CN103657403B - A kind of method of batch-type plasma-catalytic reaction system and process waste gas thereof - Google Patents
A kind of method of batch-type plasma-catalytic reaction system and process waste gas thereof Download PDFInfo
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Abstract
The invention discloses a kind of method of batch-type plasma-catalytic reaction system and process waste gas thereof, reaction system comprises: transfer valve; The exhaust inlet pipe be connected with transfer valve and air pump; By some cover two-part plasma adsoption catalysis reactors of transfer valve parallel connection; For detecting the Tail gas measuring device of two-part plasma adsoption catalysis reactor tail gas pollutant levels information.Adopt many cover two-part plasma adsoption catalysis reactors in parallel in the present invention, cooperatively interact between many covers two-part plasma adsoption catalysis reactor, wherein a part of two-part plasma adsoption catalysis reactor carries out exhaust-gas treatment, another part two-part plasma adsoption catalysis reactor carries out adsorbent and catalyst regeneration, alternate cycles is carried out, realize the batch-type process of waste gas, ensure that exhaust treatment efficiency maintains higher level, realize the in-situ regeneration of absorption/catalyst simultaneously.
Description
Technical field
The present invention relates to the reaction system that plasma-catalytic administers gaseous contaminant, be specifically related to a kind of method of batch-type plasma-catalytic reaction system and process waste gas thereof.
Background technology
The heterogeneous adsoption catalysis reactor of plasma is generally divided into one-part form (IPC) and two-part (PPC), such as, publication number is the reactor that the Chinese invention patent application of CN102179145A discloses a kind of plasma-catalytic govern coordinately VOCs, comprise cylindrical shell, cylindrical shell is quartz glass tube, the outside wall surface coated metal conducting objects of quartz glass tube, metallic conduction thing connects the external electrode of ac high voltage source as dielectric barrier discharge; Inner barrel middle arranges stainless steel tube, and stainless steel tube ground connection is as electrode in dielectric barrier discharge; The perforate of stainless steel tube tube wall, and connect external air source; Form discharge air-gap between quartz glass tube and stainless steel tube, in discharge air-gap, fill adsorbent and catalyst; One end of cylindrical shell is air inlet end, and the other end is gas outlet end, and air inlet end and gas outlet end are respectively equipped with airflow uniform distribution plate.
Publication number is that CN101920156A discloses a kind of two-section low-temperature plasma waste gas purifying device that effectively can reduce energy consumption and control accessory substance, comprise high speed plasma oxidator, aerosol grower and low speed plasma collecting and treating apparatus, described high speed plasma oxidator comprises the first reactor and the first power supply, described low speed plasma collecting and treating apparatus comprises the second reactor and second source, is connected respectively before and after described aerosol grower with the first reactor and the second reactor.Waste gas enters the first reactor and carries out oxidation processes, gas after the preliminary purification obtained and solid phase byproduct enter aerosol grower, solid phase byproduct is collected in the second reactor after coalescence, growth in aerosol grower, thus reach the object making full use of active material and remove accessory substance, realize energy consumption low, the effect of non-secondary pollution.
No matter but be one-part form or two-part, have the common shortcoming being difficult to overcome, be exactly the passivation of catalyst and the saturation problem of adsorbent.In the heterogeneous adsoption catalysis reactor of plasma, because long gaseous contaminant and accessory substance thereof are piled up at adsorbent and catalyst coating, adsorbent starts slowly saturated, catalyst is also by passivation gradually, the treatment effeciency of subsequent contamination thing starts slowly to reduce, until the exhaust emissions concentration of pollutant exceedes certain value in system.Thus need to regularly replace the catalyst in reactor and adsorbent, and period gaseous contaminant tail gas concentration will have the risk exceeded standard, even when changing adsorbent and catalyst, emission-control equipment needs a period of time of stopping transport.This has not only increased the weight of operating cost, also add operation easier, make whole service process become loaded down with trivial details in Practical Project uses.
Summary of the invention
The invention provides a kind of method of batch-type plasma-catalytic reaction system and process waste gas thereof, solve that adsorbent is saturated, the in-situ regeneration problem of catalyst, not only saved operating cost, and simplified Engineering operation.
A kind of batch-type plasma-catalytic reaction system, comprising:
Transfer valve;
The exhaust inlet pipe be connected with transfer valve and air pump;
By some cover two-part plasma adsoption catalysis reactors of transfer valve parallel connection;
For detecting the Tail gas measuring device of the exhaust pollutant concentration information of described two-part plasma adsoption catalysis reactor.
Described transfer valve is preferably cross valve.
Adopt many cover two-part plasma adsoption catalysis reactors in parallel in the present invention, cooperatively interact between many covers two-part plasma adsoption catalysis reactor, wherein a part of two-part plasma adsoption catalysis reactor carries out exhaust-gas treatment, another part two-part plasma adsoption catalysis reactor carries out adsorbent and catalyst regeneration, alternate cycles is carried out, realize the batch-type process of waste gas, ensure that exhaust treatment efficiency maintains higher level, realize the in-situ regeneration of absorption/catalyst simultaneously.
As preferably, be also provided with the exhaust pollutant concentration information for gathering from described Tail gas measuring device and control the electrical signal control of transfer valve and air pump.This electrical signal control can adopt electrical signal control commonly known in the art, such as comparator.Arrange the automatic switchover that electrical signal control can realize between waste gas and air, ensure at least a set of two-part plasma adsoption catalysis reactor for treatment waste gas, at least a set of two-part plasma adsoption catalysis reactor carries out adsorbing/catalyst regeneration.
As the preferred technical scheme of one, described two-part plasma adsoption catalysis reactor is set to two covers parallel with one another.
Waste gas passes into reaction system and carries out purified treatment by two-period form plasma adsoption catalysis reactor, along with the increase of running time, the inactivation passivation gradually of adsorbent and catalyst, system afterbody detector detects that in tail gas, the concentration of pollutant raises gradually, when rising to a certain setting value, detector gives the alarm, electrical signal control starts, and cross valve rotates and waste gas is switched to another two-period form plasma adsoption catalysis reactor.Meanwhile, air blasts in the gas circuit of first last road by air pump startup, and under the continuous effect of plasma adsoption catalysis reactor, its high activity particle produced (comprises O
3, O, OH etc.), by being adsorbed on the pollutant oxidation removal in adsorbent and catalyst surface and duct, to realize the in-situ regeneration of adsorbent and catalyst.And plasma process can increase the specific area of absorption/catalyst, improve space distribution, fortifying catalytic performance, improve the overall contaminant-removal properties of absorption/catalyst.When the oxidation product of pollutant is (as CO, CO
2) concentration maintain reduced levels a period of time after, electrical signal control starts, and air pump and high voltage source are closed, and in-situ regeneration process terminates, and two-period form plasma adsoption catalysis reactor is stand-by.
When adopting two cover arranged side by side, Tail gas measuring device can be equipped with one by every suit, so just Real-Time Monitoring can be realized, also a Tail gas measuring device can be shared by two covers, so just periodic monitor is carried out to the tail gas of two cover plasma adsoption catalysis reactors, preferably, each outfit Tail gas measuring device, Real-Time Monitoring is carried out to tail gas, the switching of automatic control switch valve and air pump.
The present invention preferably adopts two cover two-part plasma adsoption catalysis reactors in parallel, wherein for two-part plasma adsoption catalysis reactor itself, this area can be adopted to know generally acknowledged conventional equipment altogether, in the present invention, in order to improve treatment effect further, cost-saving, the basis of parallel connection is improved the corona discharge region of two-part plasma adsoption catalysis reactor.
That is: described two-part plasma adsoption catalysis reactor comprise connect successively corona discharge region, airflow uniform distribution district and adsoption catalysis district, described corona discharge region is connected with transfer valve, described corona discharge region is the alveolate texture of several cylinders composition, and each cylinder is as a discharge cell.
Sparking electrode in described discharge cell adopts wolf's fang stick electrode, i.e. following preferred embodiment:
Described discharge cell comprises cylindrical shell and is positioned at the Centromedian sparking electrode of cylindrical shell, and described sparking electrode comprises: the stainless steel inner core being positioned at cylindrical shell; Be coated on the stainless steel iron sheet on stainless steel inner core; Be positioned at several prickles on stainless steel iron sheet.
Further preferably, described prickle is the isosceles triangle shape of turning up to same direction, and the height of described prickle is 0.5 ~ 1cm and the thorn point of all prickles is positioned on the same face of cylinder.
Further preferably, described prickle is uniformly distributed on stainless steel iron sheet, and distribution density is 300 ~ 500/m
2.
Further preferably, the discharging gap in described discharge cell is 3 ~ 5cm.Discharging gap refers to the distance of prickle tip to outer casing inner wall.
The diameter of described stainless steel inner core is 1 ~ 2cm, and the thickness of described stainless steel iron sheet is 1 ~ 2mm; Described cylindrical shell adopts stainless steel.
The anode of sparking electrode of the present invention adopts wolf's fang stick electrode, and prickle is evenly distributed, easy to process, and the height of prickle is consistent, and in prickle point discharge, discharge current is large.By controlling the base length of isosceles triangle, the density of prickle can well be controlled, improving the prickle distributive law of unit are, increase power-discharging density, avoid the corona blocking problem caused by crossing closely between prickle simultaneously, improve discharge effect, the generation of accelerating oxidation free love base.After treatment system of the present invention adopts the preferred sparking electrode of the present invention, better to the regeneration effect of the treatment effect of waste gas and absorption/catalyst, better economize on resources.
Present invention also offers and a kind ofly utilize described batch-type plasma-catalytic reaction system to carry out the method for exhaust-gas treatment, comprise the steps:
(1) waste gas is sent into wherein at least a set of two-part plasma adsoption catalysis reactor by transfer valve, discharge as tail gas after Corona discharge Treatment, uniform process and adsoption catalysis process successively, gaseous contaminant concentration information in real time or in periodic monitor tail gas, and be transferred to electrical signal control, guarantee in this step that at least a set of two-part plasma adsoption catalysis reactor is in idle state;
(2) when gaseous contamination substrate concentration reaches setting value, absorption/catalyst in this cover two-part plasma adsoption catalysis reactor is saturated, electrical signal control sends switching signal to transfer valve and air pump, controlling transfer valve switches in two-part plasma adsoption catalysis reactor idle in step (1) by waste gas, the air blasted by air pump switches to and carries out in step (1), in the two-part plasma adsoption catalysis reactor of exhaust-gas treatment, regenerating absorption/catalyst;
Step (1) and step (2) alternate cycles are carried out.
For the system that two cover two-part plasma adsoption catalysis reactors are arranged side by side: comprise the steps:
(1) waste gas is entered by transfer valve and wherein discharges as tail gas after Corona discharge Treatment, even gas distribution process and adsoption catalysis process successively in a set of two-part plasma adsoption catalysis reactor, gaseous contaminant concentration information in real time or in periodic monitor tail gas, and be transferred to electrical signal control, another set of two-part plasma adsoption catalysis reactor idle state in this step;
(2) when gaseous contamination substrate concentration reaches setting value, adsorbent in this cover two-part plasma adsoption catalysis reactor and catalyst saturated, electrical signal control sends switching signal to transfer valve and air pump, air pump is opened, controlling transfer valve switches in another set of two-part plasma adsoption catalysis reactor by waste gas, the air blasted by air pump switches to and carries out in step (1), in the two-part plasma adsoption catalysis reactor of exhaust-gas treatment, regenerating adsorbent and catalyst;
Step (1) and step (2) alternate cycles are carried out.
The recovery time of adsorbent and catalyst is shorter than the time of exhaust-gas treatment, guarantees that sequencing batch reactor can carry out continuously.
As preferably, the adsorbent of all two-part plasma adsoption catalysis reactors is organobentonite, and catalyst cupport on the sorbent; Catalyst cupport on the sorbent after carry out plasma modification again.
Organobentonite is obtained by conventional method, and catalyst cupport is on organobentonite, and loading process adopts this area conventional method.Modification is carried out again afterwards by plasma method.
The modifying process of described plasma modification is:
The organobentonite of catalyst load is had to put into needle plate type plasma reactor, simultaneously at T
temperature=80-100 DEG C, H
absolute humidityslowly passed into by air in needle plate type plasma reactor under=3 ~ 5% condition, regulation voltage 15 ~ 20kV, energy density is 50-200J/L, and discharge time is 3-6h.
The needle plate type plasma reactor that described needle plate type plasma reactor is known to the skilled person.
Bentonite enriches in Mineral Resources in China, is distributed in 23 province and municipalities, proved reserves more than 2,000,000,000 tons.Bentonite, after organically-modified, has good adsorption capacity to organic matter.Organobentonite is again after plasma modification, and its adsoption catalysis ability promotes further.Its principle can produce the active material with strong oxidizing property in plasma electric field (to comprise O
3, O, OH etc.), these active materials can make the organic matter in organobentonite comprise the whole oxidized removing of surfactant CTMAB and cosurfactant DDA, form a large amount of micropores after oxidation, contribute to absorption.There is physical aspect and chemical valence state change in catalyst simultaneously in plasma discharge processes, and its oxidability promotes further.
Described catalyst is one or more in silver, manganese, titanium, aluminium, cobalt and their oxide thereof, can load on organobentonite.Silver, manganese, titanium, aluminium, cobalt and their oxide thereof can (100 ~ 300 DEG C) react at a lower temperature as catalyst, avoid the condition of high temperature that gaseous contaminant is degraded, contribute to the compound of oxidative free radical at these catalyst surfaces simultaneously, extend radical life, improve the degradation effect of gaseous contaminant.In the selection of catalyst, need to consider economy and ready availability simultaneously.Conventional catalyst has: TiO
2, Al
2o
3, Ag/TiO
2, Ag/Al
2o
3, TiO
2/ Al
2o
3, Ag/TiO
2, MnO
2, CoO
3, WO
3deng.
The present invention compared with prior art has following beneficial effect:
1, achieve the uninterrupted purified treatment of gaseous contaminant, solve change adsorbent and catalyst in reactor time space in the gaseous contaminant problem that cannot be processed, reduce operation easier and complexity to a certain extent.
2, achieve the in-situ regeneration of adsorbent and catalyst, effectively can solve the problem of the saturated and catalyst structure of adsorbent in reactor, greatly reduce operating cost.And be innocuous substance by contaminant degradation, solve the problem that the adsorbent cemented out forms secondary pollution.
3, the unmanned management of gaseous contaminant gas purification is achieved, system adopts Automated condtrol, gaseous contamination substrate concentration in tail gas is detected by the detection for gaseous contaminants device timing of tail gas, when gaseous contaminant exceedes finite concentration, electric signal switch controller gives the alarm signal, cross valve automatically switches, and gaseous contaminant gas circuit is automatically switched to another set of reactor.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of duty of the present invention.
Fig. 2 is the structural representation of the another kind of duty of the present invention.
Fig. 3 is the structural representation of discharge cell of the present invention.
Detailed description of the invention
As shown in Figures 1 to 3, a kind of batch-type plasma reaction system, comprises the two-part plasma adsoption catalysis reactor that many covers are in parallel, in present embodiment, in parallel for two covers.
Air inlet pipe is connected with the air inlet of transfer valve 1, the plasma adsoption catalysis reactors (first two-part plasma adsoption catalysis reactor 2 and the second two-part plasma adsoption catalysis reactor 3) such as transfer valve 1 is preferably cross valve, two cover two-parts are by this four-way valve connection in parallel.
First two-part plasma adsoption catalysis reactor 2 comprises corona discharge region 201, airflow uniform distribution district (not shown) and adsoption catalysis district 202, corona discharge region 201 is connected with cross valve, airflow uniform distribution district and adsoption catalysis district 202 all adopt the conventional equipment of this area, improve in present embodiment and be mainly corona discharge region 201, arrange some discharge cells arranged side by side in corona discharge region, the cross section of corona discharge region becomes cellular.
The structure of discharge cell as shown in Figure 3, is cylindrical shape, and comprise cylindrical shell 203 and be positioned at the sparking electrode of cylindrical shell 203 center, cylindrical shell 203 adopts stainless steel casing.
Sparking electrode is set to wolf's fang stick electrode, and this wolf's fang stick electrode comprises: the stainless steel inner core 204 being positioned at cylindrical shell 203 center; Be coated on the stainless steel iron sheet 205 on stainless steel inner core 204; Be positioned at several prickles 206 on stainless steel iron sheet 205.
The diameter of stainless steel inner core 204 is 1 ~ 2cm, and the thickness of stainless steel iron sheet 205 is 1 ~ 2mm; The internal diameter of cylindrical shell 203 is 5 ~ 6cm, and the thick discharging gap met in discharge cell for 1mm(is 3 ~ 5cm); , discharge voltage is 15-20kv, and energy density is 50-200J/L.
Prickle 206 is the isosceles triangle shape of turning up to same direction, and the height of prickle is 0.5 ~ 1cm and the thorn point of all prickles is in the same plane; Prickle 206 is uniformly distributed on stainless steel iron sheet 205, and distribution density is 300 ~ 500/m
2; Stainless steel sleeve is negative electrode, and wolf's fang stick electrode is anode.
Second two-part plasma adsoption catalysis reactor 3 comprises corona discharge region 301, air-flow Yun Bu district's (not shown) and adsoption catalysis district 302, and its internal structure is consistent with the first two-part plasma adsoption catalysis reactor 2.
A Tail gas measuring device 6 is respectively configured at the adsoption catalysis district afterbody of two cover two-part plasma adsoption catalysis reactors, also a Tail gas measuring device 6 can be shared, in present embodiment, adopt the mode sharing a Tail gas measuring device 6, this Tail gas measuring device 6 is connected to the gas outlet in corresponding adsoption catalysis district.
Electrical signal control 5 connects Tail gas measuring device 6 and transfer valve 1, air pump 4 and is controlled by electrical signal control 5 and being communicated in two-way process gas circuit of interval.Electrical signal control 5 preferably adopts digital signal controller (DCS).
Adsorbent in the adsoption catalysis district of two cover two-part plasma adsoption catalysis reactors is organobentonite, catalyst is carried on adsorbent with sol-gal process, and the organically-modified process of adsorbent and the loading process of catalyst all adopt this area routine techniques.In present embodiment, the modifying process of adsorbent and the loading process of catalyst as follows:
Bentonite preferably obtains from the montmorillonite ore deposit in the Inner Mongol, and its cation exchange capacity is 0.965mol/100g after testing, and be ground into 100 object fine graineds, its modifying process is:
Get surfactant softex kw (CTMAB) solution that 100g and the 1000mL concentration prepared in advance are 0.965mol/L fully to mix, under 60 DEG C of conditions, stir 2h, filter and place 24h at 100 DEG C of condition thermostatic drying chambers and dry obtained organobentonite (CTMAB-Bent); Obtained organobentonite (CTMAB-Bent) is ground to 100 order fine graineds, and get 2g and mix with mass ratio 1:1:120 with lauryl amine (DDA), silester (TEOS), under 60 DEG C of conditions, stir 4h, filter also natural air drying 12h and obtain supported sorbents organobentonite.
Catalyst cupport is on organobentonite, and loading process is: refer to and take a certain amount of organobentonite, carries out acidification with the sulfuric acid solution of 1mol/L, in the water-bath of 90 DEG C, carry out water-bath.Take out after water-bath 6h and filter, and dry 2h under 100 DEG C of conditions, then calcine 2h under 500 DEG C of conditions.Take the organobentonite of above-mentioned 5g process, put into the beaker of 250ml, then put into magnetic rotor, add 80ml absolute ethyl alcohol, stir with magnetic stirring apparatus, slowly add 10ml butyl titanate, then add red fuming nitric acid (RFNA) and the 10ml deionized water of 1ml0.1mol/L.Stir after 24 and take out, filter, filter paper washes with water to neutrality, then dry 6h under 100 DEG C of conditions, under 500 DEG C of conditions, finally calcine 6h make load and have TiO
2organobentonite.Described adsorption catalyst powder need increase its grain diameter by granulation, prevents it from being taken away by air-flow.
Catalyst cupport is placed on the sorbent in plasma electric field and carries out plasma modification, and process is as follows:
To load be had to have the machine bentonite of catalyst to put into needle plate type plasma reactor, simultaneously at T
temperature=80-100 DEG C, H
absolute humidityslowly be passed into by air in needle plate type plasma reactor under=3 ~ 5% condition, regulation voltage 15 ~ 20kV, energy density is 50-200J/L, and discharge time is after 3-6h, and the bentonite of taking-up is used for exhaust-gas treatment.
The technological process being carried out exhaust-gas treatment by this system is as follows:
(1) waste gas is entered in the first two-part plasma adsoption catalysis reactor 2 by transfer valve and discharges as tail gas after Corona discharge Treatment, uniform process and adsoption catalysis process successively, gaseous contaminant content information in real time or in periodic monitor tail gas, and being transferred to electrical signal control 5, in this step, the second two-part plasma adsoption catalysis reactor 3 leaves unused;
(2) when gaseous contaminant content reaches setting value (discharge standard according to different pollutant sets), absorption/catalyst in first two-part plasma adsoption catalysis reactor 2 is saturated, electrical signal control 5 sends switching signal to transfer valve 1 and air pump 4, controlling transfer valve 1 switches in the second two-part plasma adsoption catalysis reactor 3 by waste gas, the air that air pump 4 blasts is switched in the first two-part plasma adsoption catalysis reactor 2, absorption/catalyst is regenerated;
Step (1) and step (2) alternate cycles are carried out.
When employing many covers two-part plasma adsoption catalysis reactor is parallel, control mode is analogized by above-mentioned control mode.
Application examples 1
Laboratory simulation gas, exhaust-gas treatment amount 15L/min, toluene is as target contaminant, and its initial concentration is 260mg/m
3.System two cover two-period form plasma adsoption catalysis reactors arranged side by side, warning concentration is 60mg/m
3.The recovery time is 4 ~ 6h to two-period form plasma adsoption catalysis reactor at 35 ~ 40h running time.System runs 120h continuously, and the removal efficiency of toluene is generally all more than 80%, respond well.
Application examples 2
Certain pharmaceutical factory's formulating plant, exhaust-gas treatment amount is 2000m
3/ h, major pollutants are non-methane hydrocarbon material, its initial concentration <300mg/m
3.System two cover two-period form plasma adsoption catalysis reactors arranged side by side, warning concentration is 100mg/m
3.Long-term follow according to Practical Project is monitored, and two-period form plasma adsoption catalysis reactor can maintain 30 ~ 50d running time, and the recovery time is 5 ~ 10d.System runs more than 9 months continuously, and the removal efficiency of toluene is at least more than 70%.In addition according to measuring and calculating, adsorbent amount only has about 1/2 of regular activated CAM, greatly reduces operating cost.
Claims (9)
1. a batch-type plasma-catalytic reaction system, is characterized in that, comprising:
Transfer valve;
The exhaust inlet pipe be connected with transfer valve and air pump;
By some cover two-part plasma adsoption catalysis reactors of transfer valve parallel connection;
For detecting the Tail gas measuring device of the exhaust pollutant concentration information of described two-part plasma adsoption catalysis reactor;
Described two-part plasma adsoption catalysis reactor comprise connect successively corona discharge region, airflow uniform distribution district and adsoption catalysis district, described corona discharge region is connected with transfer valve, described corona discharge region is the alveolate texture of several cylinders composition, and each cylinder is as a discharge cell.
2. batch-type plasma-catalytic reaction system according to claim 1, is characterized in that, is also provided with the exhaust pollutant concentration information for gathering from described Tail gas measuring device and controls the electrical signal control of transfer valve and air pump.
3. batch-type plasma-catalytic reaction system according to claim 1, it is characterized in that, described two-part plasma adsoption catalysis reactor is set to two covers parallel with one another.
4. batch-type plasma-catalytic reaction system according to claim 1, it is characterized in that, described discharge cell comprises cylindrical shell and is positioned at the Centromedian sparking electrode of cylindrical shell, and described sparking electrode comprises: the stainless steel inner core being positioned at cylindrical shell; Be coated on the stainless steel iron sheet on stainless steel inner core; Be positioned at several prickles on stainless steel iron sheet.
5. batch-type plasma-catalytic reaction system according to claim 4, it is characterized in that, described prickle is the isosceles triangle shape of turning up to same direction, and the height of described prickle is 0.5 ~ 1cm and the thorn point of all prickles is positioned on the same face of cylinder.
6. batch-type plasma-catalytic reaction system according to claim 4, it is characterized in that, described prickle is uniformly distributed on stainless steel iron sheet, and distribution density is 300 ~ 500/m
2.
7. batch-type plasma-catalytic reaction system according to claim 4, it is characterized in that, the discharging gap in described discharge cell is 3 ~ 5cm.
8. utilize batch-type plasma-catalytic reaction system described in claim 1 to carry out a method for exhaust-gas treatment, it is characterized in that, comprise the steps:
(1) waste gas is sent into wherein at least a set of two-part plasma adsoption catalysis reactor by transfer valve, discharge as tail gas after Corona discharge Treatment, uniform process and adsoption catalysis process successively, gaseous contaminant concentration information in real time or in periodic monitor tail gas, and be transferred to electrical signal control, guarantee in this step that at least a set of two-part plasma adsoption catalysis reactor is in idle state;
(2) when gaseous contamination substrate concentration reaches setting value, absorption/catalyst in this cover two-part plasma adsoption catalysis reactor is saturated, electrical signal control sends switching signal to transfer valve and air pump, controlling transfer valve switches in two-part plasma adsoption catalysis reactor idle in step (1) by waste gas, the air blasted by air pump switches to and carries out in step (1), in the two-part plasma adsoption catalysis reactor of exhaust-gas treatment, regenerating absorption/catalyst;
Step (1) and step (2) alternate cycles are carried out.
9. method according to claim 8, it is characterized in that, the adsorbent of all two-part plasma adsoption catalysis reactors is organobentonite, and catalyst cupport is on the sorbent; Catalyst cupport on the sorbent after carry out plasma modification again; The modifying process of described plasma modification is:
The organobentonite of catalyst load is had to put into needle plate type plasma reactor, simultaneously at T
temperature=80-100 DEG C, H
absolute humidityslowly passed into by air in needle plate type plasma reactor under=3 ~ 5% condition, regulation voltage 15 ~ 20kV, energy density is 50-200J/L, and discharge time is 3-6h.
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| CN106390701A (en) * | 2016-10-31 | 2017-02-15 | 浙江富春江环保热电股份有限公司 | Multilevel plasma ultralow intensified smoke emission control system and multilevel plasma ultralow intensified smoke emission control method |
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| CN107486253B (en) * | 2017-08-30 | 2021-01-05 | 大连民族大学 | Ag/Al deactivated by dielectric barrier discharge plasma2O3Method for in-situ regeneration of catalyst |
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