CN214809839U - Catalytic oxidation system - Google Patents
Catalytic oxidation system Download PDFInfo
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- CN214809839U CN214809839U CN202021947971.4U CN202021947971U CN214809839U CN 214809839 U CN214809839 U CN 214809839U CN 202021947971 U CN202021947971 U CN 202021947971U CN 214809839 U CN214809839 U CN 214809839U
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- 230000003197 catalytic effect Effects 0.000 title claims abstract description 123
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 93
- 230000003647 oxidation Effects 0.000 title claims abstract description 92
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- 239000002912 waste gas Substances 0.000 claims abstract description 29
- 238000010438 heat treatment Methods 0.000 claims description 33
- 230000005855 radiation Effects 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 2
- 239000010410 layer Substances 0.000 abstract description 31
- 239000012855 volatile organic compound Substances 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 7
- 238000012546 transfer Methods 0.000 abstract description 4
- 239000002356 single layer Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 49
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 21
- 239000010815 organic waste Substances 0.000 description 17
- 239000002957 persistent organic pollutant Substances 0.000 description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 6
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 238000004880 explosion Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 229910052763 palladium Inorganic materials 0.000 description 3
- 229910052697 platinum Inorganic materials 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 239000011149 active material Substances 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 229910017052 cobalt Inorganic materials 0.000 description 2
- 239000010941 cobalt Substances 0.000 description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 229910052878 cordierite Inorganic materials 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 2
- 238000013022 venting Methods 0.000 description 2
- 230000004913 activation Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The utility model provides a catalytic oxidation system, including heat transfer unit, preheating unit, catalytic oxidation unit and safety auxiliary unit, preheating unit, catalytic oxidation unit are in same device box, and device box front end and end set up air intake and air outlet respectively, heat transfer unit is connected with preheating unit, catalytic oxidation unit respectively, the catalytic oxidation unit includes at least two-layer catalytic bed that is used for loading the catalyst. The embodiment of the scheme is characterized in that the catalytic oxidation unit is provided with a plurality of stages of catalytic beds, so that the waste gas is oxidized in the catalytic oxidation unit in stages, the VOCs in the waste gas is controlled to be oxidized and released in a single-layer catalytic bed, the activity of the catalyst is prevented from being reduced due to the rapid rise of the temperature of the catalytic bed, and the operation cost is reduced.
Description
Technical Field
The utility model relates to an organic waste gas purifies technical field, concretely relates to handle high concentration volatility organic waste gas's catalytic oxidation system.
Background
Volatile Organic Compounds (VOCs) are important objects for controlling national air pollution, and a plurality of environmental protection standards are provided for VOCs emission in recent years. In the organic waste gas purification process, a method for reducing the decomposition temperature of organic pollutants in waste gas by using a catalyst and accelerating the complete oxidation of the organic pollutants is called catalytic oxidation. Oxygen and organic pollutants are adsorbed on the catalyst on the surface layer of the porous material, so that the contact chance of oxygen and organic gas is increased, meanwhile, the existence of the catalyst reduces the activation energy of the oxidative decomposition reaction of the organic pollutants, improves the reaction activity of the organic pollutants, enables the organic pollutants and the oxygen to generate the oxidation reaction, generates non-toxic and harmless inorganic micromolecules such as CO2 and H2O, and generates heat at the same time.
The conventional catalytic oxidation system mainly comprises a heat exchange unit, a preheating unit, a catalytic oxidation unit and a necessary safety protection unit. In the actual waste gas treatment process, when the concentration of VOCs in the waste gas is too high (not exceeding 25% of the lower explosion limit), the heat emitted by the VOCs in the catalytic oxidation process cannot be timely removed, so that the temperature of a catalytic bed layer rises and exceeds the optimal catalytic temperature range of a catalyst, the catalytic effect and the service life of the catalyst are influenced, and even more, if the temperature of the catalytic bed layer continuously rises, the temperature approaches and reaches the impact-resistant temperature of the catalyst, so that the catalytic oxidation system is shut down; or fresh cold air is supplemented to the catalytic oxidation system to dilute the concentration of the VOCs in the exhaust gas and reduce the operating temperature of the catalytic oxidation system so as to maintain the heat balance of the catalytic oxidation system, which can lead to the increase of the exhaust gas treatment amount of the catalytic oxidation system and increase the investment and operation cost of the whole catalytic oxidation system.
SUMMERY OF THE UTILITY MODEL
The technical problem solved by the utility model is to provide a catalytic oxidation system of reduce cost.
For solving the technical problem, the utility model provides a catalytic oxidation system, including heat transfer unit, preheating unit, catalytic oxidation unit and safety auxiliary unit, preheating unit, catalytic oxidation unit are in same device box, and device box front end and end set up air intake and air outlet respectively, heat transfer unit is connected with preheating unit, catalytic oxidation unit respectively, catalytic oxidation unit includes at least two-layer catalytic bed that is used for loading the catalyst.
Preferably, the catalytic oxidation system, wherein: the heat exchange unit, the preheating unit and the catalytic oxidation unit are arranged in the same device box body.
Preferably, the catalytic oxidation system, wherein: the heat exchange unit adopts at least one of a tube type heat exchanger, a plate type heat exchanger and a heat accumulating type heat exchanger.
Preferably, the catalytic oxidation system, wherein: the preheating unit comprises a heating assembly, the heating assembly adopts a resistance heating pipe, an infrared radiation heating assembly or an electromagnetic heating assembly, and the heating assembly is provided with radiating fins.
Preferably, the catalytic oxidation system, wherein: the preheating unit comprises a temperature detector, the temperature detector is arranged at the rear end of the heating assembly and used for detecting the temperature of the waste gas at the outlet of the preheating unit, and the temperature detector is connected with the heating assembly.
Preferably, the catalytic oxidation system, wherein: the catalytic oxidation unit includes gaseous flow straightener set up in catalytic oxidation unit's import, gaseous flow straightener includes gaseous vortex device, gaseous vortex device adopts honeycomb perforated plate, shutter or baffling board.
Preferably, the catalytic oxidation system, wherein: and a heat exchange tube and a temperature sensor are arranged between every two catalyst bed layers, and the heat exchange tube is connected with the temperature sensor.
Preferably, the catalytic oxidation system, wherein: the heat exchange tube adopts one of a heat light tube, a finned tube, a threaded tube and a spiral groove tube.
Preferably, the catalytic oxidation system, wherein: the active material of the catalyst is at least one of platinum, palladium, copper, chromium, nickel, vanadium, manganese, iron and cobalt, the catalytic bed layer is made of porous material, and the porous material comprises at least one of ceramic, cordierite and composite alumina.
Preferably, the catalytic oxidation system, wherein: the safety auxiliary unit comprises a flame arrester and a rupture disk safety device.
The embodiment of the scheme provides a catalytic oxidation system for treating high-concentration volatile organic waste gas, which comprises the following steps: the pretreated low-temperature organic waste gas exchanges heat with the high enthalpy purified gas from the catalytic oxidation unit at first in the heat exchange unit, the temperature of the organic waste gas is increased for the first time, then the organic waste gas enters the preheating unit, the temperature of the organic waste gas is increased to the required temperature, the high-temperature organic waste gas uniformly enters the catalytic bed layer through the gas flow equalizing device, and organic pollutants in the waste gas are decomposed into CO under the action of a catalyst2And H2O and other inorganic micromolecules emit heat simultaneously to obtain high enthalpy value purified gas, and the purified gas is discharged after the heat exchange unit exchanges heat with the low-temperature organic waste gas, so that the energy-saving and environment-friendly effects are achieved. The embodiment of the scheme is characterized in that the catalytic oxidation unit is provided with a plurality of stages of catalytic beds, so that the waste gas is oxidized in the catalytic oxidation unit in stages, the VOCs in the waste gas is controlled to be oxidized and released in a single-layer catalytic bed, the activity of the catalyst is prevented from being reduced due to the rapid rise of the temperature of the catalytic bed, and the operation cost is reduced.
Drawings
Fig. 1 is a schematic structural diagram of the catalytic oxidation system of the present invention.
Fig. 2 is a schematic structural diagram of the preheating unit and the catalytic oxidation unit device box body in the present invention.
Labeled as: 1: a flame arrestor; 2: a heat exchange unit; 3: a device case; 31: an air inlet; 32: an air outlet; 33: a heat-insulating layer; 34: explosion venting sheets; 4: a preheating unit; 41: a heating assembly; 42: a temperature detector; 5: a catalytic oxidation unit; 51: a gas flow straightener; 52: a catalytic bed layer; 53: a heat exchange pipe; 54: a temperature sensor. Arrows in the drawing indicate the flow of gas and heat medium.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary and intended to be used for explaining the present invention, and should not be construed as limiting the present invention.
As shown in fig. 1-2, an embodiment of the present disclosure provides a catalytic oxidation system, which includes a heat exchange unit 2, a preheating unit 4, a catalytic oxidation unit 5, and a safety auxiliary unit, where the preheating unit 4 and the catalytic oxidation unit 5 are located in a same device box 3, an air inlet 31 and an air outlet 32 are respectively disposed at the front end and the tail end of the device box 3, the heat exchange unit 2 is respectively connected with the preheating unit 4 and the catalytic oxidation unit 5, and the catalytic oxidation unit 5 includes at least two catalyst beds 52 for filling catalysts.
The embodiment of the scheme provides a catalytic oxidation system for treating high-concentration volatile organic waste gas, which comprises the following steps: the pretreated low-temperature organic waste gas exchanges heat with the high enthalpy purified gas discharged from the catalytic oxidation unit 5 in the heat exchange unit 2, the temperature of the organic waste gas is increased for the first time, the organic waste gas enters the preheating unit 4, the temperature of the organic waste gas is increased to the required temperature, the high-temperature organic waste gas uniformly enters the catalytic bed 52 through the gas flow equalizing device 51, and organic pollutants in the waste gas are decomposed into CO under the action of a catalyst2And H2O and other inorganic micromolecules emit heat simultaneously to obtain purified gas with high enthalpy, and the purified gas is discharged after the heat exchange unit 2 exchanges heat with the low-temperature organic waste gas. In the embodiment of the scheme, the catalytic oxidation unit 5 is provided with the multi-stage catalytic bed layer 52, so that the exhaust gas is subjected to staged oxidation in the catalytic oxidation unit 5, the oxidation heat release of VOCs in the exhaust gas in the single-layer catalytic bed layer 52 is controlled, and the reduction of the catalyst activity caused by the rapid temperature rise of the catalytic bed layer 52 is prevented.
Preferably, the inner side of the device box body 3 is provided with a heat preservation layer 33, so that the temperature of the outer surface of the device box body 3 is reduced.
The heat exchange unit 2, the preheating unit 4 and the catalytic oxidation unit 5 are arranged in the same device box body 3, can be independently arranged and are connected with the preheating unit 4 and the catalytic oxidation unit 5 through pipelines.
The heat exchange unit 2 adopts at least one of a tube type heat exchanger, a plate type heat exchanger and a heat accumulating type heat exchanger.
The preheating unit 4 comprises a heating component 41, the heating component 41 adopts a resistance heating pipe, an infrared radiation heating component 41 or an electromagnetic heating component 41, and the heating component 41 is provided with radiating fins. The heating effect is strengthened.
The preheating unit 4 comprises a temperature sensor 5442, the temperature sensor 5442 is arranged at the rear end of the heating assembly 41 and is used for detecting the temperature of the exhaust gas at the outlet of the preheating unit 4, and the temperature sensor 5442 is connected with the heating assembly 41. The heating power of the heating module 41 is controlled according to the gas temperature detected by the temperature sensor 5442.
The catalytic oxidation unit 5 comprises a gas flow equalizing device 51, and the gas flow equalizing device 51 is arranged at the inlet of the catalytic oxidation unit 5, so that gas can uniformly pass through the catalytic bed layer 52. The gas flow straightener 51 comprises a gas turbulator, which is a honeycomb perforated plate, louver or baffle.
And a heat exchange pipe 53 and a temperature sensor are arranged between every two catalyst beds 52, and the heat exchange pipe 53 is connected with the temperature sensor. The heat exchange pipe 53 is connected with the outside by a heat energy device, a low-temperature heat medium is introduced into the heat exchange pipe 53, and the low-temperature heat medium exchanges heat with the high enthalpy gas passing through the catalytic bed 52, so that the heat of the gas is removed in time. The temperature sensor detects the temperature of the waste gas entering the next-stage catalytic bed layer 52 after passing through the heat exchange tube 53, the temperature sensor is interlocked with the flow of the heating medium, and the flow of the heating medium entering the heat exchange tube 53 is controlled according to the temperature of the waste gas detected by the temperature sensor 5442, so that the temperature of the waste gas entering the next-stage catalytic bed layer 52 is controlled to be in the optimal temperature range of catalytic oxidation, the catalytic oxidation efficiency is improved, and the service life of the catalyst is prolonged. After absorbing part of the heat emitted by the catalytic oxidation unit 5, the heat medium in the heat exchange pipe 53 can be sent to a device needing to utilize heat energy, and the heat generated by catalytic oxidation can be recycled, so that the purpose of saving energy is achieved.
The heat exchange tube 53 is one of a heat light tube, a finned tube, a threaded tube, and a spiral grooved tube.
The active material of the catalyst is at least one of platinum, palladium, copper, chromium, nickel, vanadium, manganese, iron and cobalt, and the catalyst bed 52 is a porous material comprising at least one of ceramic, cordierite and composite alumina.
The safety auxiliary unit comprises a flame arrester 1 and a rupture disk safety device.
To treat 10000Nm3H containing toluene, 4000mg/m3Taking exhaust gas with the temperature of 30 ℃ as an example, and combining fig. 1 and fig. 2 to show, designing the catalytic oxidation system according to the embodiment of the present invention:
firstly, a flame arrester 1 is arranged on an air inlet pipeline.
Secondly, the heat exchange unit 2 adopts a tube type heat exchanger, and the heat exchange efficiency is 55 percent.
And thirdly, the preheating unit 4 and the catalytic oxidation unit 5 are arranged in the same device box body 3, the inner side of the box body is provided with a heat preservation layer 33, and the upper part of the box body is provided with an explosion venting sheet 34.
The preheating unit 4 is provided with a heating component 41 and a temperature detector 42, and the heating component 41 is heated by infrared radiation.
The front end of the catalytic oxidation unit 5 is provided with a gas flow equalizing device 51, the catalytic bed layers 52 are provided with two layers, a heat exchange pipe 54 is arranged between the catalytic bed layers, low-temperature water is introduced into the heat exchange pipe to exchange heat with high-temperature waste gas, and the excessive heat generated by the catalytic oxidation is removed in time.
Sixthly, the catalyst takes honeycomb ceramics as a carrier, and noble metal platinum and palladium catalysts are dipped in the catalyst. The loading of catalyst in each layer is 0.65m3Total loading of 1.30m3。
The waste gas enters the catalytic oxidation system of the embodiment of the scheme after being pretreated, firstly, the heat exchange unit 2 exchanges heat with the high enthalpy purified gas discharged from the catalytic oxidation unit 5, the temperature of the waste gas is raised to 250 ℃, the temperature of the waste gas does not need to be further raised, the heating component 41 of the preheating unit 4 is closed, the waste gas uniformly enters the first catalytic bed layer 52 through the gas flow equalizing device 51, and part of toluene is decomposed into CO under the action of the catalyst2And H2O and other inorganic micromolecules simultaneously emit a large amount of heat, the enthalpy value of the waste gas is increased, the high-enthalpy waste gas from one layer of catalytic bed layer exchanges heat with the low-temperature water in the heat exchange tube 54, and the temperature is reduced to 300 DEG CEnters the second catalytic bed layer 52, and the toluene which is not decomposed in the exhaust gas is further decomposed into CO under the action of the catalyst2And H2O and other inorganic small molecules release a large amount of heat at the same time, and the enthalpy value of the waste gas is increased again. The high-temperature waste gas enters a heat exchanger of the heat exchange unit 2 to exchange heat with the low-temperature waste gas, and the temperature is reduced to 110 ℃ and then the high-temperature waste gas is discharged.
In the embodiment, the catalytic oxidation unit is provided with two catalytic bed layers, so that the toluene in the exhaust gas is oxidized in the catalytic oxidation unit in a grading manner, the heat release of the toluene in the exhaust gas in the oxidation of a single catalytic bed layer is controlled, and the reduction of the activity of the catalyst caused by the rapid rise of the temperature of the catalytic bed layer is prevented; meanwhile, a heat exchange tube and a temperature detector are arranged between two catalytic bed layers, and the temperature of the waste gas entering the next catalytic bed layer is accurately controlled, so that the waste gas is in the optimal temperature range (300-400 ℃) for catalytic oxidation at each catalytic bed layer.
In the example, after the waste gas was treated by the catalytic oxidation system, the concentration of toluene in the discharged purified gas was 19.6mg/m3The decomposition rate of toluene in the waste gas reaches 99.51 percent, and the requirement of environmental protection and discharge is met; meanwhile, the excess heat generated by catalytic oxidation can heat 15 tons of cold water with the temperature of 20 ℃ to 40 ℃, so that the aim of recycling waste heat is fulfilled.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and those skilled in the art can make many variations and modifications of the technical solution of the present invention without departing from the scope of the technical solution of the present invention.
Claims (8)
1. A catalytic oxidation system, characterized by: the device comprises a heat exchange unit, a preheating unit, a catalytic oxidation unit and a safety auxiliary unit, wherein the preheating unit and the catalytic oxidation unit are positioned in the same device box, the front end and the tail end of the device box are respectively provided with an air inlet and an air outlet, the heat exchange unit is respectively connected with the preheating unit and the catalytic oxidation unit, and the catalytic oxidation unit comprises at least two catalytic bed layers for filling catalysts; the preheating unit comprises a heating assembly, the heating assembly adopts a resistance heating pipe, an infrared radiation heating assembly or an electromagnetic heating assembly, and the heating assembly is provided with radiating fins.
2. The catalytic oxidation system of claim 1, wherein: the heat exchange unit, the preheating unit and the catalytic oxidation unit are arranged in the same device box body.
3. The catalytic oxidation system of claim 1, wherein: the heat exchange unit adopts at least one of a tube type heat exchanger, a plate type heat exchanger and a heat accumulating type heat exchanger.
4. The catalytic oxidation system of claim 3, wherein: the preheating unit comprises a temperature detector, the temperature detector is arranged at the rear end of the heating assembly and used for detecting the temperature of the waste gas at the outlet of the preheating unit, and the temperature detector is connected with the heating assembly.
5. The catalytic oxidation system of claim 1, wherein: the catalytic oxidation unit includes gaseous flow straightener set up in catalytic oxidation unit's import, gaseous flow straightener includes gaseous vortex device, gaseous vortex device adopts honeycomb perforated plate, shutter or baffling board.
6. The catalytic oxidation system of claim 1, wherein: and a heat exchange tube and a temperature sensor are arranged between every two catalyst bed layers, and the heat exchange tube is connected with the temperature sensor.
7. The catalytic oxidation system of claim 6, wherein: the heat exchange tube adopts one of a heat light tube, a finned tube, a threaded tube and a spiral groove tube.
8. The catalytic oxidation system of claim 1, wherein: the safety auxiliary unit comprises a flame arrester and a rupture disk safety device.
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| CN202021947971.4U CN214809839U (en) | 2020-09-09 | 2020-09-09 | Catalytic oxidation system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021947971.4U CN214809839U (en) | 2020-09-09 | 2020-09-09 | Catalytic oxidation system |
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| CN214809839U true CN214809839U (en) | 2021-11-23 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116672884A (en) * | 2023-07-14 | 2023-09-01 | 浙江大学 | Catalytic oxidation system and catalytic oxidation method for efficiently converting and removing VOCs in coal chemical industry |
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2020
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116672884A (en) * | 2023-07-14 | 2023-09-01 | 浙江大学 | Catalytic oxidation system and catalytic oxidation method for efficiently converting and removing VOCs in coal chemical industry |
| CN116672884B (en) * | 2023-07-14 | 2024-01-16 | 浙江大学 | Catalytic oxidation system and catalytic oxidation method for efficiently converting and removing VOCs in coal chemical industry |
| CN117732242A (en) * | 2023-07-14 | 2024-03-22 | 浙江大学 | Catalytic oxidation system for efficiently converting and removing VOCs based on double-steam-bag cooperation |
| CN117732242B (en) * | 2023-07-14 | 2024-06-04 | 浙江大学 | Catalytic oxidation system for efficiently converting and removing VOCs based on double-steam-bag cooperation |
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Granted publication date: 20211123 |