CN109821408B - Device and method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation - Google Patents
Device and method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation Download PDFInfo
- Publication number
- CN109821408B CN109821408B CN201910182953.7A CN201910182953A CN109821408B CN 109821408 B CN109821408 B CN 109821408B CN 201910182953 A CN201910182953 A CN 201910182953A CN 109821408 B CN109821408 B CN 109821408B
- Authority
- CN
- China
- Prior art keywords
- reaction tube
- reaction
- ozone
- waste gas
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 42
- 230000003647 oxidation Effects 0.000 title claims abstract description 32
- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 128
- 239000002912 waste gas Substances 0.000 claims abstract description 64
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 34
- 230000003197 catalytic effect Effects 0.000 claims abstract description 18
- 230000002195 synergetic effect Effects 0.000 claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims description 80
- 239000007789 gas Substances 0.000 claims description 18
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 9
- 239000011521 glass Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 7
- 125000006850 spacer group Chemical group 0.000 claims description 7
- 239000002131 composite material Substances 0.000 claims description 6
- 239000010453 quartz Substances 0.000 claims description 5
- 229910052723 transition metal Inorganic materials 0.000 claims description 5
- 239000003365 glass fiber Substances 0.000 claims description 4
- 210000005239 tubule Anatomy 0.000 claims description 4
- 239000000741 silica gel Substances 0.000 claims description 3
- 229910002027 silica gel Inorganic materials 0.000 claims description 3
- 150000003624 transition metals Chemical class 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 229910052748 manganese Inorganic materials 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims 1
- 230000015556 catabolic process Effects 0.000 abstract description 7
- 238000006731 degradation reaction Methods 0.000 abstract description 7
- 238000006555 catalytic reaction Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000009776 industrial production Methods 0.000 abstract description 3
- 239000005416 organic matter Substances 0.000 abstract 1
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 27
- 239000002957 persistent organic pollutant Substances 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- MZZUATUOLXMCEY-UHFFFAOYSA-N cobalt manganese Chemical group [Mn].[Co] MZZUATUOLXMCEY-UHFFFAOYSA-N 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000011278 co-treatment Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005470 impregnation Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000004576 sand Substances 0.000 description 3
- 235000013162 Cocos nucifera Nutrition 0.000 description 2
- 244000060011 Cocos nucifera Species 0.000 description 2
- 239000000969 carrier Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 210000001503 joint Anatomy 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 208000005623 Carcinogenesis Diseases 0.000 description 1
- 208000031320 Teratogenesis Diseases 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000036952 cancer formation Effects 0.000 description 1
- 231100000504 carcinogenesis Toxicity 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000007794 irritation Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000007886 mutagenicity Effects 0.000 description 1
- 231100000299 mutagenicity Toxicity 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a device and a method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation. The device comprises a first reaction tube and a second reaction tube, wherein a filter, a waste gas preheating zone and a high-temperature catalytic reaction zone are arranged in the first reaction tube, and waste gas filtered by the filter enters the high-temperature catalytic reaction zone after being preheated by the waste gas preheating zone to complete catalytic oxidation reaction; then the waste gas enters a second reaction pipe, ozone is introduced into the second reaction pipe, simultaneously catalytic oxidation synergistic treatment is carried out, and finally an exhaust system is connected. Through the organic matter degradation treatment of the first reaction tube and the second reaction tube, the removal efficiency of the volatile organic matters can reach 97%, and the high-efficiency treatment of the volatile organic matters is realized. The device has the advantages of simple structure, convenient operation, low energy consumption, high treatment efficiency and the like in the volatile organic compound treatment, and can be widely applied to treating the volatile organic compounds generated in industrial production.
Description
Technical Field
The invention relates to the technical field of pollution control of volatile organic compounds, in particular to a device and a method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation.
Background
With the development of related industries such as chemical industry and petrochemical industry in China, a large number of volatile organic compounds (VOCs for short) including aromatics and derivatives thereof, alkanes, alkenes, alcohols, esters and the like are randomly discharged into the atmosphere. The environment-friendly organic pollutant not only directly harms human health and environmental safety, but also reacts with free radicals in the atmosphere, such as ozone, NOx, hydroxyl and the like to form photochemical smog and destroy the ozone layer, and becomes a main atmospheric pollutant.
Volatile Organic Compounds (VOCs) are a general name of a class of compounds, have irritation, teratogenesis, carcinogenesis and mutagenicity, are inflammable and explosive, and greatly threaten the health of human bodies and ecological systems.
Ozone is a gas with strong oxidizing properties that decomposes in air to form oxygen radicals and produce strong oxidizing radicals such as hydroxyl radicals, which react with most organic pollutants. The catalytic oxidation technology has become the mainstream VOCs treatment method at present due to the excellent performance, and is one of the most efficient treatment methods. Meanwhile, in the aspect of energy, the catalytic method can be well and effectively combined with the synergistic removal of various pollutants, so that the effects of energy conservation and emission reduction are achieved. Ozone-catalytic co-oxidation treatment of volatile organic pollutants is a technology that is of great interest and promising.
Disclosure of Invention
The invention aims to provide a device and a method for treating volatile organic compounds through ozone-catalytic synergistic oxidation. Volatile organic pollutants are treated through the synergistic effect of ozone oxidation and catalytic oxidation, and organic waste gas is purified. The method has the advantages of simple equipment, convenient operation, low energy consumption, high treatment efficiency and the like in the volatile organic compound treatment, and can be widely applied to treating various volatile organic compounds generated in industrial production.
The invention adopts the following technical scheme to achieve the aim.
A device for treating volatile organic compounds by ozone-catalytic oxidation comprises a first reaction tube, a second reaction tube, an ozone generating device and an exhaust system; the waste gas enters the first reaction pipe and the second reaction pipe in sequence and is exhausted through an exhaust system; the first reaction tube and the second reaction tube are of opening structures with air inlets and air outlets at two ends respectively, and openings at two ends are respectively provided with a rubber plug with a hole; the glass tubules are respectively inserted into the air outlet holes and the air inlet holes of the rubber plugs with holes of the first reaction tube and the second reaction tube, so that the first reaction tube and the second reaction tube are connected in series; the first reaction tube and the second reaction tube are respectively arranged in two tubular resistance furnaces, and the temperature in the two reaction tubes is respectively controlled by the tubular resistance furnaces; a filter is arranged in the first reaction tube close to the air inlet, m spacers are radially arranged behind the filter at intervals in the rear direction of the position 1/4-1/2 of the length of the first reaction tube, and m-1 catalyst cavities are enclosed in the first reaction tube; ozone generated by the ozone generating device enters a second reaction tube through a glass thin tube inserted into an air inlet of the second reaction tube through a hose and a flowmeter, n spacers are radially arranged in the second reaction tube at intervals, and n-1 catalyst cavities are enclosed in the second reaction tube; wherein: the spacer is a sand core plate, and a single catalyst or a composite catalyst of a porous carrier loaded with transition metal elements is arranged in the catalyst cavity.
In the present invention, m and n are integers of 2 or more.
In the invention, the first reaction tube and the second reaction tube are both made of quartz materials; the rubber plug with the hole is made of high-temperature-resistant silica gel material, and the filter is an HEPA filter with a filter element formed by glass fiber filter materials.
In the invention, the porous carrier is active carbon particles or aluminum oxide, and the transition metal is any one or more of Mn, Co, Fe or Cu.
In the invention, the temperature in the first reaction tube is controlled between 100-150 ℃, and the temperature in the second reaction tube is controlled between 80-100 ℃.
The invention also provides a method for carrying out ozone-catalytic oxidation synergistic treatment on volatile organic compounds by adopting the device, which comprises the following specific steps: filtering the waste gas in a first reaction tube by a filter to remove solid particles in the waste gas, and carrying out catalytic oxidation reaction after preheating treatment; then enters a second reaction pipe to perform catalytic oxidation reaction under the action of ozone, and finally the treated waste gas is accessed into an exhaust system.
In the invention, the flow rate of the waste gas passing through the first reaction tube and the second reaction tube is controlled within the range of 10-15L/min, and the flow rate is controlled within the range of 0.24-0.35 m/s.
In the invention, the introduction amount of ozone in the second reaction tube is controlled to be 20-35mL/min, the introduction amount of ozone is properly increased along with the increase of the gas flow in the reaction tube, but the introduction amount is not too high, and the ozone is ensured to be discharged after the reaction is finished.
In the invention, the filter in the first reaction pipe is an HEPA filter of which the filter element is made of a glass fiber filter material, and the HEPA filter has the function of intercepting solid particles in the exhaust gas so as to prevent the solid particles from entering catalyst pores of the first reaction pipe, so that the contact area between the exhaust gas and the catalyst is reduced due to the blockage of the catalyst pores, the adsorption of volatile organic compounds by a porous carrier and the catalytic reaction of the volatile organic compounds and active molecules of transition metals are seriously influenced, and the purification efficiency of the exhaust gas is obviously reduced.
In the invention, the spacers in the two reaction tube bodies are sand chips, the sand core pieces contain a large number of micropore structures, the air permeability is good, the waste gas can normally pass through the sand core pieces, and the flow resistance of the waste gas can be reduced as much as possible.
In the invention, the waste gas preheating zone is arranged between the filter and the first partition plate in the first reaction tube, the length of the waste gas preheating zone is fixed and is about 1/4-1/2 of the length of the tube body of the first reaction tube, and the arrangement purpose is that the retention time of waste gas entering the tube body is short due to the small volume of the tube body, the actual temperature of the waste gas possibly degrading in the treatment process is difficult to reach the set temperature, and the degradation efficiency is influenced. The preheating zone can preheat the waste gas before the waste gas is degraded, so that the continuous stability of the subsequent degradation efficiency is ensured.
In the invention, the air inlets and the air outlets of the two reaction tubes are blocked by rubber stoppers with holes, so that the air tightness is ensured, and meanwhile, a glass thin tube is used for introducing air into the rubber holes to guide the air, so that waste gas cannot leak in the treatment process.
In the invention, the two reaction tubes are made of quartz, and compared with the common glass tube made of quartz, the quartz glass tube has the advantages of high temperature resistance, good thermal stability, difficult cracking in the reaction process, wear resistance and stronger oxidation resistance.
According to the invention, the first reaction tube and the second reaction tube are both arranged in the tubular resistance furnace, and a program temperature control system of the tubular resistance furnace can ensure constant temperature in the waste gas treatment process, so that the high efficiency and stability of the degradation efficiency are ensured.
In the invention, the two reaction tubes are in a butt joint type, can be disassembled and assembled, are convenient for putting in and taking out the catalyst, and can increase or reduce the quantity of the catalyst according to the requirement so as to increase or reduce the consumption of the catalyst in due time according to the content and concentration of waste gas and prevent unnecessary resource waste.
Compared with the prior art, the invention has the following remarkable effects:
the equipment and the device are simple, the operation is convenient, the advantages of low energy consumption, high treatment efficiency, no secondary pollution and the like are realized in the volatile organic compound treatment, and the method can be widely applied to the treatment of volatile organic pollutants generated in industrial production.
The ozone oxidation technology and the catalytic oxidation technology are combined, so that the energy consumption of the single volatile organic pollutant oxidation technology can be reduced, the waste gas purification efficiency can be maximized, the synergistic effect of the ozone oxidation technology and the catalytic oxidation technology ensures that the treated waste gas can completely reach the standard and can not pollute the atmospheric environment.
In the invention, when the control conditions are that the temperature of the first reaction tube is 100-120 ℃, the temperature of the second reaction tube is 80-90 ℃, the catalyst is a manganese-cobalt composite catalyst, and the ozone introduction amount is 25-30mL/min, the benzene can reach the emission standard and is discharged without pollution.
In the invention, when the conditions are controlled such that the temperature of the first reaction tube is 130-.
The cavity for loading the catalyst is divided into a plurality of sections, the catalyst loading capacity can be controlled according to the flow rate, the concentration and the like of the waste gas, the use amount of the catalyst is reduced as much as possible under the condition of ensuring the emission reaching the standard, and the resource waste is prevented.
The pipe body in the invention is in a butt joint type, so that the catalyst can be conveniently put in and taken out, and the pipe body can be cleaned and dried.
Drawings
FIG. 1 is an overall process flow diagram of an apparatus and method for ozone-catalytic oxidation co-treatment of volatile organic compounds.
FIG. 2 is a schematic diagram showing the overall configuration of an apparatus for ozone-catalytic oxidation co-treatment of volatile organic compounds in example 1 of the present invention.
FIG. 3 is a schematic diagram showing the overall configuration of an apparatus for ozone-catalytic oxidation co-treatment of volatile organic compounds in example 2 of the present invention.
Reference numbers in the figures:
1-exhaust gas inlet; 2-a high efficiency filter; 3-a waste gas preheating zone; 4-a first catalyst cavity; 5-a second catalyst cavity; 6-sand chip; 7-rubber plug with hole; 8-exhaust gas outlet holes; 9-tubular resistance furnace; 10-a catalyst; 11-plastic thin tube; 12-an ozone generator; 13-flexible glue tube; 14-a flow meter; 15-ozone inlet hole; 16-a third catalyst cavity; 17-a fourth catalyst cavity; 18-an exhaust system; 19-a first reaction tube; 20-second reaction tube.
Detailed Description
The process flow and features of the present invention will be described in detail below with reference to the accompanying drawings, wherein the described embodiments are only a part, but not all, of the invention, and the technical solutions of the invention will be clearly described.
As shown in fig. 1, when the device for co-processing volatile organic compounds by ozone-catalytic oxidation of the present invention is used for waste gas treatment, waste gas is preheated in the first reaction tube and subjected to high temperature catalytic oxidation reaction, and then enters the second reaction tube to perform co-processing volatile organic compounds by ozone-catalytic oxidation reaction, the reaction in the second reaction tube is low temperature catalytic oxidation reaction, and the treated gas is connected with the exhaust system. The device of the invention utilizes the synergistic effect of ozone oxidation and catalytic oxidation to treat volatile organic compounds, thereby achieving the purpose of waste gas purification.
Example 1
As shown in figure 2, the device comprises a waste gas inlet hole 1, a high efficiency filter 2 (which is an HEPA filter with a filter element formed by a glass fiber filter material), a waste gas preheating zone 3, a first catalyst cavity 4, a second catalyst cavity 5, a sand core sheet 6, a perforated rubber plug 7, a waste gas outlet hole 8, a tubular resistance furnace 9, a catalyst 10, a glass tubule 11, an ozone generator 12, a flexible rubber tube 13, a flowmeter 14, an ozone inlet hole 15, a third catalyst cavity 16, a fourth catalyst cavity 17, an exhaust system 18, a first reaction tube 19, a second reaction tube 20, the perforated rubber plug 7 arranged at the head end of the first reaction tube 19, the perforated rubber plug made of high temperature resistant silica gel material and provided with the waste gas inlet hole 1, the high efficiency filter 2 arranged in the gas flowing direction, the first sand core sheet 6 arranged at the position of about 10cm from the left to the right of the high efficiency filter 2, then, two sand chips 6 are sequentially arranged at a distance of 5cm, a waste gas outlet hole 8 is arranged on the rubber plug 7 with the hole, and the waste gas outlet hole 8 of the first reaction tube 19 and the waste gas inlet hole 1 of the second reaction tube 20 are connected through a glass tubule 11.
Ozone is introduced into the second reaction tube 20 through the ozone inlet hole 15 together with the gas in the first reaction tube 19, the ozone generated by the ozone generator 12 is controlled by the flowmeter 14, and the introduction amount of the ozone in the second reaction tube is controlled at 30 mL/min.
The first reaction tube 19 and the second reaction tube 20 are made of quartz materials, the first reaction tube 19 and the second reaction tube 20 are respectively arranged in the tubular resistance furnace 9, the length of a single reaction tube is about 10cm longer than that of the tubular resistance furnace 9, and the two ends of the inlet and the outlet of the reaction tube are 5cm arranged outside the tubular resistance furnace 9.
The first reaction tube 19 includes 2 catalyst cavities, a first catalyst cavity 4 and a second catalyst cavity 5, in this embodiment, the first catalyst cavity 4 is loaded with the catalyst 10, the second catalyst cavity 5 is not loaded with any catalyst, the total length of the catalyst along the tube body is 5cm, and the loading capacity is 50 g.
The second reaction tube 20 comprises 2 catalyst cavities, a third catalyst cavity 16 and a fourth catalyst cavity 17, in this embodiment, the third catalyst cavity 16 is loaded with the supported catalyst 10, the fourth catalyst cavity 17 is not loaded with any catalyst, the total length of the catalyst along the tube body is 7.5cm, and the loading amount is 75 g.
In this embodiment, the catalysts 10 loaded in the catalyst cavities of the first reaction tube 19 and the second reaction tube 20 are all manganese-cobalt-loaded composite high-efficiency stable catalysts prepared by using granular activated carbon carriers. The catalyst 10 is obtained by loading manganese cobalt active components on coconut shell activated carbon by adopting an excess impregnation method through the steps of sequentially impregnating, drying, roasting in a 500-DEG C tubular resistance furnace and the like.
The waste gas treated by the second reaction tube 20 is connected with the exhaust system 18 through an air outlet, and the purified waste gas reaching the standard is organically discharged.
The device and the method for treating volatile organic compounds by using the ozone-catalytic oxidation synergistic treatment method of the embodiment specifically comprise the following steps:
(1) the flow of the toluene-containing waste gas is controlled to be 15L/min, the flow rate is 0.35m/s, the concentration is 500ppm, the toluene-containing waste gas enters the first reaction tube 19 through the air inlet, the high-efficiency filter 2 arranged at the head end of the tube body effectively intercepts solid particles in the waste gas, and the performance of the catalyst is not reduced in the subsequent treatment.
(2) The intercepted gas enters a waste gas pretreatment chamber for preheating treatment, the heated waste gas enters a first catalyst cavity 4 for catalytic reaction, and the temperature in the first reaction tube 19 is controlled at 130 ℃.
(3) The waste gas after catalytic oxidation degradation enters the second reaction tube 20 through the air inlet, the toluene waste gas in the tube body passes through the third catalyst cavity 16 again, at the moment, ozone also enters the second reaction tube 20 through the air inlet, the ozone introduction amount is 30mL/min, the ozone-catalytic oxidation synergistic treatment of volatile organic pollutants is carried out, the temperature of the second reaction tube 20 is controlled at 90 ℃, at the moment, the treatment efficiency of the waste gas can reach 96%, and then the purified gas is discharged through the exhaust system.
Comparative example 1
The difference between the comparative example and the example 1 is that the second reaction tube does not introduce ozone in the reaction process, and the catalytic oxidation reaction of the catalyst is carried out independently, and the specific steps are as follows;
(1) the flow of the toluene-containing waste gas is controlled to be 15L/min, the flow rate is 0.35m/s, the concentration is 500ppm, the toluene-containing waste gas enters the first reaction tube 19 through the air inlet, the high-efficiency filter 2 arranged at the head end of the tube body effectively intercepts solid particles in the waste gas, and the performance of the catalyst is not reduced in the subsequent treatment.
(2) The intercepted gas enters a waste gas pretreatment chamber for preheating treatment, the heated waste gas sequentially passes through a first catalyst cavity 4 and a second catalyst cavity 5 for catalytic reaction, and the temperature of a first reaction pipe 19 is controlled at 130 ℃.
(3) The waste gas after catalytic oxidation degradation enters the second reaction tube 20 through the air inlet, the toluene waste gas in the tube body sequentially passes through the third catalyst cavity 16 and the fourth catalyst cavity 17, the temperature of the second reaction tube 20 is controlled at 90 ℃, the treatment efficiency of the waste gas can reach 85 percent, and then the purified gas is discharged through the exhaust system 18.
Example 2
As shown in fig. 3, the difference between this embodiment and embodiment 1 is that the first reaction tube 19 includes 2 catalyst cavities, in this embodiment, the first catalyst cavity 4 and the second catalyst cavity 5 are both loaded with the loaded manganese-cobalt composite catalyst, the total length of the catalyst along the tube body is 10cm, and the loading amount is 100 g.
The second reaction tube 20 includes 2 catalyst cavities, in this embodiment, the third catalyst cavity 16 and the fourth catalyst cavity 17 are both loaded with the catalyst 10, the total length of the catalyst 10 along the tube body is 15cm, and the loading amount is 150 g.
In this embodiment, the catalysts 10 loaded in the catalyst cavities of the first reaction tube 19 and the second reaction tube 20 are all supported manganese cobalt composite catalysts prepared by using granular activated carbon carriers. The catalyst 10 is prepared by loading manganese cobalt active components on coconut shell activated carbon by adopting an excess impregnation method through the steps of impregnation, drying, roasting in a 500 ℃ tubular resistance furnace and the like in sequence.
The specific steps of treating the volatile organic pollutants by adopting the device and the method for treating the volatile organic pollutants by using the ozone-catalytic oxidation synergistic method of the embodiment are as follows:
(1) the flow of the toluene-containing waste gas is controlled to be 15L/min, the flow rate is 0.35m/s, the concentration is 500ppm, the toluene-containing waste gas enters the first reaction tube 19 through the air inlet, the high-efficiency filter 2 arranged at the head end of the tube body effectively intercepts solid particles in the waste gas, and the performance of the catalyst is not reduced in the subsequent treatment.
(2) The intercepted gas enters a waste gas pretreatment chamber for preheating treatment, the heated waste gas sequentially passes through a first catalyst cavity 4 and a second catalyst cavity 5 for catalytic reaction, and the temperature of a first reaction pipe 19 is controlled at 130 ℃.
(3) The waste gas after catalytic oxidation degradation enters the second reaction tube 20 through the air inlet, the toluene waste gas in the tube body sequentially passes through the third catalyst cavity 16 and the fourth catalyst cavity 17, at the moment, ozone also enters the second reaction tube 20 through the air inlet, the ozone introduction amount is 35mL/min, the ozone-catalytic oxidation synergistic treatment of volatile organic pollutants is carried out, the temperature of the second reaction tube 20 is controlled at 90 ℃, at the moment, the treatment efficiency of the waste gas can reach 98%, and then the purified gas is discharged through the exhaust system 18.
The above-described embodiments are only a part of the present invention, and do not limit the scope of the present invention, and the present invention may have various changes and modifications, which fall within the scope of the present invention without departing from the teaching of the present invention.
Claims (9)
1. The device for treating the volatile organic compounds by ozone-catalytic oxidation is characterized by comprising a first reaction pipe, a second reaction pipe, an ozone generating device and an exhaust system; the waste gas enters the first reaction pipe and the second reaction pipe in sequence and is exhausted through an exhaust system; the first reaction tube and the second reaction tube are of opening structures with air inlets and air outlets at two ends respectively, and openings at two ends are respectively provided with a rubber plug with a hole; the glass tubules are respectively inserted into the air outlet holes and the air inlet holes of the rubber plugs with holes of the first reaction tube and the second reaction tube, so that the first reaction tube and the second reaction tube are connected in series; the first reaction tube and the second reaction tube are respectively arranged in two tubular resistance furnaces, and the temperature in the two reaction tubes is respectively controlled by the tubular resistance furnaces; a filter is arranged in the first reaction tube close to the air inlet, m spacers are radially arranged behind the filter at intervals in the rear direction of the position 1/4-1/2 of the length of the first reaction tube, and m-1 catalyst cavities are enclosed in the first reaction tube; ozone generated by the ozone generating device enters a second reaction tube through a glass thin tube inserted into an air inlet of the second reaction tube through a hose and a flowmeter, n spacers are radially arranged in the second reaction tube at intervals, and n-1 catalyst cavities are enclosed in the second reaction tube; wherein: the spacer is a sand core plate, and a single catalyst or a composite catalyst of a porous carrier loaded with transition metal elements is arranged in the catalyst cavity.
2. The apparatus of claim 1, wherein m and n are integers greater than or equal to 2.
3. The apparatus of claim 1, wherein the first reaction tube and the second reaction tube are made of quartz; the rubber plug with the hole is made of high-temperature-resistant silica gel material, and the filter is an HEPA filter with a filter element formed by glass fiber filter materials.
4. The device of claim 1, wherein the porous carrier is activated carbon particles or alumina, and the transition metal is any one or more of Mn, Co, Fe, or Cu.
5. The apparatus as claimed in claim 1, wherein the temperature in the first reaction tube is controlled to be between 100 ℃ and 150 ℃ and the temperature in the second reaction tube is controlled to be between 80 ℃ and 100 ℃.
6. The method for treating volatile organic compounds by using the device of claim 1 for ozone-catalytic oxidation synergistic treatment is characterized in that the waste gas is filtered by a filter in a first reaction tube to remove solid particles in the waste gas, and then is subjected to catalytic oxidation reaction after being preheated; then enters a second reaction pipe to perform catalytic oxidation reaction under the action of ozone, and finally the treated waste gas is accessed into an exhaust system.
7. The method as set forth in claim 6, wherein the flow rate of the exhaust gas passing through the first reaction tube and the second reaction tube is controlled to be in the range of 10 to 15L/min, and the flow rate is controlled to be in the range of 0.24 to 0.35 m/s.
8. The method as claimed in claim 6, wherein the amount of ozone introduced into the second reaction tube is controlled to be 20 to 35 mL/min.
9. The method as set forth in claim 6, wherein the temperature in the first reaction tube is controlled to be between 100 ℃ and 150 ℃ and the temperature in the second reaction tube is controlled to be between 80 ℃ and 100 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910182953.7A CN109821408B (en) | 2019-03-12 | 2019-03-12 | Device and method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910182953.7A CN109821408B (en) | 2019-03-12 | 2019-03-12 | Device and method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109821408A CN109821408A (en) | 2019-05-31 |
| CN109821408B true CN109821408B (en) | 2021-10-19 |
Family
ID=66868866
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910182953.7A Active CN109821408B (en) | 2019-03-12 | 2019-03-12 | Device and method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109821408B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113244768B (en) * | 2021-04-27 | 2023-03-28 | 湖北迪晟环保科技有限公司 | Light oxygen exhaust-gas treatment equipment for industrial waste gas purification |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102476029A (en) * | 2010-11-29 | 2012-05-30 | 杰智环境科技股份有限公司 | Catalyst-containing purifying apparatus used for processing organic waste gas |
| CN107281918A (en) * | 2017-08-22 | 2017-10-24 | 苏州碧峰环保科技有限公司 | The multistage catalytic oxidation treatment device of organic exhaust gas |
| CN108993141A (en) * | 2018-10-17 | 2018-12-14 | 深圳汇盛环保科技有限公司 | A kind of emission-control equipment |
| CN208302463U (en) * | 2018-03-15 | 2019-01-01 | 苏州迈沃环保工程有限公司 | A kind of VOCs exhaust gas advanced purification system |
| CN208372833U (en) * | 2018-05-22 | 2019-01-15 | 南京鼎靔达工程技术有限公司 | The processing system of VOCs in a kind of oil gas |
| US10245553B2 (en) * | 2015-12-21 | 2019-04-02 | Korea Institute Of Science And Technology | Apparatus for decomposing low concentration of volatile organic compounds by high flow |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150118138A1 (en) * | 2013-10-31 | 2015-04-30 | Korea Institute Of Science And Technology | Apparatus and method for decomposing an ultra-low concentration of volatile organic compounds |
| CN104857824B (en) * | 2015-05-27 | 2018-02-02 | 中山大学 | The waste gas processing method and device of vacuum-ultraviolet light catalyzing cooperation catalytic ozonation |
| CN206447617U (en) * | 2016-12-05 | 2017-08-29 | 上海乐泽环境工程有限公司 | A kind of bion pulling flow type electrocatalysis oxidation apparatus |
| CN206950989U (en) * | 2017-06-12 | 2018-02-02 | 中国石油天然气集团公司 | A kind of VOCs exhaust fume catalytics oxidation furnaces |
| CN207886979U (en) * | 2018-01-24 | 2018-09-21 | 上海第二工业大学 | A kind of electrodeless ultraviolet catalytic organic waste gas treatment device of drawer type |
-
2019
- 2019-03-12 CN CN201910182953.7A patent/CN109821408B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102476029A (en) * | 2010-11-29 | 2012-05-30 | 杰智环境科技股份有限公司 | Catalyst-containing purifying apparatus used for processing organic waste gas |
| US10245553B2 (en) * | 2015-12-21 | 2019-04-02 | Korea Institute Of Science And Technology | Apparatus for decomposing low concentration of volatile organic compounds by high flow |
| CN107281918A (en) * | 2017-08-22 | 2017-10-24 | 苏州碧峰环保科技有限公司 | The multistage catalytic oxidation treatment device of organic exhaust gas |
| CN208302463U (en) * | 2018-03-15 | 2019-01-01 | 苏州迈沃环保工程有限公司 | A kind of VOCs exhaust gas advanced purification system |
| CN208372833U (en) * | 2018-05-22 | 2019-01-15 | 南京鼎靔达工程技术有限公司 | The processing system of VOCs in a kind of oil gas |
| CN108993141A (en) * | 2018-10-17 | 2018-12-14 | 深圳汇盛环保科技有限公司 | A kind of emission-control equipment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109821408A (en) | 2019-05-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101250940B1 (en) | The treating system of odors and volatile organic compounds simultaneously | |
| WO1997012671A1 (en) | Heat treated activated carbon for denitration, process for preparing the same, method of denitration using the same, and system of denitration using the same | |
| CN107970751B (en) | Novel method and device for treating organic waste gas | |
| CN101391177A (en) | Gas purification method of low concentration organic compound | |
| CN105921009A (en) | Light-oxygen combined waste gas treatment device and treatment method thereof | |
| CN102869441A (en) | Method and device for treating gas discharged from a carbon dioxide recovery device | |
| CN109821408B (en) | Device and method for cooperatively treating volatile organic compounds through ozone-catalytic oxidation | |
| CN109414647B (en) | Method for low-temperature gas cleaning and catalyst used for method | |
| CN108786449A (en) | A kind of novel V0Cs adsorption activations desorption low-temperature catalytic treating method and its processing unit | |
| JP5810488B2 (en) | Wastewater treatment system | |
| CN101322916B (en) | Sulfur-containing compound gas cleaning filter medium device and method as well as used catalyst adsorption material thereof | |
| CN206082107U (en) | Industry organic waste gas purification device | |
| CN110513176B (en) | Tail gas purification device for heavy diesel vehicle | |
| CN108745328B (en) | Regeneration method of volatile organic pollutant adsorbent | |
| CN106890566A (en) | A kind of reactor of plasma body cooperative ultraviolet catalytic cleaning organic waste gas | |
| CN208082083U (en) | A kind of activated carbon adsorption is in catalysis oxidation waste gas pollution control and treatment equipment | |
| CN205965504U (en) | Waste gas processing system | |
| CN212790409U (en) | Waste gas treatment device for coal chemical industry sewage treatment | |
| CN204699585U (en) | A kind of device removing coking nitrogen oxides in effluent | |
| CN110960972A (en) | Environment-friendly exhaust treatment device | |
| CN113318582A (en) | Process for adsorbing, desorbing and catalytically oxidizing VOCs (volatile organic compounds) by using activated carbon in pharmaceutical industry | |
| CN207856604U (en) | A kind of organic waste gas treatment device | |
| KR20210122943A (en) | Concentrated Oxidation Rotor For VOCs Treatment Executing Combination Process of Adsorption Process and Catalytic Oxidation Process | |
| CN211659683U (en) | Environment-friendly exhaust treatment device | |
| JP4295548B2 (en) | Nitrogen oxide removing catalyst, denitration method and apparatus using the same |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20231130 Address after: 201209 Shanghai Pudong New Area Jinhai Road 2588 A Block 3 Floors Patentee after: Shanghai wobai Environmental Development Co.,Ltd. Address before: 201209 No. 2360 Golden Sea Road, Shanghai, Pudong New Area Patentee before: Shanghai Polytechnic University |
|
| TR01 | Transfer of patent right |