CN203400631U - Persistent organic pollutant catalytic degradation device for flue gas treatment - Google Patents
Persistent organic pollutant catalytic degradation device for flue gas treatment Download PDFInfo
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- CN203400631U CN203400631U CN201320503601.5U CN201320503601U CN203400631U CN 203400631 U CN203400631 U CN 203400631U CN 201320503601 U CN201320503601 U CN 201320503601U CN 203400631 U CN203400631 U CN 203400631U
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Abstract
The utility model discloses a persistent organic pollutant catalytic degradation device for flue gas treatment, and belongs to the field of fuel gas treatment equipment. The persistent organic pollutant catalytic degradation device comprises a reactor, a fuel gas inlet, an ammonia gas inlet, a gas outlet and a catalyst module box. The reactor is of a hollow structure, and the two ends of the reactor are provided with openings which are used as the inlet and the outlet. The fuel gas inlet and the ammonia gas inlet are formed in the inlet at one end of the reactor and are communicated with the reactor, and sealing is carried out among the fuel gas inlet, the ammonia gas inlet and the inlet of the reactor. The gas outlet is formed in the outlet at the other end of the reactor and communicated with the reactor, and sealing is carried out between the gas outlet and the outlet of the reactor. The catalyst module box is arranged in the reactor and located at the position, away from the fuel gas inlet and the ammonia gas inlet, of the gas outlet. Through the coordination of the reactor provided with the catalyst module box inside, the fuel gas inlet, the ammonia gas inlet and the gas outlet, the persistent organic pollutant catalytic degradation device can carry out catalytic degradation on persistent organic pollutants in fuel gas, and is high in modular degree and standardized degree and convenient to use and transport.
Description
Technical Field
The utility model relates to a flue gas treatment facility field especially relates to a Persistent Organic Pollutants (POPs) catalytic degradation device for handling flue gas.
Background
POPs (Persistent Organic Pollutants) are a very difficult-to-degrade Organic substance, and taking PCDD/Fs as an example, if the chemical molecular structure is to be destroyed under gas phase conditions, a high temperature above 800 ℃ is usually required. In order to lower the operating temperature of the degradation process, the reaction conditions are generally lowered by using a supported metal catalyst. The metal materials currently used in the catalysts mainly include noble metals and transition metal oxides.
The noble metal is the catalyst which is firstly used for catalyzing and degrading chlorine-containing volatile organic compounds (Cl-VOC) such as POPs, and the common noble metal catalyst is that VIII subgroup metals such as Pd, Pt, Rh, Ni, Au, Ir and the like are loaded on Al2O3、TiO2、CeO2、ZrO2And the like, and materials such as activated carbon, silica, zeolite, ceramics, red mud, polymers and the like by adopting an immersion method. In recent years, a number of researchers have studied the catalytic activity of various supported noble metals for degrading PCDD/Fs or their indicator compounds, such as: chlorophenols, chlorobenzene, and polychlorinated biphenyls (PCBs).
The cost of noble metal catalyst is very high, the industrial large-scale use is still blank in China, and with the development of scientific technology, the catalyst with low cost and good performance has been developed in recent years. How to make the catalyst exert the optimal degradation efficiency in industrial application becomes a problem to be solved at present.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a persistent organic pollutant catalytic degradation device for handling the flue gas for POPs in the flue gas can take place abundant reaction with the catalyst, thereby solve not to have a device at present and can effectively utilize the catalyst in order to get rid of the problem of POPs.
The technical scheme for solving the technical problems is as follows:
the utility model relates to a persistent organic pollutant catalytic degradation device for handling flue gas, a serial communication port, include:
the device comprises a reactor, a flue gas inlet, an ammonia gas inlet, a gas outlet and a catalyst module box; wherein,
the interior of the reactor is of a hollow structure, and two ends of the reactor are respectively provided with an opening as an inlet and an outlet;
the flue gas inlet and the ammonia gas inlet are arranged on an inlet at one end of the reactor and are communicated with the inside of the reactor, and the flue gas inlet and the ammonia gas inlet are sealed with the inlet of the reactor;
the gas outlet is arranged on the outlet at the other end of the reactor and is communicated with the inside of the reactor, and the gas outlet and the outlet of the reactor are sealed;
the catalyst module box is arranged in the reactor and is arranged at the gas outlet far away from the flue gas inlet and the ammonia gas inlet.
The utility model has the advantages that: through the matching of the reactor with the catalyst module box inside, the flue gas inlet, the ammonia gas inlet and the gas outlet, POPs entering the flue gas can be catalyzed and degraded. The device has high modularization and standardization degree, can be suitable for the existing catalyst module, and is convenient to transport, install and lift.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the description of the embodiments will be briefly described below, and it is obvious that the drawings in the description below are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic view of a POPs catalytic degradation device provided by an embodiment of the present invention;
fig. 2 is a sectional view taken along line a-a of fig. 1.
Detailed Description
The technical solutions in the embodiments of the present invention are described below clearly and completely, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiment of the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The embodiments of the present invention are described in further detail below.
The embodiment of the utility model provides a persistent organic pollutant catalytic degradation device for handling flue gas, a POPs catalytic degradation device promptly, as shown in FIG. 1, the device includes: the device comprises a reactor 5, a flue gas inlet 1, an ammonia gas inlet 2, a gas outlet 7 and a catalyst module box 6;
wherein, the reactor 5 is of a hollow structure, and two ends of the reactor are respectively provided with an opening as an inlet and an outlet;
the flue gas inlet 1 and the ammonia gas inlet 2 are arranged on an inlet at one end of the reactor and are communicated with the inside of the reactor, and the flue gas inlet 1, the ammonia gas inlet 2 and the inlet of the reactor are sealed;
the gas outlet 7 is arranged on the outlet at the other end of the reactor 5 and is communicated with the inside of the reactor 5, and the gas outlet 7 is sealed with the outlet of the reactor;
a catalyst module box 6 is arranged inside the reactor, the catalyst module box 6 being arranged at a gas outlet 7 remote from the flue gas inlet 1 and the ammonia gas inlet 2.
The device is provided with the ammonia gas inlet, and the ammonia gas inlet is contacted with the catalyst in the catalyst module box and reacts with the catalyst, so that the POPs can be degraded, and the NOx contained in the flue gas can be degraded.
In the above device, the reactor 5 is a square long cylinder structure made of stainless steel, and the length of the cylinder body satisfies the following conditions: the contact time of the flue gas in the reactor and the catalyst module in the catalyst module box 6 is more than or equal to 0.3 second. The length of the middle part of the reactor is 300mm, the highest filling height of the catalyst is 0.22m, and when the flow velocity of the entering flue gas is 2.2m/s, the contact time of the flue gas in the reactor and the catalyst module in the catalyst module box 6 can be ensured to be more than or equal to 0.3 second.
In the device, the flue gas inlet 1 and the ammonia gas inlet 2 are arranged on an inlet at one end of the reactor 5 through the first flange 3, a groove corresponding to the protruding part at the edge of the opening can be arranged at the contact part of the first flange 3 and the opening of the reactor 5, and the graphite sealing gasket 9 is arranged in the groove, so that the first flange 3 and the opening can be kept better sealed.
In the device, the flue gas inlet 1 is arranged at the central part of the flange 3;
the two ammonia inlets 2 are respectively arranged at two sides of the flue gas inlet 1;
the inner diameter of the flue gas inlet 1 is larger than that of the ammonia gas inlet 2.
In the above device, the gas outlet 7 is provided at the outlet of the other end of the reactor 5 through a second flange 8.
In the above device, a graphite gasket 4 is provided between the second flange 8 and the outlet of the reactor 5. A groove corresponding to the raised portion of the outlet edge may be provided at the contact portion of the second flange 8 with the outlet of the reactor 5, and the graphite packing 4 may be provided in the groove, so that a better seal may be maintained between the first flange 3 and the outlet.
In the device, the geometric specific surface area of the catalyst module box 6 is more than or equal to 410m2/m3The porosity is 75%, the compression strength is more than 1.5MPa in the axial direction and more than 0.8MPa in the radial direction, a plurality of catalyst modules are arranged in the catalyst module box 6 in a layered mode, and the number of the catalyst modules in each layer is 4 multiplied by 5.
In the above apparatus, the shape of the catalyst module in the catalyst module case 6 is: honeycomb, corrugated, plate, sheet or granular.
In the device, the flue gas inlet 1 is provided with the heater. When the temperature of the flue gas is lower than the reaction temperature of the catalyst, the temperature can be increased by adjusting the heater of the flue gas inlet 1.
In the device, the maximum speed deviation of the flue gas entering the first layer of catalyst modules of the catalyst module box 6 is +/-15% of the average speed value, the maximum temperature deviation is +/-10% of the average speed value, and the maximum included angle between the direction of the flue gas entering the first layer of catalyst modules and the vertical direction is +/-10 degrees.
In the device, all the components can be made of stainless steel materials, the sealing effect is good, and the long-term operation can be realized under the condition that the smoke temperature is not higher than 430 ℃ without any damage; after POPs smoke enters the device, the smoke directly contacts with the catalyst in the catalyst module box under the action of airflow and reacts to achieve the effect of degrading the POPs.
The above degradation apparatus is further described with reference to the following specific examples.
The device is suitable for the specification of a used catalyst module, wherein the specification of the used catalyst module is 220mmx60mmx60mm, the aperture is 3mm, the inner wall is 0.5mm, and the outer wall is 1.5mm, so that the catalyst of the catalyst module can exert the best effect.
The flow velocity of the flue gas in the reactor was 2.2m/s, the maximum catalyst loading height was 0.22m, and the length of the middle part of the reactor was 300 mm. In order to avoid the over-long retention time of the mixed flue gas on the upper part (catalyst-free part) of the reactor, the effective (heating part) length of the upper part and the lower part of the reactor is designed to be 200 mm. The residence time in the reactor was 0.3 s;
therefore, the reactor is designed to be square in the excircle and inner part, the caliber is 62X 62mm, the height is 820mm, the size design of the catalyst is met, the highest filling height of the catalyst is 220mm, and the length of the middle part of the reactor is 300 mm; in order to avoid overlong residence time of the mixed flue gas on the upper part (catalyst-free part) of the reactor, the effective (heating part) length of the upper part and the lower part of the reactor is designed to be 200 mm; the catalyst adopts a transition metal oxide type catalyst V2O5-WO3/TiO2The optimum reaction temperature is 350 ℃ which is within the design temperature of the device.
The utility model discloses a degradation device, the key parameter of fully considering POPs and catalyst reaction, temperature, dwell time and contact mode etc for POPs in the flue gas takes place abundant reaction with the catalyst under the device, persistent organic pollutant such as dioxin in the flue gas can effectively degrade.
The above description is only for the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are all covered by the protection scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (9)
1. A persistent organic pollutant catalytic degradation device for treating flue gas, comprising:
the device comprises a reactor (5), a flue gas inlet (1), an ammonia gas inlet (2), a gas outlet (7) and a catalyst module box (6); wherein,
the reactor (5) is of a hollow structure, and two ends of the reactor are respectively provided with an opening as an inlet and an outlet;
the flue gas inlet (1) and the ammonia gas inlet (2) are arranged on an inlet at one end of the reactor (5) and are communicated with the inside of the reactor (5), and the flue gas inlet (1), the ammonia gas inlet (2) and the inlet of the reactor (5) are sealed;
the gas outlet (7) is arranged on the outlet at the other end of the reactor (5) and is communicated with the inside of the reactor (5), and the gas outlet (7) is sealed with the outlet of the reactor (5);
the catalyst module box (6) is arranged in the reactor (5), and the catalyst module box (6) is arranged at the gas outlet (7) far away from the flue gas inlet (1) and the ammonia gas inlet (2).
2. The apparatus according to claim 1, characterized in that the reactor (5) is a square, rectangular tubular structure made of stainless steel.
3. The apparatus according to claim 1 or 2, characterized in that the flue gas inlet (1) and the ammonia gas inlet (2) are arranged on an inlet at one end of the reactor (5) by means of a first flange (3).
4. The device according to claim 3, characterized in that the flue gas inlet (1) is arranged in the central part of the first flange (3);
the two ammonia inlets (2) are respectively arranged at two sides of the flue gas inlet (1);
the inner diameter of the flue gas inlet (1) is larger than that of the ammonia gas inlet (2).
5. The apparatus according to claim 1 or 2, characterized in that the gas outlet (7) is arranged at the outlet of the other end of the reactor (5) via a second flange (8).
6. The apparatus according to claim 5, characterized in that a graphite gasket (4) is provided between the second flange (8) and the outlet of the reactor (5).
7. The apparatus as claimed in claim 1 or 2, characterized in that the geometric specific surface area of the catalyst module cartridge (6) is ≥ 410m2/m3The porosity is 75%, the axial compressive strength is more than 1.5MPa, the radial compressive strength is more than 0.8MPa, a plurality of catalyst modules are arranged in the catalyst module box (6) in a layered mode, and the number of the catalyst modules in each layer is 4 multiplied by 5.
8. The apparatus according to claim 7, characterized in that the catalyst modules in the catalyst module cassette (6) are shaped: honeycomb, corrugated, plate, sheet or granular.
9. The apparatus according to claim 1 or 2, characterized in that the flue gas inlet (1) is provided with a heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320503601.5U CN203400631U (en) | 2013-08-16 | 2013-08-16 | Persistent organic pollutant catalytic degradation device for flue gas treatment |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320503601.5U CN203400631U (en) | 2013-08-16 | 2013-08-16 | Persistent organic pollutant catalytic degradation device for flue gas treatment |
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| CN203400631U true CN203400631U (en) | 2014-01-22 |
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| CN201320503601.5U Expired - Lifetime CN203400631U (en) | 2013-08-16 | 2013-08-16 | Persistent organic pollutant catalytic degradation device for flue gas treatment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103406023A (en) * | 2013-08-16 | 2013-11-27 | 中持（北京）科技发展有限公司 | POPs (Persistent Organic Pollutants) catalytic degradation device |
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2013
- 2013-08-16 CN CN201320503601.5U patent/CN203400631U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103406023A (en) * | 2013-08-16 | 2013-11-27 | 中持（北京）科技发展有限公司 | POPs (Persistent Organic Pollutants) catalytic degradation device |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140122 Effective date of abandoning: 20150624 |
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| RGAV | Abandon patent right to avoid regrant |