CN113587104B - Waste pyrolysis waste gas purification system and process - Google Patents
Waste pyrolysis waste gas purification system and process Download PDFInfo
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- CN113587104B CN113587104B CN202110939473.8A CN202110939473A CN113587104B CN 113587104 B CN113587104 B CN 113587104B CN 202110939473 A CN202110939473 A CN 202110939473A CN 113587104 B CN113587104 B CN 113587104B
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- 239000002912 waste gas Substances 0.000 title claims abstract description 29
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 27
- 238000000746 purification Methods 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 20
- 230000008569 process Effects 0.000 title claims abstract description 12
- 239000002699 waste material Substances 0.000 title claims description 29
- 239000007789 gas Substances 0.000 claims abstract description 237
- 238000002485 combustion reaction Methods 0.000 claims abstract description 106
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 100
- 239000003546 flue gas Substances 0.000 claims abstract description 99
- 230000003197 catalytic effect Effects 0.000 claims abstract description 69
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 61
- 239000000428 dust Substances 0.000 claims abstract description 61
- 238000006298 dechlorination reaction Methods 0.000 claims abstract description 48
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 40
- 230000023556 desulfurization Effects 0.000 claims abstract description 40
- 238000001179 sorption measurement Methods 0.000 claims abstract description 34
- 239000002131 composite material Substances 0.000 claims abstract description 26
- 229910052799 carbon Inorganic materials 0.000 claims description 45
- 239000003054 catalyst Substances 0.000 claims description 34
- 238000001816 cooling Methods 0.000 claims description 28
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 20
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 20
- 239000000460 chlorine Substances 0.000 claims description 20
- 229910052801 chlorine Inorganic materials 0.000 claims description 20
- 239000011593 sulfur Substances 0.000 claims description 20
- 229910052717 sulfur Inorganic materials 0.000 claims description 20
- 239000000463 material Substances 0.000 claims description 13
- 150000001875 compounds Chemical class 0.000 claims description 7
- -1 particulate matters Substances 0.000 abstract description 18
- 239000003344 environmental pollutant Substances 0.000 abstract description 7
- 231100000719 pollutant Toxicity 0.000 abstract description 7
- 230000007613 environmental effect Effects 0.000 abstract description 5
- 239000000779 smoke Substances 0.000 abstract description 4
- 239000000567 combustion gas Substances 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 238000007084 catalytic combustion reaction Methods 0.000 abstract description 2
- 239000002085 irritant Substances 0.000 abstract description 2
- 231100000021 irritant Toxicity 0.000 abstract description 2
- 239000012495 reaction gas Substances 0.000 abstract description 2
- 239000002918 waste heat Substances 0.000 abstract description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract 1
- 239000003795 chemical substances by application Substances 0.000 description 58
- 229910002651 NO3 Inorganic materials 0.000 description 34
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 34
- 238000001035 drying Methods 0.000 description 31
- 239000011259 mixed solution Substances 0.000 description 30
- 239000000203 mixture Substances 0.000 description 30
- 230000003009 desulfurizing effect Effects 0.000 description 29
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 26
- 239000000292 calcium oxide Substances 0.000 description 26
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 26
- 239000012752 auxiliary agent Substances 0.000 description 25
- 230000000382 dechlorinating effect Effects 0.000 description 25
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 23
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 22
- 150000003057 platinum Chemical class 0.000 description 22
- 238000003756 stirring Methods 0.000 description 21
- 238000000227 grinding Methods 0.000 description 19
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 19
- 239000000243 solution Substances 0.000 description 19
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 18
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 16
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical group [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 16
- 239000000395 magnesium oxide Substances 0.000 description 14
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 14
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 14
- 229910052751 metal Inorganic materials 0.000 description 13
- 239000002184 metal Substances 0.000 description 13
- 229910000019 calcium carbonate Inorganic materials 0.000 description 12
- 239000004568 cement Substances 0.000 description 12
- 238000005507 spraying Methods 0.000 description 12
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 11
- 238000002156 mixing Methods 0.000 description 11
- 239000002808 molecular sieve Substances 0.000 description 11
- 239000002893 slag Substances 0.000 description 11
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 11
- 239000007921 spray Substances 0.000 description 11
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 10
- 239000002245 particle Substances 0.000 description 9
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 8
- 239000003463 adsorbent Substances 0.000 description 8
- 239000012298 atmosphere Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 description 7
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 7
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 description 7
- 229910017604 nitric acid Inorganic materials 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 7
- 238000007789 sealing Methods 0.000 description 7
- 238000007873 sieving Methods 0.000 description 7
- 239000004698 Polyethylene Substances 0.000 description 6
- 239000008367 deionised water Substances 0.000 description 6
- 229910021641 deionized water Inorganic materials 0.000 description 6
- 238000011049 filling Methods 0.000 description 6
- 238000001914 filtration Methods 0.000 description 6
- 238000005470 impregnation Methods 0.000 description 6
- 229920000573 polyethylene Polymers 0.000 description 6
- 238000004056 waste incineration Methods 0.000 description 6
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 5
- 239000010881 fly ash Substances 0.000 description 5
- 238000011068 loading method Methods 0.000 description 5
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 4
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 229910004298 SiO 2 Inorganic materials 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000009264 composting Methods 0.000 description 3
- 238000000465 moulding Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005202 decontamination Methods 0.000 description 2
- 230000003588 decontaminative effect Effects 0.000 description 2
- 239000010791 domestic waste Substances 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000003980 solgel method Methods 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000001027 hydrothermal synthesis Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000003911 water pollution Methods 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
- F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
-
- 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
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- 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
- F23J15/027—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 cyclone separators
-
- 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
- F23J2215/20—Sulfur; 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
- F23J2217/40—Intercepting solids by cyclones
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/30—Sorption devices using carbon, e.g. coke
Abstract
The invention discloses a waste gas purification system and a waste gas purification process by pyrolysis of garbage, wherein the system comprises a garbage combustion chamber, a heat exchanger I, a cyclone dust collector, an electric collection dust removal composite tar removal device, an activated carbon adsorption tower, a dry desulfurization reactor, a dry dechlorination reactor, a catalytic combustor, a chimney, a heat exchanger II and a heat exchanger III; the process comprises the steps of preliminary purification of flue gas, heat exchange and temperature rise, combustion purification, heat exchange and temperature reduction and combustion air heating. The flue gas generated by the pyrolysis of the garbage is subjected to multiple heat exchange with dechlorination reaction gas, catalytic combustion gas and air through the heat exchanger, so that the waste heat in different waste gases can be fully utilized, and the air is heated to a certain temperature and then enters the garbage combustion chamber to carry out pyrolysis treatment on the garbage, thereby achieving the purposes of environmental protection and energy saving; the invention can effectively remove pollutants such as particulate matters, smoke dust, dioxin, tar and SO in the garbage combustion flue gas 2 HCl, other irritant gases and the like, and the treated tail gas can reach the discharge standard.
Description
Technical Field
The invention belongs to the technical field of waste pyrolysis waste gas purification treatment, and particularly relates to a waste pyrolysis waste gas purification system and process.
Background
The rapid development of urbanization wastes resources to promote economy, and more cities have the dilemma of garbage surrounding cities. The great amount of solid waste produced in daily life of city brings great pressure to environment, and the urban waste produces great amount of harmful components during collecting, transporting and treating, so as to pollute atmosphere, soil, water source, etc. and is one of the great environmental problems faced in China. At present, the domestic municipal solid waste treatment mainly comprises three technologies of landfill, composting and incineration. The landfill technology occupies land, landfill leachate can cause serious water pollution, but the composting treatment method mainly comprises mixing and collecting urban garbage in China at present, so that the garbage is wide in source, complex and changeable in components, and a large amount of components which cannot be fermented and degraded exist in the garbage, so that the composting fermentation is incomplete, and the problem of secondary pollution is easy to generate.
In the urban garbage treatment technology at the present stage, incineration is used as a technology with lower cost, better effect and higher benefit, but the combined heat and power investment of the garbage incineration is large, the requirement on equipment process management is higher, and the conventional garbage incineration is mainly used for urban large-scale garbage treatment (daily treatment capacity is more than 50 tons). And the remote rural town garbage production amount is small, the garbage station dispersion range is wide, and the requirement of garbage incineration on the scale cannot be met. The garbage pyrolysis technology can stably treat garbage under the condition of relatively low temperature without adding extra fuel, has small investment on single equipment, is relatively suitable for daily treatment of domestic garbage with the daily treatment capacity of 5-20 tons, and has obvious advantages in rural town garbage treatment. However, some technology still exists in garbage pyrolysis facilities Defects, thereby generating a great amount of smoke, dust, cancerogenic substances dioxin and harmful gases such as CO and SO in the garbage incineration process 2 、NO X The HCL, benzene compounds and the like are harmful to human health and influence the atmospheric environment of towns and villages.
The following patents exist for the waste incineration flue gas purification treatment technology known from patent search:
patent 1: application number CN201821882519.7, which discloses a municipal solid waste combustion flue gas purification system comprising a flue gas purification device and an adsorbent regeneration device, wherein: the flue gas purifying device comprises a cooling device, a fly ash spraying and decontaminating device, a calcium-spraying-based adsorbent desulfurizing device, an activated carbon spraying and decontaminating device, an induced draft fan and a bag-type dust remover which are connected in sequence; the adsorbent regeneration equipment comprises a recovery device, a regeneration device and a spraying treatment liquid decontamination device which are connected in sequence. The patent can effectively remove pollutants in the flue gas through the flue gas purifying equipment, wherein fly ash trapped in the bag-type dust remover is used as a first-step adsorbent, and the reutilization of wastes is realized while the pollutants are adsorbed; in addition, the patent is also provided with catalyst regeneration equipment, and the pollutants on the deactivated adsorbent are subjected to desorption reaction by heating to form regenerated adsorbent, and the regenerated adsorbent is sent into the spray fly ash decontamination device for recycling, so that the production cost can be effectively reduced.
Patent 2: the application number CN201920129294.6 provides a garbage combustion flue gas filtering device, which comprises a spray tower, wherein a filter cylinder which is horizontally arranged and cylindrical is rotationally connected at the middle position inside the spray tower, and a plurality of filtering holes are uniformly formed in the circumferential side wall of the filter cylinder; both ends of the filter cartridge are open, and both ends of the filter cartridge are rotationally connected to the side walls at both sides of the spray tower through bearings; the filter cartridge is driven to rotate by a driving mechanism; a cleaning component for cleaning the outer side wall of the filter cylinder is also arranged in the spray tower; the inner upper part of the spray pipe is fixedly connected with a horizontally arranged spray pipe, wherein the lower part of the spray pipe is provided with a plurality of spray heads facing the filter cartridge; wherein the spray pipe is communicated with a water outlet end of a water pump fixedly arranged on the outer wall of the spray tower through a water guide pipe; this patent is good to the filter effect of rubbish burning flue gas, can clean the cartridge filter moreover to reduce the probability that the cartridge filter blockked up.
Patent 3: application number CN202010828280.0, this patent discloses a method for treating domestic waste and waste gas by low-temperature pyrolysis, which comprises the following steps: step 1, inputting waste gas into a spraying device, spraying the waste gas by using a spraying liquid to remove part of smoke dust and tar substances and part of SO (sulfur dioxide) 2 、NO x HF, HCl, heavy metals and dioxins and water-soluble contaminants; step 2, the waste gas treated by the spraying device in the step 1 is treated by a filtering and purifying device, and the waste gas in the filtering and purifying device sequentially passes through a defogging layer, a composite adsorbing material layer, a biological composite material layer and an adsorbing layer to remove residual pollutants; and 3, carrying out on-line monitoring on the gas treated by the filtering and purifying device, and discharging after the gas reaches the standard. The waste gas of the patent application is monitored by an on-line monitoring system after being treated by a spraying device and a filtering and purifying device, and meets the domestic garbage incineration pollution control standard and meets the standard for emission.
According to the above three purification patent technologies for the garbage combustion flue gas, it can be found that the designed system or method involves a spraying device, and the spraying device is used for cleaning the flue gas in garbage incineration to remove acid gas or other water-soluble organic pollutants, wherein the spraying liquid is an alkaline solution, acid-alkali liquid wastewater is easy to generate after the flue gas is treated, the subsequent treatment process is complex, and secondary pollution is easy to generate. In addition, the heat value in the flue gas cannot be effectively utilized, the temperature of the flue gas discharged after treatment is high, and the environment-friendly requirement is difficult to achieve. According to the control requirements on the discharge of waste incineration flue gas in the domestic waste incineration pollution control standard (GB 18485-2014), and the formal implementation of the new revised 'national solid waste pollution environmental control method' of the people's republic of China' 9/1/2020, the waste incineration facility must be provided with a flue gas treatment facility to ensure that various pollutants in the waste incineration flue gas reach the standard and discharge, prevent heavy metals, organic pollutants and the like from being discharged into an environmental medium, and simultaneously achieve the aim of recycling waste and create additional economic value if the heat and waste gas generated by the waste incineration are recovered. Therefore, it is very necessary to develop a garbage pyrolysis waste gas purification system and process which can effectively recover heat while ensuring the flue gas purification effect.
Disclosure of Invention
A first object of the present invention is to provide a waste gas purification system for pyrolysis of waste.
A second object of the present invention is to provide a process for a waste gas purification system for pyrolysis of waste.
The first object of the invention is realized by comprising a garbage combustion chamber, a heat exchanger I, a cyclone dust collector, an electric collection dust removal compound tar removal device, an active carbon adsorption tower, a dry desulfurization reactor, a dry dechlorination reactor, a catalytic combustor, a chimney, a heat exchanger II and a heat exchanger III, wherein a garbage combustion flue gas outlet of the garbage combustion chamber is connected with a high-temperature gas inlet of the heat exchanger I through a pipeline, a high-temperature gas outlet of the heat exchanger I is connected with a cyclone dust collector gas inlet of the cyclone dust collector through a pipeline, a cyclone dust collector gas outlet is connected with a device gas inlet of the electric collection dust removal compound tar removal device through a pipeline, a device gas outlet is connected with an adsorption tower gas inlet of the active carbon adsorption tower through a pipeline, an adsorption tower gas outlet is connected with a dry desulfurization reactor gas inlet of the dry desulfurization reactor through a pipeline, the gas outlet of the dry desulfurization reactor is connected with the gas inlet of the dry dechlorination reactor through a pipeline, the gas outlet of the dry dechlorination reactor is connected with the low-temperature gas inlet of the heat exchanger I through a pipeline, the upper end of the pipe wall of the garbage combustion chamber 1 is provided with a pipe wall outlet, the lower end of the pipe wall is provided with a pipe wall inlet, the low-temperature gas outlet of the heat exchanger I is connected with the pipe wall inlet through a pipeline, the pipe wall outlet is connected with the low-temperature gas inlet of the heat exchanger II through a pipeline, the low-temperature gas outlet of the heat exchanger II is connected with the high-temperature gas inlet of the heat exchanger II through a pipeline, the high-temperature gas outlet of the heat exchanger II is connected with the high-temperature gas inlet of the heat exchanger III 11 through a pipeline, the high-temperature gas outlet of the heat exchanger III is connected with the chimney inlet of a chimney through a pipeline, the low-temperature gas inlet of the heat exchanger III is an air inlet, the low-temperature gas outlet of the heat exchanger III is respectively connected with the garbage combustion chamber air inlet of the garbage combustion chamber and the catalytic burner air inlet of the catalytic burner through pipelines.
The second aim of the invention is realized in such a way that the combustion flue gas of the garbage combustion chamber enters a heat exchanger I to exchange heat and cool, and then the flue gas is treated by a cyclone dust collector, an electric collection dust removal composite tar removal device, an active carbon adsorption tower, a dry desulfurization reactor and a dry dechlorination reactor in sequence to obtain low-temperature primary purified gas;
the primary purified gas is subjected to heat exchange and temperature rise through a heat exchanger I, a garbage combustion chamber and a heat exchanger II respectively, and then enters a catalytic combustor for treatment to obtain high-temperature purified gas;
the high-temperature purified gas is sent to a heat exchanger II for heat exchange and cooling, and then the heat exchange and cooling are carried out in a heat exchanger III, so that the temperature of air is increased by heat exchange; the purified gas after cooling is discharged outside through a chimney; the air after temperature rise is sent to a garbage combustion chamber and a catalytic combustor to be used as combustion air.
Compared with the prior art, the invention has the following technical effects:
1. the flue gas generated by the pyrolysis of the garbage is subjected to multiple heat exchange with dechlorination reaction gas, catalytic combustion gas and air through the heat exchanger, so that the waste heat in different waste gases can be fully utilized, and the air is heated to a certain temperature and then enters the garbage combustion chamber to carry out pyrolysis treatment on the garbage, thereby achieving the purposes of environmental protection and energy saving;
2. An active carbon adsorption tower, a dry desulfurization reactor and a dry dechlorination reactor are arranged behind the electric collection dust removal composite tar removal device, and the active carbon adsorption tower can further remove residual tar, dioxin and other substances in the garbage pyrolysis flue gas; the high-efficiency desulfurizing agent prepared from calcium oxide, an auxiliary agent, silica sol and water is arranged in the dry desulfurization reactor, SO that SO in the flue gas can be treated 2 Dry removal is carried out, so that secondary pollution caused by acid-base waste liquid is avoided; carbon doped gamma-Al modified by alkaline earth metal in dry dechlorination reactor 2 O 3 The composite material has larger specific surface area and pore volume, stronger adsorption capacity and stronger selectivity, and can be used for HF and HF in flue gasHCl is efficiently and selectively adsorbed, and the adsorption capacity is large;
3. the catalytic combustor adopts Ti-MCM-41 or TS-1 molecular sieve as a carrier, pt and PtS 2 As active component, mnO 2 、Co 2 O 3 、CeO 2 The catalyst prepared from one or more auxiliary agents with any ratio has good sulfur resistance and chlorine resistance, has low activation temperature, can stably catalyze and burn at 120-200 ℃, has a CO conversion rate of 94% after catalyzing and burning at 150 ℃, and can effectively prevent carbon monoxide from exceeding standard emission;
4. the outlet gas of the catalytic combustor is treated by the heat exchanger, SO that the temperature of the gas can be effectively reduced, and the invention can effectively remove pollutants in the garbage combustion flue gas, such as particulate matters, smoke dust, dioxin, tar and SO 2 HCl, other irritant gases and the like meet the domestic garbage incineration pollution control standard (GB 18485-2014), and the treated tail gas can reach the emission standard.
Drawings
FIG. 1 is a schematic diagram of a system architecture of the present invention;
in the figure: 1: garbage combustion chamber, 1-1: waste combustion flue gas outlet, 1-2: pipe wall outlet, 1-3: pipe wall inlet, 1-4: garbage combustion chamber air inlet, 1-5 garbage flue gas collector ports, 2: heat exchanger i, 2-1: high-temperature gas inlet of heat exchanger I, 2-2: high-temperature gas outlet of heat exchanger I, 2-3: low-temperature gas inlet of heat exchanger I, 2-4: low-temperature gas outlet of heat exchanger I, 3: cyclone dust collector, 3-1: cyclone gas inlet, 3-2: cyclone gas outlet, 4: electric collection dust removal composite tar removal device, 4-1: device gas inlet, 4-2: device gas outlet, 5: activated carbon adsorption tower, 5-1: adsorption tower gas inlet, 5-2: adsorption tower gas outlet, 6: dry desulfurization reactor, 6-1: gas inlet of dry desulfurization reactor, 6-2: gas outlet of dry desulfurization reactor, 7: dry dechlorination reactor, 7-1: gas inlet of dry dechlorination reactor, 7-2: gas outlet of dry dechlorination reactor, 8: catalytic burner, 8-1: catalytic burner gas inlet, 8-2: catalytic burner gas outlet, 8-3 catalytic burner air inlet, 9: chimney, 9-1: chimney inlet, 10: heat exchanger ii, 10-1: heat exchanger ii low temperature gas inlet, 10-2: low-temperature gas outlet of heat exchanger II, 10-3: heat exchanger ii high temperature gas inlet, 10-4: heat exchanger ii high temperature gas outlet, 11: heat exchanger iii, 11-1: high-temperature gas inlet of heat exchanger III, 11-2: high-temperature gas outlet of heat exchanger III, 11-3: low temperature gas inlet of heat exchanger III, 11-4: and a low-temperature gas outlet of the heat exchanger III.
Detailed Description
The invention is further described below with reference to the accompanying drawings, without limiting the invention in any way, and any alterations or substitutions based on the teachings of the invention are intended to fall within the scope of the invention.
As shown in figure 1, the invention comprises a garbage combustion chamber 1, a heat exchanger I2, a cyclone dust collector 3, an electric collection dust removal compound tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6, a dry dechlorination reactor 7, a catalytic combustor 8, a chimney 9, a heat exchanger II 10 and a heat exchanger III 11, wherein a garbage combustion flue gas outlet 1-1 of the garbage combustion chamber 1 is connected with a high-temperature gas inlet 2-1 of the heat exchanger I through a pipeline, a high-temperature gas outlet 2-2 of the heat exchanger I is connected with a cyclone dust collector gas inlet 3-1 of the cyclone dust collector 3 through a pipeline, the cyclone dust collector gas outlet 3-2 is connected with a device gas inlet 4-1 of the electric collection dust removal compound tar removal device 4 through a pipeline, the device gas outlet 4-2 is connected with an adsorption tower gas inlet 5-1 of the active carbon adsorption tower 5 through a pipeline, the adsorption tower gas outlet 5-2 is connected with the dry desulfurization reactor gas inlet 6-1 of the dry desulfurization reactor 6 through a pipeline, the dry desulfurization reactor gas outlet 6-2 is connected with a dry dechlorination reactor gas inlet 7-1 of the dry dechlorination reactor 7 through a pipeline, the low-temperature gas inlet 7-1 of the dry desulfurization reactor is connected with a low-temperature gas inlet 1 of the heat exchanger 1 through a pipeline, the low-temperature gas inlet 2 is connected with the low-temperature gas inlet 1 through a pipeline wall 1 of the heat exchanger 1 through a pipeline, the pipeline wall 2-2 is connected with the low-temperature gas inlet 1-1 through a pipeline wall 1-3, the low-temperature gas inlet 1 is connected with the low-temperature gas inlet 1-temperature pipeline 1-1 through a pipeline, the pipeline wall of the pipeline is arranged, the low-temperature gas outlet 10-2 of the heat exchanger II is connected with the catalytic combustor gas inlet 8-1 of the catalytic combustor 8 through a pipeline, the catalytic combustor gas outlet 8-2 is connected with the high-temperature gas inlet 10-3 of the heat exchanger II through a pipeline, the high-temperature gas outlet 10-4 of the heat exchanger II is connected with the high-temperature gas inlet 11-1 of the heat exchanger III 11 through a pipeline, the high-temperature gas outlet 11-2 of the heat exchanger III is connected with the chimney inlet 9-1 of the chimney 9 through a pipeline, the low-temperature gas inlet 11-3 of the heat exchanger III is an air inlet, and the low-temperature gas outlet 11-4 of the heat exchanger III is respectively connected with the garbage combustion chamber air inlet 1-4 of the garbage combustion chamber 1 and the catalytic combustor air inlet 8-3 of the catalytic combustor 8 through pipelines.
The garbage combustion chamber 1 comprises a garbage room and a combustion chamber, the temperature in the combustion chamber is 700 ℃, high-temperature flue gas generated by garbage pyrolysis is collected by a collector and then is discharged from a garbage combustion flue gas outlet 1-1, the temperature of the outlet flue gas is 170-190 ℃, and the flow of the flue gas is 1000-10000 m 3 /h。
And the outlet flue gas temperature of the high-temperature gas outlet 2-2 of the heat exchanger I is 120-130 ℃.
The outlet gas temperature of the pipe wall outlet 1-2 is 140-160 ℃, and the outlet gas temperature of the heat exchanger II gas outlet 10-2 is 170-190 ℃; the outlet gas temperature of the high-temperature gas outlet 10-4 of the heat exchanger II is 170-190 ℃; the outlet gas temperature of the high-temperature gas outlet 11-2 of the heat exchanger III is 140-150 ℃.
The cyclone dust collector 3 primarily removes substances such as large particles, fly ash and the like in the flue gas.
The electric dust collection and removal composite tar removal device 4 can be an electrostatic dust collector, and fine particles and tar substances in the waste combustion gas are removed through the electrostatic dust collector.
The activated carbon adsorption tower 5 adopts activated carbon as an adsorbent to further remove a small amount of tar and dioxin substances remained in the waste gas of garbage combustion.
The desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, specifically, grinding and mixing the calcium oxide, the auxiliary agent and the silica sol in a container, dropwise adding 30mL of water to bond each component, continuously grinding and grinding for 60min at the dropwise adding rate of 1-2 drops/min to ensure that each component is uniform, molding, and drying the obtained mixture at 80 ℃ for 12h to obtain the desulfurizer; calcium oxide and auxiliary agent The mass ratio is 32-94:5-62, and the silica sol accounts for 3-20% of the sum of the mass of the calcium oxide and the auxiliary agent; the auxiliary agent comprises one or more of ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag; desulfurizing agent for removing SO from exhaust gas 2 A predominately sulfide-containing component; when the auxiliary agent is preferably a mixture of iron oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag, the mass ratio of the iron oxide, the manganese oxide, the magnesium oxide, the calcium carbonate, the cement and the carbon slag in the mixture is preferably 1-10:1-4:1-8:5-20:1-8:1-12.
The dechlorinating agent adopted by the dry dechlorination reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared by adopting an isovolumetric impregnation method or a sol-gel method. The specific preparation process of the dechlorinating agent comprises the steps of dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.5-1.5 g/L, the concentration of the carbon source is 0.5-2 g/L, 60-70wt% nitric acid is added into the mixed solution according to the proportion of 1-2 mL/L, aluminum nitrate is added into the mixed solution according to the proportion of 1-1.5 g/L in vigorous stirring, nitrate is added according to the proportion of 0.2-0.8 g/L, and the nitrate is magnesium nitrate and/or calcium nitrate; sealing, stirring at room temperature for 4-6 hours, drying the mixture, and adding N 2 Roasting for 4-6 hours at 500-600 ℃ in the atmosphere, tabletting and sieving to obtain 40-60 mesh particles, namely the dechlorinating agent; deep purification is carried out on chloride-containing components such as HCl, HF and the like in the pyrolysis waste gas of the garbage by the dechlorinating agent; the outlet gas temperature of the gas outlet 7-2 of the dry dechlorination reactor is 50-70 ℃; the outlet gas temperature of the low-temperature gas outlet 2-4 of the heat exchanger I is 100-120 ℃.
The catalytic combustor 8 contains sulfur-resistant and chlorine-resistant catalyst materials, and can catalyze and oxidize CO in the waste gas to convert the CO 2 Further, the concentration of CO in the discharged flue gas is effectively reduced, and the temperature of the outlet gas of the gas outlet 8-2 of the catalytic burner is 200-250 ℃.
The sulfur-resistant and chlorine-resistant catalyst material is prepared from the following components in percentage by weight: 93% -97% of carrier, 0.01% -0.5% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41 or TS-1 molecular sieve, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 、Co 2 O 3 、CeO 2 One or more of any ratio.
The carrier Ti-MCM-41 or TS-1 molecular sieve is prepared by adopting a hydrothermal method, active components are loaded on the carrier by an impregnation method, and the catalyst is obtained after drying, calcining and tabletting to 40-60 meshes, specifically, the nitrate of platinum salt and promoter metal is dissolved in water to obtain an impregnation liquid, and the mesoporous carrier is added into the impregnation liquid and is dried and roasted under the stirring condition; wherein the nitrate of the promoter metal is manganese nitrate, the mass ratio of platinum salt to nitrate is 0.043-0.048:1, the concentration of platinum salt in the impregnating solution is 0.03-0.3 mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the catalyst is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5 hours, and the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor
The Ti-MCM-41 molecular sieve comprises 2-10% of Ti and 90-98% of Si in percentage by weight.
The heat exchangers I2, II 10 and III 11 are tubular heat exchangers, wherein two ends of one heat exchange tube are respectively connected with the high-temperature gas inlet and the high-temperature gas outlet, and two ends of the other heat exchange tube are respectively connected with the low-temperature gas inlet and the low-temperature gas outlet, so that heat exchange is carried out between gases in the two heat exchange tubes.
The process of the garbage pyrolysis waste gas purification system comprises the steps that combustion flue gas of a garbage combustion chamber 1 enters a heat exchanger I2 to exchange heat and cool, and then the flue gas is treated by a cyclone dust collector 3, an electric dust collection and removal composite tar removal device 4, an activated carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas;
the primary purified gas is subjected to heat exchange and temperature rise through a heat exchanger I2, a garbage combustion chamber 1 and a heat exchanger II 10 respectively, and then enters a catalytic combustor 8 for treatment to obtain high-temperature purified gas;
the high-temperature purified gas is sent to a heat exchanger II 10 for heat exchange and cooling, and then is subjected to heat exchange and cooling in a heat exchanger III 11 to heat exchange and heat air; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
The working principle and the working process of the system are as follows: the flue gas generated by the combustion of the garbage in the garbage combustion chamber 1 enters the heat exchanger I2 through the garbage flue gas collector port 1-5, the garbage combustion flue gas outlet 1-1 and the high-temperature gas inlet 2-1 of the heat exchanger I; then the flue gas is discharged from a high-temperature gas outlet 2-2 of the heat exchanger I to a cyclone dust collector 3 to primarily remove substances such as large particles, fly ash and the like in the flue gas; the flue gas after dust removal is discharged to an electric collection dust removal composite tar removal device 4 to remove fine particles and tar matters; removing residual tar and dioxin substances from the flue gas through an active carbon adsorption tower 5, purifying sulfide components through a dry desulfurization reactor 6, and purifying chloride components through a dry dechlorination reactor 7 to obtain primary purified gas, wherein the gas temperature is 50-70 ℃; the primary purified gas enters the heat exchanger I from the low-temperature gas inlet of the heat exchanger I to exchange heat and raise temperature, and after the temperature is raised, enters the combustion chamber from the low-temperature gas outlet 2-4 of the heat exchanger I and the pipe wall inlet 1-3, and enters the heat exchanger II from the pipe wall outlet 1-2 and the low-temperature gas inlet 10-1 of the heat exchanger II to exchange heat and raise temperature continuously; after heating, the mixture enters the catalytic combustor 8 from the gas outlet 10-2 of the heat exchanger II and the gas inlet 8-1 of the catalytic combustor to be treated, so that the concentration of CO in the gas is reduced; the high-temperature purified gas is discharged from the gas outlet 8-2 of the catalytic combustor, enters the heat exchanger II from the high-temperature gas inlet 10-3 of the heat exchanger II to exchange heat and cool, enters the heat exchanger III from the high-temperature gas outlet 10-4 of the heat exchanger II and the high-temperature gas inlet 11-1 of the heat exchanger III to exchange heat and cool again to heat and cool combustion air, so that combustion air is warmed, the cooled purified gas is sent to the chimney 9 and discharged outside, and the warmed air is sent to the garbage combustion chamber 1 and the catalytic combustor 8 from the low-temperature gas outlet 11-4 of the heat exchanger III.
The present invention will be further described with reference to examples 1 to 9.
Example 1
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 180 ℃, and the flow rate of the flue gas is 1000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 122 ℃; then the flue gas sequentially passes through a cyclone dust collector 3, an electric collection dust removal and tar removal device 4, an activated carbon adsorption tower 5 and a dry desulfurization reactionThe reactor 6 and the dry dechlorination reactor 7 are treated to obtain low-temperature primary purified gas, wherein the gas temperature is 60 ℃;
wherein the desulfurizing agent used in the dry desulfurizing reactor 6 was a mixture of 27.5g of calcium oxide, 5g of iron oxide, 7.5g of calcium carbonate, 5g of carbon slag, 2.5g of cement and 8.3g of silica sol (SiO therein 2 30 wt.%) grinding and mixing in a polyethylene beaker, dropwise adding 30mL of deionized water to bond each component, wherein the dropping rate is 1-2 drops/min, continuously grinding and grinding for 60min to ensure that each component is uniform, forming, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizing agent, and loading the desulfurizing agent into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.5g/L, the concentration of the carbon source in the mixed solution is 0.5g/L, 60 wt% of nitric acid is added into the mixed solution according to the proportion of 1mL/L, aluminum nitrate is added into the mixed solution according to the proportion of 1g/L in vigorous stirring, nitrate is added according to the proportion of 0.2g/L, and the nitrate is calcium nitrate; after sealing, stirring is carried out at room temperature for 4 hours, the mixture is dried and then taken up in N 2 Roasting for 4 hours at 500 ℃ in atmosphere, tabletting and sieving to obtain 40-mesh particles which are dechlorination agent, and filling the dechlorination agent into a dry dechlorination reactor 7;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 118 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 150 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 180 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 1000 m/h, so that high-temperature purified gas is obtained, and the temperature is 225 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 94.7% of carrier, 0.3% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 The Ti-MCM-41 molecular sieve comprises 5% of Ti and 95% of Si, and is prepared by dissolving platinum salt and nitrate of promoter metal in water to obtain impregnating solution, and adding mesoporous carrier into the impregnating solutionDrying and roasting the mixture in the liquid under stirring; wherein the nitrate of the promoter metal is manganese nitrate, the mass ratio of platinum salt to nitrate is 0.0476:1, the concentration of platinum salt in the impregnating solution is 0.03mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the catalyst is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃ and the roasting time is 5 hours, so that the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;
The high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 180 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 140 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 2
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of outlet flue gas is 183 ℃, and the flow rate of flue gas is 1500m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 128 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 62 ℃;
wherein the desulfurizing agent used in the dry desulfurizing reactor 6 was a mixture of 27.5g of calcium oxide, 5g of iron oxide, 7.5g of calcium carbonate, 5g of carbon slag, 2.5g of cement and 8.3g of silica sol (SiO therein 2 30 wt.%) grinding and mixing in a polyethylene beaker, dropwise adding 30mL of deionized water to bond each component, wherein the dropping rate is 1-2 drops/min, continuously grinding and grinding for 60min to ensure that each component is uniform, forming, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizing agent, and loading the desulfurizing agent into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared through dissolving template agent and carbon source in absolute alcohol to obtain mixed solution with template agent concentration of 1.5g/L and carbon source concentration of 2g/L, adding 70wt% nitric acid into the mixed solution in the ratio of 2mL/L, adding aluminum nitrate in the ratio of 1.5g/L while stirring vigorously, adding nitrate in the ratio of 0.8g/L, adding nitric acidThe salt is magnesium nitrate; after sealing, stirring is carried out at room temperature for 6 hours, the mixture is dried and then taken up in N 2 Roasting for 6 hours at 600 ℃ in atmosphere, tabletting and sieving to obtain 60-mesh particles, namely a dechlorinating agent, and filling the dechlorinating agent into a dry dechlorinating reactor 7;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to raise the temperature to 117 ℃, the waste combustion chamber 1 is subjected to heat exchange to raise the temperature to 153 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to raise the temperature to 183 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 1500 m/h, so that high-temperature purified gas is obtained, and the temperature is 213 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 94.7% of carrier, 0.3% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 The preparation method comprises the specific steps of dissolving platinum salt and nitrate of promoter metal in water to obtain impregnating solution, adding a mesoporous carrier into the impregnating solution, and drying and roasting under stirring conditions, wherein the content of Ti in the Ti-MCM-41 molecular sieve is 5% and the content of Si is 95%; wherein the nitrate of the promoter metal is manganese nitrate, the mass ratio of platinum salt to nitrate is 0.0476:1, the concentration of platinum salt in the impregnating solution is 0.03mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the catalyst is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃ and the roasting time is 5 hours, so that the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;
the high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 183 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 142 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 3
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of outlet flue gas is 185 ℃, and the flow rate of the flue gas is 2000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 130 ℃; then the flue gas sequentially passes through a cyclone dust collector 3, an electric collection dust removal and tar removal device 4 and an active carbon adsorption tower 5. The dry desulfurization reactor 6 and the dry dechlorination reactor 7 are used for treatment to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;
wherein the desulfurizing agent used in the dry desulfurizing reactor 6 was a mixture of 28.5g of calcium oxide, 2.5g of magnesium oxide, 5g of iron oxide, 1.5g of manganese oxide, 7.5g of calcium carbonate, 2.5g of cement and 8.3g of silica sol (SiO therein 2 30 wt.%) grinding and mixing in a polyethylene beaker, dropwise adding 30mL of deionized water to bond each component, wherein the dropping rate is 1-2 drops/min, continuously grinding and grinding for 60min to ensure that each component is uniform, forming, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizing agent, and loading the desulfurizing agent into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared by dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 1.0g/L, the concentration of the carbon source in the mixed solution is 1.25g/L, 65 wt% of nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added into the mixed solution according to the proportion of 1.25g/L in vigorous stirring, and nitrate is added according to the proportion of 0.5g/L, wherein the nitrate is magnesium nitrate and calcium nitrate; after sealing, stirring is carried out at room temperature for 5 hours, the mixture is dried and then taken up in N 2 Roasting for 5 hours at 550 ℃ in atmosphere, tabletting and sieving to obtain 50-mesh particles, namely a dechlorination agent, and filling the dechlorination agent into a dry dechlorination reactor 7;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 120 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 155 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 185 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 2000 m/h, so that high-temperature purified gas is obtained, and the temperature is 215 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 94.7% of carrier, 0.3% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 The Ti-MCM-41 molecular sieve contains Ti 5 wt% and Si 95 wt%, and is prepared through dissolving platinum salt and nitrate of promoter metalDissolving in water to obtain an impregnating solution, adding the mesoporous carrier into the impregnating solution, and drying and roasting under the stirring condition; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of platinum salt to nitrate is 0.043:1, the concentration of platinum salt in the impregnating solution is 0.3mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the impregnating solution is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5 hours, and the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;
The high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 185 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 145 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 4
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of outlet flue gas is 185 ℃, and the flow rate of flue gas is 5500m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 130 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;
wherein, the desulfurizing agent adopted by the dry desulfurizing reactor 6 is selected from calcium oxide, magnesium oxide, ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement, carbon slag and silica sol (wherein SiO 2 30 wt.%) grinding and mixing in a polyethylene beaker, wherein the mass ratio of calcium oxide to auxiliary agent is 32:5, silica sol accounts for 3% of the sum of the mass of the calcium oxide and the auxiliary agent, the mass ratio of ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag is 1:1:1:5:1:12, dropwise adding 30mL of deionized water to bond each component, the dropwise adding rate is 1-2 drops/min, continuously grinding and grinding for 60min to ensure that each component is uniform, molding, drying the obtained mixture at 80 ℃ for 12h to obtain a desulfurizing agent, and loading the desulfurizing agent into a dry desulfurizing reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared by the steps of,Dissolving a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of a template agent in the mixed solution is 0.9g/L, the concentration of the carbon source is 1.3g/L, 60 wt% of nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added into the mixed solution according to the proportion of 1.3g/L in vigorous stirring, nitrate is added according to the proportion of 0.5g/L, and the mass ratio of the nitrate to the magnesium nitrate to the calcium nitrate is 1:1; after sealing, stirring is carried out at room temperature for 5 hours, the mixture is dried and then taken up in N 2 Roasting for 5 hours at 550 ℃ in atmosphere, tabletting and sieving to obtain 50-mesh particles, namely a dechlorination agent, and filling the dechlorination agent into a dry dechlorination reactor 7;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 120 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 155 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 185 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 2000 m/h, so that high-temperature purified gas is obtained, and the temperature is 215 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 93% of carrier, 0.01% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 The preparation method comprises the specific steps of dissolving platinum salt and nitrate of promoter metal in water to obtain impregnating solution, adding a mesoporous carrier into the impregnating solution, and drying and roasting under stirring conditions, wherein the content of Ti in the Ti-MCM-41 molecular sieve is 2% and the content of Si is 98%; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of platinum salt to nitrate is 0.043:1, the concentration of platinum salt in the impregnating solution is 0.03mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the impregnating solution is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5 hours, and the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;
the high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 185 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 145 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 5
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of outlet flue gas is 185 ℃, and the flow rate of the flue gas is 3000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 130 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;
Wherein, the desulfurizing agent adopted by the dry desulfurizing reactor 6 is selected from calcium oxide, magnesium oxide, ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement, carbon slag and silica sol (wherein SiO 2 30 wt.%) grinding and mixing in a polyethylene beaker, wherein the mass ratio of calcium oxide to auxiliary agent is 94:62, the silica sol accounts for 20% of the sum of the mass of the calcium oxide and the auxiliary agent, the mass ratio of ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement and carbon slag is 10:4:8:20:8:1, dropwise adding 30mL of deionized water to bond each component, the dropwise adding rate is 1-2 drops/min, continuously grinding and grinding for 60min to ensure that each component is uniform, molding, drying the obtained mixture at 80 ℃ for 12h to obtain the desulfurizing agent, and loading the desulfurizing agent into a dry desulfurizing reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The preparation method comprises the steps of dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.9g/L, the concentration of the carbon source in the mixed solution is 1.3g/L, 60 wt% of nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added into the mixed solution according to the proportion of 1.3g/L in vigorous stirring, nitrate is added according to the proportion of 0.5g/L, and the nitrate is magnesium nitrate and calcium nitrate, wherein the mass ratio of the magnesium nitrate to the calcium nitrate is 1:1; after sealing, stirring is carried out at room temperature for 5 hours, the mixture is dried and then taken up in N 2 Roasting for 5 hours at 550 ℃ in atmosphere, tabletting and sieving to obtain 50-mesh particles, namely a dechlorination agent, and filling the dechlorination agent into a dry dechlorination reactor 7;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 120 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 155 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 185 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 2000 m/h, so that high-temperature purified gas is obtained, and the temperature is 215 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 97% of carrier, 0.5% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 The preparation method comprises the specific steps of dissolving platinum salt and nitrate of promoter metal in water to obtain impregnating solution, adding a mesoporous carrier into the impregnating solution, and drying and roasting under stirring conditions, wherein the content of Ti in the Ti-MCM-41 molecular sieve is 10% and the content of Si is 90%; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of platinum salt to nitrate is 0.048:1, the concentration of platinum salt in the impregnating solution is 0.3mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the catalyst is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5 hours, and the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;
The high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 185 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 145 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 6
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of outlet flue gas is 185 ℃, and the flow rate of the flue gas is 3000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 130 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 65 ℃;
wherein, the desulfurizing agent adopted by the dry desulfurizing reactor 6 is selected from calcium oxide, magnesium oxide, ferric oxide, manganese oxide, magnesium oxide, calcium carbonate, cement, carbon slag and silica sol (wherein SiO 2 30 wt.%) in a polyethylene beaker, the mass ratio of calcium oxide to auxiliary agent is 50:59, the silica sol accounts for17% of the sum of the mass of the calcium oxide and the additive, wherein the mass ratio of the ferric oxide to the manganese oxide to the magnesium oxide to the calcium carbonate to the cement to the carbon slag is 5.5:2.5:4.5:12.5:4.5:6.5, 30mL of deionized water is dropwise added to bond all the components, the dropping speed is 1-2 drops/min, grinding is continued for 60min to uniformly grind all the components, the components are molded, the obtained mixture is dried at 80 ℃ for 12h to obtain a desulfurizing agent, and the desulfurizing agent is filled into a dry desulfurization reactor 6; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The preparation method comprises the steps of dissolving a template agent and a carbon source in absolute ethyl alcohol to obtain a mixed solution, wherein the concentration of the template agent in the mixed solution is 0.9g/L, the concentration of the carbon source in the mixed solution is 1.3g/L, 60 wt% of nitric acid is added into the mixed solution according to the proportion of 1.5mL/L, aluminum nitrate is added into the mixed solution according to the proportion of 1.3g/L in vigorous stirring, nitrate is added according to the proportion of 0.5g/L, and the nitrate is magnesium nitrate and calcium nitrate, wherein the mass ratio of the magnesium nitrate to the calcium nitrate is 1:1; after sealing, stirring is carried out at room temperature for 5 hours, the mixture is dried and then taken up in N 2 Roasting for 5 hours at 550 ℃ in atmosphere, tabletting and sieving to obtain 50-mesh particles, namely a dechlorination agent, and filling the dechlorination agent into a dry dechlorination reactor 7;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 120 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 155 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 185 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 2000 m/h, so that high-temperature purified gas is obtained, and the temperature is 215 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 95% of carrier, 0.255% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 The preparation method comprises the steps of dissolving platinum salt and nitrate of promoter metal in water to obtain impregnating solution, adding mesoporous carrier into the impregnating solution, and drying and roasting under stirring conditions, wherein the content of Ti in the Ti-MCM-41 molecular sieve is 6% and the content of Si is 94%; wherein the nitrate of the promoter metal is manganese nitrate and cobalt nitrate, the mass ratio of platinum salt to nitrate is 0.0455:1, and the dipping liquidThe concentration of the medium platinum salt is 0.165mol/L, the drying temperature is 60 ℃, the drying time is 4 hours, then the medium platinum salt is dried for 1 hour at the temperature of 70 ℃, the roasting temperature is 550 ℃, the roasting time is 5 hours, and the sulfur-resistant and chlorine-resistant catalyst is prepared, and the catalyst is filled in a catalytic combustor;
the high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 185 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 145 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 7
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 170 ℃, and the flow rate of the flue gas is 1000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 120 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 50 ℃;
Wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, the mass ratio of the calcium oxide to the auxiliary agent is 32:5, and the silica sol accounts for 3% of the sum of the masses of the calcium oxide and the auxiliary agent; the auxiliary agent is ferric oxide; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared by adopting an isovolumetric impregnation method;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 100 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 140 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 170 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 1000 m/h, so that high-temperature purified gas is obtained, and the temperature is 200 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 93% of carrier, 0.01% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 Co promoter is Co 2 O 3 ；
The high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 170 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 140 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 8
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 190 ℃, and the flow rate of the flue gas is 10000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 130 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 70 ℃;
wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, the mass ratio of the calcium oxide to the auxiliary agent is 94:62, and the silica sol accounts for 20 percent of the sum of the mass of the calcium oxide and the auxiliary agent; the auxiliary agent is manganese oxide; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material is prepared by a sol-gel method;
the primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 120 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 160 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 190 ℃, and then the primary purified gas enters a catalytic combustor 8 for treatment, wherein the flow rate of flue gas is 1000 m/h, so that high-temperature purified gas is obtained, and the temperature is 250 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 97% of carrier, 0.5% of active component and the balance of cocatalyst, wherein the carrier is Ti-MCM-41, and the active components are Pt and PtS 2 The catalyst promoter is CeO 2 ；
The high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 190 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 150 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Example 9
The temperature in the combustion chamber of the garbage combustion chamber 1 is 700 ℃, the temperature of the outlet flue gas is 180 ℃, and the flow rate of the flue gas is 3000m 3 H, enabling the flue gas to enter a heat exchanger I for heat exchange and cooling to 125 ℃; then the flue gas is treated by a cyclone dust collector 3, an electric collection dust removal composite tar removal device 4, an active carbon adsorption tower 5, a dry desulfurization reactor 6 and a dry dechlorination reactor 7 in sequence to obtain low-temperature primary purified gas, wherein the gas temperature is 60 ℃;
wherein, the desulfurizer adopted by the dry desulfurization reactor 6 is obtained by mixing and drying calcium oxide, an auxiliary agent, silica sol and water, the mass ratio of the calcium oxide to the auxiliary agent is 63:33.5, and the silica sol accounts for 11.5% of the sum of the mass of the calcium oxide and the auxiliary agent; the auxiliary agent is magnesium oxide; the dechlorinating agent adopted by the dry dechlorinating reactor 7 is alkaline earth metal modified carbon doped gamma-Al 2 O 3 The composite material adopts an isovolumetric impregnation method;
The primary purified gas is subjected to heat exchange by a heat exchanger I2 to be heated to 110 ℃, the waste combustion chamber 1 is subjected to heat exchange to be heated to 150 ℃, the heat exchange by a heat exchanger II 10 is subjected to heat exchange to be heated to 180 ℃, and then the primary purified gas enters a catalytic combustor 8 to be treated, wherein the flow rate of flue gas is 1000 m/h, so that high-temperature purified gas is obtained, and the temperature is 225 ℃;
wherein, the sulfur-resistant and chlorine-resistant catalyst material in the catalytic combustor 8 is prepared from the following compositions in percentage by weight: 95% of carrier, 0.255% of active component and the balance of cocatalyst, wherein the carrier is TS-1 molecular sieve, and the active components are Pt and PtS 2 The cocatalyst is MnO 2 、Co 2 O 3 、CeO 2 ；
The high-temperature purified gas is sent to a heat exchanger II to exchange heat and cool to 180 ℃, and then is subjected to heat exchange in a heat exchanger III 11 to exchange heat and cool to 145 ℃ so as to heat the air and raise the temperature; the purified gas after cooling is discharged outside through a chimney 9; the warmed air is sent to the garbage combustion chamber 1 and the catalytic burner 8 as combustion air.
Claims (7)
1. A garbage pyrolysis waste gas purification system comprises a garbage combustion chamber (1), a heat exchanger I (2), a cyclone dust collector (3), an electric collection dust removal compound tar removal device (4), an active carbon adsorption tower (5), a dry desulfurization reactor (6), a dry dechlorination reactor (7), a catalytic combustor (8), a chimney (9), a heat exchanger II (10) and a heat exchanger III (11), and is characterized in that a garbage combustion flue gas outlet (1-1) of the garbage combustion chamber (1) is connected with a high-temperature gas inlet (2-1) of the heat exchanger I through a pipeline, the high-temperature gas outlet (2-2) of the heat exchanger I is connected with a cyclone dust collector gas inlet (3-1) of the cyclone dust collector (3) through a pipeline, the cyclone dust collector gas outlet (3-2) is connected with a device gas inlet (4-1) of the electric collection dust removal compound tar removal device (4), the device gas outlet (4-2) of the electric collection dust removal compound tar removal device is connected with an adsorption tower gas inlet (5-1) of the active carbon adsorption tower (5) through a pipeline, the active carbon adsorption tower gas outlet (5-2) is connected with the dry desulfurization reactor gas inlet (6-1) of the dry desulfurization reactor (6-1), the gas outlet (6-2) of the dry desulfurization reactor is connected with the gas inlet (7-1) of the dry dechlorination reactor (7) through a pipeline, the gas outlet (7-2) of the dry dechlorination reactor is connected with the low-temperature gas inlet (2-3) of the heat exchanger I through a pipeline, the upper end of the pipe wall of the garbage combustion chamber (1) is provided with a pipe wall outlet (1-2), the lower end of the pipe wall is provided with a pipe wall inlet (1-3), the low-temperature gas outlet (2-4) of the heat exchanger I is connected with the pipe wall inlet (1-3) through a pipeline, the pipe wall outlet (1-2) is connected with the low-temperature gas inlet (10-1) of the heat exchanger II through a pipeline, the low-temperature gas outlet (10-2) of the heat exchanger II is connected with the gas inlet (8-1) of the catalytic combustor I through a pipeline, the high-temperature gas outlet (8-2) of the catalytic combustor II is connected with the high-temperature gas inlet (10-3) of the heat exchanger II through a pipeline, the high-temperature gas outlet (10-4) of the heat exchanger II is connected with the high-temperature gas inlet (11-III) of the heat exchanger III through a pipeline, the low-temperature gas outlet (11-9) of the heat exchanger III is connected with the low-temperature gas inlet (11-9) of the heat exchanger through a chimney through a pipeline, the low-temperature gas outlet (11-4) of the heat exchanger III is respectively connected with the garbage combustion chamber air inlet (1-4) of the garbage combustion chamber (1) and the catalytic burner air inlet (8-3) of the catalytic burner (8) through pipelines.
2. The waste gas purification system for pyrolysis of waste according to claim 1, wherein the waste combustion chamber (1) comprises a waste chamber and a combustion chamber, the temperature in the combustion chamber is 700 ℃, high-temperature flue gas generated by pyrolysis of waste is collected by the collector and then is discharged from the waste combustion flue gas outlet (1-1), the temperature of the outlet flue gas is 170-190 ℃, and the flow rate of the flue gas is 1000-10000 m 3 /h。
3. The waste pyrolysis waste gas purification system according to claim 1, wherein the outlet flue gas temperature of the high-temperature gas outlet (2-2) of the heat exchanger I is 120-130 ℃.
4. The waste pyrolysis waste gas purification system according to claim 1, wherein the outlet gas temperature of the pipe wall outlet (1-2) is 140-160 ℃, and the outlet gas temperature of the heat exchanger II gas outlet (10-2) is 170-190 ℃; the outlet gas temperature of the high-temperature gas outlet (10-4) of the heat exchanger II is 170-190 ℃; the outlet gas temperature of the high-temperature gas outlet (11-2) of the heat exchanger III is 140-150 ℃.
5. The waste gas purification system for garbage pyrolysis according to claim 1, wherein the outlet gas temperature of the gas outlet (7-2) of the dry dechlorination reactor is 50-70 ℃; the outlet gas temperature of the low-temperature gas outlet (2-4) of the heat exchanger I is 100-120 ℃.
6. The waste gas purification system for garbage pyrolysis according to claim 1, wherein the catalytic combustor (8) contains sulfur-resistant and chlorine-resistant catalyst materials, and the outlet gas temperature of the catalytic combustor gas outlet (8-2) is 200-250 ℃.
7. A process of a waste gas purification system for garbage pyrolysis according to any one of claims 1-6, which is characterized in that combustion flue gas of a garbage combustion chamber (1) enters a heat exchanger I (2) for heat exchange and temperature reduction, and then the flue gas is sequentially treated by a cyclone dust collector (3), an electric collection dust removal composite tar removal device (4), an activated carbon adsorption tower (5), a dry desulfurization reactor (6) and a dry dechlorination reactor (7) to obtain low-temperature primary purified gas;
the primary purified gas is subjected to heat exchange and temperature rise respectively through a heat exchanger I (2), a garbage combustion chamber (1) and a heat exchanger II (10), and then enters a catalytic combustor (8) for treatment to obtain high-temperature purified gas;
the high-temperature purified gas is sent to a heat exchanger II (10) for heat exchange and cooling, and then the heat exchange and cooling are carried out in a heat exchanger III (11) to heat exchange and heat air; the purified gas after cooling is discharged outside through a chimney (9); the heated air is sent to a garbage combustion chamber (1) and a catalytic combustor (8) to be used as combustion air.
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| CN112892180A (en) * | 2021-02-20 | 2021-06-04 | 周鼎力 | Method for treating garbage by catalytic decomposition of dioxin |
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