CN202909626U - Catalytic fluidized bed flue gas denitration reaction device - Google Patents
Catalytic fluidized bed flue gas denitration reaction device Download PDFInfo
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- CN202909626U CN202909626U CN2012205753916U CN201220575391U CN202909626U CN 202909626 U CN202909626 U CN 202909626U CN 2012205753916 U CN2012205753916 U CN 2012205753916U CN 201220575391 U CN201220575391 U CN 201220575391U CN 202909626 U CN202909626 U CN 202909626U
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- catalyst
- reaction tower
- flue gas
- airflow
- distribution board
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Abstract
The utility model relates to a catalytic fluidized bed flue gas denitration reaction device, which comprises a reaction tower and an outlet flue; the upper part of the reaction tower is made into a fume expansion section and communicated with the outlet flue; a plurality of catalyst support orifice plates are fixedly mounted in the middle of the reaction tower; granular catalysts are stacked on the catalyst support orifice plates; an airflow-distribution board is fixedly mounted on the reaction tower below the catalyst support plate; openings are uniformly formed in the airflow-distribution board; an inlet flue is formed at a right-angled turning at the lower part of the reaction tower, and a denitration reactant adding device is fixedly mounted on the inlet flue; an inlet flue deflector is mounted in the reaction tower at the right-angled turning; and an outlet flue deflector is mounted in the outlet flue, the right-angled turning at the lower part of the outlet flue is made into a gravitation settlement area, an ash hopper is fixedly mounted at the lower bottom of the outlet flue, and a catalyst returning device is arranged and communicated with the airflow-distribution board of the reaction tower and the ash hopper. The catalytic fluidized bed flue gas denitration reaction device utilizes the principle of a fluidized bed, reduces the diameter of the reaction tower, saves space and materials and improves catalyst utilization rate and reactant utilization rate.
Description
Technical field
The utility model belongs to field of Environment Protection, relates to denitrating flue gas, especially a kind of fluid catalytic cracking bed denitrating flue gas reaction unit.
Background technology
Denitrating flue gas is the environmental practice that present coal-burning power plant must implement, and usually utilizes selective catalytic reduction (SCR method) to carry out denitration, utilizes fixed bde catalyst that the denitration reaction in the flue gas is carried out catalysis.The gaseous ammonia of the NOx that contains in the flue gas and denitrating system preparation reacts at catalyst surface, generates the nitrogen G﹠W, reaches the purpose that pollutant NOx is removed.
According to above principle as can be known, the surface area of the speed of reaction and the performance of catalyst, catalyst has direct relation, in the situation that use catalyst of the same race, catalyst area just becomes the most important parameters of control denitrating system performance.In actual design, the area of fixed bde catalyst is commonly used its numerical value of this parameter characterization of specific area, and the concept of specific surface area of catalyst is the surface area size of per volume of catalyst, the m of unit
2/ m
3Expression.This shows, increase specific surface area of catalyst and can reduce catalyst amount, thereby reduce the volume of the reactor of containing catalyst.
The form that fixed bde catalyst uses has three kinds usually: flat catalyst, corrugated plate dst catalyst and cellular catalyst, in these three kinds of catalyst, the specific area maximum be cellular catalyst, can reach 400m
3/ m
2If further increase specific area, the structural strength of catalyst can not be born the load of self again, so the specific area of fixed bde catalyst has certain limit.
In normally used three kinds of catalyst, flue gas all is to flow through from the hole of catalyst, to reach the purpose that contacts with catalyst surface.Because hole has certain interval, the intensity that catalyst surface contacts with flue gas a little less than, need relatively for a long time that contact just can reach the reaction purpose, so smoke gas flow also is the restriction that the shortest time is arranged through the time of catalyst surface, this causes the used in amounts of catalyst to be greater than limiting value equally.
As from the foregoing, the intensity that increases specific area, increase flue gas and the catalyst Contact of catalyst can increase the catalytic effect of per volume of catalyst, thereby reaches the purpose that reduces reactor volume.
The utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art part, and a kind of denitrating flue gas reaction unit that utilizes fluid catalyst to carry out denitrating flue gas is provided, and to increase the catalyst effect of catalyst in the flue gas denitrification system, reduces the volume of reaction unit.
The purpose of this utility model is achieved through the following technical solutions:
A kind of fluid catalytic cracking bed denitrating flue gas reaction unit, comprise reaction tower and exhaust pass, it is characterized in that: the top of described reaction tower is made the flue gas expansion segment and is communicated with exhaust pass, the middle part of reaction tower is fixed with multi-layer catalyst and supports orifice plate, this catalyst supports to pile up on the orifice plate pellet type catalyst, reaction tower below the catalyst gripper shoe is fixed with airflow-distribution board, uniformly on this airflow-distribution board be shaped with perforate, the right-angle folding transformation of ownership becomes gas approach in the bottom of reaction tower, is fixed with denitration reaction agent adding apparatus at gas approach; The gas approach deflector is installed in the reaction tower of position, right-angle folding transfer part; The exhaust pass deflector is installed in exhaust pass, and this exhaust pass bottom right-angle folding transformation of ownership becomes the gravitational settling district, is fixed with ash bucket at the exhaust pass position of going to the bottom, and is communicated with the airflow-distribution board of reaction tower and ash bucket the catalyst reflux is installed.
And described catalyst is loose structure, and density is about 0.2-0.4t/m
3, the catalyst granules diameter is at 20mm, and catalyst height is at 400～600mm, and the catalyst gripper shoe is the 1-5 layer, and it supports the orifice plate opening diameter is 15mm.
And described airflow-distribution board airflow-distribution board opening diameter is at 200～300mm, and setting prevents the anti-gray umbrella that catalyst falls on perforate top, and this anti-gray umbrella is directly over perforate, and diameter is than the large 100mm of perforate.
Advantage of the present utility model and good effect are:
1, the utility model utilizes the fluid bed principle, has reduced the reaction tower diameter, has saved space and material, has improved utilization rate and the reactant utilization rate of catalyst.
2, the utility model catalyst utilization is high, and the catalyst use amount is little.
3, reactant of the present utility model and flue gas mix, and improve the reactant utilization rate, reduce reactant escape amount, are convenient to catalyst regeneration.
Description of drawings
Figure l is structural representation of the present utility model;
Fig. 2 is the A section structure enlarged diagram of Fig. 1.
The specific embodiment
The utility model is described in further detail as an example of the accompanying drawing embodiment example for the below, and following examples are descriptive, is not determinate, can not limit protection domain of the present utility model with this.
A kind of fluid catalytic cracking bed denitrating flue gas reaction unit as shown in fig. 1, comprises reaction tower 1 and exhaust pass 5, and the top of reaction tower is made the flue gas expansion segment and is communicated with exhaust pass, and the expansion segment flue gas flow rate is about 1/4～1/2 of the interior flow velocity of tower; The middle part of reaction tower is fixed with multi-layer catalyst and supports orifice plate 3, and this catalyst supports to pile up on the orifice plate pellet type catalyst 2, and this catalyst is loose structure, and density is about 0.2-0.4t/m
3, the catalyst gripper shoe is the 1-5 layer, is two-layer shown in the present embodiment accompanying drawing; The catalyst granules diameter supports the orifice plate opening diameter about 15mm about 20mm, catalyst height is about 400～600mm.Reaction tower below the catalyst gripper shoe is fixed with airflow-distribution board 10, uniformly on this airflow-distribution board is shaped with perforate 9, arranges on its perforate top and prevents the anti-gray umbrella that catalyst falls; The airflow-distribution board opening diameter is about 200～300mm, and the anti-gray umbrella is directly over perforate, and diameter is than the large 100mm of perforate.The right-angle folding transformation of ownership becomes gas approach 12 in the bottom of reaction tower, is fixed with denitration reaction agent adding apparatus 13 at gas approach; Gas approach deflector 11 is installed in the reaction tower of position, right-angle folding transfer part, is used for flue gas is introduced reaction tower, and can makes the air velocity distribution homogenising.
Be communicated with the airflow-distribution board of reaction tower and ash bucket catalyst reflux 8 is installed, this reflux is used for the catalyst granules that deduster catches is transmitted back to reaction tower.
Reaction tower is used for making pellet type catalyst to produce fluidized state, to increase flue gas and catalyst contact strength; The reaction tower gas approach is used for flue gas and reactant are carried out blending, and sends into uniformly flue gas in the reaction tower; Tail gas after the reactor outlet flue is used for processing is discharged the denitration reaction device, and removes the catalyst granules of taking out of in the flue gas in this stage, simultaneously with the catalyst granules recycle and reuse that catches.
The inner inlet porting flue of gas approach deflector is used for making the air velocity distribution homogenising, be used for reactant is injected flue gas at the denitration reaction agent adding apparatus of gas approach deflector front end setting, and blending is even.
Operation principle of the present utility model is:
Pending flue gas enters reaction tower through the reaction tower gas approach, and inject the denitration reaction agent by denitration reaction agent adding apparatus (prior art) herein, after mixing, reactant and flue gas through the rectification of gas approach deflector, enter more equably the catalyst fluidized bed reaction tower.In the catalyst fluidized bed reaction tower, flue gas is through the further homogenising of airflow-distribution board, enter catalyst and support orifice plate and fluid catalyst, it is the baffle plate device that leaves uniform perforate that catalyst supports orifice plate, can make flue gas passing through from bottom to top from perforate, the diameter of perforate can block catalyst granules and not fall less than the diameter of fluid catalyst particle.During this section of flue gas process, because flowing of flue gas drives catalyst layer and be half fluidized state that suspends, by the flue gas flow rate of control reaction tower when designing, realize the control to the fluidisation state strength, make it in a controlled fluidisation extent and scope.Catalyst granules has small part and falls to airflow-distribution board through catalyst support orifice plate, and this part particle can be through in the mozzle inflow catalyst reflux in the middle of the airflow-distribution board.Therefore airflow-distribution board also has the catalyst granules of separation whereabouts and the effect of flue gas.
Flue gas is through after the two catalyst layers, flue gas enters the flue gas expansion segment, and this partial reaction tower section is long-pending larger, and flue gas flow rate is lower, the catalyst of the larger particles of taking out of with flue gas has played the effect of gas solid separation along with the reduction of flue gas flow rate falls after rise to the fluid catalyst layer.Flow out reaction tower by flue gas after this section, enter reactor outlet flue part.
After flue gas enters the reactor outlet flue, rectification through the exhaust pass deflector, enter in the gravitational settling deduster, this deduster sectional area is larger, and flue gas flow rate reduces, in addition the effect of deflector and flue gas turning, the catalyst granules that carries in the flue gas is separated, enter in the ash bucket, and fall in the catalyst reflux by deadweight, reclaim catalyst recycling.Outside the flue gas outflow system by device.
Claims (3)
1. fluid catalytic cracking bed denitrating flue gas reaction unit, comprise reaction tower and exhaust pass, it is characterized in that: the top of described reaction tower is made the flue gas expansion segment and is communicated with exhaust pass, the middle part of reaction tower is fixed with multi-layer catalyst and supports orifice plate, this catalyst supports to pile up on the orifice plate pellet type catalyst, reaction tower below the catalyst gripper shoe is fixed with airflow-distribution board, uniformly on this airflow-distribution board be shaped with perforate, the right-angle folding transformation of ownership becomes gas approach in the bottom of reaction tower, is fixed with denitration reaction agent adding apparatus at gas approach; The gas approach deflector is installed in the reaction tower of position, right-angle folding transfer part; The exhaust pass deflector is installed in exhaust pass, and this exhaust pass bottom right-angle folding transformation of ownership becomes the gravitational settling district, is fixed with ash bucket at the exhaust pass position of going to the bottom, and is communicated with the airflow-distribution board of reaction tower and ash bucket the catalyst reflux is installed.
2. fluid catalytic cracking bed denitrating flue gas reaction unit according to claim 1, it is characterized in that: described catalyst is loose structure, and density is about 0.2-0.4t/m
3, the catalyst granules diameter is at 20mm, and catalyst height is at 400～600mm, and the catalyst gripper shoe is the 1-5 layer, and it supports the orifice plate opening diameter is 15mm.
3. fluid catalytic cracking bed denitrating flue gas reaction unit according to claim 1, it is characterized in that: described airflow-distribution board airflow-distribution board opening diameter is at 200～300mm, setting prevents the anti-gray umbrella that catalyst falls on perforate top, this anti-gray umbrella is directly over perforate, and diameter is than the large 100mm of perforate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205753916U CN202909626U (en) | 2012-11-05 | 2012-11-05 | Catalytic fluidized bed flue gas denitration reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205753916U CN202909626U (en) | 2012-11-05 | 2012-11-05 | Catalytic fluidized bed flue gas denitration reaction device |
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| Publication Number | Publication Date |
|---|---|
| CN202909626U true CN202909626U (en) | 2013-05-01 |
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| CN2012205753916U Withdrawn - After Issue CN202909626U (en) | 2012-11-05 | 2012-11-05 | Catalytic fluidized bed flue gas denitration reaction device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102989313A (en) * | 2012-11-05 | 2013-03-27 | 航天环境工程有限公司 | Flue gas denitration reaction device of catalytic fluidized bed |
| CN104056549A (en) * | 2014-07-04 | 2014-09-24 | 长沙理工大学 | Smoke SCR denitration system for fluidized fuel gas kiln |
| CN112933920A (en) * | 2021-02-01 | 2021-06-11 | 中国科学院过程工程研究所 | Desulfurization, denitrification and dedusting integrated reaction device for flue gas and desulfurization, denitrification and dedusting method |
-
2012
- 2012-11-05 CN CN2012205753916U patent/CN202909626U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102989313A (en) * | 2012-11-05 | 2013-03-27 | 航天环境工程有限公司 | Flue gas denitration reaction device of catalytic fluidized bed |
| CN104056549A (en) * | 2014-07-04 | 2014-09-24 | 长沙理工大学 | Smoke SCR denitration system for fluidized fuel gas kiln |
| CN112933920A (en) * | 2021-02-01 | 2021-06-11 | 中国科学院过程工程研究所 | Desulfurization, denitrification and dedusting integrated reaction device for flue gas and desulfurization, denitrification and dedusting method |
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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: 20130501 Effective date of abandoning: 20140910 |
|
| RGAV | Abandon patent right to avoid regrant |