CN117599609A - Three-tower type RTO dioxin waste gas treatment method - Google Patents
Three-tower type RTO dioxin waste gas treatment method Download PDFInfo
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- CN117599609A CN117599609A CN202410005095.XA CN202410005095A CN117599609A CN 117599609 A CN117599609 A CN 117599609A CN 202410005095 A CN202410005095 A CN 202410005095A CN 117599609 A CN117599609 A CN 117599609A
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- 239000002912 waste gas Substances 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 24
- 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 title claims 10
- 239000000919 ceramic Substances 0.000 claims abstract description 150
- 239000007789 gas Substances 0.000 claims abstract description 74
- 239000003054 catalyst Substances 0.000 claims abstract description 62
- 239000012855 volatile organic compound Substances 0.000 claims abstract description 42
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims abstract description 5
- 238000002485 combustion reaction Methods 0.000 claims description 57
- 238000007599 discharging Methods 0.000 claims description 20
- 238000011049 filling Methods 0.000 claims description 19
- 238000007664 blowing Methods 0.000 claims description 10
- 125000004122 cyclic group Chemical group 0.000 claims description 10
- 229920000728 polyester Polymers 0.000 claims description 7
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 7
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 7
- 230000004048 modification Effects 0.000 claims description 5
- 238000012986 modification Methods 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims 3
- 238000010304 firing Methods 0.000 claims 2
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 claims 1
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 claims 1
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 claims 1
- 229910000505 Al2TiO5 Inorganic materials 0.000 claims 1
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 claims 1
- 239000005642 Oleic acid Substances 0.000 claims 1
- 239000011230 binding agent Substances 0.000 claims 1
- 239000002131 composite material Substances 0.000 claims 1
- 229910052878 cordierite Inorganic materials 0.000 claims 1
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 claims 1
- 238000001035 drying Methods 0.000 claims 1
- 238000001125 extrusion Methods 0.000 claims 1
- 238000000227 grinding Methods 0.000 claims 1
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 claims 1
- 239000000314 lubricant Substances 0.000 claims 1
- 229920000609 methyl cellulose Polymers 0.000 claims 1
- 239000001923 methylcellulose Substances 0.000 claims 1
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 claims 1
- 239000004014 plasticizer Substances 0.000 claims 1
- 238000002360 preparation method Methods 0.000 claims 1
- AABBHSMFGKYLKE-SNAWJCMRSA-N propan-2-yl (e)-but-2-enoate Chemical compound C\C=C\C(=O)OC(C)C AABBHSMFGKYLKE-SNAWJCMRSA-N 0.000 claims 1
- 239000002994 raw material Substances 0.000 claims 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims 1
- 229910010271 silicon carbide Inorganic materials 0.000 claims 1
- 229910000314 transition metal oxide Inorganic materials 0.000 claims 1
- 239000002383 tung oil Substances 0.000 claims 1
- GFQYVLUOOAAOGM-UHFFFAOYSA-N zirconium(iv) silicate Chemical compound [Zr+4].[O-][Si]([O-])([O-])[O-] GFQYVLUOOAAOGM-UHFFFAOYSA-N 0.000 claims 1
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 abstract description 7
- -1 dioxin compound Chemical class 0.000 abstract description 6
- 230000003647 oxidation Effects 0.000 abstract description 5
- 238000007254 oxidation reaction Methods 0.000 abstract description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 4
- 230000006378 damage Effects 0.000 abstract description 3
- 206010007269 Carcinogenicity Diseases 0.000 abstract description 2
- 239000001569 carbon dioxide Substances 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 2
- 231100000260 carcinogenicity Toxicity 0.000 abstract description 2
- 230000007670 carcinogenicity Effects 0.000 abstract description 2
- 239000012528 membrane Substances 0.000 abstract description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 abstract description 2
- 230000001172 regenerating effect Effects 0.000 abstract description 2
- 239000007787 solid Substances 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract 1
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 26
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 16
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 16
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 8
- 239000005751 Copper oxide Substances 0.000 description 8
- 229910000431 copper oxide Inorganic materials 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 229910000510 noble metal Inorganic materials 0.000 description 8
- 229910052763 palladium Inorganic materials 0.000 description 8
- 229910052697 platinum Inorganic materials 0.000 description 8
- 229910052703 rhodium Inorganic materials 0.000 description 8
- 239000010948 rhodium Substances 0.000 description 8
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 8
- 229910052723 transition metal Inorganic materials 0.000 description 8
- 150000003624 transition metals Chemical class 0.000 description 8
- XHCLAFWTIXFWPH-UHFFFAOYSA-N [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] Chemical group [O-2].[O-2].[O-2].[O-2].[O-2].[V+5].[V+5] XHCLAFWTIXFWPH-UHFFFAOYSA-N 0.000 description 7
- 150000002013 dioxins Chemical class 0.000 description 7
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 7
- 229910001935 vanadium oxide Inorganic materials 0.000 description 7
- 229910001928 zirconium oxide Inorganic materials 0.000 description 7
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 6
- 239000010815 organic waste Substances 0.000 description 5
- 238000009841 combustion method Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005338 heat storage Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 238000007084 catalytic combustion reaction Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000035939 shock Effects 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur 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
- B01D53/86—Catalytic processes
- B01D53/8659—Removing halogens or halogen compounds
- B01D53/8662—Organic halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
-
- 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
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/20—Organic adsorbents
- B01D2253/202—Polymeric adsorbents
-
- 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
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Incineration Of Waste (AREA)
- Catalysts (AREA)
Abstract
The invention relates to a three-tower type RTO dioxin waste gas treatment method, and belongs to the technical field of waste gas treatment. VOCs waste gas is a collective term of volatile organic compounds, and the VOCs waste gas not only pollutes the environment, but also causes serious harm to the life and the body of people. The RTO thermal oxidation purification device is a regenerative oxidation furnace, and the principle is that organic matters in the exhaust gas are oxidized into corresponding carbon dioxide and water at high temperature, so that the exhaust gas is purified, and the heat released during the decomposition of the exhaust gas is recovered. The catalyst module is added in the ceramic heat accumulator, so that the removal of the dioxin compound with strong carcinogenicity is further ensured; a layer of filter membrane is added between the catalyst module and the honeycomb ceramic heat accumulator, so that the problem of blockage caused by solid particles entering the ceramic heat accumulator can be reduced.
Description
Technical Field
The invention belongs to the technical field of waste gas treatment, and relates to a three-tower type RTO dioxin waste gas treatment method.
Background
VOCs waste gas is also called organic waste gas, is a collective term of volatile organic compounds, and a plurality of production enterprises have VOCs waste gas products, such as waste gas in automobile industry, waste gas in medicine industry, waste gas in coking industry and the like, and the VOCs waste gas not only pollutes the environment, but also causes serious harm to the life and the body of people. At present, common organic waste gas treatment methods include a direct combustion method, a cooling solidification treatment method, a catalytic combustion method and the like, but the methods are generally high in cost, poor in efficiency and poor in energy-saving effect. The direct combustion technology can be classified into a direct combustion method and a thermal storage combustion method according to a heat recovery mode, and nitrogen oxides and dioxin with strong carcinogenicity are easily generated when the thermal storage combustion method is incomplete in combustion, so that secondary pollution is caused. The cooling solidification treatment method condenses the exhaust gas only by physical change and cannot truly treat the organic exhaust gas. The catalytic combustion has lower temperature than thermal incineration, which can obviously reduce the running cost of equipment, but when the waste gas contains sulfur and halogen organic compounds which can cause catalyst poisoning, the catalytic combustion method is not suitable.
The technology adopted at present is that after the concentration of the chlorine-containing organic waste gas is reduced by independent pretreatment, the chlorine-containing organic waste gas is converged with other waste gas and enters an RTO incinerator, the flow is complex, and the investment is large. The RTO thermal oxidation purifying equipment is a regenerative oxidation furnace, the principle is that organic matters in the waste gas are oxidized into corresponding carbon dioxide and water at high temperature, so that the waste gas is purified, the heat released during the decomposition of the waste gas is recovered, the high-temperature gas generated by oxidation flows through a special ceramic heat accumulator, the ceramic body is heated to store heat, and the heat is used for preheating the organic waste gas which enters later; thus saving the fuel consumption of waste gas temperature rise, the ceramic heat storage chambers are divided into two, more than two are included, and each heat storage chamber sequentially undergoes procedures of heat storage, heat recovery and the like, and the ceramic heat storage chambers work continuously and repeatedly.
Disclosure of Invention
The invention aims to provide a three-tower type RTO dioxin waste gas treatment method which can remove VOCs waste gas more efficiently.
The aim of the invention can be achieved by the following technical scheme:
the ceramic heat accumulator is added with a catalyst filling module, and a layer of filter screen is added between the catalyst filling module and the ceramic heat accumulator, and the waste gas treatment flow is as follows:
s1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the VOCs waste gas passes through a preheated ceramic regenerator A and is filled into a module through a catalyst in the ceramic regenerator A;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
Further, the catalyst is a ceramic carrier high-efficiency catalyst capable of oxidizing dioxin.
The catalyst added can be replaced according to the main component of the gas, and common VOCs catalysts include noble metal catalysts (platinum, palladium, rhodium) and transition metal catalysts (alumina, zirconia, copper oxide). The ceramic carrier catalyst has excellent chemical stability and high temperature stability, and can exert good catalytic effect at high temperature and high pressure.
Further, the temperature range of the ceramic heat accumulator is 30-760 ℃.
Further, the ceramic heat accumulator is made of honeycomb materials.
Furthermore, the first layer of the honeycomb material close to the high-temperature part of the hearth adopts a macroporous thick-wall structure, and the other part adopts a small-hole thin-wall structure.
In order to reduce the bed resistance and enable the gas to pass smoothly, the RTO device adopts structured packing, and the honeycomb ceramic heat accumulator has the advantages of large specific surface area, small resistance loss, small coefficient of thermal expansion and contraction, good heat resistance and the like. Ceramic honeycomb filler is made into a columnar heat accumulator and integrally built in a heat accumulator chamber of the RTO. In order to improve the heat recovery efficiency, the specific surface area is improved to the greatest extent in design, so that heat exchange is realized to the greatest extent, and under the same material and use conditions, the more small holes mean that the heat recovery efficiency is higher, but the heat shock resistance is reduced. In order to ensure that the heat accumulator has better heat shock resistance and bearing capacity in multi-layer stacking, a first layer at a high-temperature part adopts a large-hole thick-wall structure, and the rest part adopts a small-hole thin-wall structure.
Further, the filter screen is PTFE polyester coated filter paper subjected to low-temperature plasma modification treatment.
Further, the parameters of the low temperature plasma process are as follows: low temperature plasma with energy higher than 4.4 eV.
The energy of C-F bond in PTFE polyester is 4.4 eV, the energy of C-C bond is 3.4 eV, and the low temperature plasma with energy higher than 4.4 eV is used for bombarding the surface of PTFE polyester, so that the molecular bond on the surface of PTFE polyester breaks and combines with free radical in the plasma to form polar group on the surface of PTFE polyester, thereby obviously improving the adhesive property of the surface of the material. The modified PTFE polyester coated filter paper can adsorb more particles, and prevent the particles from entering the ceramic heat accumulator to cause blockage.
Further, the combustion temperature of the combustion chamber is higher than 760 ℃.
Further, the regenerator requires a cross section hollow tower wind speed of no more than 2 m/s.
Further, the three-tower RTO circulation operation period is 90-180S.
The invention has the beneficial effects that:
in the first aspect of the invention, the catalyst filling module is added in the ceramic heat accumulator, the ceramic carrier high-efficiency catalyst capable of oxidizing dioxin is put in the module, so that the strong carcinogenic dioxin compound generated by VOCs waste gas can be removed more efficiently,
according to the invention, a layer of modified filter membrane is added between the catalyst module and the ceramic heat accumulator, so that the catalyst can be reduced from falling into the honeycomb ceramic heat accumulator, and solid particulate matters are reduced from gathering, so that the catalyst is prevented from being sucked into the ceramic heat accumulator to cause blockage and damage of the ceramic heat accumulator.
According to the third aspect of the invention, two honeycomb ceramic heat accumulators with different apertures are selected, a first layer close to a high-temperature part of a hearth adopts a macroporous thick-wall structure, the rest part adopts a small-hole thin-wall structure, the high-temperature part adopts an excessively fine eyelet structure, the strength of the ceramic heat accumulator can be influenced, and the rest part adopts the small-hole thin-wall structure, so that the specific surface area of the ceramic heat accumulator can be effectively increased.
Drawings
The present invention is further described below with reference to the accompanying drawings for the convenience of understanding by those skilled in the art.
FIG. 1 is a schematic diagram of a catalyst packing module.
Detailed Description
In order to further describe the technical means and effects adopted by the present invention for achieving the intended purpose, the following detailed description will be given with reference to fig. 1 and the preferred embodiment.
Example 1
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow of the introduced waste gas in the embodiment is 10000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (with the methylene dichloride content of 1000 ppm) firstly passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 1m 3 The temperature of the catalyst is 200-500 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (aluminum oxide, zirconium oxide and copper oxide) can be selected in the invention;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons emitted was < 40mg/m and dioxin compounds were not detected.
Example 2
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow of the introduced waste gas in the embodiment is 10000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (wherein the dichloromethane content is 1500 ppm) passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, wherein the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 1m 3 The temperature of the catalyst is 200-500 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (aluminum oxide, zirconium oxide and copper oxide) can be selected in the invention;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons emitted was < 50mg/m 2. Mu.m, and dioxin compounds were not detected.
Example 3
S1: VOCs (volatile organic Compounds)Waste gas is introduced into a regenerator in a three-tower RTO, and the flow rate of the introduced waste gas in the embodiment is 10000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (wherein the dichloromethane content is 1500 ppm) passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, wherein the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 3m 3 The temperature of the catalyst is 200-500 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (aluminum oxide, zirconium oxide and copper oxide) can be selected in the invention;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons emitted was < 40mg/m and dioxin compounds were not detected.
Example 4
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow of the introduced waste gas in the embodiment is 10000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (wherein the dichloromethane content is 1500 ppm) passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, wherein the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 3m 3 The temperature of the catalyst is 150-450 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (alumina) can be selected in the invention,Zirconium oxide, copper oxide);
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons discharged was < 45mg/m 2. Mu.m, and dioxin compounds were not detected.
Example 5
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow rate of the introduced waste gas in the embodiment is 30000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (wherein the dichloromethane content is 1500 ppm) passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, wherein the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 3m 3 The temperature of the catalyst is 150-450 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (aluminum oxide, zirconium oxide and copper oxide) can be selected in the invention;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons emitted was < 40mg/m and dioxin compounds were not detected.
Example 6
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow rate of the introduced waste gas in the embodiment is 30000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (wherein the dichloromethane content is 1500 ppm) passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, wherein the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 6m 3 The temperature of the catalyst is 150-450 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (aluminum oxide, zirconium oxide and copper oxide) can be selected in the invention;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons discharged was < 35mg/m and dioxin compounds were not detected.
Example 7
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow rate of the introduced waste gas in the embodiment is 30000m 3 And/h, wherein the waste gas containing 2000 ppm VOCs (with the dichloromethane content of 1500 ppm) firstly passes through the preheated ceramic heat accumulator A and passes through a catalyst filling module in the ceramic heat accumulator A, wherein the catalyst selected in the embodiment is vanadium oxide, and the filling amount is 6m 3 The temperature of the catalyst is 200-500 ℃, and noble metal catalysts (platinum, palladium and rhodium) and transition metal catalysts (aluminum oxide, zirconium oxide and copper oxide) can be selected in the invention;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
In this example, the concentration of non-methane total hydrocarbons discharged was < 30 mg/m 2 and dioxin compounds were not detected.
Comparative example 1
S1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the flow rate of the introduced waste gas in the embodiment is 30000m 3 And/h, wherein the waste gas contains 2000 ppm VOCs (wherein the dichloromethane content is 1500 ppm), firstly passing through a preheated ceramic heat accumulator A, and the comparative example has no catalyst module
S2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
The concentration of non-methane total hydrocarbons discharged in this example was < 70 mg/m, the dioxin compound was 0.02 ng-TEQ/m.
Experimental data were collated as follows:
according to the data of the embodiment and the comparative example, the evolution rate of VOCs waste gas can be effectively improved and the dioxin compound can be removed by adding the catalyst module, and the effect of removing the dioxin compound is better no matter the concentration of dichloromethane. When the catalyst consumption is higher, the higher the catalyst placement temperature section is, the better exhaust gas treatment effect is achieved.
The invention is used when in use:
the present invention is not limited to the above embodiments, but is capable of modification and variation in detail, and other modifications and variations can be made by those skilled in the art without departing from the scope of the present invention.
Claims (10)
1. The three-tower RTO structure comprises a combustion chamber, three regenerators and ceramic regenerators, and is characterized in that the ceramic regenerators are modified, a catalyst filling module is added in the ceramic regenerators, and a layer of filter screen is added between the catalyst filling module and the ceramic regenerators, and the waste gas treatment process is as follows:
s1: VOCs waste gas is introduced into a regenerator in a three-tower RTO, and the VOCs waste gas passes through a preheated ceramic regenerator A and is filled into a module through a catalyst in the ceramic regenerator A;
s2, enabling VOCs waste gas to enter a combustion chamber for combustion and decomposition, enabling the decomposed gas to pass through a ceramic heat accumulator B at high temperature, preheating the ceramic heat accumulator B, and discharging the decomposed clean gas while passing through the ceramic heat accumulator B;
s3, back blowing purified gas of the untreated waste gas remained in the ceramic heat accumulator A into a combustion chamber for incineration treatment, and discharging decomposed gas through the ceramic heat accumulator C, wherein the ceramic heat accumulator C is heated;
s4: the waste gas is preheated through the ceramic heat accumulator C and then enters the combustion chamber to burn, the gas after being purified in the ceramic heat accumulator B is back blown back to the combustion chamber to burn, the decomposed gas is discharged through the ceramic heat accumulator A, and meanwhile, the ceramic heat accumulator A is heated;
and (5) performing cyclic operation according to the flow.
2. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, wherein the ceramic heat accumulator modification step is as follows:
the preparation method comprises the steps of adding binder methylcellulose, lubricant tung oil, plasticizer glycerol and dispergator oleic acid into raw materials of 20 wt% cordierite, 10 wt% aluminum titanate, 10 wt% zirconite and 10 wt% silicon carbide, uniformly grinding particles, putting the particles into a mould for extrusion molding, drying and firing at high temperature.
3. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, which is characterized in that: the firing temperature of the ceramic heat accumulator is 400-500 ℃.
4. The method for treating waste gas of three-tower RTO dioxin according to claim 1, wherein the temperature of the regenerator is in the range of 30-760 ℃.
5. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, which is characterized in that: the catalyst is a transition metal oxide and a composite oxide thereof.
6. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, which is characterized in that: the filter screen is PTFE polyester coated filter paper subjected to low-temperature plasma modification treatment.
7. The method for treating waste gas of three-tower type RTO dioxin according to claim 6, which is characterized in that: the parameters of the low-temperature plasma process are as follows: low temperature plasma with energy higher than 4.4 eV.
8. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, which is characterized in that: the combustion temperature of the combustion chamber is higher than 760 ℃.
9. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, which is characterized in that: the regenerator requires a section hollow tower wind speed of not more than 2 m/s.
10. The method for treating waste gas of three-tower type RTO dioxin according to claim 1, which is characterized in that: the three-tower RTO circulation operation period is 90-180S.
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