CN106984189A - A kind of RTO emissions three-phase catalytic deodorization process - Google Patents
A kind of RTO emissions three-phase catalytic deodorization process Download PDFInfo
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- CN106984189A CN106984189A CN201710305352.1A CN201710305352A CN106984189A CN 106984189 A CN106984189 A CN 106984189A CN 201710305352 A CN201710305352 A CN 201710305352A CN 106984189 A CN106984189 A CN 106984189A
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- 230000003197 catalytic effect Effects 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 39
- 238000004332 deodorization Methods 0.000 title abstract description 11
- 239000007789 gas Substances 0.000 claims abstract description 32
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 239000000779 smoke Substances 0.000 claims abstract description 15
- 230000001877 deodorizing effect Effects 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 11
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 6
- 230000015556 catabolic process Effects 0.000 claims abstract description 5
- 238000006731 degradation reaction Methods 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims description 50
- 239000012071 phase Substances 0.000 claims description 50
- 239000003054 catalyst Substances 0.000 claims description 45
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 22
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 claims description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 18
- 239000003546 flue gas Substances 0.000 claims description 18
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 16
- 238000006555 catalytic reaction Methods 0.000 claims description 15
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 14
- 229910052593 corundum Inorganic materials 0.000 claims description 14
- 239000007921 spray Substances 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 14
- 239000008367 deionised water Substances 0.000 claims description 12
- 229910021641 deionized water Inorganic materials 0.000 claims description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 12
- 229910002551 Fe-Mn Inorganic materials 0.000 claims description 11
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 11
- 238000006116 polymerization reaction Methods 0.000 claims description 11
- 238000003756 stirring Methods 0.000 claims description 11
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 10
- 150000002505 iron Chemical class 0.000 claims description 9
- 239000011572 manganese Substances 0.000 claims description 9
- 238000001291 vacuum drying Methods 0.000 claims description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- 239000007790 solid phase Substances 0.000 claims description 8
- UOGMEBQRZBEZQT-UHFFFAOYSA-L manganese(2+);diacetate Chemical compound [Mn+2].CC([O-])=O.CC([O-])=O UOGMEBQRZBEZQT-UHFFFAOYSA-L 0.000 claims description 7
- 229940071125 manganese acetate Drugs 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 5
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000000227 grinding Methods 0.000 claims description 4
- 229910052748 manganese Inorganic materials 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 4
- 238000000975 co-precipitation Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000000843 powder Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 238000000967 suction filtration Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 2
- 238000011049 filling Methods 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 239000012286 potassium permanganate Substances 0.000 claims description 2
- 238000001179 sorption measurement Methods 0.000 claims description 2
- 238000002604 ultrasonography Methods 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims 1
- 150000003839 salts Chemical class 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 2
- 238000004140 cleaning Methods 0.000 abstract 1
- 230000008878 coupling Effects 0.000 abstract 1
- 238000010168 coupling process Methods 0.000 abstract 1
- 238000005859 coupling reaction Methods 0.000 abstract 1
- 239000003205 fragrance Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 7
- 239000005416 organic matter Substances 0.000 description 4
- 239000012855 volatile organic compound Substances 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003973 paint Substances 0.000 description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000006253 efflorescence Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 206010037844 rash Diseases 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—Gas phase processes, e.g. by using aerosols
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/889—Manganese, technetium or rhenium
- B01J23/8892—Manganese
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/26—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups B01J31/02 - B01J31/24
- B01J31/32—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups B01J31/02 - B01J31/24 of manganese, technetium or rhenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
- B01D2258/0291—Flue gases from waste incineration plants
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Catalysts (AREA)
Abstract
The invention belongs to exhaust-gas treatment field, it is related to a kind of RTO emissions three-phase catalytic deodorization process.This method is, by smoke cooling tower and three-phase catalytic odor removal, to reach the effect of cleaning of off-gas by the gas after RTO burning disposals.The sour gas that wherein smoke cooling tower reduction gas temperature is gone in removing exhaust gas simultaneously, it is ensured that follow up device is continually and steadily run.Three-phase catalytic odor removal reaches deodorizing effect with the odorant in gas, liquid, solid coupling catalytic degradation tail gas.This method has simple to operate, processing cost low, the advantages of plant investment is small.
Description
Technical field
The invention belongs to waste gas pollution control and treatment field, it is related to a kind of RTO emissions three-phase catalytic deodorization process.
Background technology
In recent years, with the continuous improvement in terms of environmental protection for volatile organic matter (VOCs) emission request, heat accumulating type burns
Stove (RTO) technology of burning more next moon in terms of VOCs treatment is universal, at present in petrochemical industry, chemical pharmacy, paint spray booth, paint
It is used widely with coating material production etc. industry.RTO is as a kind of efficient VOCs treatment technology, and it is controlled for organic exhaust gas
Reason provides an effective method, is that the manufacturing enterprise such as chemical industry, medicine VOCs treatment opens new chapter.
Compared with traditional catalysis burning (RCO), direct-fired thermal oxidation furnace (TO), RTO has thermal efficiency height, can handle big
In air quantity the features such as low concentration gas, when concentration is slightly higher, secondary waste heat recovery can be carried out, the part energy is saved.But RTO is in operation
During there is also can not thorough purified treatment organic matter phenomenon, there is a small amount of organic of sour gas and undegraded completion
Secondary material produced in thing, and burning process etc. causes peculiar smell.
For RTO issuable above mentioned problems in the process of running, for RTO main equipments without a wide range of whole
It is net by the way that to RTO tail gas progress subsequent treatment tail gas can be played under conditions of cost-effective and workload on the premise of changing
The effect of change, technical support is provided for the deep popularization of RTO technologies.
The content of the invention
The technical problem to be solved in the invention is：For current RTO technologies issuable stench in the process of running
There is provided a kind of tail gas clean-up technology efficiently, inexpensive for pollution problem.
A kind of RTO emissions three-phase catalytic deodorizing method, this method comprises the following steps：
(1) tail gas after being burned by RTO is passed through smoke cooling tower, flue-gas temperature is down to 50~60 DEG C；
(2) flue gas after cooling down enters the progress of three-phase catalytic system by the air inlet of three-phase catalytic odor removal lower end
Reason, described three-phase catalytic odor removal is mainly made up of ozone generator, main reaction tower, circulating pump and connecting pipe, valve；
Ozone generator is connected by pipeline with the liquid storage tank of main reaction tower bottom；Gas phase catalyst ozone is with liquid-phase catalyst in liquid storage
Pond is delivered to the spray equipment of main reaction top of tower by circulating pump after being sufficiently mixed, gas, liquid mixed catalyst is from upper spray
The catalytic reaction zone filled with solid-phase catalyst is finally returned to the liquid storage tank of main reaction tower bottom in the middle part of lower process main reaction tower；
Flue gas into main reaction tower is run from bottom to top, by solid catalysis reaction zone, is contacted with solid, liquid, gas three phase catalyst, quilt
Discharged after solid, liquid, gas three phase catalyst joint catalytic degradation from the exhaust outlet of main reaction top of tower.
As a preference of the present invention, described smoke cooling tower is alkali adsorption tower, removed while flue-gas temperature is reduced
Sour gas present in flue gas, alkali lye is NaOH solution, and concentration is 5~10wt%.
As a preference of the present invention, the material of described main reaction tower is stainless steel.
As a preference of the present invention, described ozone add concentration (i.e. ozone generator produce ozone concentration) 50~
Between 100ppm.
As a preference of the present invention, described liquid-phase catalyst is any one in hydrogen peroxide, sodium hypochlorite；Hydrogen peroxide
Concentration is in 1~5wt%, and sodium hypochlorite concentration is in 5~10wt%.
As a preference of the present invention, described solid catalysis is selected from MnO2/ high molecular polymerization iron salt catalyst, Fe-Mn/
Al2O3One kind of catalyst；MnO2MnO in/high molecular polymerization iron salt catalyst2Load capacity is 1~10wt%, Fe-Mn/Al2O3
Fe load capacity is in 1~10wt% in catalyst, and Mn load capacity is in 1~10wt%.
As a preference of the present invention, described MnO2/ high molecular polymerization iron salt catalyst, which is prepared by the following method, to be obtained：
Poly-ferric chloride is placed in a certain amount of deionized water, stirs simultaneously ultrasound 15-20 minutes, and then addition manganese acetate is dissolved in above-mentioned
It is stirred continuously in solution, KMnO is slowly added dropwise again afterwards4Solution, temperature control reacts 45-60min at 75 DEG C, after the completion of reaction
Filtering, with deionized water cyclic washing 5-6 times, is subsequently placed into vacuum drying chamber and is dried, obtain MnO2/ high molecular polymerization
Iron salt catalyst；Wherein the mass ratio of poly-ferric chloride and manganese acetate is 1:0.018775~0.18775；Poly-ferric chloride with
KMnO4Quality mol ratio is 10g：1-10mol.
As a preference of the present invention, described Fe-Mn/Al2O3Catalyst, which is prepared by the following method, to be obtained：Weigh 0.22
~2.5g FeCl3, plus deionized water dissolving, by 7.5g Al2O3Powder adds FeCl3In solution, stir 8-9 hours, by solution
The dry 12-14h of 110-120 DEG C of vacuum drying chamber is put into after 85-90 DEG C of water bath method；Muffle furnace 600-620 is put into after grinding
DEG C 5.5-6 hour obtained 1-10% of roasting Fe/Al2O3Catalyst；Then Mn is loaded with coprecipitation：It is 3 to weigh mass ratio:4
Fe/Al2O3And manganese acetate, plus deionized water dissolving, stirring 18h. and then the dense ammonia that slowly progressively increases during being stirred continuously
Water, to pH value of solution=12, stirs suction filtration after 1-1.5h.The dry 12-14h of 110-120 DEG C of vacuum drying chamber is subsequently placed into, after drying
Grinding, is put into 550-600 DEG C of Muffle furnace and is calcined 3.5-4 hours, the Fe-Mn/Al that Fe and Mn load capacity is 1-10% is made2O3
Catalyst.
For the three-phase catalytic odor removal of RTO emissions three-phase catalytic deodorizing method of the present invention, mainly by
Ozone generator, main reaction tower, circulating pump and connecting pipe, valve composition；Main reaction tower bottom is liquid storage tank, ozone generator
It is connected by pipeline with the liquid storage tank of main reaction tower bottom；The smoke air inlet of main reaction tower is arranged above liquid storage tank；It is main anti-
Answer and be provided with spray equipment, spray equipment in the middle part of tower directly over the catalytic reaction zone for filling solid-phase catalyst, main reaction top of tower
Inlet is connected with liquid storage tank by circulating pump and pipeline；Main reaction top of tower side is provided with flue gas exhaust mouthful.
A kind of RTO emissions three-phase catalytic deodoration system, includes smoke cooling tower and three-phase catalytic of the present invention
Odor removal.
Beneficial effect：
1st, the invention provides a kind of RTO emission three-phase catalytic deodorization process efficiently, inexpensive, with device knot
The advantages of structure is simple, simple to operate, processing cost is low, investment is small.
2nd, smoke cooling tower of the present invention can effectively reduce gas temperature while removing the sour gas in flue gas
Body, it is ensured that subsequent treatment facility being capable of normal table operation.
3rd, three-phase catalytic deodorization process of the present invention can quickly, in efficient degradation tail gas burn and insufficient have
Machine thing, reduces secondary pollution, and the ordorless smell of tail gas handled through present invention process meets emission standard for odor pollutants, is
The deep popularization of RTO technologies provides technical support.
4、MnO2/ high molecular polymerization iron salt catalyst, Fe-Mn/Al2O3Catalytic performance is good, service life length, catalyst are strong
Degree is higher, is resistant to certain hydraulic load and is unlikely to catalyst efflorescence.
Brief description of the drawings
Fig. 1 is three-phase catalytic odor removal schematic diagram.
1 is ozone generator, and 2 be main reaction tower, and 3 be circulating pump, and 4 be liquid storage tank, and 5 be catalytic reaction zone,
6 be spray equipment.
Embodiment：
Embodiment 1
A kind of RTO emissions three-phase catalytic deodoration system, includes smoke cooling tower and three-phase catalytic odor removal and company
Adapter road；Three-phase catalytic odor removal is main by ozone generator 1, main reaction tower 2, circulating pump 3 and connecting pipe, valve group
Into；The bottom of main reaction tower 2 is liquid storage tank 4, and ozone generator 1 is connected by pipeline with the liquid storage tank 4 of main reaction tower bottom；It is main anti-
The smoke air inlet of tower 2 is answered to be arranged at the top of liquid storage tank 4；To fill the catalytic reaction zone 5 of solid-phase catalyst in the middle part of main reaction tower,
Spray equipment 6 is provided with directly over main reaction top of tower, spray equipment inlet is connected with liquid storage tank by circulating pump 3 and pipeline；
The top-side of main reaction tower 2 is provided with flue gas exhaust mouthful.
The method that RTO emission three-phase catalytic deodorizations are carried out using said system, this method is comprised the following steps：
(1) tail gas after being burned by RTO is passed through smoke cooling tower, flue-gas temperature is down to 50~60 DEG C；
(2) flue gas after cooling down enters the progress of three-phase catalytic system by the air inlet of three-phase catalytic odor removal lower end
Reason, described three-phase catalytic odor removal is main by ozone generator, stainless steel main reaction tower, circulating pump and connecting pipe, valve
Door composition；Ozone generator is connected by pipeline with the liquid storage tank of main reaction tower bottom；Gas phase catalyst ozone and liquid-phase catalysis
Agent is delivered to the spray equipment of main reaction top of tower after liquid storage tank is sufficiently mixed by circulating pump, and gas, liquid mixed catalyst is certainly
Upper spray and be finally returned to main reaction tower bottom filled with the catalytic reaction zone of solid-phase catalyst in the middle part of lower process main reaction tower
Liquid storage tank；Flue gas into main reaction tower is run from bottom to top, by solid catalysis reaction zone, with solid, liquid, gas three-phase catalytic
Agent is contacted, and combines the exhaust outlet discharge after catalytic degradation from main reaction top of tower by solid, liquid, gas three phase catalyst.
Embodiment 2
Weigh 10g high molecular polymerization molysite to be placed in a certain amount of deionized water, stir and ultrasonic 20 minutes.Then addition
1.8755g manganese acetates are dissolved in above-mentioned solution and are stirred continuously, and 10molKMnO is slowly added dropwise again afterwards4Solution, temperature control exists
75 DEG C of reaction 45min.Filtered after the completion of reaction, with deionized water cyclic washing 5-6 time, be subsequently placed into vacuum drying chamber and carry out
Dry, obtain the MnO that mass fraction is 10%2/ high molecular polymerization iron salt catalyst.
Embodiment 3
Weigh 2.5gFeCl3, plus deionized water dissolving, by 7.5gAl2O3Powder (crossing 60 mesh sieves) adds FeCl3In solution,
8 lab scales are stirred, solution is put into the dry 12h of 120 DEG C of vacuum drying chamber after 85 DEG C of water bath methods.Muffle furnace is put into after grinding
The Fe/Al of 600 DEG C of roastings, 6 hours systems2O3.Then Mn is loaded with coprecipitation：It is 3 to weigh mass ratio:4 Fe/Al2O3And second
Sour manganese, plus deionized water dissolving, stirring 18h. and then the slow concentrated ammonia liquor that progressively increases during being stirred continuously, to pH value of solution=
Suction filtration after 12, stirring 1.5h.It is subsequently placed into the dry 12h of 120 DEG C of vacuum drying chamber.Ground after drying, be put into 550 DEG C of roastings of Muffle furnace
Burn 4 hours, Fe-Mn/Al is made2O3Catalyst, wherein Fe load capacity are that 2%, Mn load capacity is 1%.
Embodiment 4
RTO emission three-phase catalytic deodorizations are carried out according to the method for embodiment 1.
RTO handles amine organic matter, and air quantity is 20000m3/ h, ignition temperature is 800 DEG C, has burning insufficient in tail gas
Amine substance, a small amount of benzene class and hydrogen chloride gas, there are problems that odor pollution.Purified treatment, RTO outlets are carried out to its tail gas
By cooling tower (NaOH concentration is 5wt%), temperature is down to 50 DEG C afterwards, and by three-phase catalytic deodorization, (ozone concentration is 80ppm, double
Oxygen water concentration is 4%, and solid-phase catalyst is MnO2/ high molecular polymerization iron salt catalyst [MnO2Load capacity is 3%]), tail gas is without evil
Foul smell taste, meets emission standard for odor pollutants.
Embodiment 5
RTO emission three-phase catalytic deodorizations are carried out according to the method for embodiment 1.
The main device that the present embodiment is used includes：Smoke cooling tower, three-phase catalytic odor removal.
RTO processing thioether, mercaptan organic matter, air quantity is 30000m3/h, and ignition temperature has burning at 820 DEG C, in tail gas not
, there is odor pollution in sufficient sulfurous organic compound, secondary pollution and sour gas.Purified treatment is carried out to its tail gas,
Gas passes through three-phase catalytic deodorization (ozone concentration by being cooled to 55 DEG C after smoke cooling tower (NaOH solution concentration is 7.5%)
For 50ppm, liquor natrii hypochloritis's concentration is 5%, and solid-phase catalyst is Fe-Mn/Al2O3[Fe load capacity is that 2%, Mn load capacity is
1%]), the ordorless smell of tail gas, meets emission standard for odor pollutants.
Claims (10)
1. a kind of RTO emissions three-phase catalytic deodorizing method, it is characterised in that this method comprises the following steps：
(1) tail gas after being burned by RTO is passed through smoke cooling tower, flue-gas temperature is down to 50~60 DEG C；
(2) flue gas after cooling down is handled by the air inlet of three-phase catalytic odor removal lower end into three-phase catalytic system, institute
The three-phase catalytic odor removal stated mainly is made up of ozone generator, main reaction tower, circulating pump and connecting pipe, valve；Ozone
Generator is connected by pipeline with the liquid storage tank of main reaction tower bottom；Gas phase catalyst ozone fills with liquid-phase catalyst in liquid storage tank
It is delivered to the spray equipment of main reaction top of tower after point mixing by circulating pump, gas, liquid mixed catalyst is from upper spray and lower warp
Cross the liquid storage tank that the catalytic reaction zone filled with solid-phase catalyst in the middle part of main reaction tower is finally returned to main reaction tower bottom；Into
The flue gas of main reaction tower is run from bottom to top, by solid catalysis reaction zone, is contacted with solid, liquid, gas three phase catalyst, consolidated,
Discharged after liquid, gas three phase catalyst joint catalytic degradation from the exhaust outlet of main reaction top of tower.
2. RTO emissions three-phase catalytic deodorizing method according to claim 1, it is characterised in that described flue gas cooling
Tower is alkali adsorption tower, removes sour gas present in flue gas while flue-gas temperature is reduced, alkali lye is NaOH solution, concentration
For 5~10wt%.
3. RTO emissions three-phase catalytic deodorizing method according to claim 1, it is characterised in that described main reaction tower
Material be stainless steel.
4. RTO emissions three-phase catalytic deodorizing method according to claim 1, it is characterised in that described ozone is added
Concentration is between 50~100ppm.
5. RTO emissions three-phase catalytic deodorizing method according to claim 1, it is characterised in that described liquid-phase catalysis
Agent is any one in hydrogen peroxide, sodium hypochlorite；Hydrogen peroxide concentration is in 1~5wt%, and sodium hypochlorite concentration is in 5~10wt%.
6. RTO emissions three-phase catalytic deodorizing method according to claim 1, it is characterised in that described solid catalysis
Selected from MnO2/ high molecular polymerization iron salt catalyst, Fe-Mn/Al2O3One kind of catalyst；MnO2/ high molecular polymerization molysite is catalyzed
MnO in agent2Load capacity is 1~10wt%, Fe-Mn/Al2O3Fe load capacity is in 1~10wt% in catalyst, and Mn load capacity is 1
~10wt%.
7. RTO emissions three-phase catalytic deodorizing method according to claim 6, it is characterised in that described MnO2/ high score
Sub- polymeric ferric salt catalyst, which is prepared by the following method, to be obtained：Weigh poly-ferric chloride to be placed in a certain amount of deionized water, stir
Simultaneously ultrasound 15-20 minutes are mixed, then addition manganese acetate, which is dissolved in above-mentioned solution, is stirred continuously, and KMnO is slowly added dropwise again afterwards4
Solution, temperature control reacts 45-60min at 75 DEG C, is filtered after the completion of reaction, with deionized water cyclic washing 5-6 times, then puts
Enter in vacuum drying chamber and be dried, obtain MnO2/ high molecular polymerization iron salt catalyst；Wherein poly-ferric chloride and manganese acetate
Mass ratio is 1:0.018775~0.18775；Poly-ferric chloride and KMnO4Quality mol ratio is 10g：1-10mol.
8. RTO emissions three-phase catalytic deodorizing method according to claim 6, it is characterised in that described Fe-Mn/
Al2O3Catalyst, which is prepared by the following method, to be obtained：Weigh 0.22~2.5g FeCl3, plus deionized water dissolving, by 7.5g
Al2O3Powder adds FeCl3In solution, stir 8-9 hours, solution is put into vacuum drying chamber after 85-90 DEG C of water bath method
110-120 DEG C of dry 12-14h；The Fe/Al that 1-10% is made for 5.5-6 hours in 600-620 DEG C of roasting of Muffle furnace is put into after grinding2O3
Catalyst；Then Mn is loaded with coprecipitation：It is 3 to weigh mass ratio:4 Fe/Al2O3And manganese acetate, plus deionized water dissolving,
Stirring 18h. and then the slow concentrated ammonia liquor that progressively increases during being stirred continuously, to pH value of solution=12, stir suction filtration after 1-1.5h.With
After be put into the dry 12-14h of 110-120 DEG C of vacuum drying chamber, ground after drying, be put into 550-600 DEG C of roasting 3.5-4 of Muffle furnace small
When, the Fe-Mn/Al that Fe and Mn load capacity is 1-10% is made2O3Catalyst.
9. for the three-phase catalytic odor removal of the RTO emission three-phase catalytic deodorizing methods described in claim 1, its feature
It is that described three-phase catalytic odor removal is main by ozone generator, main reaction tower, circulating pump and connecting pipe, valve group
Into；Main reaction tower bottom is liquid storage tank, and ozone generator is connected by pipeline with the liquid storage tank of main reaction tower bottom；Main reaction tower
Smoke air inlet be arranged above liquid storage tank；It is the catalytic reaction zone of filling solid-phase catalyst, main reaction in the middle part of main reaction tower
Spray equipment is provided with directly over top of tower, spray equipment inlet is connected with liquid storage tank by circulating pump and pipeline；Main reaction tower
Top-side is provided with flue gas exhaust mouthful.
10. a kind of RTO emissions three-phase catalytic deodoration system, it is characterised in that include smoke cooling tower and claim 9 institute
The three-phase catalytic odor removal stated.
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| CN109794148A (en) * | 2019-03-15 | 2019-05-24 | 深圳市兴能保环境科技有限公司 | A kind of method and device of Yi Hua enterprise RTO exhaust-gas treatment upgrading optimization |
| CN110772912A (en) * | 2019-09-30 | 2020-02-11 | 广州紫科环保科技股份有限公司 | Purification equipment for comprehensive waste gas of biological pharmaceutical factory |
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