CN107952366A - More bed catalyst reactors and application thereof - Google Patents
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- CN107952366A CN107952366A CN201711292193.2A CN201711292193A CN107952366A CN 107952366 A CN107952366 A CN 107952366A CN 201711292193 A CN201711292193 A CN 201711292193A CN 107952366 A CN107952366 A CN 107952366A
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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
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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
- B01D53/46—Removing components of defined structure
- B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
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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
- B01D53/8668—Removing organic compounds not provided for in B01D53/8603 - B01D53/8665
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1021—Platinum
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1023—Palladium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1025—Rhodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1026—Ruthenium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/206—Rare earth metals
- B01D2255/2065—Cerium
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- 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
Abstract
The problem of the present invention relates to a kind of more bed catalyst reactors and application thereof, mainly solve the supporting electric heater of catalyst oxidation reactor needs in the prior art and drive, and equipment investment is big.The present invention is by using a kind of more bed catalyst reactors, including hollow reactor body, the catalyst for catalytic oxidation being arranged in reactor body, it is characterized in that air inlet is provided with reactor body, gas outlet, catalyst are divided at least two layers, are low-temperature catalytic oxidation catalyst positioned at air inlet side, remaining preferably solves the above problem for the technical solution of common catalyzed oxidation reaction catalyst and application thereof, available in exhaust-gas treatment containing VOCs.
Description
Technical field
The present invention relates to a kind of more bed catalyst reactors and application thereof, suitable for the adsorption treatment of volatile organic waste gas
Field.
Background technology
Volatile organic matter (Volatile Organic Compounds abbreviation VOCs) refers to that boiling point is 50 under normal pressure
~260 DEG C of organic compound, can be divided into aromatic hydrocarbon (benzene,toluene,xylene), ketone, aldehydes, amine by its chemical constitution
Class, halo class, unsaturated hydro carbons etc..VOCs is harmful to the Health and Living environment of people, and foul smelling, if people sucks for a long time
The organic exhaust gas of low concentration, can trigger cough, uncomfortable in chest, the asthma even chronic respiratory disease such as pulmonary emphysema, be generally acknowledged at present
Strong carcinogenic substance.In September, 2013, State Council prints and distributes《Prevention and control of air pollution action plan》, promote volatile organic matter pollution
Administer.Implement volatile organic matter comprehensive improvement in industries such as paint, coating, adhesive, organic chemical industry, packages printings.According to
《Discharge standard of air pollutants》(GB16297-1996) regulation, to organic extraordinary pollutant concentration of VOC emission mouth
Have and be distinctly claimed, it is specified that the emission limits of 33 kinds of atmosphere pollutions.Environmental protection, prevents and remedies pollution, and is not only enterprise and in itself may be used
Inherently required, and the social enviroment protection responsibility that enterprise should undertake of sustainable development strategy.Implementing VOC exhaust-gas treatments has now
Real, urgent necessity.
Catalysis oxidation is also known as non-flaming combustion or catalysis burning, it utilizes solid catalyst and oxygen at 200 DEG C -450 DEG C
Organic matter is converted into carbon dioxide and water by gas.Catalysis oxidation is more much lower than the temperature directly burnt, and process safety, organic matter are gone
Except rate is high, energy consumption is low, NOx secondary pollutions are not produced, industry volatile organic waste gas is mostly using at catalysis oxidation at present
Reason..Because catalyst granules is small, reaction process pressure drop is big, high energy consumption, in order to reduce the gas flow rate of catalyst bed windward side,
It is general all to do reactor short and stout or not only narrow but also high, cause that reactor shell material utilization amount is big, and reactor cost is higher.
A kind of deflector type catalyst oxidation reactor is disclosed in patent CN20413447U, its type of reactor is hollow
Tower structure, its left and right inside catalyst oxidation reactor respectively set 3 pieces of baffle plates, one layer are uniformly smeared in each baffle plate bottom
Relatively thin precious metal catalyst.Although such a structure can reduce the pressure drop of reactor well, gas is in tower due to folding
The influence of flowing plate, skewness, there are dead band, exhaust gas conversion rate are low for flowing.And whole catalytic oxidizing equipment needs to add using electricity
Hot device makes exhaust inlet temperatures reach firing temperature, adds equipment investment.
The content of the invention
The first technical problem to be solved by the present invention is that catalyst oxidation reactor needs supporting electrical heating in the prior art
The problem of device is driven, and equipment investment is big, there is provided a kind of new more bed catalyst reactors, need not with catalyst oxidation reactor
The advantages of supporting electric heater is driven, and equipment investment is small.The second technical problem to be solved by the present invention is to provide a kind of with solving
The purposes of the corresponding more bed catalyst reactors of one of technical problem certainly.
One of to solve the above problems, the technical solution adopted by the present invention is as follows：A kind of more bed catalyst reactors, including
Hollow reactor body, the catalyst for catalytic oxidation being arranged in reactor body, it is characterised in that set on reactor body
Air inlet, gas outlet are equipped with, catalyst is divided at least two layers, is low-temperature catalytic oxidation catalyst positioned at air inlet side, remaining
For common catalyzed oxidation reaction catalyst；Low-temperature catalytic oxidation catalyst is low temperature formaldehyde through catalytic oxidation catalyst, is closed for nanometer
Gold grain load C eO2Carrier, contains noble metal I；Common catalyzed oxidation reaction catalyst is II supported catalyst of noble metal.
In above-mentioned technical proposal, it is preferable that reactor is vertical or horizontal.
In above-mentioned technical proposal, it is preferable that reactor is cylinder tank.
In above-mentioned technical proposal, it is preferable that catalyst granules is divided into two layers of arrangement.
In above-mentioned technical proposal, it is highly preferred that reactor is vertical, air inlet is located at reactor head, catalyst bed
Upper strata is low-temperature catalytic oxidation catalyst.
In above-mentioned technical proposal, it is preferable that low-temperature catalytic oxidation catalyst can catalysis oxidation firing temperature be less than 100 DEG C
Chemicals；Common catalyzed oxidation reaction catalyst is II supported catalyst of noble metal, and noble metal II is Ru, Rh, Pt, with quality
Fraction meter, the content of the content 0.1-0.3%, Rh of Ru are 0.5-0.9%, the content 0.02-0.08% of Pt；Low-temperature catalytic oxidation
Catalyst is low temperature formaldehyde through catalytic oxidation catalyst, is Nanoalloy particulate load CeO2Carrier, contains noble metal I, noble metal I
For Ru, Rh, Pt, Pd, in terms of mass fraction, the content of the content 0.1-0.3%, Rh of Ru is 0.2-0.8%, the content of Pt
The content 1-2% of 0.2-0.5%, Pt.
In above-mentioned technical proposal, it is preferable that noble metal I is Ru, Rh, Pt, Pd, in terms of mass fraction, the content of Ru
The content of 0.25%, Rh be 0.5%, Pt content 0.35%, the content 1.25% of Pt；Common catalyzed oxidation reaction catalyst
Carrier is aluminium oxide, and noble metal II is Ru, Rh, Pt, and in terms of mass fraction, the content 0.2% of Ru, the content of Rh is 0.7%,
The content 0.05% of Pt.
In above-mentioned technical proposal, it is preferable that low-temperature catalytic oxidation reaction bed temperature is 60~160 DEG C；It is common catalyzed
Oxidation reaction catalyst bed temperature is 200~405 DEG C.
In above-mentioned technical proposal, it is preferable that the concentration of VOCs is 2000~6500mg/m in the exhaust gas that air inlet enters3；
The concentration of VOC is 0~100mg/m in exhaust gas in reactor outlet3。
For solve the above problems two, the technical solution adopted by the present invention is as follows：A kind of use of more bed catalyst reactors
On the way, in the catalytic purification processing of the exhaust gas containing VOCs.
The present invention provides a kind of more bed catalyst reactors, and catalyst is divided into two layers, is low temperature first close to air inlet side
Aldehyde catalyst for catalytic oxidation, other is common catalyst oxidation reactor, makes full use of formaldehyde low-temperature catalytic oxidation reaction heat pre-
Hot phase logistics, without setting electric heater, effectively reduces investment and energy consumption, achieves preferable technique effect.
Brief description of the drawings
Fig. 1 is one of more bed catalyst reactor schematic diagrames of the present invention；
Fig. 2 is one of catalyst oxidation reactor schematic diagram of the prior art；
In Fig. 1-Fig. 2,1- air inlet 2- low-temperature catalytic oxidation catalyst 3- catalyst for catalytic oxidation 4- gas outlets.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Embodiment 1】
A kind of catalyst oxidation reactor of more beds, its structure are shown in Fig. 1, and reactor is cylindric, size OD800*
5000mm, air inlet port dimensions OD150, gas outlet size OD150, built-in 2 layers of catalyst for catalytic oxidation, upper strata are low-temperature catalyzed oxygen
Change catalyst granules, be Nanoalloy particulate load CeO2Carrier, containing Ru, Rh, Pt, Pd noble metal, in terms of mass fraction,
The content 0.25% of Ru, the content of Rh are the content 0.35% of 0.5%, Pt, the content 1.25% of Pt, particle diameter 3mm, porosity
0.4, bed height 1000mm, lower catalyst agent are that (for noble-metal-supported catalyst, carrier is oxygen to common catalyzed oxidation catalyst
Change aluminium, containing Ru, Rh, Pt noble metal, in terms of mass fraction, the content 0.2% of Ru, the content of Rh is the content of 0.7%, Pt
0.05%), bed height 3000mm.500m3The VOCs exhaust gas of/h, wherein concentration of formaldehyde 4500mg/m3, other VOCs components
Concentration is 1200mg/m3, temperature 60 C, pressure 0.05atm, enters reactor by air inlet (1), is then passed through low temperature formaldehyde
Catalyst oxidation reactor (bed inlet temperature be 60 DEG C), the formaldehyde in exhaust gas release reaction heat by catalysis oxidation, make exhaust gas
Temperature appreciate 200 DEG C, then common catalyst bed of entering, other VOCs components in exhaust gas be broken down into carbon dioxide and
Water, VOCs components conversion ratio 99%, temperature is appreciated 250 DEG C after leaving catalyst bed, and purified gas is by gas outlet
(2) discharge, exhaust gas qualified discharge directly after catalyst oxidation reactor is handled.
【Embodiment 2】
A kind of catalyst oxidation reactor of more beds, its structure are shown in Fig. 1, and reactor is cylindric, size OD100*
600mm, air inlet port dimensions OD20, gas outlet size OD20, built-in 2 layers of catalyst for catalytic oxidation, upper strata is low-temperature catalytic oxidation
Catalyst granules, is Nanoalloy particulate load CeO2Carrier, contains Ru, Rh, Pt, Pd noble metal, in terms of mass fraction, Ru's
Content 0.25%, the content of Rh are the content 0.35% of 0.5%, Pt, the content 1.25% of Pt, particle diameter 3mm, porosity 0.4,
Bed height 100mm, lower catalyst agent be common catalyzed oxidation catalyst (for noble-metal-supported catalyst, carrier is aluminium oxide,
Containing Ru, Rh, Pt noble metal, in terms of mass fraction, the content 0.2% of Ru, the content of Rh is the content of 0.7%, Pt
0.05%), bed height 400mm.50m3The VOCs exhaust gas of/h, wherein concentration of formaldehyde 1500mg/m3, other VOCs components it is dense
Spend for 4500mg/m3, 160 DEG C, pressure 0.05atm of temperature, enters reactor by air inlet (1), is then passed through low temperature formaldehyde
Catalyst oxidation reactor (bed temperature be 160--205 DEG C), the formaldehyde in exhaust gas are released reaction heat by catalysis oxidation, are made
The temperature of exhaust gas is appreciated 205 DEG C, then common catalyst bed of entering, other VOCs components in exhaust gas are broken down into titanium dioxide
Carbon and water, VOCs components conversion ratio 99%, temperature is appreciated 335 DEG C after leaving catalyst bed, and purified gas passes through outlet
Mouth (2) discharge, exhaust gas qualified discharge directly after catalyst oxidation reactor is handled.
【Embodiment 3】
A kind of catalyst oxidation reactor of more beds, its structure are shown in Fig. 1, and reactor is cylindric, size OD100*
600mm, air inlet port dimensions OD20, gas outlet size OD20, built-in 2 layers of catalyst for catalytic oxidation, upper strata is low-temperature catalytic oxidation
Catalyst granules, is Nanoalloy particulate load CeO2Carrier, contains Ru, Rh, Pt, Pd noble metal, in terms of mass fraction, Ru's
Content 0.25%, the content of Rh are the content 0.35% of 0.5%, Pt, the content 1.25% of Pt, particle diameter 3mm, porosity 0.4,
Bed height 100mm, lower catalyst agent be common catalyzed oxidation catalyst (for noble-metal-supported catalyst, carrier is aluminium oxide,
Containing Ru, Rh, Pt noble metal, in terms of mass fraction, the content 0.2% of Ru, the content of Rh is the content of 0.7%, Pt
0.05%), bed height 400mm.50m3The VOCs exhaust gas of/h, wherein methanol concentration 1500mg/m3, other VOCs components it is dense
Spend for 500mg/m3, 160 DEG C, pressure 0.05atm of temperature, enters reactor by air inlet (1), is then passed through low-temp methanol
Catalyst oxidation reactor (bed temperature be 160-205 DEG C), the methanol in exhaust gas release reaction heat by catalysis oxidation, make to give up
The temperature of gas is appreciated 205 DEG C, then common catalyst bed of entering, other VOCs components in exhaust gas are broken down into carbon dioxide
And water, VOCs components conversion ratio 99%, temperature is appreciated 225 DEG C after leaving catalyst bed, and purified gas is by gas outlet
(2) discharge, exhaust gas qualified discharge directly after catalyst oxidation reactor is handled.
【Embodiment 4】
A kind of catalyst oxidation reactor of more beds, its structure are shown in Fig. 1, and reactor is cylindric, and to be horizontal, size is
OD100*600mm, air inlet port dimensions OD20, gas outlet size OD20, built-in 2 layers of catalyst for catalytic oxidation, upper strata is urged for low temperature
Change oxidation catalyst particles, be Nanoalloy particulate load CeO2Carrier, containing Ru, Rh, Pt, Pd noble metal, with mass fraction
Meter, the content 0.25% of Ru, the content of Rh are the content 0.35% of 0.5%, Pt, the content 1.25% of Pt, particle diameter 3mm, hole
Rate 0.4, bed height 100mm, for common catalyzed oxidation catalyst, (for noble-metal-supported catalyst, carrier is for lower catalyst agent
Aluminium oxide, containing Ru, Rh, Pt noble metal, in terms of mass fraction, the content 0.2% of Ru, the content of Rh is containing for 0.7%, Pt
Measure 0.05%), bed height 400mm.50m3The VOCs exhaust gas of/h, wherein methanol concentration 1300mg/m3, other VOCs components
Concentration is 5200mg/m3, 160 DEG C, pressure 0.05atm of temperature, enters reactor by air inlet (1), is then passed through low temperature first
Alcohol catalysis oxidation reactor (bed temperature be 160-200 DEG C), the methanol in exhaust gas are released reaction heat by catalysis oxidation, are made
The temperature of exhaust gas is appreciated 200 DEG C, then common catalyst bed of entering, other VOCs components in exhaust gas are broken down into titanium dioxide
Carbon and water, VOCs components conversion ratio 99%, temperature is appreciated 405 DEG C after leaving catalyst bed, and purified gas passes through outlet
Mouth (2) discharge, exhaust gas qualified discharge directly after catalyst oxidation reactor is handled.
【Comparative example 1】
A kind of conventional catalyst oxidation reactor, its structure are shown in Fig. 1, and reactor is cylindric, size OD800*
5000mm, air inlet port dimensions OD150, gas outlet size OD150, built-in catalyst for catalytic oxidation, particle diameter 3mm, porosity 0.4,
Bed height 4000mm.500m3The VOCs exhaust gas of/h, the wherein concentration of VOCs components are 1200mg/m3, temperature 60 C, pressure
For 0.05atm, reactor is entered by air inlet (1), into catalyst bed, because intake air temperature is too low, the conversion of VOCs components
Rate is almost nil, and catalyst for catalytic oxidation is almost without playing catalytic effect.【Comparative example 2】
A kind of conventional catalyst oxidation reactor, its structure are shown in Fig. 1, and reactor is cylindric, size OD800*
5000mm, air inlet port dimensions OD150, gas outlet size OD150, built-in catalyst for catalytic oxidation, particle diameter 3mm, porosity 0.4,
Bed height 4000mm.500m3The VOCs exhaust gas of/h, the wherein concentration of VOCs components are 1200mg/m3, 200 DEG C of temperature, pressure
For 0.05atm, reactor is entered by air inlet (1), into catalyst bed, VOCs components conversion ratio 99%, leaves catalysis
Temperature is appreciated 250 DEG C after agent bed, and purified gas is discharged by gas outlet (2), and exhaust gas is directly through catalyst oxidation reactor
Qualified discharge after processing.
Contrasted from embodiment 1 and comparative example 1, reactor of the present invention and the reaction being commonly used in comparative example 1
Device is compared, and loads the catalyst of same volume, catalysis oxidation VOCs exhaust gas, the VOCs component conversion ratios of the device in embodiment 1
Up to 98%, and the catalyst in embodiment 1 is almost without catalytic effect.Contrasted from embodiment 2 and comparative example 2, when will be into
Temperature degree is carried to the catalyst in comparative example 2 is entered back into after 200 degree by 160 degree, and catalyst just plays catalytic oxidation effect.By
Upper to understand, more bed catalyst oxidation reactors, can obviously reduce the inlet temperature of reactor.
The present invention provides a kind of more bed catalyst reactors, and catalyst is divided into two layers, and upper strata is low temperature formaldehyde through catalytic oxidation
Catalyst, lower floor are common catalyst oxidation reactor, make full use of formaldehyde low-temperature catalytic oxidation reaction heat to preheat gaseous stream,
Electric heater need not be set, effectively reduce investment and energy consumption, achieve preferable technique effect.
Claims (10)
1. a kind of more bed catalyst reactors, including hollow reactor body, the catalysis oxidation being arranged in reactor body
Catalyst, it is characterised in that air inlet, gas outlet are provided with reactor body, catalyst is divided at least two layers, positioned at air inlet
Mouthful side for low-temperature catalytic oxidation catalyst, remaining is common catalyzed oxidation reaction catalyst；Low-temperature catalytic oxidation catalyst is
Low temperature formaldehyde through catalytic oxidation catalyst, is Nanoalloy particulate load CeO2Carrier, contains noble metal I；Common catalyzed oxidation is anti-
It is II supported catalyst of noble metal to answer catalyst.
2. more bed catalyst reactors according to claim 1, it is characterised in that reactor is vertical or horizontal.
3. more bed catalyst reactors according to claim 1, it is characterised in that reactor is cylinder tank.
4. more bed catalyst reactors according to claim 1, it is characterised in that catalyst granules is divided into two layers of arrangement.
5. according to the more bed catalyst reactors of claim 1,2, it is characterised in that reactor is vertical, and air inlet is positioned at anti-
Answer at the top of device, catalyst bed upper strata is low-temperature catalytic oxidation catalyst.
6. more bed catalyst reactors according to claim 1, it is characterised in that low-temperature catalytic oxidation catalyst can be catalyzed
Oxidation and ignition temperature is less than 100 DEG C of chemicals；Common catalyzed oxidation reaction catalyst is II supported catalyst of noble metal, your gold
It II is Ru, Rh, Pt to belong to, and in terms of mass fraction, the content of the content 0.1-0.3%, Rh of Ru is 0.5-0.9%, the content of Pt
0.02-0.08%；Low-temperature catalytic oxidation catalyst is low temperature formaldehyde through catalytic oxidation catalyst, is Nanoalloy particulate load CeO2
Carrier, containing noble metal I, noble metal I is Ru, Rh, Pt, Pd, in terms of mass fraction, the content of the content 0.1-0.3%, Rh of Ru
For 0.2-0.8%, the content 1-2% of the content 0.2-0.5%, Pt of Pt.
7. more bed catalyst reactors according to claim 6, it is characterised in that noble metal I is Ru, Rh, Pt, Pd, with quality
Fraction meter, the content 0.25% of Ru, the content of Rh are the content 0.35% of 0.5%, Pt, the content 1.25% of Pt；It is common catalyzed
The carrier of oxidation reaction catalyst is aluminium oxide, and noble metal II is Ru, Rh, Pt, in terms of mass fraction, the content 0.2% of Ru, and Rh
Content be 0.7%, Pt content 0.05%.
8. more bed catalyst reactors according to claim 1, it is characterised in that low-temperature catalytic oxidation reaction bed temperature
For 60-160 DEG C；Common catalyzed oxidation reaction catalyst bed temperature is 200-405 DEG C.
9. more bed catalyst reactors according to claim 1, it is characterised in that VOCs's is dense in the exhaust gas that air inlet enters
Spend for 2000~6500mg/m3；The concentration of VOC is 0~100mg/m in exhaust gas in reactor outlet3。
10. a kind of purposes of more bed catalyst reactors, more bed catalyst reactors described in by claim 1-9 are used to contain
In the catalytic purification processing of VOCs exhaust gas.
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| CN113209816A (en) * | 2020-01-21 | 2021-08-06 | 中国石油化工股份有限公司 | Catalyst grading method for catalytic oxidation of sulfur-containing VOCs and method for catalytic oxidation of sulfur-containing VOCs |
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