CN206715626U - Runner high efficiency cleaning system - Google Patents
Runner high efficiency cleaning system Download PDFInfo
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- CN206715626U CN206715626U CN201720144294.4U CN201720144294U CN206715626U CN 206715626 U CN206715626 U CN 206715626U CN 201720144294 U CN201720144294 U CN 201720144294U CN 206715626 U CN206715626 U CN 206715626U
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- gas
- desorption
- runner
- incineration
- cleaning system
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- 238000004140 cleaning Methods 0.000 title claims abstract description 49
- 238000003795 desorption Methods 0.000 claims abstract description 154
- 238000001179 sorption measurement Methods 0.000 claims abstract description 98
- 239000012855 volatile organic compound Substances 0.000 claims abstract description 98
- 238000012545 processing Methods 0.000 claims abstract description 57
- 239000007789 gas Substances 0.000 claims description 251
- 238000000034 method Methods 0.000 claims description 46
- 238000000746 purification Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 15
- 230000008676 import Effects 0.000 claims description 10
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 1
- 238000010521 absorption reaction Methods 0.000 abstract description 10
- 239000000463 material Substances 0.000 description 19
- 238000002485 combustion reaction Methods 0.000 description 11
- 238000005338 heat storage Methods 0.000 description 11
- 238000009825 accumulation Methods 0.000 description 9
- 238000010586 diagram Methods 0.000 description 9
- 229910021536 Zeolite Inorganic materials 0.000 description 8
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 8
- 239000010457 zeolite Substances 0.000 description 8
- 239000012530 fluid Substances 0.000 description 7
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 6
- 150000001875 compounds Chemical class 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 150000002894 organic compounds Chemical class 0.000 description 5
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- -1 acetic acid propylene glycol monomethyl ether ester Chemical class 0.000 description 3
- 229910052878 cordierite Inorganic materials 0.000 description 3
- 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 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000000809 air pollutant Substances 0.000 description 2
- 231100001243 air pollutant Toxicity 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- FFUAGWLWBBFQJT-UHFFFAOYSA-N hexamethyldisilazane Chemical compound C[Si](C)(C)N[Si](C)(C)C FFUAGWLWBBFQJT-UHFFFAOYSA-N 0.000 description 2
- 229910052863 mullite Inorganic materials 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 102220500397 Neutral and basic amino acid transport protein rBAT_M41T_mutation Human genes 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- XSTXAVWGXDQKEL-UHFFFAOYSA-N Trichloroethylene Chemical compound ClC=C(Cl)Cl XSTXAVWGXDQKEL-UHFFFAOYSA-N 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 150000008282 halocarbons Chemical class 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000011224 oxide ceramic Substances 0.000 description 1
- 229910052574 oxide ceramic Inorganic materials 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- LLHKCFNBLRBOGN-UHFFFAOYSA-N propylene glycol methyl ether acetate Chemical compound COCC(C)OC(C)=O LLHKCFNBLRBOGN-UHFFFAOYSA-N 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Chemical group 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 230000010148 water-pollination Effects 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Treating Waste Gases (AREA)
Abstract
A kind of runner high efficiency cleaning system, it includes one first runner and a cremation facilities.First runner have one first adsorption zone and one first desorption area, the first adsorption zone to adsorb VOCs and send out one first adsorption treatment gas；Then for desorption VOCs and send out one first desorption processing gas in the first desorption area.Cremation facilities generate gas after an incineration to the VOC s burning disposals being desorbed first in processing gas.Characteristic of the present utility model is, gas is further imported the absorption end of the first runner and handles or be imported into again the desorption end of the first runner as desorption gas after the incineration that cremation facilities are discharged, reduce the flow or not even not externally discharge that gas is externally discharged after incinerating, so as to further reduce the discharge total amount of VOC.
Description
Technical field
The utility model on a kind of processing system of VOC, especially with regard to one kind using runner and
The processing system of cremation facilities.
Background technology
Organic solvent is widely used in many industries, and its partial organic solvent is readily volatilized into gas at room temperature
Body, thus it is referred to as VOC (Volatile Organic Compounds, VOCs), wherein most volatility
Organic compound has bio-toxicity, therefore externally needs to be acted upon before discharge.
The use of cremation facilities by VOC incineration process is a kind of common processing mode；Wherein, for
The relatively low source exhaust gas of content of volatile organic compound, the suction/desorption runner that can also often arrange in pairs or groups is to VOC
Carry out concentration.For existing high efficiency runner to the treatment effeciency of VOC generally up to 90-95%, its is dense
Demagnification rate is generally up to 10-25 times, that is, the more pending gas of VOC concentration that desorption gas is loaded with is high
Go out 10-25 times, these desorption gas are subsequently imported into cremation facilities, and existing cremation facilities are to VOC
Treatment effeciency is then up to 95-99%.However, it is contemplated that it is organic that 10-25 times of volatility is up to containing concentration rate in desorption gas
Compound, the incineration tail gas of cremation facilities actually still contain many VOCs.
Because environmental regulation becomes tight, discharge standard is gradually stepped up, and existing exhaust treatment system can not be fully met《It is empty
Gas total amount of pollutant control plan》Decrement standard, therefore how to improve VOC processing system processing effect
Rate, it is worth this area personage to consider in fact.
On the other hand, after incinerating volatile organic compound from waste gas using cremation facilities, the volatilization of low concentration can still be discharged
Property organic compound, and if the nitrogenous, sulfur-bearing of processing, the VOC containing halogen or containing higher boiling, can also after processing
Produce the derivative pollution things such as nitrogen oxides, oxysulfide SOx or derivative shot-like particles SS；But shown by air quality monitoring data,
The substituted suspended particulates of the derivative pollution thing such as VOC and NOx, SOx or SS, which turn into, influences air pollution index
(PSI) phenomenon of major pollutants, and be《Air pollutants total amount control plan》One of decrement project of standard development, it is therefore necessary
Strengthen the discharge of the derivative pollution thing such as control VOC and NOx, SOx or SS, these demands must also give comprehensive
Close and consider.
In order to be effectively treated to VOC, it is thus proposed that " volatility is organic by TW M444870
Thing secondary concentration processing system " new patent, it handled the first runner desorption end tail gas using incinerator in the past in order to improve
Lack caused by (such as its first figure), disclose then and utilize the second runner (such as its second figure)) or more runner (such as its 4th
Figure) handle the technology of the first runner desorption end tail gas, and the desorption end tail gas of the second runner then still passes through incinerator (its drawing
Do not illustrate) it is acted upon；In other words, the technology disclosed in TW M444870 is still related to the use of incinerator.However, due to turning
Take turns and incinerator be usually less than to the removal efficiency of VOC, although therefore TW M444870 attempt to utilize second turn
Wheel substitutes the incinerator commonly used to handle the desorption end tail gas of the first runner, but due to the VOC of the second runner
Removal efficiency is relatively low, and it adsorbs the burning compared with incinerator shown in its first figure on the contrary of VOC concentration contained by the tail gas of end
It is taller to change tail gas.Also therefore, TW M444870 not only add equipment cost (need to set up extra runner), its outer waste air
VOC concentration but go up not down, it is clear that and can not solve the problems, such as to be previously mentioned.
The content of the invention
It can not gradually meet air pollutants total amount control meter in view of existing VOC treatment technology
The standard drawn, the main purpose of the utility model are to provide a kind of efficient VOC processing system.
In order to reach above-mentioned and other purpose, the utility model provides a kind of runner high efficiency cleaning system, and it is locating
Pending gas of the reason containing VOC, and it includes one first runner and a cremation facilities.First runner has
One first adsorption zone and one first desorption area, the first adsorption zone is for importing pending gas, to adsorb in pending gas extremely
Few a part of VOC simultaneously sends out one first adsorption treatment gas；First desorption area is then for importing one first desorption
Gas, to be desorbed VOC and the desorption processing gas of submitting one first that the first runner is adsorbed.Incineration is set
Standby to have one to incinerate unit, an air inlet and an exhaust outlet, air inlet and exhaust outlet connect incineration unit, and air inlet is for importing
First desorption processing gas, incinerate unit then to by first be desorbed processing gas in VOC burning disposal
And gas after an incineration is generated, exhaust outlet is then to discharge gas after at least a part of incineration, wherein at least a part of institute
Gas is imported into first adsorption zone or the first desorption area after stating incineration.
In order to reach above-mentioned and other purpose, the utility model also provides a kind of runner high efficiency purification method, and it can be answered
For foregoing runner high efficiency cleaning system, and it includes following operation procedure：
First adsorption operation program：The pending gas containing VOC is imported to first adsorption zone,
And send out one first adsorption treatment gas after first adsorption zone adsorbs at least a part of VOC；
First desorption operation procedure：One first desorption gas is imported to the first desorption area, first desorption gas should
The VOC that first runner is adsorbed is desorbed from first runner and sends out one first desorption processing gas；And
Incinerate operation procedure：The first desorption processing gas is imported into the incineration unit via the air inlet, and warp this burn
Change the VOC burning disposal that unit is desorbed first in processing gas and generate gas after an incineration, the incineration
At least a part of of gas is discharged via the exhaust outlet afterwards, and gas is imported into first suction after the wherein at least a part of incineration
Attached area or the first desorption area.Wherein, the first adsorption operation program and the first desorption operation procedure are substantially carried out simultaneously.
Based on above-mentioned design, characteristic of the present utility model is, gas is further after the incineration that cremation facilities are discharged
The desorption end that the absorption end for importing the first runner handled or be imported into again the first runner reduces incineration as desorption gas
The flow or not even not externally discharge that gas is externally discharged afterwards, so as to further reduce the row of VOC
Go out total amount.
In other embodiment of the present utility model, gas reacts by reprocessing after the incineration that cremation facilities are discharged
Device is purified again, so that it is derivative dirty further to remove the VOC after incineration in gas, NOx, SOx or SS etc.
Contaminate the discharge capacity of thing.
Brief description of the drawings
Fig. 1 is the configuration schematic diagram of the utility model first embodiment.
Fig. 2 is the front-view schematic diagram suitable for runner of the present utility model.
Fig. 3 is the configuration schematic diagram of the utility model second embodiment.
Fig. 4 is the configuration schematic diagram of the utility model 3rd embodiment.
Fig. 5 is the front-view schematic diagram suitable for another runner of the present utility model.
Fig. 6 is the configuration schematic diagram of the utility model fourth embodiment.
Fig. 7 is the configuration schematic diagram of the embodiment of the utility model the 5th.
Embodiment
Fig. 1 is refer to, illustrated is the first of the utility model runner high efficiency cleaning system (calling cleaning system 1 in the following text)
Embodiment, it includes one first runner 10, one second runner 20, a cremation facilities 30, the heat of a first heat exchanger 40, one second
The blowdown stack 60 of exchanger 50 and one, the cleaning system 1 can be used to handle the pending gas containing VOC,
The source of the pending gas can be but be not limited to petrochemical industry processing procedure waste gas, be given up using the processing procedure waste gas and burning of organic solvent
Gas, contained VOC is probably, but is not limited to, toluene, dimethylbenzene, p-xylene, ethylbenzene, styrene,
Formaldehyde, acetaldehyde, isopropanol (IPA), acetic acid propylene glycol monomethyl ether ester (PGMEA), HMDS (HMDS, trichloro ethylene
(TCE)), MEA (MEA) and dimethyl sulfoxide (DMSO) (DMSO), other possible VOCs be probably alkanes,
Aromatic hydrocarbons, alkenes, halogenated hydrocarbon, esters, aldehydes and ketone compounds.
It please arrange in pairs or groups with reference to figure 2, the first runner 10 rotates when working in a rotation direction, and the wheel face of the first runner 10 can be according to
Work purpose divides into one first adsorption zone 11, one first desorption area 12 and 1 first and cools down isolated area 13, wherein the first cooling
Isolated area 13 is between the first adsorption zone 11 and the first desorption area 12 so that the sorbing material that the first runner 10 is carried is in work
Area 12 and first is sequentially desorbed by the first adsorption zone 11, first when making and cools down isolated area 13, used sorbing material regards institute
Depending on the VOC that need to be adsorbed, sorbing material can be but be not limited to hydrophily or different water-based zeolite, activated carbon,
Activated alumina, silica gel or its combination, wherein hydrophilic zeolite is, for example, A types, 13X types or low silica-alumina ratio y-type zeolite, different water-based
Zeolite then be, for example, ZSM-5 types, MCM types (Mobil composite of matter) or high silica alumina ratio y-type zeolite, the MCM
Type zeolite for example can be the MCM-41 of tool hexagonal crystal structure (hexagonal), the MCM-48 of tool cubic structure (cubic), tool
The M41S races such as MCM-50 of layer structure (lamellar) zeolite.
It is similar to the first runner 10, the wheel face of the second runner 20 can equally be divided into according to work purpose one second adsorption zone,
One second desorption area and one second cooling isolated area, its front-view schematic diagram is suitable with Fig. 2, and the second cooling isolated area is inhaled between second
Between attached area and the second desorption area so that the sorbing material that the second runner 20 is carried sequentially passes through the second absorption at work
The sorbing material identical or different with the first runner can be used in area, the second desorption area and the second cooling isolated area, the second runner, and
Depending on the VOC of required absorption.In addition, first, second runner 10,20 may also include other and not join substantially
With the component such as suction, the runner support of desorption, wheel shaft, support frame, do not illustrated in schema only.
Cremation facilities 30 have one to incinerate unit 31, an air inlet 32 and an exhaust outlet 33.It is applicable in the utility model
Cremation facilities include but is not limited to recovery formula direct combustion incinerator, heat accumulating type direct combustion incinerator and catalyst incinerator, wherein accumulation of heat
The common person of formula direct combustion incinerator such as dual grooved heat accumulation incinerator, three slot type heat accumulation incinerators and rotary valve type heat accumulation incinerator.
In the present embodiment, cremation facilities 30 are a dual grooved heat accumulation incinerator, thus incinerate unit 31 have two heat storage tanks 311,312 and
The combustion chamber 313 being communicated between two heat storage tanks 311,312, two heat storage tanks 311,312 respectively have an air inlet 32 and row
Gas port 33, the pipeline for linking these air inlets 32,33 are provided with control valve group (not illustrating), allow heat storage tank 311,312 one of which
Air inlet 32 is only opened, and allows another one only to open exhaust outlet 33, control valve group then controls the keying of air inlet 32, exhaust outlet 33
And periodically adjusting airflow direction so that air-flow can sequentially flow through heat storage tank 311, combustion chamber 313 and heat storage tank 312, or
Sequentially flow through heat storage tank 312, combustion chamber 313 and heat storage tank 311.Thermal medium (heat is filled with heat storage tank 311,312
Media), to carry out heat exchange with flowing through the gas of cremation facilities 30, applicable thermal medium can be but be not limited to aluminum oxide
Ceramic (Alumina Oxide Porcelain), porous mullite (Mullite), cordierite (Cordierite), porous
Cordierite and other can accumulation of heat ceramics or gravel.
First, second heat exchanger 40,50 is the out of the ordinary heat exchange for being used for two bursts of gas streams, the heat exchange of the gas stream
It is to instigate heat to be delivered to cold fluid from hot fluid, applicable heat exchanger can be but be not limited to rolled plate heat exchanger, board-like
Heat exchanger and shell-and-tube exchanger.Gas can be from the burning for incinerating unit 31 after a part of incineration of foregoing cremation facilities 30
Room 313 branches to first, second heat exchanger 40,50 and is used as foregoing hot fluid.In the present embodiment, after the incineration of hot fluid
Gas system sequentially flows through first, second heat exchanger 40,50.
Above-mentioned cleaning system 1 can be applied to runner high efficiency purification method (calling purification method in the following text), and the purification method includes
Following operation procedure：
First adsorption operation program：Pending gas containing VOC is imported the first of the first runner 10
Adsorption zone 11, at least a part of VOC, the gas after processing are adsorbed through the sorbing material in the first adsorption zone 11
Body is sent out as the first adsorption treatment gas by the opposite side of the first runner 10.
Second adsorption operation program：First adsorption treatment gas is imported to the second adsorption zone of the second runner 20 again, through
Sorbing material in two adsorption zones adsorbs at least a part of VOC, the gas after processing as the second absorption at
Process gases is sent out by the opposite side of the second runner 20.Generally only contain via the second adsorption treatment gas after adsorption treatment twice
The VOC of denier, it can be taken out by blower fan 71 toward blowdown stack 60 or make other application.
First desorption operation procedure：The sorbing material of first runner 10 has adsorbed in the first adsorption operation program quite to be counted
The VOC of amount, therefore this operation procedure imports the first desorption area of the first desorption gas to the first runner 10
12, the first desorption gas is desorbed the VOC that the first runner 10 is adsorbed, then containing height
The gas of intensity volatile organic compound is sent out as the first desorption processing gas from the opposite side of the first runner 10；In order to improve
Efficiency is desorbed, the first desorption gas can be promoted to higher temperature, therefore in the present embodiment, and the first desorption gas is into the
Before one desorption area 12, more first it is imported into the first cooling isolated area 13 and preheats, be then re-introduced into first heat exchanger 40 with burning
Gas carries out heat exchange after change；In the present embodiment, the first desorption gas is made up of cleaned air and a part of pending gas,
Only it is not limited thereto.
Second desorption operation procedure：The sorbing material of second runner 20 has adsorbed in the second adsorption operation program quite to be counted
The VOC of amount, therefore this operation procedure imports the second desorption area of the second desorption gas to the second runner 20,
The second desorption gas is desorbed the VOC that the second runner 20 is adsorbed, then contain higher concentration
The gas of VOC is sent out as the second desorption processing gas from the opposite side of the second runner 20；In order to improve desorption
Efficiency, the second desorption gas can also be promoted to higher temperature, therefore in the present embodiment, and the second desorption gas is into second
It is desorbed before area, is more imported into the preheating of the second cooling isolated area, gas after being then re-introduced into second heat exchanger 50 and incinerating
Carry out heat exchange；In the present embodiment, the second desorption gas is shunted by some of the first adsorption treatment gas；In addition,
Because the content of the VOC of the second desorption processing gas is worked as with pending gas phase, therefore can be with pending gas
The first adsorption zone 11 that the first runner 10 is imported behind body interflow carries out the first adsorption operation program, and the second desorption processing gas again
The waste heat of body can lift pending gas into the temperature before the first adsorption zone 11, reduce relative humidity, and therefore can make first
The clearance of the VOC of runner 10 improves, and now hydrophobic zeolite adsorption material preferably can be used in the first runner 10
Material.
Incinerate operation procedure：The first desorption processing gas containing high concentration VOC is by another blower fan 72
Extract and imported via air inlet 32 and incinerate unit 31, it is through incinerating unit 31 that the volatility in first desorption processing gas is organic
Gas after generation one is incinerated after compound burning disposal, some of gas is discharged by exhaust outlet 33 after incineration, and another part is burnt
Gas then uses from the shunting of combustion chamber 313 for incinerating unit 31 as heat-exchange gas after change, gas after the incineration after heat exchange
Then collaborate again with gas after the incineration discharged from exhaust outlet 33, can be closed under gas is conventional after the incineration behind interflow with pending gas
Stream, so as to which the waste heat of gas after incinerating can be used to be lifted the temperature of pending gas, its relative humidity is reduced, and be subsequently imported into
When first adsorption zone 11 of the first runner 10 carries out the first adsorption operation program again, there can be higher adsorption efficiency.
Working characteristics based on runner, foregoing first adsorption operation program, the second adsorption operation program, the first desorption operation
Program and the second desorption operation procedure are substantially simultaneous.In the case of generally, it is also essence to incinerate operation procedure
It is simultaneous.
In a numerical simulation, the cleaning system 1 is imported into 2000SCMM pending gas, and wherein volatility has
Machine compounds content is 20ppmv, after the second of pending gas and 100SCMM is desorbed processing gas and 125SCMM incineration
Behind gas interflow, the concentration of VOC is about 17.6ppmv, and wherein 2100SCMM is imported into the first runner 10
First adsorption zone carries out the first adsorption operation program, and 125SCMM pending gas is imported into the first desorption area and taken off as first
Attached gas simultaneously carries out the first desorption operation procedure；Wherein, the VOC clearance of the first runner 10 is 95%, dense
Demagnification rate is about 18 times, and the VOC clearance of the second runner 20 is 90%, and concentration rate is about 19 times, is incinerated
The VOC clearance of equipment 30 is 98%；On this condition, 2100SCMM the first adsorption treatment gas
Content of volatile organic compound can be reduced to 0.88ppmv, and wherein 2000SCMM the first adsorption treatment gas is imported into second turn
Second adsorption zone of wheel 20 carries out the second adsorption operation program, the volatile organic compound of the second adsorption treatment gas after processing
Thing content can further be reduced to about 0.09ppmv, and import blowdown stack 60 with 2000SCMM flow；On the other hand,
100SCMM the first adsorption treatment gas is imported into the second desorption area of the second runner 20 as the second desorption gas and carries out the
Two desorption operation procedures, then send out 100SCMM the second desorption processing gas, and its VOC concentration is about
17ppmv, and with pending gas mixing, improve its temperature and reduce its relative humidity；In addition, the first desorption operation procedure
In the first desorption processing gas sent out, the concentration of VOC is about 320ppmv, and with 125SCMM stream
Amount imports cremation facilities 30 and carries out incineration operation procedure, after wherein 15SCMM high temperature incinerates gas be sequentially oriented to first, the
Two heat exchangers 40,50 are used as heat exchange, and gas collaborates after then being incinerated again with remaining 110SCMM, turns into total flow
125SCMM, VOC concentration about 6.4ppmv incineration after gas, then again with pending gas mixing again
Processing.
Finally, blowdown stack is with total amount 2000SCMM, VOC concentration about 0.09ppmv emission
Externally discharge, that is, the VOC total removal rate of this cleaning system is up to more than 99.5%, is very excellent
Treatment effeciency.
Compared to cleaning system is commonly used, this cleaning system is not in the case where additionally increasing cremation facilities, the row of significantly reducing
The VOC concentration of tail gas is put, and heat energy can be reclaimed fully, so as to realize the effect of energy-conservation.Further, since often
Lower the second adsorption treatment gas only after the processing of the second runner of rule can be discharged externally, and gas is not discharged externally then after incineration,
It thereby can further reduce the content of the VOC of emission.
It refer to Fig. 3, illustrated is the second embodiment of the utility model cleaning system, the cleaning system 400 and the
The Main Differences of one embodiment are, eliminate second heat exchanger, and a part of of the second adsorption treatment gas shunts, and with
Gas interflow is used as the second desorption gas after incineration after heat exchange, and the second desorption area for being then directed into the second runner 420 is entered
Row second is desorbed operation procedure.Advantage of this embodiment is that further save heat exchanger build and safeguard into
This, and heat energy is more fully utilized, realize the purpose of energy-conservation.
In a numerical simulation, the cleaning system 400 is imported into 2000SCMM pending gas, wherein volatility
Organic compound content is 20ppmv, the second desorption processing gas of pending gas and 115SCMM and 110SCMM incineration
Afterwards behind gas interflow, the concentration of VOC is about 17.6ppmv, and wherein 2100SCMM is imported into the first runner 410
The first adsorption zone carry out the first adsorption operation program, 125SCMM pending gas is imported into the first desorption area as first
Desorption gas simultaneously carries out the first desorption operation procedure；Wherein, the VOC clearance of the first runner 410 is
95%, concentration rate is about 18 times, and the VOC clearance of the second runner 420 is 90%, and concentration rate is about
19 times, the VOC clearance of cremation facilities 430 is 98%；On this condition, 2100SCMM the first absorption
The content of volatile organic compound of processing gas can be reduced to 0.88ppmv, be then directed into the second absorption of the second runner 420
Area carries out the second adsorption operation program, and the content of volatile organic compound of the second adsorption treatment gas after processing can be further
About 0.09ppmv is reduced to, and blowdown stack 460 is imported with 2000SCMM flow；On the other hand, at 100SCMM the second absorption
The gas interflow after the incineration of heat exchange process is used as the second desorption gas to process gases with 15SCMM, and is imported into the second runner
420 the second desorption area carries out the second desorption operation procedure, then sends out 115SCMM the second desorption processing gas, it volatilizees
Property organic compound concentrations are about 17ppmv, then again with pending gas mixing, improve its temperature and to reduce its relative
Humidity；In addition, in the first desorption processing gas that the first desorption operation procedure is sent out, the concentration of VOC is about
For 320ppmv, and cremation facilities 430 are imported with 125SCMM flow and carry out incineration operation procedure, wherein 15SCMM high temperature burns
Gas is directed to first heat exchanger 440 as heat exchange and is used after change, then the second adsorption treatment with foregoing 100SCMM again
Gas interflow is used as the second desorption gas.On the other hand, remaining 110SCMM, VOC concentration about 6.4ppmv
Incineration after gas and pending gas mixing and import the first runner 410 again and carry out the first adsorption operation program.
Finally, blowdown stack is with total amount 2000SCMM, VOC concentration about 0.09ppmv emission
Externally discharge, that is, the present embodiment still can reach the high efficiency similar to first embodiment after a heat exchanger is omitted
Processing is horizontal.
Fig. 4 is refer to, illustrated is the 3rd embodiment of the utility model cleaning system, and the cleaning system 500 includes
One first runner 510, one second runner 520, a cremation facilities 530, again and again a heat exchanger 540, purification reactor 550 and one
Ozone supply unit 560.
It please arrange in pairs or groups and be rotated with reference to figure 5, the first runner 510 when working in a rotation direction, the wheel face of the first runner 510 can
One first adsorption zone 511 and one first desorption area 512 are divided into according to work purpose so that the absorption that the first runner 510 is carried
Material sequentially passes through the first adsorption zone 511 and the first desorption area 512 at work.In the present embodiment, the first runner 510 is substantial
Only it is made up of the first adsorption zone 511 and the first desorption area 512, without including cooling down isolated area, only the first runner 510 may also include
Other do not participate in the components such as suction, the runner support of desorption, wheel shaft, support frame substantially, are not illustrated in schema only.
Second runner 520 can according to work purpose divide into one second adsorption zone, one second desorption area and one second cooling every
From area, its front-view schematic diagram is suitable with Fig. 2, and the second cooling isolated area is between the second adsorption zone and the second desorption area so that
The sorbing material that second runner 520 is carried at work sequentially by the second adsorption zone, second desorption area and second cooling every
From area.
Cremation facilities 530 have one to incinerate unit 531, an air inlet 532 and an exhaust outlet 533.In the present embodiment, incinerate
Equipment 530 is a rotary valve type heat accumulation incinerator, therefore incinerates unit 531 and include a rotary valve 5311, multiple be filled with accumulation of heat
The combustion chamber 5313 of heat storage tank 5312 and one of material, heat storage tank 5312 are communicated between rotary valve 5311 and combustion chamber 5313, entered
Gas port 532 and exhaust outlet 533 are then located at rotary valve 5311.
Heat exchanger 540 is the heat exchange for two bursts of gas streams, and the heat exchange of the gas stream is to instigate heat from heat
Fluid is delivered to cold fluid, and gas can be from the combustion chamber 5313 for incinerating unit 531 after a part of incineration of foregoing cremation facilities 530
Branch to heat exchanger 540 and be used as foregoing hot fluid.
The gas to after incinerating to ozone supply of ozone supply unit 560, then purification reactor 550 have a reative cell
551 and a water feed unit 552 in the reative cell 551, water feed unit 552 be, for example, a sprayer and can be used to improve
Vapor content in reative cell 551, catalyst adsorption material 553 can be separately provided with reative cell 551.
Above-mentioned cleaning system 500 can be applied to following purification methods, and the purification method includes following operation procedure：
First adsorption operation program：Pending gas containing VOC is imported the of the first runner 510
One adsorption zone 511, at least a part of VOC is adsorbed through the sorbing material in the first adsorption zone 511, after processing
Gas as the first adsorption treatment gas by the first runner 510 opposite side send out.
Second adsorption operation program：First adsorption treatment gas is imported to the second adsorption zone of the second runner 520 again, through
Sorbing material in two adsorption zones adsorbs at least a part of VOC, the gas after processing as the second absorption at
Process gases is sent out by the opposite side of the second runner 520.Generally only contain via the second adsorption treatment gas after adsorption treatment twice
There is the VOC of denier, can be taken out by blower fan 571 toward blowdown stack or make other application.
First desorption operation procedure：The sorbing material of first runner 510 has adsorbed quite in the first adsorption operation program
The VOC of quantity, therefore this operation procedure imports the first desorption of the first desorption gas to the first runner 510
Area 512, the first desorption gas is desorbed the VOC that the first runner 510 is adsorbed, then contain
The gas for having high concentration VOC is sent out as the first desorption processing gas from the opposite side of the first runner 510.
Second desorption operation procedure：The sorbing material of second runner 520 has adsorbed quite in the second adsorption operation program
The VOC of quantity, therefore this operation procedure imports the second desorption of the second desorption gas to the second runner 520
Area, the second desorption gas is set to be desorbed the VOC that the second runner 520 is adsorbed, then containing higher
The gas of intensity volatile organic compound is sent out as the second desorption processing gas from the opposite side of the second runner 520；In order to carry
Height desorption efficiency, the second desorption gas can be promoted to higher temperature, therefore in the present embodiment, the second desorption gas is entering
Before second desorption area, the preheating of the second cooling isolated area is more imported into, gas after being then re-introduced into heat exchanger 540 and incinerating
Carry out heat exchange；In the present embodiment, the second desorption gas is shunted by some of the first adsorption treatment gas, and second
Desorption processing gas carries on as before and has higher temperature, therefore can directly be imported into the first desorption conduct of area 512 of the first runner 510
First desorption gas uses.
Incinerate operation procedure：The first desorption processing gas containing high concentration VOC is by another blower fan
572 extract and are imported via air inlet 532 and incinerate unit 531, through incinerating unit 531 by the volatilization in the first desorption processing gas
Property organic compound burning disposal after generation one incinerate after gas, after incineration gas some discharged by exhaust outlet 533, it is another
Gas then uses from the shunting of combustion chamber 5313 for incinerating unit 531 as heat-exchange gas after part is incinerated, and passes through heat exchanger
Gas contains a small amount of VOC after 540 incineration, therefore can be led the first adsorption zone of past first runner 510
511 are handled again, after the incineration gas import before the first runner 510 and can first with pending gas mixing.
Operation procedure is purified again：Ozone is imported into reative cell 551, make ozone and aqueous vapor can in reative cell 551 effect and
Generate high activity hydroxyl free radical, and then can by NOx that may be present in gas after incineration it is (not soluble in water) purification reaction into
Nitric acid (highly-water-soluble) or will likely existing SOx purification reactions (not soluble in water) into sulfuric acid (highly-water-soluble) or will likely deposit
Higher boiling organic suspension particulate SS purification reactions into carbon dioxide and water, finally send out gas after a purification.
Working characteristics based on runner, foregoing first adsorption operation program, the second adsorption operation program, the first desorption operation
Program and the second desorption operation procedure are substantially simultaneous.In the case of generally, incinerate operation procedure and purify again
Operation procedure is also that essence is simultaneous.
In a numerical simulation, VOC of the gas original containing 4.24ppmv after incineration, 100ppmv
NOx, 5ppmv SOx and 1mg/Nm3 SS, it can be purified after purified treatment again as the only volatile organic containing 0.424ppmv
Compound, 20ppmv NOx, 0.5ppmv SOx and 0.5mg/Nm3 SS.Thereby, the air of emission is further reduced
Pollutant concentration.
Based on previous designs, the second adsorption treatment gas and purify reaction again that the second runner of the present embodiment 520 is sent out
Gas all only contains micro VOC after the purification that room 550 is sent out, can be external directly as emission
Discharge.Compared to cleaning system is commonly used, this cleaning system significantly reduces discharge in the case where additionally not increasing cremation facilities
The VOC concentration of tail gas, and heat energy can be reclaimed fully, realize the effect of energy-conservation.
It refer to Fig. 6, illustrated is the fourth embodiment of the utility model cleaning system, the cleaning system of the present embodiment
600 is most identical with 3rd embodiment, is in place of difference, flows through gas after the incineration of heat exchanger 640 and does not re-direct the
First adsorption zone of one runner 610, and cleaning system 600 further includes a thermometer 671, a control valve 672 and a controller
673, controller 673 is connected with thermometer 671 and the signal of control valve 672 respectively, and thermometer 671 is detecting the first desorption gas
Temperature, control valve 672 then collaborates to the flow of the second desorption processing gas, control to adjust gas after the incineration after heat exchange
Device 673 processed then controls control valve 672 to adjust aforementioned flow according to the temperature that thermometer 671 is sensed, and wherein not with second
After the incineration at desorption processing gas interflow gas then with gas interflow after incineration discharge from exhaust outlet 633.
Accordingly, if thermometer 671 measures the temperature of the first desorption gas less than acquiescence operating temperature, controller 673
Control valve 672 can be controlled, control valve is heightened the flow of the desorption processing gas of gas flow second after incineration, due to gas after incineration
The temperature of body is desorbed the temperature of processing gas higher than second, therefore the temperature of the first desorption gas after flow adjusts must can carry
Rise, until being warming up to acquiescence operating temperature.
It refer to Fig. 7, illustrated is the 5th embodiment of the utility model cleaning system, the cleaning system of the present embodiment
700 are characterized mainly in that, cremation facilities 730 are one or three slot type heat accumulation incinerators, and flow through the incineration of first heat exchanger 740
Gas does not re-direct another heat exchanger afterwards, and directly collaborates with gas after the incineration discharged from exhaust outlet 733；Replace
Ground, cleaning system 700 separately include one to raise the heating device 770 of the second desorption gas temperature, heating device 770 can be but
The heat exchanger of other forms is not limited to, its thermal source can be steam, deep fat, hot-air or electric heating；In addition, burning behind interflow
After gas is first via purification reactor 760 is purified operation procedure again again after change, after more collaborating with the first adsorption treatment gas,
The second adsorption zone for being imported into the second runner 720 carries out the second adsorption operation program, thereby further reduces volatile organic
After compound concentration, just externally discharge, and there is very excellent VOC clearance.
Finally, it is necessary to illustrate again, the utility model is only to lift in preceding taking off constituent components disclosed in embodiment
Example explanation, not it is used for limiting the scope of this case, the replacement of other equivalent elements or change, also should be this case applies for a patent model
Enclose and covered.
Claims (22)
1. a kind of runner high efficiency cleaning system, to handle the pending gas for containing VOC, including：
One first runner, there is one first adsorption zone and one first desorption area, first adsorption zone is for importing the pending gas
Body, to adsorb at least a part of VOC in the pending gas and send out one first adsorption treatment gas
Body；The first desorption area is for importing one first desorption gas, to be desorbed the volatile organic compound that first runner is adsorbed
Thing simultaneously sends out one first desorption processing gas；And
One cremation facilities, there is an incineration unit, an air inlet and an exhaust outlet, the air inlet and exhaust outlet to connect the incineration
Unit, the air inlet is for importing the first desorption processing gas, and the incineration unit is to by the first desorption processing gas
VOC burning disposal and generate gas after an incineration, the exhaust outlet is discharging at least a part of incineration
Gas afterwards, gas is imported into first adsorption zone or the first desorption area after the wherein at least a part of incineration.
2. runner high efficiency cleaning system as claimed in claim 1, further include one second runner, have one second adsorption zone and
One second desorption area, second adsorption zone is for importing the first adsorption treatment gas, to adsorb the first adsorption treatment gas
In at least a part of VOC and send out one second adsorption treatment gas；The second desorption area is for importing one the
Two desorption gas, to be desorbed VOC and the desorption processing gas of submitting one second that second runner is adsorbed
Body.
3. runner high efficiency cleaning system as claimed in claim 2, wherein some of the first adsorption treatment gas point
Stream is used as second desorption gas.
4. runner high efficiency cleaning system as claimed in claim 2, at the second desorption that wherein the second desorption area is sent out
Process gases is imported into the first adsorption zone of first runner.
5. runner high efficiency cleaning system as claimed in claim 1, wherein first runner are with more one between first suction
The first cooling isolated area between attached area and the first desorption area, first desorption gas are first between the first desorption area is imported
It is imported into the first cooling isolated area.
6. runner high efficiency cleaning system as claimed in claim 2, wherein second runner are with more one between second suction
The second cooling isolated area between attached area and the second desorption area, second desorption gas are first between the second desorption area is imported
It is imported into the second cooling isolated area.
7. runner high efficiency cleaning system as claimed in claim 2, further include a first heat exchanger, gas after the incineration
Some is sent out from the incineration unit and flows through the first heat exchanger, first desorption gas import this first be desorbed
The first heat exchanger is first imported into before area and carries out heat exchange with gas after the incineration.
8. runner high efficiency cleaning system as claimed in claim 7, further include a second heat exchanger, gas after the incineration
Some is sent out from the incineration unit and flows through the second heat exchanger, second desorption gas import this second be desorbed
The second heat exchanger is first imported into before area and carries out heat exchange with gas after the incineration.
9. runner high efficiency cleaning system as claimed in claim 8, wherein after the incineration sent out from the incineration unit gas according to
Sequence flows through first, second heat exchanger.
10. runner high efficiency cleaning system as claimed in claim 8 or 9, wherein flowing through first, second heat exchanger extremely
After the incineration of few one of which gas again with gas interflow after incineration discharge from the exhaust outlet.
11. runner high efficiency cleaning system as claimed in claim 1, wherein gas is imported into first runner after the incineration
The first adsorption zone.
12. runner high efficiency cleaning system as claimed in claim 10, wherein gas is imported into after incineration behind the interflow
First adsorption zone of first runner.
13. the runner high efficiency cleaning system as described in claim 2 or 6, wherein one of described second adsorption treatment gas portion
Part shunting is used as second desorption gas.
14. runner high efficiency cleaning system as claimed in claim 2, wherein after the incineration gas it is a part of from the incineration
Unit is sent out, and is sent after a part of shunting of the first, second adsorption treatment gas one of which with described from the incineration unit
Gas collaborates and is used as second desorption gas after the incineration gone out.
15. runner high efficiency cleaning system as claimed in claim 2, it is first de- that the second desorption processing gas is imported into this
Attached area and be used as first desorption gas.
16. runner high efficiency cleaning system as claimed in claim 15, a heat exchanger is further included, gas after the incineration
Some is sent out from the incineration unit and flows through the heat exchanger, and second desorption gas is before the second desorption area is imported
First it is imported into the heat exchanger and carries out heat exchange with gas after the incineration.
17. runner high efficiency cleaning system as claimed in claim 2, a heat exchanger is further included, gas after the incineration
Some is sent out from the incineration unit and flows through the heat exchanger, and second desorption gas is before the second desorption area is imported
First it is imported into the heat exchanger and carries out heat exchange, at least one of gas after the incineration after heat exchange with gas after the incineration
Part is collaborated with the described second desorption processing gas and is imported into the first desorption area and is used as first desorption gas.
18. runner high efficiency cleaning system as claimed in claim 17, further include a thermometer, a control valve and a control
Device, the controller are connected with the thermometer and the control valve signal, and the thermometer is detecting the temperature of first desorption gas
Degree, the control valve are collaborated to the flow of the second desorption processing gas to adjust gas after the incineration, and the controller is to root
The control valve is controlled to adjust the flow according to the temperature that the thermometer is sensed.
19. runner high efficiency cleaning system as claimed in claim 2, further includes a heating device, to improve described second
The temperature of desorption gas.
20. the runner high efficiency cleaning system as described in any one in claim 15 to 18, wherein first runner essence by
The adsorption zone and the desorption district's groups into.
21. runner high efficiency cleaning system as claimed in claim 1 or 2, further includes purification reactor again and again and an ozone supplies
To unit, the ozone supply unit is to gas after ozone supply to the incineration, and purification reactor has a reative cell again for this
And gas after the importing incineration ozoniferous is supplied, gas after the incineration ozoniferous to be purified again and sends out a purification
Gas afterwards.
22. runner high efficiency cleaning system as claimed in claim 21, wherein this purification reactor supplies with more a water again
Unit, to improve the vapor content in the reative cell.
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|---|---|---|---|
| CN201720144294.4U CN206715626U (en) | 2017-02-17 | 2017-02-17 | Runner high efficiency cleaning system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720144294.4U CN206715626U (en) | 2017-02-17 | 2017-02-17 | Runner high efficiency cleaning system |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108452637A (en) * | 2017-02-17 | 2018-08-28 | 杰智环境科技股份有限公司 | Tandem runner high efficiency purification system and tandem runner high efficiency purification method |
| CN110201489A (en) * | 2018-02-28 | 2019-09-06 | 中微惠创科技（上海）有限公司 | A kind of vinyl chloride exhaust treatment system and a kind of gas concentration unit |
| CN114432836A (en) * | 2020-11-06 | 2022-05-06 | 杰智环境科技股份有限公司 | Organic waste gas adsorption, desorption, concentration and purification system and method capable of returning temperature and controlling humidity |
| CN115405941A (en) * | 2022-08-30 | 2022-11-29 | 江苏乾宏环保科技有限公司 | Double-tower alternate heat accumulation type RTO waste gas incineration device and incineration method thereof |
| TWI836468B (en) * | 2021-08-12 | 2024-03-21 | 莊錦烽 | High-efficiency exhaust gas purification system and high-efficiency exhaust gas purification method |
-
2017
- 2017-02-17 CN CN201720144294.4U patent/CN206715626U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108452637A (en) * | 2017-02-17 | 2018-08-28 | 杰智环境科技股份有限公司 | Tandem runner high efficiency purification system and tandem runner high efficiency purification method |
| CN110201489A (en) * | 2018-02-28 | 2019-09-06 | 中微惠创科技（上海）有限公司 | A kind of vinyl chloride exhaust treatment system and a kind of gas concentration unit |
| CN110201489B (en) * | 2018-02-28 | 2021-10-22 | 中微惠创科技（上海）有限公司 | Chloroethylene tail gas treatment system and gas concentration device |
| CN114432836A (en) * | 2020-11-06 | 2022-05-06 | 杰智环境科技股份有限公司 | Organic waste gas adsorption, desorption, concentration and purification system and method capable of returning temperature and controlling humidity |
| TWI836468B (en) * | 2021-08-12 | 2024-03-21 | 莊錦烽 | High-efficiency exhaust gas purification system and high-efficiency exhaust gas purification method |
| CN115405941A (en) * | 2022-08-30 | 2022-11-29 | 江苏乾宏环保科技有限公司 | Double-tower alternate heat accumulation type RTO waste gas incineration device and incineration method thereof |
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