CN116951422A - High-temperature flue gas treatment system of garbage incinerator - Google Patents
High-temperature flue gas treatment system of garbage incinerator Download PDFInfo
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- CN116951422A CN116951422A CN202310802088.8A CN202310802088A CN116951422A CN 116951422 A CN116951422 A CN 116951422A CN 202310802088 A CN202310802088 A CN 202310802088A CN 116951422 A CN116951422 A CN 116951422A
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- flue gas
- cyclone separator
- sorting
- waste heat
- temperature flue
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 152
- 239000003546 flue gas Substances 0.000 title claims abstract description 152
- 239000010813 municipal solid waste Substances 0.000 title claims abstract description 27
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 73
- 238000006243 chemical reaction Methods 0.000 claims abstract description 51
- 239000002918 waste heat Substances 0.000 claims abstract description 41
- 239000002245 particle Substances 0.000 claims abstract description 31
- 238000006298 dechlorination reaction Methods 0.000 claims abstract description 22
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 18
- 239000007787 solid Substances 0.000 claims abstract description 18
- 239000000428 dust Substances 0.000 claims abstract description 15
- 238000000746 purification Methods 0.000 claims abstract description 8
- 239000007921 spray Substances 0.000 claims abstract description 4
- 230000000382 dechlorinating effect Effects 0.000 claims description 63
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 22
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 22
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 22
- 238000012806 monitoring device Methods 0.000 claims description 19
- 239000000920 calcium hydroxide Substances 0.000 claims description 14
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 14
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 14
- 238000005192 partition Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 9
- 238000012544 monitoring process Methods 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 3
- 239000002893 slag Substances 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 230000015572 biosynthetic process Effects 0.000 abstract description 3
- 230000008021 deposition Effects 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 21
- 239000000460 chlorine Substances 0.000 description 12
- 239000000779 smoke Substances 0.000 description 12
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 11
- 229910052801 chlorine Inorganic materials 0.000 description 11
- 238000010438 heat treatment Methods 0.000 description 11
- 239000000463 material Substances 0.000 description 11
- 230000006872 improvement Effects 0.000 description 10
- 238000005260 corrosion Methods 0.000 description 9
- 230000007797 corrosion Effects 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 239000010881 fly ash Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 6
- 239000000843 powder Substances 0.000 description 5
- 239000000292 calcium oxide Substances 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000009825 accumulation Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 3
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000284 extract Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- 230000036632 reaction speed Effects 0.000 description 3
- 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 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 235000019580 granularity Nutrition 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000019635 sulfation Effects 0.000 description 1
- 238000005670 sulfation reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
- B01D53/685—Halogens or halogen compounds by treating the gases with solids
-
- 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
- F23G5/46—Recuperation of heat
-
- 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
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2045—Hydrochloric acid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
- B01D2258/0291—Flue gases from waste incineration plants
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a high-temperature flue gas treatment system of a garbage incinerator, which comprises: the device comprises an incinerator, a waste heat boiler, a deacidification reaction tower, a cyclone separator and a wind sorting device; the incinerator, the cyclone separator, the waste heat boiler and the deacidification reaction tower are sequentially connected, a high-temperature flue gas inlet and a dechlorination agent feeding port are respectively arranged at the side part of the cyclone separator, the wind power sorting device is connected with the bottom of the cyclone separator and is used for sorting solid particles collected at the bottom of the cyclone separator and feeding the dechlorination agent separated from the solid particles into the cyclone separator again; the high-temperature flue gas output by the incinerator firstly enters a cyclone separator for dechlorination and dust removal, then enters a waste heat boiler for waste heat utilization, finally enters a deacidification reaction tower for deacidification reaction with lime hydrate spray, and the deacidified flue gas enters a dust removal system for further purification and then is discharged. The invention has the advantages of compact structure, high dechlorination efficiency, reduced rate of ash deposition and slag formation of the waste heat boiler, contribution to improving the heat exchange efficiency of the boiler, and the like.
Description
Technical Field
The invention belongs to the technical field of flue gas treatment, and particularly relates to a high-temperature flue gas treatment system of a garbage incinerator.
Background
The mechanical grate furnace is suitable for burning various solid fuels and is widely applied to the field of garbage incineration. Because the content of chlorine element in the garbage is higher, hydrogen chloride generated after combustion can contact a heating surface to cause high-temperature chlorine corrosion, and the safety of equipment is endangered. The mechanical grate furnace is limited by the structure, and is difficult to realize efficient dechlorination in the furnace by directly adding an adsorbent such as a dechlorinating agent and the like into the furnace like a circulating fluidized bed, and the heating surface is in contact with hydrogen chloride in high-temperature flue gas, so that high-temperature chlorine corrosion of the heating surface is extremely easy to cause.
In the fuel combustion process, the partially combusted particles enter a waste heat boiler along with the flue gas in the form of fly ash under the carrying of the flue gas, and are adhered to a heating surface to form accumulated ash.
Under the high-temperature environment of the hearth, the chloride with low melting point quickly evaporates to form FeCl 3 Vapor and is easy to combine with H 2 O、SO 2 、SO 3 And the reaction is carried out to generate Fe 2 (SO 4 ) 3 HCl gas. FeCl condensed on water-cooled wall 3 HCl is produced while sulfation is continued, so that the concentration of HCl in the deposition layer is far greater than that in the flue gas, and the oxidation protection film layer on the metal surface is more easily subjected to acid corrosion. Therefore, after the ash is heated, due to the components in the fly ashComplexity also exacerbates the chlorine corrosion of the heated surfaces.
Meanwhile, the traditional urban solid waste incineration treatment system is characterized in that a flue gas purification system is arranged behind a waste heat boiler, and is generally deacidified by a semi-dry method and a dry method, so that the flue gas reaches the environmental emission standard, and the flue gas has a relatively low cost and has the advantage of no waste water generation, thus having a large market share.
The semi-dry method has very fast gas-liquid phase reaction speed between the dechlorinating agent and the pollutant in the fume, and the gas-solid phase reaction is very weak after the moisture in the dechlorinating agent is dried. However, the temperature of the flue gas needs to be maintained above the acid dew point temperature of the flue gas, and the moisture in the dechlorinating agent is rapidly evaporated by the flue gas, so that the duration of the liquid phase of the dechlorinating agent is short, a large amount of dechlorinating agent is not fully reacted, and the dechlorinating agent is wasted. Taking a city garbage incineration power plant in a certain province as an example, the concentration of HCl in the raw flue gas before conversion is about 850mg/Nm 3 、SO 2 The concentration before conversion is about 500mg/Nm 3 The concentration of the HCl before conversion of the clean fume emission index is less than 10mg/Nm 3 、SO 2 The concentration before conversion is about 50mg/Nm 3 . According to the measurement and calculation of production practice data, the utilization rate of the dechlorinating agent (calcium hydroxide emulsion) of the semi-dry deacidification is about 28-38%, and a large amount of dechlorinating agent (slaked lime) is wasted.
For example, chinese patent application CN201911000035.4 discloses an in-furnace dechlorination scheme, in which a replaceable adsorbent filtering layer unit is arranged at a fixed position in front of a horizontal flue in an incinerator to implement flue gas dechlorination. In order to ensure the dechlorination effect, the residence time of the flue gas in the adsorbent filtering layer unit needs to be prolonged. The solution idea of this scheme is that increase filtering layer thickness and unit quantity can lead to flue gas circulation resistance greatly increased. Meanwhile, the filter layer unit of the scheme is designed into a drawer type which can be inserted and taken out, the filter layer unit needs to be pulled out during replacement, high-temperature flue gas can be leaked under the condition that a boiler continuously operates, and the environment pollution risk and the safe operation risk are caused. Therefore, this scheme has difficulty in engineering practical application.
Disclosure of Invention
Aiming at the defects that incineration treatment equipment is easy to suffer from chlorine corrosion and a waste heat boiler is easy to accumulate ash and form slag in the prior art, the invention provides the high-temperature flue gas treatment system of the waste incinerator, which has the advantages of compact structure, high dechlorination efficiency, reduction of the rate of accumulated ash and form slag of the waste heat boiler and contribution to improvement of the heat exchange efficiency of the boiler.
In order to solve the technical problems, the invention adopts the following technical scheme:
a garbage incinerator high temperature flue gas treatment system comprising: the device comprises an incinerator, a waste heat boiler, a deacidification reaction tower, a cyclone separator and a wind sorting device; the incinerator, the cyclone separator, the waste heat boiler and the deacidification reaction tower are sequentially connected, a high-temperature flue gas inlet and a dechlorination agent feeding port are respectively arranged at the side part of the cyclone separator, the wind power sorting device is connected with the bottom of the cyclone separator and is used for sorting solid particles collected at the bottom of the cyclone separator and feeding the dechlorination agent separated from the solid particles into the cyclone separator again; the high-temperature flue gas output by the incinerator firstly enters a cyclone separator for dechlorination and dust removal, then enters a waste heat boiler for waste heat utilization, finally enters a deacidification reaction tower for deacidification reaction with lime hydrate spray, and the deacidified flue gas enters a dust removal system for further purification and then is discharged.
As a further improvement of the invention, the output end of the waste heat boiler is provided with a smoke suction fan, the output end of the smoke suction fan is connected with the wind power sorting device through a connecting pipeline, the smoke suction fan sucks the smoke output by the waste heat boiler, the smoke is conveyed into the wind power sorting device for providing power required by sorting the dechlorinating agent, and the sorted dechlorinating agent is thrown into the cyclone separator again.
As a further improvement of the invention, the pneumatic sorting device comprises a first ejector, a rotary ash discharging valve, a hood, a sorting bin and a partition plate; the top of the sorting bin is connected with the bottom of the cyclone separator through a pipeline with a valve, the bottom of the sorting bin is connected with a connecting pipeline through a pipeline with a valve, a partition plate which is obliquely arranged is arranged in the sorting bin, a plurality of blast caps are arranged on the partition plate, an output pipeline with a first ejector and an output pipeline with a rotary ash discharge valve are respectively arranged on the upper part of the sorting bin, the first ejector is connected with the connecting pipeline, the flue gas conveyed by the connecting pipeline is used for providing jet power, and the output end of the first ejector is connected to the cyclone separator through the pipeline; the flue gas extracted by the flue gas suction fan is conveyed through a connecting pipeline, enters the sorting bin from the bottom of the sorting bin, and is screened by solid particles collected on the sorting partition plate, and sorting is realized by utilizing the density difference of the solid particles; unreacted dechlorinating agent is sprayed into the cyclone separator through the first sprayer, and the reacted dechlorinating agent is discharged through the rotary ash discharge valve.
As a further improvement of the invention, the output end of the flue gas suction fan is also connected with the bottom of the deacidification reaction tower through a connecting pipeline, the flue gas suction fan extracts flue gas output by the waste heat boiler, and the flue gas is conveyed to the bottom of the deacidification reaction tower and is used for conveying dry particles collected at the bottom of the deacidification reaction tower to the wind power separation device so as to separate unreacted slaked lime, and the separated slaked lime is put into the cyclone separator again.
As a further improvement of the invention, the bottom of the deacidification reaction tower is provided with a crusher and a second ejector, the air inlet end of the second ejector is communicated with the output end of the flue gas suction fan through a connecting pipeline, and the dry particles collected by the deacidification reaction tower are conveyed into the crusher to be crushed and then enter the second ejector, and the flue gas conveyed by the flue gas suction fan is blown into the wind power sorting device.
As a further improvement of the invention, a vibrator is arranged at the outer side of the bottom of the sorting bin and is used for vibrating the reacted dechlorinating agent collected on the separation plate and discharging the dechlorinating agent through the rotary ash discharging valve.
As a further improvement of the invention, a first monitoring device is arranged at the inlet of the bottom of the sorting bin so as to monitor the pressure and flow of the flue gas entering the sorting bin.
As a further improvement of the invention, a double-layer flap valve is arranged at the top of the sorting bin, and a gate valve is arranged on a pipeline connected with the bottom of the cyclone separator.
As a further improvement of the invention, the inlet and the outlet of the cyclone separator are respectively provided with a second monitoring device and a third monitoring device, the second monitoring device is used for monitoring the temperature of the high-temperature flue gas entering the cyclone separator and the concentration of hydrogen chloride, and the third monitoring device is used for monitoring the temperature of the flue gas output by the cyclone separator and the concentration of hydrogen chloride.
As a further improvement of the invention, the contact reaction time of the high-temperature flue gas and the dechlorinating agent in the cyclone separator is more than 5s.
Compared with the prior art, the invention has the advantages that:
1. according to the high-temperature flue gas treatment system of the garbage incinerator, the cyclone separator is arranged between the incinerator and the waste heat boiler to treat the high-temperature flue gas, so that particle impurities carried in the high-temperature flue gas are removed, dechlorination reaction is carried out on the high-temperature flue gas by using the dechlorinating agent, the chlorine content in the high-temperature flue gas is reduced, the fly ash content in the flue gas entering the waste heat boiler is reduced, the accumulated ash of a heating surface in the waste heat boiler is reduced, and the problem of ash hardening of the heating area of the waste heat boiler is solved from the source; in the cooling process of the flue gas after dechlorination and dust removal in the waste heat boiler, as chlorine elements in the flue gas are greatly reduced, particulates are reduced, the Cl source and the catalyst amount for secondary synthesis of dioxin are blocked, the secondary synthesis amount of dioxin in the flue gas is greatly reduced, and the risk of chlorine corrosion of the waste heat boiler is reduced. Meanwhile, the wind force sorting device is arranged at the bottom of the cyclone separator, solid particles collected at the bottom of the cyclone separator are screened, and the dechlorinating agent separated from the solid particles is thrown into the cyclone separator again, so that the utilization rate of dechlorinating agent materials is improved.
2. According to the high-temperature flue gas treatment system for the garbage incinerator, the power for recycling the dechlorinating agent material is derived from the flue gas suction fan, the system resistance is small, the suction air temperature is high, the temperature is generally about 200 ℃, and the risks of material blockage and hardening are low. Meanwhile, exhaust-heat boiler smoke is adopted as dechlorinating agent material conveying power, smoke discharging loss of the exhaust-heat boiler is not additionally increased, the influence on the economical efficiency of an incinerator system is small, and meanwhile, in the operation process, the risk of leakage of high-temperature smoke is avoided, and the operation is safe and reliable.
3. According to the high-temperature flue gas treatment system of the garbage incinerator, the wind force sorting device adopting the pneumatic sorting principle is arranged, the partition plates are properly and obliquely arranged, the plurality of wind caps are arranged on the partition plates, flue gas with certain wind pressure provided by the flue gas suction fan is used as sorting power, solid particles discharged from the inside of the cyclone separator are screened by utilizing different densities and different granularities, so that separation of CaSO4, caCl2 and CaO is realized, the top of the wind force sorting device is connected with the inlet of the cyclone separator, and flue gas blown into the sorting device and the screened dechlorinating agent reenter the cyclone separator for separation, so that the concentration of the dechlorinating agent is increased, and the hydrogen chloride removal efficiency is improved.
4. According to the high-temperature flue gas treatment system of the garbage incinerator, the on-line monitoring devices are arranged at the inlet and the outlet of the cyclone separator, the temperature of inlet and outlet flue gas and the hydrogen chloride concentration index are obtained in real time, the dosage of the added dechlorinating agent is regulated and controlled according to data feedback, and the chlorine content of the flue gas is accurately controlled. The dechlorination reaction efficiency is improved by controlling the temperature of the flue gas in the cyclone separator.
5. According to the high-temperature flue gas treatment system of the garbage incinerator, the flue gas subjected to dechlorination enters the waste heat boiler to exchange heat, then the lime slurry sprayed by atomization is utilized in the deacidification reaction tower to carry out semi-dry deacidification, and the dry slaked lime powder which is not fully utilized after deacidification is conveyed into the cyclone separator by virtue of pneumatic conveying to be secondarily utilized, so that the effective utilization rate of materials is improved, and the system operation cost is reduced by changing phases.
Drawings
Fig. 1 is a schematic diagram of the structure principle of the high-temperature flue gas treatment system of the garbage incinerator.
Fig. 2 is a schematic diagram of the structural principle of the wind power sorting device in the high-temperature flue gas treatment system of the garbage incinerator.
Fig. 3 is a schematic diagram of the principle of the high-temperature flue gas and dechlorinating agent entering and exiting the cyclone separator in the high-temperature flue gas treatment system of the garbage incinerator.
Legend description: 1. an incinerator; 2. a waste heat boiler; 3. deacidifying reaction tower; 4. a cyclone separator; 5. a gate valve; 6. a wind power sorting device; 61. a first injector; 62. rotating an ash discharge valve; 63. an air quantity adjusting valve; 64. a first monitoring device; 65. a vibrator; 66. double-layer flap valve; 67. a hood; 68; sorting bin; 69. a partition plate; 7. a slag extractor; 8. a second monitoring device; 9. a third monitoring device; 10. a smoke suction fan; 11. a crusher; 12. a second ejector; 13. a connecting pipe; 14. and a heating surface.
Detailed Description
The invention is further described below in connection with the drawings and the specific preferred embodiments, but the scope of protection of the invention is not limited thereby.
Examples
As shown in fig. 1 to 3, the high-temperature flue gas treatment system of the garbage incinerator of the present invention comprises: an incinerator 1, a waste heat boiler 2, a deacidification reaction tower 3, a cyclone separator 4 and a wind power sorting device 6. The incinerator 1, the cyclone separator 4, the waste heat boiler 2 and the deacidification reaction tower 3 are sequentially connected, a high-temperature flue gas inlet and a dechlorinating agent feeding port are respectively arranged on the side part of the cyclone separator 4, the wind power sorting device 6 is connected with the bottom of the cyclone separator 4 and is used for sorting solid particles collected at the bottom of the cyclone separator 4 and feeding the dechlorinating agent separated from the solid particles into the cyclone separator 4 again. The high-temperature flue gas output by the incinerator 1 firstly enters a cyclone separator 4 for dechlorination and dust removal, then enters a waste heat boiler 2 for waste heat utilization, finally enters a deacidification reaction tower 3 for deacidification reaction with lime hydrate spray, and the deacidified flue gas enters a dust removal system for further purification and is discharged. The small-particle dechlorinating agent active part with small density and large specific surface area is separated by the wind power separation device and is connected to the feeding port of the dechlorinating agent circulating system on the cyclone separator 4, and is conveyed into the cyclone separator 4 by the wind power conveying system for recycling, so that the concentration of the dechlorinating agent is increased, and the hydrogen chloride removal efficiency is improved.
The flue gas in the combustion chamber of the incinerator enters the cyclone separator 4, the flue gas enters along the tangential direction of the cyclone separator 4, moves downwards in the cyclone separator 4 along the tangential direction, and the dechlorinating agent powder is sprayed into the cyclone separator 4 in the direction opposite to the flue gas cyclone flow and is fully mixed with the flue gas. The flue gas is mixed with dechlorinating agent in cyclone 4, reacted, adsorbed, solidified and stripped of hydrogen chloride component. The ash components after adsorption are dechlorinating agent, calcium chloride and a small amount of calcium sulfite, flow along with the flue gas and fall into an ash bucket under the action of centrifugal force and gravity. HCl and particulate matters in the flue gas are removed in front of the furnace, so that the use amount of a deacidification agent of a flue gas purification system behind the furnace is reduced, the production amount of hazardous waste (fly ash) can be reduced, and the method has important significance for reducing environmental risks.
The cyclone separator 4 has a cylindrical structure at the upper part and an inverted cone structure at the lower part. The flue gas enters tangentially from the side surface of the cyclone separator 4, flows downwards in the tangential direction and the axial direction in the cyclone separator 4, and the carried fly ash particles and the sprayed dechlorinating agent powder are thrown to the periphery of the separator under the action of the centrifugal force of the flue gas cyclone, and fall into a lower ash bucket under the action of gravity.
It can be understood that the dechlorinating agent can be calcium oxide/calcium hydroxide powder, the reaction speed of the dechlorinating agent and HCl in the flue gas is related to the concentration of HCl in the flue gas, the concentration of HCl is different, the reaction speed is different, and in order to realize the full utilization of the dechlorinating agent, a set of wind power separation device 6 is arranged outside the cyclone separator 4 so as to realize the cyclic utilization of the dechlorinating agent. The circulation rate of the dechlorinating agent is not preferably lower than 6 so as to ensure that the dechlorinating agent is fully utilized.
As shown in fig. 3, two cyclones 4 may be provided, arranged at the side of the incinerator 1. The high-temperature flue gas treatment system of the embodiment is also suitable for the transformation of various mechanical grate furnaces. The cyclone separator 4 can remove large-particle fly ash in the flue gas in advance in a cyclone dust removing mode, so that the rate of dust accumulation and slag bonding of the waste heat boiler 2 is greatly reduced, the heat resistance of the dust accumulation and slag bonding of the waste heat boiler 2 is reduced while chlorine corrosion is slowed down, and the heat exchange efficiency of the waste heat boiler 2 is indirectly improved. The mixture of the dechlorinating agent particles, the deacidification reaction products and the fly ash collected at the bottom of the cyclone separator 4 is separated by the wind power separation device 6, wherein the fine particle part contains a large amount of unreacted dechlorinating agent particles, has larger specific surface area and higher reactivity, and is recycled and sprayed into the cyclone separator 4 again for recycling, so that the reaction time of the dechlorinating agent is prolonged, and the efficient utilization of the dechlorinating agent is realized.
As shown in fig. 1, in this embodiment, a flue gas suction fan 10 is disposed at the output end of the exhaust-heat boiler 2, the output end of the flue gas suction fan 10 is connected with the wind-force sorting device 6 through a connecting pipe 13, the flue gas suction fan 10 extracts flue gas output by the exhaust-heat boiler 2, and the flue gas is conveyed into the wind-force sorting device 6 for providing power required for sorting dechlorinating agents, and the sorted dechlorinating agents are thrown into the cyclone separator 4 again. The flue gas suction fan 10 is controlled by adopting variable frequency control or baffle control and is used for adjusting the flue gas amount so as to adjust the reaction temperature in the cyclone separator 4.
As shown in fig. 2, the pneumatic sorting apparatus 6 includes a first ejector 61, a rotary ash valve 62, a hood 67, a sorting bin 68, and a partition plate 69. The top of the sorting bin 68 is connected with the bottom of the cyclone 4 through a pipeline with a valve, the bottom of the sorting bin 68 is connected with the connecting pipeline 13 through a pipeline with a valve, a partition plate 69 which is obliquely arranged is arranged in the sorting bin 68, a plurality of wind caps 67 are arranged on the partition plate 69, an output pipeline with a first ejector 61 and an output pipeline with a rotary ash discharging valve 62 are respectively arranged on the upper part of the sorting bin 68, the first ejector 61 is connected with the connecting pipeline 13, the flue gas conveyed by the connecting pipeline 13 is utilized to provide jet power, and the output end of the first ejector 61 is connected to the cyclone 4 through a pipeline. The flue gas extracted by the flue gas suction fan 10 is conveyed through the connecting pipeline 13, enters the sorting bin 68 from the bottom of the sorting bin 68, and is screened by the solid particles collected on the separating plate 69, and sorting is realized by utilizing the density difference of the solid particles. Unreacted dechlorinating agent is sprayed into the cyclone 4 through the first sprayer 61, and the reacted dechlorinating agent is discharged through the rotary dust discharging valve 62. The first injector 61 may be a venturi injector in particular.
In this embodiment, the flue gas for transporting the dechlorinating agent is extracted from the exhaust flue at the outlet of the exhaust-heat boiler 2, and the heat loss of the exhaust gas of the boiler can be reduced by using the flue gas transport of the exhaust-heat boiler. Meanwhile, in the pneumatic conveying process, the antichlor which is not fully reacted can react with acid gas in the sucked flue gas, so that the contact time of the antichlor and the flue gas is prolonged, and the aim of efficiently utilizing the antichlor is fulfilled.
As shown in fig. 1, in this embodiment, the output end of the flue gas suction fan 10 is further connected to the bottom of the deacidification reaction tower 3 through a connecting pipe 13, the flue gas suction fan 10 extracts the flue gas output by the waste heat boiler 2, and the flue gas is conveyed to the bottom of the deacidification reaction tower 3, so as to convey the dry particulate matters collected at the bottom of the deacidification reaction tower 3 to the wind-force separation device 6, so as to separate out unreacted slaked lime, and the separated slaked lime is thrown into the cyclone separator 4 again.
The main components of the dry particles after deacidification in the deacidification reaction tower 3 are unreacted slaked lime, and the products after adsorption reaction, such as calcium chloride, calcium sulfite, calcium sulfate, part of fly ash carried in the flue gas, and the like. As shown in fig. 1, in this embodiment, a crusher 11 and a second ejector 12 are disposed at the bottom of the deacidification reaction tower 3, an air inlet end of the second ejector 12 is communicated with an output end of the flue gas suction fan 10 through a connecting pipeline 13, and dry particulate matters collected by the deacidification reaction tower 3 are conveyed into the crusher 11 to be crushed and then enter the second ejector 12, and flue gas conveyed by the flue gas suction fan 10 is blown into the wind-force sorting device 6. The second injector 12 may specifically employ a venturi injection device.
In this embodiment, a smoke suction fan 10 is disposed at the output end of the exhaust-heat boiler 2, and a small amount of smoke is sucked from the outlet of the exhaust-heat boiler 2. The outlet pipeline of the fan is divided into two paths, and venturi tubes are arranged on the outlet pipeline of the fan and are used for sucking and blowing solid powder falling from the bottom of the deacidification reaction tower 3 and the bottom of the cyclone separator 4 through the wind power separation device 6. One path of the mixed particles passes through the bottom of the deacidification reaction tower 3, and the mixed particles are conveyed to a sorting device at the bottom of the cyclone separator 4 after the deacidification falling from the bottom of the deacidification reaction tower 3 for screening. The other path is connected with a wind force sorting device 6 at the bottom of the cyclone separator 4, and the recycled materials (dechlorinating agent and deacidified mixture of the reaction tower) screened out by the wind force sorting device 6 are conveyed to a feed inlet of the cyclone separator 4.
In the present embodiment, as shown in fig. 2, a vibrator 65 is provided at the outer side of the bottom of the sorting bin 68, and the vibrator 65 is used to vibrate the reacted dechlorinating agent collected on the partition plate 69 and discharge the dechlorinating agent through the rotary ash valve 62. In this embodiment, the solid waste discharged through the rotary ash discharge valve 62, which has no recycling value, finally enters the slag extractor 7.
As shown in FIG. 2, in this embodiment, the bottom of the sorting bin 68A first monitoring device 64 is arranged at the inlet of the part to monitor the pressure and flow of the flue gas entering the sorting bin 68 so as to ensure that the materials in the sorting bin 68 are in a micro-boiling state, thereby facilitating the unreacted slaked lime and CaSO generated by the reaction 4 、CaCl 2 Sieving.
In the present embodiment, as shown in fig. 2, a double-layer flap valve 66 is arranged at the top of the sorting bin 68, and a gate valve 5 is arranged on a pipeline connecting the double-layer flap valve 66 with the bottom of the cyclone separator 4.
In this embodiment, as shown in fig. 1, the inlet and outlet of the cyclone separator 4 are respectively provided with a second monitoring device 8 and a third monitoring device 9, the second monitoring device 8 is used for monitoring the temperature of the flue gas entering the cyclone separator 4 and the concentration of hydrogen chloride, and the third monitoring device 9 is used for monitoring the temperature of the flue gas and the concentration of hydrogen chloride output by the cyclone separator 4.
The dechlorinating agent used in the embodiment is calcium oxide/calcium hydroxide, and the deacidifying agent of the flue gas purifying system is calcium hydroxide. The calcium oxide is utilized to have the characteristic of higher dechlorination efficiency at 600-800 ℃. Further, the highest efficient temperature range of dechlorination is 600-700 ℃. To ensure that the dechlorinating agent reaction temperature is acceptable, a suitable heating surface 14 can be arranged in front of the cyclone 4 to reduce the flue gas temperature and ensure that the flue gas temperature entering the cyclone 4 is in a high-efficiency reaction zone. Meanwhile, an insulating layer (namely refractory lining material) is arranged in the cyclone separator 4 to ensure that the temperature in the cyclone separator 4 is qualified. The temperature in the cyclone 4 can be suitably adjusted by the flow of flue gas for transporting the dechlorinating agent material.
In this embodiment, in order to fully react HCl gas in the flue gas with the dechlorinating agent, the time for the contact reaction between the high-temperature flue gas and the dechlorinating agent in the cyclone 4 should be greater than 5s. It is therefore necessary to design the cyclone separator specifically according to the design parameters of the incinerator. Taking an incinerator for daily treatment of household garbage 850t/D as an example, the flue gas flow rate is designed to be D y ＝159kNm 3 And/h. The flow rate of the flue gas under the working condition of 800 ℃ is about D y ’ ＝159×(273+800)/(273+20)＝587.7m 3 And/h. The converted smoke flow is about d y ’ ＝163.15m 3 /h。In order to achieve the aim of 5 seconds of the flue gas staying in the cyclone separator, the diameter and the height of the cyclone separator are required. Meanwhile, in order to realize smooth outflow of the deposited ash at the bottom of the cyclone separator, the deposited ash is prevented from bridging and blocking, and the angle between the cone line and the horizontal plane is not too small (more than 70 degrees).
In the embodiment, the deacidification and dust removal system behind the combustion chamber and in front of the waste heat boiler is provided, and in the flue gas purification system behind the waste heat boiler, the deacidification agent materials which are not fully utilized in the semi-dry deacidification process are recycled, so that the problems of blockage of a through flow channel between heating surface tube panels, low utilization rate of the flue gas purification semi-dry deacidification agent materials and the like caused by high-temperature corrosion (chlorine corrosion) of a heating surface and ash accumulation hardening of the heating surface are solved.
While the invention has been described with reference to preferred embodiments, it is not intended to be limiting. Any person skilled in the art can make many possible variations and modifications to the technical solution of the present invention or equivalent embodiments using the method and technical solution disclosed above without departing from the spirit and technical solution of the present invention. Therefore, any simple modification, equivalent substitution, equivalent variation and modification of the above embodiments according to the technical substance of the present invention, which do not depart from the technical solution of the present invention, still fall within the scope of the technical solution of the present invention.
Claims (10)
1. A high temperature flue gas treatment system for a waste incinerator, comprising: an incinerator (1), a waste heat boiler (2), a deacidification reaction tower (3), a cyclone separator (4) and a wind sorting device (6); the incinerator (1), the cyclone separator (4), the waste heat boiler (2) and the deacidification reaction tower (3) are sequentially connected, a high-temperature flue gas inlet and a dechlorination agent feeding port are respectively arranged on the side part of the cyclone separator (4), and the wind force sorting device (6) is connected with the bottom of the cyclone separator (4) and is used for sorting solid particles collected at the bottom of the cyclone separator (4) and feeding dechlorination agents separated from the solid particles into the cyclone separator (4) again; the high-temperature flue gas output by the incinerator (1) firstly enters a cyclone separator (4) for dechlorination and dust removal, then enters a waste heat boiler (2) for waste heat utilization, finally enters a deacidification reaction tower (3) for deacidification reaction with lime hydrate spray, and the deacidified flue gas enters a dust removal system for further purification and then is discharged.
2. The high-temperature flue gas treatment system of the garbage incinerator according to claim 1, wherein the output end of the waste heat boiler (2) is provided with a flue gas suction fan (10), the output end of the flue gas suction fan (10) is connected with a wind power sorting device (6) through a connecting pipeline (13), the flue gas suction fan (10) sucks the flue gas output by the waste heat boiler (2), and the flue gas is conveyed into the wind power sorting device (6) for providing power required by sorting dechlorinating agents and putting the sorted dechlorinating agents into the cyclone separator (4) again.
3. The high-temperature flue gas treatment system of a garbage incinerator according to claim 2, wherein the wind sorting device (6) comprises a first ejector (61), a rotary dust discharging valve (62), a hood (67), a sorting bin (68) and a partition plate (69); the top of the sorting bin (68) is connected with the bottom of the cyclone separator (4) through a pipeline with a valve, the bottom of the sorting bin (68) is connected with a connecting pipeline (13) through a pipeline with a valve, a partition plate (69) which is obliquely arranged is arranged in the sorting bin (68), a plurality of wind caps (67) are arranged on the partition plate (69), an output pipeline with a first ejector (61) and an output pipeline with a rotary ash discharging valve (62) are respectively arranged on the sorting bin (68), the first ejector (61) is connected with the connecting pipeline (13), the flue gas conveyed by the connecting pipeline (13) is used for providing jet power, and the output end of the first ejector (61) is connected to the cyclone separator (4) through the pipeline; the flue gas extracted by the flue gas suction fan (10) is conveyed through a connecting pipeline (13), enters the sorting bin (68) from the bottom of the sorting bin (68), and is screened by solid particles collected on the separating plate (69), and sorting is realized by utilizing the density difference of the solid particles; unreacted dechlorinating agent is sprayed into the cyclone separator (4) through the first sprayer (61), and the dechlorinating agent after reaction is discharged through the rotary ash discharging valve (62).
4. The high-temperature flue gas treatment system of the garbage incinerator according to claim 3, wherein the output end of the flue gas suction fan (10) is further connected with the bottom of the deacidification reaction tower (3) through a connecting pipeline (13), the flue gas output by the waste heat boiler (2) is pumped by the flue gas suction fan (10), and is conveyed to the bottom of the deacidification reaction tower (3) for conveying dry particles collected at the bottom of the deacidification reaction tower (3) to the wind power sorting device (6) so as to sort out unreacted slaked lime, and the separated slaked lime is thrown into the cyclone separator (4) again.
5. The high-temperature flue gas treatment system of the garbage incinerator according to claim 4, wherein a crusher (11) and a second ejector (12) are arranged at the bottom of the deacidification reaction tower (3), an air inlet end of the second ejector (12) is communicated with an output end of a flue gas suction fan (10) through a connecting pipeline (13), and dry particles collected by the deacidification reaction tower (3) are conveyed into the crusher (11) to be crushed and then enter the second ejector (12), and flue gas conveyed by the flue gas suction fan (10) is blown into a wind-force sorting device (6).
6. The high-temperature flue gas treatment system of a garbage incinerator according to any one of claims 3 to 5, wherein a vibrator (65) is arranged on the outer side of the bottom of the sorting bin (68), and the vibrator (65) is used for realizing vibration of the reacted dechlorinating agent collected on a separation plate (69) and is discharged through a rotary ash discharge valve (62).
7. A high temperature flue gas treatment system for a waste incinerator according to any one of claims 3 to 5, wherein a first monitoring device (64) is provided at the inlet at the bottom of the silo (68) to monitor the pressure and flow of flue gas into the silo (68).
8. The high-temperature flue gas treatment system of a garbage incinerator according to any one of claims 3 to 5, wherein a double-layer flap valve (66) is arranged at the top of the sorting bin (68), and a gate valve (5) is arranged on a pipeline connected with the bottom of the cyclone separator (4) through the double-layer flap valve (66).
9. The high-temperature flue gas treatment system of a garbage incinerator according to any one of claims 1 to 5, wherein a second monitoring device (8) and a third monitoring device (9) are respectively arranged at the inlet and the outlet of the cyclone separator (4), the second monitoring device (8) is used for monitoring the temperature of the high-temperature flue gas entering the cyclone separator (4) and the concentration of hydrogen chloride, and the third monitoring device (9) is used for monitoring the temperature of the flue gas and the concentration of the hydrogen chloride output by the cyclone separator (4).
10. The high-temperature flue gas treatment system of a garbage incinerator according to any one of claims 1 to 5, wherein the time for the contact reaction of the high-temperature flue gas and the dechlorinating agent in the cyclone separator (4) is more than 5s.
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