the suspension separator IV is about 500 ℃. And a feed back feeding point B is arranged at the inlet of the suspension preheater IV, and high-temperature materials generated by the Venturi fluidization deacidification and cooling system are conveyed to the feeding point B through a feed back conveying pipeline, so that the recycling of fly ash is realized. The outlet temperature of the low-calorific-value hazardous waste at the lower part of the suspension preheater IV is about 300 ℃, and the outlet at the lower part of the suspension preheater IV is connected with the inlet of the suspension preheater III;
And an outlet at the upper part of the suspension preheater IV is connected with an inlet of the suspension preheater V, and the flue gas temperature at the outlet at the upper part of the suspension preheater V is about 350 ℃. A low-calorific-value dangerous waste feeding point A is arranged at the inlet of the suspension preheater V, and low-calorific-value dangerous waste containing CaO can be added into an outlet pipeline of the suspension preheater IV through the low-calorific-value dangerous waste feeding point A; the outlet temperature of the low-calorific-value hazardous waste at the lower part of the suspension preheater five is about 150 ℃, and the outlet at the lower part of the suspension preheater five is connected with the inlet of the suspension preheater four through a feed back feeding point B;
The upper outlet flue gas temperature of the suspension preheater five is about 350 ℃.
In this embodiment, the system further includes an NH 3 + air jet mixing system 3, an SCR denitration reactor system 4, a venturi fluidization deacidification cooperative cooling system 5, an activated carbon jet mixing system 6, and a cloth bag dust removal system 7, which are connected in sequence, wherein the NH 3 + air jet mixing system is connected to an outlet of the multistage suspension preheating cooperative deacidification system, an outlet of the venturi fluidization deacidification cooperative cooling system is further connected to the multistage suspension preheating cooperative deacidification system, and an outlet of the cloth bag dust removal system is further connected to a charging port of the incineration melting furnace;
NH 3 + air sprays the hybrid system and can be used for the homogeneous mixing of NH 3, air and flue gas, SCR denitration reactor system can the selective catalytic desorption NOx in the flue gas, acid gases such as HCl in the flue gas and SO 2 can be got rid of to venturi fluidization deacidification collaborative cooling system to through deacidification agent evaporation heat absorption with flue gas temperature drop to required temperature, active carbon sprays the hybrid system and can be used for the homogeneous mixing of active carbon and flue gas, dust and active carbon granule in the sack dust pelletizing system can the desorption flue gas.
In this embodiment, the upper outlet of the suspension preheater five is connected to the inlet of the NH 3 + air injection mixing system.
In this embodiment, the SCR denitration reactor system includes a top flue gas inlet 401 and a bottom outlet 402, an NH 3 + air injection mixing system is disposed at the flue gas inlet of the SCR denitration reactor system, a three-layer denitration catalyst is disposed in the SCR denitration reactor system for selectively catalyzing NOx in flue gas to generate N 2 and H 2 O, and the temperature of the flue gas in the SCR denitration reactor system is reduced to 345 ℃;
The venturi fluidization deacidification and cooperative cooling system comprises a lower inlet 501, an upper outlet 502 and a bottom outlet 503, the lower outlet of the SCR denitration reactor system is connected with the lower inlet of the venturi fluidization deacidification and cooperative cooling system, one or more of Ca (OH) 2 solution, Na 2 CO 3 solution and NaOH solution can be sprayed into the upper part of the venturi fluidization deacidification and cooperative cooling system, on one hand, the system is used for removing HCl, SO 2, SO 3, HF and the like in flue gas, on the other hand, the system is used for reducing the temperature of the flue gas and protecting a subsequent cloth bag dust removal system, and the temperature of the flue gas in the venturi fluidization deacidification and cooperative cooling system is reduced from 345 ℃ to about 170 ℃;
the material at the bottom of the Venturi fluidization deacidification and temperature reduction system is connected with a feed back feeding point B of the suspension preheater IV through a bottom outlet and a feed back conveying pipeline 8, and the material at the bottom of the Venturi fluidization deacidification and temperature reduction system is conveyed to an inlet feeding point B of the suspension preheater IV through the bottom outlet and the feed back conveying pipeline to be recycled;
an upper outlet of the Venturi fluidization deacidification and cooling system is connected with an inlet of an activated carbon jet mixing system, activated carbon particles can be sprayed into the inlet of the cloth bag dust removal system by the activated carbon jet mixing system, the activated carbon and the flue gas are fully mixed through turbulent flow mixing, and the activated carbon jet mixing system is used for adsorbing trace amounts of dioxin and Volatile Organic Compounds (VOCs) in the flue gas; and the bottom outlet of the cloth bag dust removal system is connected with a high-heat value dangerous waste charging opening C through a feed back conveying pipeline. The activated carbon particles are carried along with the flue gas fluidization and evenly spread on the surface of the cloth bag, and the flue gas further enhances the adsorption effect of the activated carbon while filtering dust in the cloth bag. The temperature of the flue gas is reduced to about 170 ℃ after passing through the activated carbon jet mixing system and the cloth bag dust removal system, and the dust at the bottom outlet of the cloth bag dust removal system carries more activated carbon particles and is conveyed to a high-calorific-value dangerous waste feeding point C through a feed back conveying pipeline. The activated carbon particles are incinerated, incinerated and further melted in the incinerating and incinerating preheating chamber to realize harmless resource utilization.
in this embodiment, set up first outer discharge port 12 on venturi fluidization deacidification is in coordination with the pipeline between the cooling system's export and multistage suspension preheating in coordination with deacidification system, set up second outer discharge port 13 on the pipeline between the export of sack dust pelletizing system and the burning melting furnace, this first outer discharge port and the setting of second outer discharge port can further avoid the flying dust circulation to cause the enrichment of volatile heavy metal, chloride, fluoride and sulphide for the flying dust of enrichment is regularly discharged outside the system.
The working principle of the harmless treatment system for the high and low calorific value hazardous wastes in cooperation with incineration and melting is as follows:
The high-calorific-value dangerous waste is fully combusted in the incineration and incineration preheating chamber of the incineration and melting furnace, the high-temperature flue gas generated by combustion can preheat the low-calorific-value dangerous waste by means of the multistage suspension preheating system, the melting harmless treatment cost of the low-calorific-value dangerous waste is reduced, and meanwhile, after the low-calorific-value dangerous waste and the high-calorific-value dangerous waste are mixed in the incineration and melting furnace incineration chamber, the temperature of the incineration chamber can be effectively controlled, and the incineration treatment capacity of the high-calorific-value dangerous waste is improved. The preheated low-calorific-value dangerous waste and high-calorific-value dangerous waste incineration residues enter a high-temperature molten pool through a transmission device, are melted into liquid under the action of high-temperature heating, and the liquid molten slag enters a slag discharging system at the bottom through a slag discharging port of the high-temperature molten pool, so that solidification and harmlessness of the low-calorific-value dangerous waste and the high-calorific-value dangerous waste incineration residues are realized; in addition, the system can fully utilize the strong suspension mixing function of the multistage suspension preheater, and deacidification agents such as CaO and the like are added into the low-heat-value dangerous waste, so that the low-heat-value dangerous waste is preheated while acid gas in the flue gas is removed, and the operation cost of flue gas deacidification is reduced.
Although the embodiments of the present invention have been disclosed for illustrative purposes, those skilled in the art will appreciate that: various substitutions, changes and modifications are possible without departing from the spirit and scope of the invention and the appended claims, and therefore the scope of the invention is not limited to the embodiments disclosed.
Claims (9)
1. The utility model provides a high, low calorific value hazardous waste is burning melting innocent treatment system in coordination which characterized in that: the system comprises an incineration melting furnace and a multi-stage suspension preheating and deacidification cooperative system which are connected and arranged, the incineration melting furnace can carry out incineration melting harmless treatment on the hazardous waste, and the multi-stage suspension preheating and deacidification cooperative system can preheat the low-calorific-value hazardous waste and cooperatively remove acid gas in flue gas.
2. The high and low calorific value hazardous waste collaborative incineration melting harmless treatment system according to claim 1, wherein: the incineration melting furnace comprises a high-temperature molten pool, an incineration preheating chamber, a slag discharging system, an incineration preheating chamber material conveying device, a reciprocating material pushing device, a high-calorific-value dangerous waste charging opening C and an upper outlet, wherein the incineration preheating chamber is obliquely and downwards arranged along the horizontal direction, one end of the incineration preheating chamber arranged above is communicated with the upper outlet, the incineration preheating chamber arranged below the upper outlet is communicated with the high-calorific-value dangerous waste charging opening C through the reciprocating material pushing device, the other end outlet, the bottom of the high-temperature molten pool is provided with an outlet which is connected with a slag discharge system.
3. the high and low calorific value hazardous waste collaborative incineration melting harmless treatment system according to claim 2, wherein: the material conveying device of the ashing preheating chamber is a high-temperature grate, a chain or a rotary furnace type incineration conveying facility; the heating equipment of the high-temperature molten pool is high-temperature plasma, high-temperature electric arc or natural gas pure oxygen combustion.
4. the high and low calorific value hazardous waste collaborative incineration melting harmless treatment system according to claim 2, wherein: the multistage suspension preheating and deacidification cooperative system comprises a first suspension preheater, a second suspension preheater, a third suspension preheater, a fourth suspension preheater and a fifth suspension preheater, wherein the first suspension preheater, the second suspension preheater, the third suspension preheater, the fourth suspension preheater and the fifth suspension preheater are all arranged along the vertical direction, the top parts of the first suspension preheater, the second suspension preheater, the third suspension preheater, the fourth suspension preheater and the fifth suspension preheater are communicated with one another to form an inlet and an upper outlet, the inlet and the upper outlet are arranged at intervals, and the bottom parts of the first suspension preheater;
an outlet at the upper part of the incineration ashing preheating chamber is connected with an inlet of a first suspension preheater, a first urea feeding port is arranged at the inlet of the first suspension preheater, and urea can be sprayed into the flue gas of the first suspension preheater through the first urea feeding port to carry out SNCR (selective non-catalytic reduction) denitration; the lower outlet of the suspension preheater I is connected with the middle high-temperature area of the incineration ashing preheating chamber;
An outlet at the upper part of the first suspension preheater is connected with an inlet of a second suspension preheater, a second urea feeding port is arranged at the inlet of the second suspension preheater, and urea can be sprayed into the flue gas of the second suspension preheater through the second urea feeding port to carry out SNCR (selective non-catalytic reduction) denitration; the lower outlet of the suspension preheater II is connected with the inlet of the suspension preheater I;
An outlet at the upper part of the second suspension preheater is connected with an inlet of the third suspension preheater, and an outlet at the lower part of the third suspension preheater is connected with an inlet of the second suspension preheater;
an outlet at the upper part of the suspension preheater III is connected with an inlet of the suspension preheater IV, a feed back feeding point B is arranged at the inlet of the suspension preheater IV, and an outlet at the lower part of the suspension preheater IV is connected with an inlet of the suspension preheater III;
The upper outlet of the suspension preheater IV is connected with the inlet of the suspension preheater V, a low-heat-value dangerous waste feeding point A is arranged at the inlet of the suspension preheater V, low-heat-value dangerous waste containing CaO can be added into the outlet pipeline of the suspension preheater IV through the low-heat-value dangerous waste feeding point A, and the lower outlet of the suspension preheater V is connected with the inlet of the suspension preheater IV through a material returning feeding point B.
5. The high and low calorific value hazardous waste collaborative incineration melting harmless treatment system according to any one of claims 2 to 4, wherein the system further comprises an NH 3 + air injection mixing system, an SCR denitration reactor system, a Venturi fluidization deacidification collaborative cooling system, an activated carbon injection mixing system and a cloth bag dust removal system which are connected in sequence, the NH 3 + air injection mixing system is connected with an outlet of the multistage suspension preheating collaborative deacidification system, an outlet of the Venturi fluidization deacidification collaborative cooling system is further connected with the multistage suspension preheating collaborative deacidification system, and an outlet of the cloth bag dust removal system is further connected with a charging port of the incineration melting furnace;
NH 3 + air sprays the hybrid system and can mix NH 3, air and flue gas even, SCR denitration reactor system can the selective catalytic desorption NOx in the flue gas, acid gas in the flue gas can be got rid of to venturi fluidization deacidification is cooling system in coordination to through deacidification agent evaporation heat absorption with flue gas temperature drop to required temperature, active carbon sprays the hybrid system and can mix active carbon and flue gas even, dust and active carbon particle in the sack dust pelletizing system can get rid of the flue gas.
6. The system for harmlessly treating high and low calorific value hazardous wastes through collaborative incineration and melting according to claim 5, wherein an upper outlet of the suspension preheater V is connected with an inlet of an NH 3 + air injection mixing system.
7. the system for harmlessly treating high and low calorific value hazardous wastes through collaborative incineration and melting according to claim 5, wherein the SCR denitration reactor system comprises a top flue gas inlet and a bottom outlet, an NH 3 + air injection mixing system is arranged at the flue gas inlet of the SCR denitration reactor system, and a three-layer denitration catalyst is placed in the SCR denitration reactor system and used for selectively catalyzing NOx in flue gas to generate N 2 and H 2 O;
the Venturi fluidization deacidification cooperative cooling system comprises a lower inlet, an upper outlet and a bottom outlet, the lower outlet of the SCR denitration reactor system is connected with the lower inlet of the Venturi fluidization deacidification cooperative cooling system, and one or more of Ca (OH) 2 solution, Na 2 CO 3 solution and NaOH solution can be sprayed into the upper part of the Venturi fluidization deacidification cooperative cooling system;
the material at the bottom of the Venturi fluidization deacidification and cooling system is connected with a feed back feeding point B of the suspension preheater IV through a bottom outlet and a feed back conveying pipeline 8;
the upper outlet of the Venturi fluidization deacidification and cooling system is connected with the inlet of an activated carbon jet mixing system, activated carbon particles can be sprayed into the inlet of the cloth bag dust removal system by the activated carbon jet mixing system, the activated carbon and the flue gas are fully mixed through turbulent flow mixing, and the activated carbon jet mixing system is used for adsorbing trace dioxin and volatile organic compounds in the flue gas; and the bottom outlet of the cloth bag dust removal system is connected with a high-heat value dangerous waste charging opening C through a feed back conveying pipeline.
8. the high and low calorific value hazardous waste collaborative incineration melting harmless treatment system according to claim 5, wherein: the outlet of the Venturi fluidization deacidification and cooling system and the pipeline between the multistage suspension preheating and deacidification system are provided with a first outer discharge port, and the outlet of the cloth bag dust removal system and the pipeline between the incineration melting furnace are provided with a second outer discharge port.
9. use of the high and low calorific value hazardous waste collaborative incineration melting innocent treatment system according to any one of claims 1 to 8 in incineration melting innocent treatment of different calorific value hazardous waste separate feed pretreatment.
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