CN108452637A - Tandem runner high efficiency purification system and tandem runner high efficiency purification method - Google Patents
Tandem runner high efficiency purification system and tandem runner high efficiency purification method Download PDFInfo
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- CN108452637A CN108452637A CN201710086333.4A CN201710086333A CN108452637A CN 108452637 A CN108452637 A CN 108452637A CN 201710086333 A CN201710086333 A CN 201710086333A CN 108452637 A CN108452637 A CN 108452637A
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- gas
- desorption
- runner
- incineration
- tandem
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- 238000000746 purification Methods 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims description 85
- 238000003795 desorption Methods 0.000 claims abstract description 211
- 238000001179 sorption measurement Methods 0.000 claims abstract description 146
- 239000012855 volatile organic compound Substances 0.000 claims abstract description 119
- 238000012545 processing Methods 0.000 claims abstract description 72
- 238000010521 absorption reaction Methods 0.000 claims abstract description 19
- 230000008676 import Effects 0.000 claims description 22
- 238000001816 cooling Methods 0.000 claims description 20
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 150000002894 organic compounds Chemical class 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 222
- 239000000463 material Substances 0.000 description 20
- 238000010586 diagram Methods 0.000 description 12
- 238000002485 combustion reaction Methods 0.000 description 11
- 238000005338 heat storage Methods 0.000 description 11
- 238000009825 accumulation Methods 0.000 description 8
- 239000010457 zeolite Substances 0.000 description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 7
- 239000012530 fluid Substances 0.000 description 7
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 6
- 229910021536 Zeolite Inorganic materials 0.000 description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 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
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000004088 simulation 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
- 238000009835 boiling Methods 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 150000001875 compounds Chemical class 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
- 239000002245 particle Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-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
- 239000000809 air pollutant Substances 0.000 description 2
- 231100001243 air pollutant Toxicity 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 229910052878 cordierite Inorganic materials 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 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 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
- 239000000284 extract Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 229910052863 mullite Inorganic materials 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 239000000725 suspension Substances 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
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 102220500397 Neutral and basic amino acid transport protein rBAT_M41T_mutation Human genes 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-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
- SYWDWCWQXBUCOP-UHFFFAOYSA-N benzene;ethene Chemical group C=C.C1=CC=CC=C1 SYWDWCWQXBUCOP-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 230000003694 hair properties Effects 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
- FFUAGWLWBBFQJT-UHFFFAOYSA-N hexamethyldisilazane Chemical compound C[Si](C)(C)N[Si](C)(C)C FFUAGWLWBBFQJT-UHFFFAOYSA-N 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen 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
- 150000003254 radicals Chemical class 0.000 description 1
- 239000012495 reaction gas Substances 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
- 239000004575 stone 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
- 238000010792 warming Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 230000010148 water-pollination Effects 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
- B01D53/02—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
- B01D53/06—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 moving adsorbents, e.g. rotating beds
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
-
- 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
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
A kind of tandem runner high efficiency purification system comprising one first runner, one second 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.Second runner has one second adsorption zone and one second desorption area, and the second adsorption zone is adsorbing the VOCs in the first adsorption treatment gas.The VOCs burning disposals that first is desorbed in processing gas being generated gas after an incineration by cremation facilities.The characteristic of the present invention is that the absorption end tail gas of the first runner can carry out second of adsorption treatment via the second runner, to which the VOCs concentration of the second runner absorption end tail gas can be greatly reduced, achievees the purpose that high efficiency is handled.
Description
Technical field
Processing system and method for the present invention about a kind of volatile organic compounds, especially in regard to a kind of application runner and
The processing system and method for cremation facilities.
Background technology
Organic solvent is widely used in many industries, and partial organic solvent is readily volatilized at gas at room temperature
Body, thus it is referred to as volatile organic compounds (Volatile Organic Compounds, VOCs), wherein most volatility
Organic compound has bio-toxicity, therefore externally needs to be pocessed before discharge.
The use of cremation facilities by volatile organic compounds incineration process is a kind of common processing mode；Wherein, for
The lower source exhaust gas of content of volatile organic compound, the suction/desorption runner that can also often arrange in pairs or groups is to volatile organic compounds
Carry out concentration.Existing high efficiency runner to the treatment effeciency of volatile organic compounds usually up to 90-95%, it is dense
Demagnification rate is usually up to 10-25 times, that is, the more pending gas of volatile organic compounds 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 volatile organic compounds
Treatment effeciency is then up to 95-99%.However, it is contemplated that it is organic to be up to containing concentration rate 10-25 times of volatility in desorption gas
The incineration tail gas of compound, cremation facilities actually still contains many volatile organic compounds.
Since environmental regulation becomes tight, discharge standard is gradually increased, 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 volatile organic compounds processing system processing effect
Rate, real set occurrence obtain what this field personage considered.
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 volatile organic compounds containing halogen or containing higher boiling, can also after processing
Generate the derivative pollutions objects such as nitrogen oxides, oxysulfide SOx or derivative shot-like particles SS；But it is shown by air quality monitoring data,
The substituted suspended particulates of the derivative pollutions object such as volatile organic compounds and NOx, SOx or SS, which become, influences air pollution index
(PSI) the phenomenon that major pollutants, and be《Air pollutants total amount control plan》One of decrement project of standard development, therefore it is necessary
Reinforce the discharge of the derivative pollutions object such as control volatile organic compounds and NOx, SOx or SS, these demands must also give comprehensive
It closes and considers.
In order to be effectively treated to volatile organic compounds, it is thus proposed that " volatility is organic by TW M444870
End tail gas was desorbed to handle the first runner using incinerator in the past in order to improve in object secondary concentration processing system " new patent
Missing, discloses and utilizes the second runner (such as its second figure) then caused by (such as its first figure)) or more runner (such as its 4th
Figure) come handle the first runner be desorbed end tail gas technology, and the desorption end tail gas of the second runner then still penetrate incinerator (its drawing
It is not painted) it is pocessed；In other words, the revealed technologies of TW M444870 are still related to the use of incinerator.However, due to turning
Wheel is usually less than incinerator to the removal efficiency of volatile organic compounds, although therefore TW M444870 attempt to utilize second turn
Wheel replaces the incinerator commonly used to handle the desorption end tail gas of the first runner, but due to the volatile organic compounds of the second runner
Removal efficiency is relatively low, adsorbs the burning compared with incinerator shown in its first figure instead of volatile organic compounds concentration contained by the tail gas of end
It is taller to change tail gas.Also therefore, TW M444870 not only increase equipment cost (need to add additional runner), outer waste air
Volatile organic compounds concentration but go up not down, it is clear that and can not solve the problems, such as to be previously mentioned.
Invention content
It can not gradually meet air pollutants total amount control meter in view of existing volatile organic compounds treatment technology
The standard drawn, the main purpose of the present invention are to be to provide a kind of efficient volatile organic compounds processing system and side
Method.
In order to reach above-mentioned and other purposes, the present invention provides a kind of tandem runner high efficiency purification system, to
Pending gas of the processing containing volatile organic compounds, and it includes one first runner, one second runner and a cremation facilities.
There is first runner one first adsorption zone and one first desorption area, the first adsorption zone to be waited for for importing pending gas to adsorb
At least a part of volatile organic compounds and one first adsorption treatment gas of submitting in processing gas；First desorption area is then for leading
Enter one first desorption gas, the volatile organic compounds and submitting one first desorption processing that the first runner is adsorbed is desorbed
Gas.Second runner have one second adsorption zone and one second desorption area, the second adsorption zone for import the first adsorption treatment gas,
To adsorb at least a part of volatile organic compounds in the first adsorption treatment gas and send out one second adsorption treatment gas
Body；Second desorption area is then for importing one second desorption gas, the volatile organic compounds that the second runner is adsorbed is desorbed
And send out one second desorption processing gas.Cremation facilities have one to incinerate unit, an air inlet and an exhaust outlet, air inlet and row
Gas port be connected to incinerate unit, air inlet for import first desorption processing gas, incinerate unit then to by the first desorption processing
Volatile organic compounds burning disposal in gas and generate gas after an incineration, exhaust outlet is then at least a part of to be discharged
Gas after the incineration.
In order to reach above-mentioned and other purposes, the present invention also provides a kind of tandem runner high efficiency purification methods, can
Applied to aforementioned tandem runner high efficiency purification system, and it includes following operation procedure：
First adsorption operation program：The pending gas containing volatile organic compounds is imported to first adsorption zone,
And send out one first adsorption treatment gas after first adsorption zone adsorbs at least a part of volatile organic compounds；
Second adsorption operation program：The first adsorption treatment gas is directed into second adsorption zone, and through this second
Adsorption zone sends out one second adsorption treatment gas after adsorbing at least a part of volatile organic compounds；
First desorption operation procedure：One first desorption gas is imported to the first desorption area, which should
The volatile organic compounds that first runner is adsorbed is desorbed from first runner and sends out one first desorption processing gas；
Second desorption operation procedure：One second desorption gas is imported to the second desorption area, which should
The volatile organic compounds that second runner is adsorbed is desorbed from second runner and sends out one second desorption processing gas；And
Incinerate operation procedure：The first desorption processing gas is imported into the incineration unit via the air inlet, and is burnt through this
Change unit and the volatile organic compounds burning disposal that first is desorbed in processing gas is generated to gas after an incineration, the incineration
At least a part of of gas is discharged via the exhaust outlet afterwards.Wherein, the first adsorption operation program, the second adsorption operation journey
Sequence, the first desorption operation procedure and the second desorption operation procedure substantially system are carried out at the same time.
Based on above-mentioned design, characteristic of the invention is, absorption end tail gas (i.e. the first adsorption treatment gas of the first runner
Body) second of adsorption treatment can be carried out via the second runner, to which the second runner adsorbs end tail gas (i.e. the second adsorption treatment gas
Body) volatile organic compounds concentration can substantially be less than located by prior art concentration of emission, reach volatile organic compounds height
The purpose of efficiency processing.
The present invention other embodiment in, after the incineration that cremation facilities are discharged gas by further import first or
The desorption end that the absorption end of second runner handled or be imported into again first or second runner reduces and burns as desorption gas
The flow or be not discharged externally even that gas is externally discharged after change, to further reduce volatile organic compounds
Total amount is discharged.
The present invention other embodiment in, after the incineration that cremation facilities are discharged gas by reprocessing reactor into
Row purifies again, thus the derivative pollutions object such as volatile organic compounds, NOx, SOx or SS after further removal is incinerated in gas
Discharge capacity.
Description of the drawings
Fig. 1 is the configuration schematic diagram of first embodiment of the invention.
Fig. 2 is the front-view schematic diagram for being suitable for the invention runner.
Fig. 3 is the configuration schematic diagram of second embodiment of the invention.
Fig. 4 is the configuration schematic diagram of third embodiment of the invention.
Fig. 5 is the configuration schematic diagram of fourth embodiment of the invention.
Fig. 6 is the configuration schematic diagram of fifth embodiment of the invention.
Fig. 7 is the front-view schematic diagram for being suitable for the invention another runner.
Fig. 8 is the configuration schematic diagram of sixth embodiment of the invention.
Fig. 9 is the configuration schematic diagram of seventh embodiment of the invention.
Figure 10 is the configuration schematic diagram of eighth embodiment of the invention.
Specific implementation mode
Above referring to FIG. 1, illustrated is tandem runner high efficiency purification system (calling purification system 1 in the following text) of the present invention
First embodiment comprising one first runner 10, one second runner 20, a cremation facilities 30, a first heat exchanger 40,1
Two heat exchangers 50 and a blowdown stack 60, the purification system 1 can be used to handle containing the pending of volatile organic compounds
The source of gas, the pending gas can be but be not limited to petrochemical industry processing procedure exhaust gas, using the processing procedure exhaust gas of organic solvent and combustion
Exhaust gas is burnt, contained volatile organic compounds may be, but be not limited to, toluene, dimethylbenzene, p-xylene, ethylbenzene, benzene
Ethylene, formaldehyde, acetaldehyde, isopropanol (IPA), acetic acid propylene glycol monomethyl ether ester (PGMEA), hexamethyldisilazane (HMDS), trichlorine
Ethylene (TCE), monoethanolamine (MEA) and dimethyl sulfoxide (DMSO) (DMSO), other possible volatile organic compounds may be alkane
Class, 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 one first cooling isolated area 13, wherein the first cooling
Isolated area 13 is desorbed between the first adsorption zone 11 and first between 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 volatile organic compounds that need to be adsorbed, sorbing material can be but be not limited to hydrophily or different aqueous zeolite, activated carbon,
Activated alumina, silica gel or combinations thereof, wherein hydrophilic zeolite are, for example, A types, 13X types or low silica-alumina ratio y-type zeolite, different water
Property zeolite then be, for example, ZSM-5 types, MCM types (Mobil composite of matter) or high silica alumina ratio y-type zeolite, it is described
MCM type zeolites may be, for example, tool hexagonal crystal structure (hexagonal) MCM-41, tool cubic structure (cubic) MCM-48,
Have the M41S races zeolites such as the MCM-50 of layer structure (lamellar).
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, 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 volatile organic compounds of required absorption.In addition, the first, second runner 10,20 may also include other and not join substantially
With the components such as suction, the runner holder of desorption, wheel shaft, supporting rack, it is not painted in schema only.
Cremation facilities 30 have one to incinerate unit 31, an air inlet 32 and an exhaust outlet 33.In the present invention, applicable incineration
Equipment includes but not limited to that recovery formula direct combustion incinerator, heat accumulating type direct combustion incinerator and catalyst incinerator, wherein heat accumulating type are straight
Fire the common person of incinerator such as dual grooved heat accumulation incinerator, three slot type heat accumulation incinerators and rotary valve type heat accumulation incinerator.This reality
It applies in example, cremation facilities 30 are a dual grooved heat accumulation incinerator, therefore incinerate unit 31 with two heat storage tanks 311,312 and connection
Combustion chamber 313 between two heat storage tanks 311,312, two heat storage tanks 311,312 respectively have an air inlet 32 and exhaust outlet
33, the pipeline for linking these air inlets 32,33 is equipped with control valve group (not being painted), and heat storage tank 311,312 one of which is allowed only to open
Open air inlet 32, and another one allowed only to open exhaust outlet 33, control valve group then control air inlet 32, the keying of exhaust outlet 33 and it is all
Adjust airflow direction to phase property 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 media) is filled in heat storage tank 311,312,
To carry out heat exchange with the gas for flowing through cremation facilities 30, applicable thermal medium can be but be not limited to aluminium oxide ceramics
(Alumina Oxide Porcelain), porosity mullite (Mullite), cordierite (Cordierite), porosity violet are green
Stone and other can accumulation of heat ceramics or gravel.
First, second heat exchanger 40,50 is the heat exchange for being distinctly used for two bursts of gas streams, the heat exchange of the gas stream
It is that heat is instigated to be transmitted 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 aforementioned cremation facilities 30
Room 313 branches to the first, second heat exchanger 40,50 and is used as aforementioned hot fluid.In the present embodiment, after the incineration of hot fluid
Gas sequentially flows through the first, second heat exchanger 40,50.
Above-mentioned purification system 1 can be applied to tandem runner high efficiency purification method (calling purification method in the following text), the purification side
Method includes following operation procedure：
First adsorption operation program：Pending gas containing volatile organic compounds is imported the first of the first runner 10
Adsorption zone 11, through at least a part of volatile organic compounds of sorbing material absorption in the first adsorption zone 11, treated gas
Body is sent out as the first adsorption treatment gas by the other side of the first runner 10.
Second adsorption operation program：The second adsorption zone that first adsorption treatment gas is imported to the second runner 20 again, through
At least a part of volatile organic compounds of sorbing material absorption in two adsorption zones, treated gas as the second absorption at
Process gases is sent out by the other side of the second runner 20.Usually only contain via the second adsorption treatment gas after adsorption treatment twice
The volatile organic compounds of denier can take out toward blowdown stack 60 by wind turbine 71 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 volatile organic compounds of amount, therefore this operation procedure imports the first desorption area of the first desorption gas to the first runner 10
12, allow the first desorption gas that the volatile organic compounds that the first runner 10 is adsorbed to be desorbed, then contains height
The gas of intensity volatile organic compound is sent out as the first desorption processing gas from 10 other side of the first runner；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, it is more first imported into the preheating of the first cooling isolated area 13, first heat exchanger 40 is then re-introduced into and burns
Gas carries out heat exchange after change；In the present embodiment, the first desorption gas is made 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 volatile organic compounds of amount, therefore this operation procedure imports the second desorption area of the second desorption gas to the second runner 20,
Make the second desorption gas that the volatile organic compounds that the second runner 20 is adsorbed can be desorbed, then contains higher concentration
The gas of volatile organic compounds is sent out as the second desorption processing gas from 20 other side of the second runner；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 from a part of shunting of the first adsorption treatment gas；In addition,
It, can be with pending gas since the content of the volatile organic compounds of the second desorption processing gas is worked as with pending gas phase
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 promote pending gas into the temperature before the first adsorption zone 11, reduce relative humidity, and therefore can make first
The removal rate of the volatile organic compounds of runner 10 improves, at this time the preferably usable hydrophobic zeolite adsorption material of the first runner 10
Material.
Incinerate operation procedure：The first desorption processing gas containing high concentration volatile organic compounds is by another wind turbine 72
It extracts and is imported via air inlet 32 and incinerate unit 31, it is organic through incinerating the volatility that unit 31 is desorbed first in processing gas
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 is then used 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 from gas after the incineration that exhaust outlet 33 is discharged, and other application is discharged or made through blowdown stack 60.
Working characteristics based on runner, aforementioned 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 usually, it is also essence to incinerate operation procedure
It is simultaneous.
In a numerical simulation, the purification system 1 is imported into the pending gas of 2000SCMM (m3/min), wherein
Content of volatile organic compound is 20ppmv, behind the second desorption processing gas interflow of pending gas and 100SCMM, wherein
The first adsorption zone that 1975SCMM is imported into the first runner 10 carries out the first adsorption operation program, the pending gas of 125SCMM
The first desorption area is imported into as the first desorption gas and carries out the first desorption operation procedure；Wherein, the volatilization of the first runner 10
Property organic compound removal rate be 95%, concentration rate is about 16 times, the volatile organic compounds removal rate of the second runner 20
It is 90%, concentration rate is about 17 times, and the volatile organic compounds removal rate of cremation facilities 30 is 98%；With this condition,
The content of volatile organic compound of the first adsorption treatment gas of 1975SCMM can be reduced to 1ppmv, and the of wherein 1875SCMM
The second adsorption zone that one adsorption treatment gas is imported into the second runner 20 carries out the second adsorption operation program, the second suction that treated
The content of volatile organic compound of attached processing gas can further be reduced to 0.1ppmv, and imported and arranged with the flow of 1875SCMM
Put chimney 60；On the other hand, the first adsorption treatment gas of 100SCMM is imported into the second desorption area of the second runner 20 as the
Two desorption gas simultaneously carry out the second desorption operation procedure, then send out the second desorption processing gas of 100SCMM, volatility has
Machine compound concentration is about 17ppmv, and with pending gas mixing, so that its temperature is improved and reduce its relative humidity；In addition,
In the first desorption processing gas that first desorption operation procedure is sent out, the concentration of volatile organic compounds is about 320ppmv,
And cremation facilities 30 are imported with the flow of 125SCMM and carry out incineration operation procedure, gas quilt after the high temperature incineration of wherein 15SCMM
It is sequentially oriented to the first, second heat exchanger 40,50 to be used as heat exchange, gas after then incinerating with remaining 110SCMM again
Interflow, gas is sent to discharge cigarette after becoming the incineration of total flow 125SCMM, volatile organic compounds concentration about 6.4ppmv
Chimney, last blowdown stack are externally arranged with the emission of total amount 2000SCMM, volatile organic compounds concentration about 0.5ppmv
It puts.In other words, the volatile organic compounds total removal rate of this purification system is imitated up to 97.5% for quite excellent processing
Rate.
Compared to purification system, this purification system and method is commonly used in the case where additionally not increasing cremation facilities, significantly
The volatile organic compounds concentration of emission is reduced, and thermal energy can be recycled fully, to realize energy-efficient effect.
Referring to FIG. 3, illustrated is the second embodiment of purification system of the present invention, those shown is big with first embodiment
Part is identical, is in place of difference, the purification system 100 of second embodiment further includes again and again purification reactor 180 and an ozone
Feed unit 190, the gas to after incinerating to ozone supply of ozone supply unit 190, then purification reactor 180 have a reaction
Room 181 and one is set to the water feed unit 182 in reative cell 181, and water feed unit 182 is, for example, a sprayer and can be used to carry
Vapor content in high reative cell 181 can separately be equipped with catalyst adsorption material 183 in reative cell 181；Thereby, work can be purified again
Ozone is imported reative cell 181 by industry program, makes ozone that can act on and generate the hydrogen-oxygen of high activity in reative cell 181 with aqueous vapor
Free radical, so can by NOx that may be present (not soluble in water) purification reactions in gas after incineration at nitric acid (highly-water-soluble) or
Will likely existing SOx (not soluble in water) purification reactions at sulfuric acid (highly-water-soluble) or will likely existing higher boiling organic suspension
Particle SS purification reactions finally send out gas after a purification at carbon dioxide and water.
In a numerical simulation, volatile organic compounds of the gas original containing 4.24ppmv after incineration, 100ppmv
The SS of the SOx and 1mg/Nm3 of NOx, 5ppmv can be purified after purified treatment again to contain only the volatile organic of 0.424ppmv
Close object, 20ppmv NOx, 0.5ppmv SOx and 0.5mg/Nm3 SS.Thereby, the air of emission is further reduced
Pollutant concentration.
Referring to FIG. 4, for the 3rd embodiment of purification system of the present invention, the master of the purification system 200 and first embodiment
It wants difference to be, will collaborate with pending gas under gas is conventional after the incineration of the organic compound containing light-concentration volatile, incinerate
The waste heat of gas can be used to be promoted the temperature of pending gas afterwards, reduce its relative humidity, and be subsequently imported into the first runner 210
The first adsorption zone when carrying out the first adsorption operation program again, can have higher adsorption efficiency.In other words, routine is lower only
Through the second runner 220, treated that the second adsorption treatment gas can be discharged externally, and gas is not discharged externally then after incineration, thereby can
Further reduce the content of the volatile organic compounds of emission.
In a numerical simulation, the purification system 200 is imported into the pending gas of 2000SCMM, wherein volatility
Organic compound content is 20ppmv, the second desorption processing gas of pending gas and 100SCMM and the incineration of 125SCMM
Afterwards behind gas interflow, the concentration of volatile organic compounds is about 17.6ppmv, and wherein 2100SCMM is imported into the first runner 210
The first adsorption zone carry out the first adsorption operation program, the pending gas of 125SCMM is imported into the first desorption area as first
Desorption gas simultaneously carries out the first desorption operation procedure；Wherein, the volatile organic compounds removal rate of the first runner 210 is
95%, concentration rate is about 18 times, and the volatile organic compounds removal rate of the second runner 220 is 90%, and concentration rate is about
19 times, the volatile organic compounds removal rate of cremation facilities 230 is 98%；With this condition, the first absorption of 2100SCMM
The content of volatile organic compound of processing gas can be reduced to 0.88ppmv, the first adsorption treatment gas quilt of wherein 2000SCMM
The second adsorption zone for importing the second runner 220 carries out the second adsorption operation program, and treated the second adsorption treatment gas is waved
Hair property organic compound content can further be reduced to about 0.09ppmv, and import blowdown stack 260 with the flow of 2000SCMM；Separately
On the one hand, the first adsorption treatment gas of 100SCMM is imported into the second desorption area of the second runner 220 as the second desorption gas
And the second desorption operation procedure is carried out, the second desorption processing gas of 100SCMM is then sent out, volatile organic compounds is dense
Degree be about 17ppmv, and with pending gas mixing, so that its temperature is improved and reduce its relative humidity；In addition, the first desorption is made
In the first desorption processing gas that industry program is sent out, the concentration of volatile organic compounds is about 320ppmv, and with
The flow of 125SCMM imports cremation facilities 230 and carries out incineration operation procedure, and gas is by sequentially after the high temperature incineration of wherein 15SCMM
It is oriented to the first, second heat exchanger 240,250 to be used as heat exchange, gas closes after then incinerating with remaining 110SCMM again
Stream, become gas after the incineration of total flow 125SCMM, volatile organic compounds concentration about 6.4ppmv, then again with it is pending
Gas mixing is handled again.
Finally, blowdown stack is with the emission of total amount 2000SCMM, volatile organic compounds concentration about 0.09ppmv
Externally discharge, that is, the volatile organic compounds total removal rate of this purification system is up to 99.5% or more, is very excellent
Treatment effeciency.
Referring to FIG. 5, illustrated is the fourth embodiment of purification system of the present invention, the purification system 400 is real with third
The main difference for applying example is, second heat exchanger, and a part of shunting of the second adsorption treatment gas is omitted, and hand over heat
Gas interflow is used as the second desorption gas after incineration after changing, and the second desorption area for being then directed into the second runner 420 carries out the
Two desorption operation procedures.Advantage of this embodiment is that further save heat exchanger build and maintenance cost, and
Thermal energy is more fully utilized, realizes energy-efficient purpose.
In a numerical simulation, the purification system 400 is imported into the pending gas of 2000SCMM, wherein volatility
Organic compound content is 20ppmv, the second desorption processing gas of pending gas and 115SCMM and the incineration of 110SCMM
Afterwards behind gas interflow, the concentration of volatile organic compounds 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, the pending gas of 125SCMM is imported into the first desorption area as first
Desorption gas simultaneously carries out the first desorption operation procedure；Wherein, the volatile organic compounds removal rate of the first runner 410 is
95%, concentration rate is about 18 times, and the volatile organic compounds removal rate of the second runner 420 is 90%, and concentration rate is about
19 times, the volatile organic compounds removal rate of cremation facilities 430 is 98%；With this condition, the first absorption of 2100SCMM
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 treated the second adsorption treatment gas can be further
It is reduced to about 0.09ppmv, and blowdown stack 460 is imported with the flow of 2000SCMM；On the other hand, at the second absorption of 100SCMM
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 the second desorption processing gas of 115SCMM, volatilization
Property organic compound concentrations be about 17ppmv, then again with pending gas mixing, so that its temperature is improved and to reduce it opposite
Humidity；In addition, in the first desorption processing gas that the first desorption operation procedure is sent out, the concentration of volatile organic compounds is about
For 320ppmv, and cremation facilities 430 are imported with the flow of 125SCMM and carry out incineration operation procedure, the wherein high temperature of 15SCMM is burnt
Gas is directed to first heat exchanger 440 as heat exchange and is used after change, then again with the second adsorption treatment of aforementioned 100SCMM
Gas interflow is used as the second desorption gas.On the other hand, remaining 110 SCMM, volatile organic compounds concentration is about
Gas and pending gas mixing after the incineration of 6.4ppmv and import the first runner 410 again and carry out the first adsorption operation program.
Finally, blowdown stack is with the emission of total amount 2000SCMM, volatile organic compounds concentration about 0.09ppmv
Externally discharge, that is, the present embodiment still can reach high efficiency similar with 3rd embodiment after omitting a heat exchanger
Processing is horizontal.
Referring to FIG. 6, illustrated is the 5th embodiment of purification system of the present invention, which includes one the
One runner 510, one second runner 520, a cremation facilities 530, a heat exchanger 540, again and again purification reactor 550 and an ozone
Feed unit 560.
It please arrange in pairs or groups with reference to figure 7, the first runner 510 rotates when working in a rotation direction, and the wheel face of the first runner 510 can
One first adsorption zone 511 and one first is divided into according to work purpose, area 512 is desorbed so that the absorption that the first runner 510 is carried
Area 512 sequentially is desorbed by the first adsorption zone 511 and first at work in material.In the present embodiment, the first runner 510 is substantially
It is only made of the first adsorption zone 511 and first desorption area 512, without including cooling isolated area, only the first runner 510 may also include
Other do not participate in the components such as suction, the runner holder of desorption, wheel shaft, supporting rack substantially, are not painted 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, 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 be a rotary valve type heat accumulation incinerator, therefore incinerate unit 531 include a rotary valve 5311, it is multiple be filled with accumulation of heat
The heat storage tank 5312 of material and a combustion chamber 5313, heat storage tank 5312 are communicated between rotary valve 5311 and combustion chamber 5313, into
Gas port 532 and exhaust outlet 533 are then set to 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 transmitted to cold fluid, and gas can be from the combustion chamber 5313 for incinerating unit 531 after a part of incineration of aforementioned cremation facilities 530
It branches to heat exchanger 540 and is used as aforementioned 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 one be set to reative cell 551 in water feed unit 552, water feed unit 552 be, for example, a sprayer and can be used to improve
Vapor content in reative cell 551 can separately be equipped with catalyst adsorption material 553 in reative cell 551.
Above-mentioned purification system 500 can be applied to following purification methods, which includes following operation procedure：
First adsorption operation program：Pending gas containing volatile organic compounds is imported the of the first runner 510
One adsorption zone 511, through at least a part of volatile organic compounds of sorbing material absorption in the first adsorption zone 511, after processing
Gas as the first adsorption treatment gas by the first runner 510 the other side send out.
Second adsorption operation program：The second adsorption zone that first adsorption treatment gas is imported to the second runner 520 again, through
At least a part of volatile organic compounds of sorbing material absorption in two adsorption zones, treated gas as the second absorption at
Process gases is sent out by the other side of the second runner 520.It is usually contained only via the second adsorption treatment gas after adsorption treatment twice
There is the volatile organic compounds of denier, can be taken out by wind turbine 571 toward blowdown stack or makees other application.
First desorption operation procedure：The sorbing material of first runner 510 has adsorbed quite in the first adsorption operation program
The volatile organic compounds of quantity, therefore this operation procedure imports the first desorption of the first desorption gas to the first runner 510
Area 512 allows the first desorption gas that the volatile organic compounds that the first runner 510 is adsorbed to be desorbed, then contains
There is the gas of high concentration volatile organic compounds to be sent out from 510 other side of the first runner as the first desorption processing gas.
Second desorption operation procedure：The sorbing material of second runner 520 has adsorbed quite in the second adsorption operation program
The volatile organic compounds of quantity, therefore this operation procedure imports the second desorption of the second desorption gas to the second runner 520
Area makes the second desorption gas that the volatile organic compounds that the second runner 520 is adsorbed can be desorbed, and then contains higher
The gas of intensity volatile organic compound is sent out as the second desorption processing gas from 520 other side of the second runner；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, it is more imported into the preheating of the second cooling isolated area, 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 from a part of shunting of the first adsorption treatment gas and second
Desorption processing gas carries on as before with higher temperature, therefore can directly be imported into the first desorption 512 conduct of area of the first runner 510
First desorption gas uses.
Incinerate operation procedure：The first desorption processing gas containing high concentration volatile organic compounds is by another wind turbine
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 generate one incinerate after gas, after incineration gas some be discharged by exhaust outlet 533, it is another
Gas is then used 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 volatile organic compounds 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 (not soluble in water) purification reactions in gas after incineration at
Nitric acid (highly-water-soluble) or will likely existing SOx (not soluble in water) purification reactions at sulfuric acid (highly-water-soluble) or will likely deposit
Higher boiling organic suspension particle SS purification reactions at carbon dioxide and water, finally send out gas after a purification.
Working characteristics based on runner, aforementioned 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 usually, incinerates operation procedure and purify again
Operation procedure is also that essence is simultaneous.
Based on previous designs, the second adsorption treatment gas that the second runner of the present embodiment 520 is sent out and again purification reaction
Gas all only contains micro volatile organic compounds after the purification that room 550 is sent out, can be external directly as emission
Discharge.Compared to purification system, this purification system and method is commonly used in the case where additionally not increasing cremation facilities, it is greatly reduced
The volatile organic compounds concentration of emission, and thermal energy can be recycled fully, realize energy-efficient effect.
Referring to FIG. 8, illustrated is the sixth embodiment of purification system of the present invention, the purification system 600 of the present embodiment
It is identical with the 5th embodiment major part, it is in place of difference, gas does not re-direct first turn after flowing through the incineration of heat exchanger 640
First adsorption zone of wheel 610, and purification system 600 further includes a thermometer 671, a control valve 672 and a controller 673, control
Device 673 processed is connect with thermometer 671 and 672 signal of control valve respectively, and thermometer 671 is detecting the temperature of the first desorption gas
Degree, control valve 672 then collaborate to adjust gas after the incineration after heat exchange to the flow of the second desorption processing gas, controller
673 control control valve 672 according to the temperature that thermometer 671 is sensed and adjust aforementioned flow, and are not desorbed with second wherein
Gas then collaborates with from gas after the incineration that exhaust outlet 633 is discharged after the incineration at processing gas interflow.
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, the flow of the desorption of gas flow second processing gas after making control valve that incineration be turned up, due to gas after incineration
The temperature of processing gas is desorbed higher than second for the temperature of body, therefore the temperature of the first desorption gas after flow adjusts can must carry
It rises, until being warming up to acquiescence operating temperature.
Referring to FIG. 9, illustrated is the 7th embodiment of purification system of the present invention, the purification system 700 of the present embodiment
Identical with second embodiment major part, main difference is, cremation facilities 730 are one or three slot type heat accumulation incinerators, and are flowed through
Gas does not re-direct another heat exchanger after the incineration of first heat exchanger 740, and directly with the incineration that is discharged from exhaust outlet 733
Gas collaborates afterwards；Instead, purification system 700 includes separately one increasing the heating device of the second desorption gas temperature
770, heating device 770 can be but be not limited to the heat exchanger of other forms, and heat source can be steam, deep fat, hot-air or electricity
Heat.
Referring to FIG. 10, illustrated is the 8th embodiment of purification system of the present invention, the purification system 800 of the present embodiment
Identical with the 7th embodiment major part, main difference is, after gas and the first adsorption treatment gas collaborate after incinerating, quilt
The second adsorption zone for importing the second runner 820 carries out the second adsorption operation program, thereby further decreases volatile organic compound
After object concentration, just externally discharge.
Finally, it is necessary to illustrate again, composition component of the present invention disclosed by preceding taking off in embodiment is only for example
It is bright, not it is used for limiting the range of this case, the replacement of other equivalent elements or variation, also should be the claim institute of this case
Cover.
Claims (41)
1. a kind of tandem runner high efficiency purification system, to handle the pending gas for containing volatile organic compounds, packet
It includes：
One first runner has one first adsorption zone and one first desorption area, and first adsorption zone is for importing the pending gas
Body, to adsorb at least a part of volatile organic compounds in the pending gas and send out one first adsorption treatment gas
Body；The first desorption area is for importing one first desorption gas, the volatile organic compound that first runner is adsorbed is desorbed
Object simultaneously sends out one first desorption processing gas；
One second runner has one second adsorption zone and one second desorption area, and second adsorption zone is for importing first absorption
Processing gas is inhaled to adsorb at least a part of volatile organic compounds in the first adsorption treatment gas and send out one second
Attached processing gas；The second desorption area is for importing one second desorption gas, the volatility that second runner is adsorbed is desorbed
Organic compound simultaneously sends out one second desorption processing gas；And
There is one cremation facilities an incineration unit, an air inlet and an exhaust outlet, the air inlet and exhaust outlet to be connected to the incineration
Unit, the air inlet for import it is described first desorption processing gas, the incineration unit to will first be desorbed processing gas in
Volatile organic compounds burning disposal and generate gas after an incineration, the exhaust outlet is being discharged at least a part of incineration
Gas afterwards, and gas is imported into first adsorption zone, the first desorption area, second adsorption zone after at least a part of incineration
Or the second desorption area.
2. tandem runner high efficiency purification system as described in claim 1, wherein one of described first adsorption treatment gas
Part shunting is used as second desorption gas.
3. tandem runner high efficiency purification system as described in claim 1, wherein the second desorption area sent out second
Desorption processing gas is imported into the first adsorption zone of first runner.
4. tandem runner high efficiency purification system as described in claim 1, wherein first runner are with more one between this
The first cooling isolated area between first adsorption zone and the first desorption area, first desorption gas are importing the first desorption area
Between be first imported into this first cooling isolated area.
5. tandem runner high efficiency purification system as described in claim 1, wherein second runner are with more one between this
The second cooling isolated area between second adsorption zone and the second desorption area, second desorption gas are importing the second desorption area
Between be first imported into this second cooling isolated area.
6. tandem runner high efficiency purification system as described in claim 1, further includes a first heat exchanger, the incineration
The first heat exchanger is sent out from the incineration unit and flowed through to some of gas afterwards, first desorption gas importing this
It is first imported into the first heat exchanger before one desorption area and carries out heat exchange with gas after the incineration.
7. tandem runner high efficiency purification system as claimed in claim 6, further includes a second heat exchanger, the incineration
The second heat exchanger is sent out from the incineration unit and flowed through to some of gas afterwards, second desorption gas importing this
It is first imported into the second heat exchanger before two desorption areas and carries out heat exchange with gas after the incineration.
8. tandem runner high efficiency purification system as claimed in claim 7, wherein from after the incineration that the incineration unit is sent out
Gas sequentially flows through first, second heat exchanger.
9. tandem runner high efficiency purification system as claimed in claim 7 or 8 is handed over wherein flowing through first, second heat
Gas collaborates with from gas after the incineration that the exhaust outlet is discharged parallel operation again after the incineration of one at least within.
10. tandem runner high efficiency purification system as described in claim 1, wherein after the incineration gas be imported into this
First adsorption zone of one runner.
11. tandem runner high efficiency purification system as claimed in claim 9, wherein gas quilt after incineration behind the interflow
Import the first adsorption zone of first runner.
12. the tandem runner high efficiency purification system as described in claim 1 or 5, wherein the second adsorption treatment gas
Some shunting be used as second desorption gas.
13. tandem runner high efficiency purification system as described in claim 1, wherein after the incineration gas it is a part of from
The incineration unit is sent out, with described from the incineration after a part of shunting of the first, second adsorption treatment gas one of which
Unit send out incineration after gas interflow and as second desorption gas.
14. tandem runner high efficiency purification system as described in claim 1, the second desorption processing gas is imported into this
First desorption area and as first desorption gas.
15. tandem runner high efficiency purification system as claimed in claim 14, further includes a heat exchanger, after the incineration
The heat exchanger is sent out from the incineration unit and flowed through to some of gas, and second desorption gas is importing second desorption
It is first imported into the heat exchanger before area and carries out heat exchange with gas after the incineration.
16. tandem runner high efficiency purification system as described in claim 1, further includes a heat exchanger, after the incineration
The heat exchanger is sent out from the incineration unit and flowed through to some of gas, and second desorption gas is importing second desorption
It is first imported into the heat exchanger before area and carries out heat exchange with gas after the incineration, gas is extremely after the incineration after heat exchange
It is few a part of with described second be desorbed processing gas collaborate and be imported into this first area is desorbed and as first desorption gas.
17. tandem runner high efficiency purification system as claimed in claim 16, further includes a thermometer, a control valve and one
Controller, the controller are connect with the thermometer and the control valve signal, and the thermometer is detecting first desorption gas
Temperature, which collaborates to adjust gas after the incineration to the flow of the second desorption processing gas, which uses
The control valve is controlled with the temperature sensed according to the thermometer adjusts the flow.
18. tandem runner high efficiency purification system as described in claim 1, further includes a heating device, to improve
State the temperature of the second desorption gas.
19. the tandem runner high efficiency purification system as described in any one in claim 14 to 17, wherein first runner
Essence by the adsorption zone and the desorption district's groups at.
20. tandem runner high efficiency purification system as described in claim 1, further includes purification reactor again and again and an ozone
Feed unit, the ozone supply unit is to gas after ozone supply to the incineration, and purification reactor has a reaction again for this
Room and for importing gas after the incineration ozoniferous, after gas after incineration ozoniferous to be purified again and sending out a purification
Gas.
21. tandem runner high efficiency purification system as claimed in claim 20, wherein this purification reactor has more one again
Water feed unit, to improve the indoor vapor content of the reaction.
22. a kind of tandem runner high efficiency purification method is applied to a tandem runner high efficiency purification system, the tandem
Runner high efficiency purification system includes one first runner, one second runner and a cremation facilities, which has one first
There is one second adsorption zone and one second desorption area, the cremation facilities to have for adsorption zone and one first desorption area, second runner
One incinerates unit, an air inlet and an exhaust outlet, and the air inlet and the exhaust outlet are communicated in the incineration unit, which turns
It includes following operation procedure to take turns high efficiency purification method：
First adsorption operation program：The pending gas containing volatile organic compounds is imported to first adsorption zone, and is passed through
First adsorption zone sends out one first adsorption treatment gas after adsorbing at least a part of volatile organic compounds；
Second adsorption operation program：The first adsorption treatment gas is directed into second adsorption zone, and through second absorption
One second adsorption treatment gas is sent out after adsorbing at least a part of volatile organic compounds in area；
First desorption operation procedure：Import one first desorption gas to this first desorption area, first desorption gas by this first
The volatile organic compounds that runner is adsorbed is desorbed from first runner and sends out one first desorption processing gas；
Second desorption operation procedure：Import one second desorption gas to this second desorption area, second desorption gas by this second
The volatile organic compounds that runner is adsorbed is desorbed from second runner and sends out one second desorption processing gas；And
Incinerate operation procedure：The first desorption processing gas is imported into the incineration unit via the air inlet, and through the incineration list
The volatile organic compounds burning disposal that first is desorbed in processing gas is generated gas after an incineration, gas after the incineration by member
At least a part of of body is discharged via the exhaust outlet, and after at least a part of incineration gas be imported into first adsorption zone,
The first desorption area, second adsorption zone or the second desorption area；
Wherein, the first adsorption operation program, the second adsorption operation program, the first desorption operation procedure and second desorption
Operation procedure is substantially carried out at the same time.
23. tandem runner high efficiency purification method as claimed in claim 22, wherein the first adsorption treatment gas it
Some shuntings are used as second desorption gas.
24. tandem runner high efficiency purification method as claimed in claim 22, wherein the second desorption area sent out the
Two desorption processing gas are imported into the first adsorption zone of first runner.
25. tandem runner high efficiency purification method as claimed in claim 22, wherein first runner with more one between
The first cooling isolated area between first adsorption zone and the first desorption area, first desorption gas are importing first desorption
The first cooling isolated area is first imported between area.
26. tandem runner high efficiency purification method as claimed in claim 22, wherein second runner with more one between
The second cooling isolated area between second adsorption zone and the second desorption area, second desorption gas are importing second desorption
The second cooling isolated area is first imported between area.
27. tandem runner high efficiency purification method as claimed in claim 22, wherein the tandem runner high efficiency purify
System further includes a first heat exchanger, and some of gas is sent out from the incineration unit and imports first heat after the incineration
Exchanger, first desorption gas are first imported into the first heat exchanger before importing the first desorption area and are burnt with described
Gas carries out heat exchange after change.
28. tandem runner high efficiency purification method as claimed in claim 27, wherein the tandem runner high efficiency purify
System further includes a second heat exchanger, and some of gas is sent out from the incineration unit and imports second heat after the incineration
Exchanger, second desorption gas are first imported into the second heat exchanger before importing the second desorption area and are burnt with described
Gas carries out heat exchange after change.
29. tandem runner high efficiency purification method as claimed in claim 28, wherein the incineration sent out from the incineration unit
Gas sequentially flows through first, second heat exchanger afterwards.
30. the tandem runner high efficiency purification method as described in claim 28 or 29, wherein flowing through first, second heat
Gas collaborates with from gas after the incineration that the exhaust outlet is discharged exchanger again after the incineration of one at least within.
31. tandem runner high efficiency purification method as claimed in claim 22, wherein gas is imported into this after the incineration
First adsorption zone of the first runner.
32. tandem runner high efficiency purification method as claimed in claim 30, wherein gas after incineration behind the interflow
It is imported into the first adsorption zone of first runner.
33. the tandem runner high efficiency purification method as described in claim 22 or 26, wherein the second adsorption treatment gas
Some shuntings of body are used as second desorption gas.
34. tandem runner high efficiency purification method as claimed in claim 22, wherein after the incineration gas some
It sends out from the incineration unit, is burnt from this with described after a part of shunting of the first, second adsorption treatment gas one of which
Change unit send out incineration after gas interflow and as second desorption gas.
35. tandem runner high efficiency purification method as claimed in claim 22, wherein the second desorption processing gas quilt
Import this first desorption area and as first desorption gas.
36. tandem runner high efficiency purification method as claimed in claim 35, wherein the tandem runner high efficiency purify
System further includes a heat exchanger, and the heat exchanger is sent out from the incineration unit and imported to some of gas after the incineration,
Second desorption gas it is standby import the second desorption area before be first imported into the heat exchanger and with gas after the incineration
Carry out heat exchange.
37. tandem runner high efficiency purification method as claimed in claim 22, wherein the tandem runner high efficiency purify
System further includes a heat exchanger, and some of gas after the incineration is sent out from the incineration unit and imports the heat exchange
Device, second desorption gas it is standby import the second desorption area before be first imported into the heat exchanger and with gas after the incineration
Body carries out heat exchange；
Wherein, at least a part of and the second desorption processing gas of gas collaborates and is imported into this after the incineration after heat exchange
First desorption area and as first desorption gas.
38. tandem runner high efficiency purification method as claimed in claim 37, wherein the tandem runner high efficiency purify
System further includes a thermometer, a control valve and a controller, which connect with the thermometer and the control valve signal, should
To detect the temperature of first desorption gas, which collaborates to adjust gas after the incineration to second thermometer
The flow of processing gas is desorbed, and the controller controls the control valve according to the temperature that the thermometer is sensed and adjusts the stream
Amount.
39. the tandem runner high efficiency purification method as described in any one of claim 35 to 38, wherein first runner
Essence by the adsorption zone and the desorption district's groups at.
40. tandem runner high efficiency purification method as claimed in claim 22, wherein the tandem runner high efficiency purify
System further includes purification reactor again and again and an ozone supply unit, and purification reactor has a reative cell, the tandem again for this
Runner high efficiency purification method further includes：
Operation procedure is purified again：Gas after the ozone supply unit ozone supply to the incineration, after the incineration containing ozone
Gas imports the reative cell and is purified again and send out gas after a purification.
41. tandem runner high efficiency purification method as claimed in claim 40, wherein this purification reactor has more one again
Water feed unit, to improve the indoor vapor content of the reaction in purifying operation procedure again.
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| CN201710086333.4A CN108452637B (en) | 2017-02-17 | 2017-02-17 | Serial-type rotating wheel high-efficiency purification system and serial-type rotating wheel high-efficiency purification method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110465159A (en) * | 2019-07-25 | 2019-11-19 | 江苏苏净集团有限公司 | A kind of processing exhaust gas adsorption runner device |
| CN111111382A (en) * | 2018-10-30 | 2020-05-08 | 华懋科技股份有限公司 | Rotating wheel system with high-temperature desorption function and method thereof |
| CN115445387A (en) * | 2022-08-23 | 2022-12-09 | 江苏中电创新环境科技有限公司 | Treatment system and method for high-air-volume low-concentration organic waste gas |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5167679A (en) * | 1990-03-31 | 1992-12-01 | Taikisha Ltd. | Rotary gas treating apparatus |
| CN101963359A (en) * | 2009-07-24 | 2011-02-02 | 杰智环境科技股份有限公司 | Energy saving device of incineration treatment system for nitrogen nitrogen- or/and sulphur-containing volatile organic matters |
| CN203315969U (en) * | 2013-03-29 | 2013-12-04 | 无锡中舜成环保科技有限公司 | Zero-energy consumption purifying device for volatile organic compounds |
| CN104107618A (en) * | 2014-08-07 | 2014-10-22 | 石家庄天龙环保科技有限公司 | Low-concentration large-air-volume waste gas concentration and wind reduction system |
| CN205127672U (en) * | 2015-09-22 | 2016-04-06 | 江苏中研宜普科技有限公司 | Two energy -saving concentrated runners and RTO's organic waste gas processing system |
| CN105597490A (en) * | 2014-11-20 | 2016-05-25 | 杰智环境科技股份有限公司 | Organic exhaust gas adsorption/desorption, concentration and purifying system and method thereof |
| CN205252836U (en) * | 2015-11-13 | 2016-05-25 | 惠州市环发环保科技有限公司 | Runner adsorbs concentrated RTO waste gas treatment system |
| CN205481039U (en) * | 2016-02-04 | 2016-08-17 | 杰智环境科技股份有限公司 | Use concentrated purification treatment system of waste gas of incinerator heat recovery |
| CN106139821A (en) * | 2016-08-31 | 2016-11-23 | 霍普科技（天津）股份有限公司 | A kind of zeolite runner Adsorption Concentration purifier |
| CN206715626U (en) * | 2017-02-17 | 2017-12-08 | 杰智环境科技股份有限公司 | Runner high efficiency cleaning system |
-
2017
- 2017-02-17 CN CN201710086333.4A patent/CN108452637B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5167679A (en) * | 1990-03-31 | 1992-12-01 | Taikisha Ltd. | Rotary gas treating apparatus |
| CN101963359A (en) * | 2009-07-24 | 2011-02-02 | 杰智环境科技股份有限公司 | Energy saving device of incineration treatment system for nitrogen nitrogen- or/and sulphur-containing volatile organic matters |
| CN203315969U (en) * | 2013-03-29 | 2013-12-04 | 无锡中舜成环保科技有限公司 | Zero-energy consumption purifying device for volatile organic compounds |
| CN104107618A (en) * | 2014-08-07 | 2014-10-22 | 石家庄天龙环保科技有限公司 | Low-concentration large-air-volume waste gas concentration and wind reduction system |
| CN105597490A (en) * | 2014-11-20 | 2016-05-25 | 杰智环境科技股份有限公司 | Organic exhaust gas adsorption/desorption, concentration and purifying system and method thereof |
| CN205127672U (en) * | 2015-09-22 | 2016-04-06 | 江苏中研宜普科技有限公司 | Two energy -saving concentrated runners and RTO's organic waste gas processing system |
| CN205252836U (en) * | 2015-11-13 | 2016-05-25 | 惠州市环发环保科技有限公司 | Runner adsorbs concentrated RTO waste gas treatment system |
| CN205481039U (en) * | 2016-02-04 | 2016-08-17 | 杰智环境科技股份有限公司 | Use concentrated purification treatment system of waste gas of incinerator heat recovery |
| CN106139821A (en) * | 2016-08-31 | 2016-11-23 | 霍普科技（天津）股份有限公司 | A kind of zeolite runner Adsorption Concentration purifier |
| CN206715626U (en) * | 2017-02-17 | 2017-12-08 | 杰智环境科技股份有限公司 | Runner high efficiency cleaning system |
Non-Patent Citations (1)
| Title |
|---|
| 刘建民等: "《火电厂氮氧化物控制技术》", 31 December 2012, 中国电力出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111111382A (en) * | 2018-10-30 | 2020-05-08 | 华懋科技股份有限公司 | Rotating wheel system with high-temperature desorption function and method thereof |
| CN110465159A (en) * | 2019-07-25 | 2019-11-19 | 江苏苏净集团有限公司 | A kind of processing exhaust gas adsorption runner device |
| CN115445387A (en) * | 2022-08-23 | 2022-12-09 | 江苏中电创新环境科技有限公司 | Treatment system and method for high-air-volume low-concentration organic waste gas |
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Effective date of registration: 20221109 Address after: Taoyuan County, Taiwan, China Longtan District, Gaoping village, Feng Road, Gaoping section 8 Patentee after: JG ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Address before: No. 8, Gaoping Section, Zhongfeng Road, Gaoping Village, Longtan District, Taoyuan City Patentee before: JG ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Patentee before: Zhang Fengtang |