CN102068906B

CN102068906B - Light particle catalyst fluidized bed denitration reactor

Info

Publication number: CN102068906B
Application number: CN 201010597005
Authority: CN
Inventors: 崔素萍; 严建华; 兰明章; 王亚丽; 杜鑫; 秦魏; 郭红霞; 刘庆祎
Original assignee: Beijing University of Technology
Current assignee: Beijing University of Technology
Priority date: 2010-12-10
Filing date: 2010-12-10
Publication date: 2013-03-06
Anticipated expiration: 2030-12-10
Also published as: CN102068906A

Abstract

The invention discloses a light particle catalyst fluidized bed denitration reactor, and belongs to the technical field of building material industrial equipment. The reactor has a diameter variable structure to facilitate regulating gas flow rate, and mainly comprises a gas flue (1), a cone (2), a barrel (3) and the like, wherein a necking section (4) is arranged at an inlet of mixed gas of tail gas and flue gas; a catalyst unit in the reactor, namely a multi-layer particle catalyst fluidized bed takes a porous ceramic plate as a base plate (5); and granular catalyst replacement holes, namely a catalyst discharging opening (7) and a catalyst charging opening (8) are formed on the two sides of each layer in an up and down staggered mode at each intervals. The reactor can facilitate the detection of the gas flow rate, the determination of the arrangement amount of a catalyst and the replacement of the catalyst. Compared with a modular catalyst, a flowing catalyst has low pressure loss; and dust cannot be adhered to catalyst particles so as not to reduce activity or cause poisoning or failure.

Description

The catalyst bubbling bed Benitration reactor of a kind of light granules

Technical field

The invention belongs to the building material industry equipment technical field, relate to the structural design of a kind of cement plant ebullated bed flue gas denitration reactor.

Technical background

The NOx nitrogen oxide that manufacture of cement produces comprises nitric oxide NO, nitrogen dioxide NO ₂With nitrous oxide N ₂O (laughing gas) etc. have great harm to agricultural, forestry, global climate, natural environment and human body health.New dry process rotary kiln NOx emission factor is the 1.5-1.8kg/t-grog.It is estimated approximately 2,000,000 tons of 2009 discharging NOx.Beijing was from 2008, and cement producing line NOx allows concentration of emission must not surpass 500mg/Nm ³, and carry out the total amount charge.

Denitrating flue gas has also been carried out a large amount of research both at home and abroad, at present main denitration technology has Researched of Air Staging Combustion Burning Pulverized Coal, fuel-staged combustion, SNCR, SCR, plasma method, biochemical process, absorption method etc., in industry, come into operation mainly be before several method.

The denitration of SCR method is used in coal electricity industry, and it uses the vertical type catalytic reactor mostly, and fixed reactor, horizontal reactor, barrel reactor etc. are also arranged.Because the cement plant exhaust gas dust is large, and viscosity is large.Easily cause catalyst layer to stop up, increase reactor pressure decrease; And owing to K, Na in the dust, Ca etc. cause catalyst poisoning, affect the result of use of catalyst, and its use cost is improved.On cement kiln, directly use aspect the tail gas denitration certain technology difficulty is arranged.

Summary of the invention

Owing to containing a large amount of dust in the flue gas of cement plant, traditional denitration reaction catalyst easily adsorbs dust, cause catalyst poisoning or inefficacy, easy dust stratification in the reactor, for this problem, developed a kind of ebullated bed catalytic reactor of cement kiln dust, it is take the light granules that do not adhere to cement kiln dust as catalyst, flue gas can be adjusted gas flow rate and form the ebullated bed structure with light granules by reactor the time, make flue gas that preferably denitration efficiency be arranged, and because the flow regime reactor of gas can not produce dust stratification.

The present invention adopts following technical scheme:

The catalyst bubbling bed Benitration reactor of a kind of light granules, comprise flue 1, cone 2, cylindrical shell 3, it is characterized in that: the flue 1 that is positioned at reactor bottom links to each other with reducing 4, and reducing 4 links to each other with cylindrical shell 3 again, and last cylindrical shell 3 links to each other with the flue 1 that is positioned at reactor head again; Reducing 4 links to each other with parts up and down by cone 2 respectively, is provided with flange 6 in the reducing 4; The cylindrical shell moderate distance arranges the porous plate 5 that multiple tracks is used for placing the light granules catalyst, is arranged in catalyst charging hole 8 and the catalyst discharge port 7 that many hollow plates position is staggered up and down and is arranged symmetrically with at cylindrical shell; The flue 1 that is positioned at reactor head is provided with check valve 9.Described many hollow plates 5 are porous ceramic plate.

The diameter of described reducing 4 is less than the diameter of flue 1 and cylindrical shell 3.

Described reactor has double-decker, and inside is heat-insulation layer, and the outside is the steel structure layer.

The present invention can obtain following beneficial effect:

Catalyst is the light granules layer that is not easy to adhere to the cement kiln tail gas dust, takes to treat that denitration tail gas and the ammonia gas mixture body flow direction from bottom to top suspend light granules, increases the reaction efficiency of mist and catalyst; Simultaneously flue gas is from bottom to top by reactor, by the layout to reducing 4, and can the adjustments of gas flow velocity, when unstable for gas flow rate, be convenient to catalyst bubbling bed formation, and adapt to the catalyst granules of different sizes, when catalyst was adjusted catalyst, this structure still had serviceability.In flange 6 and

catalyst window

7,8 setting, can make things convenient for determining and the replacing of catalyst of the detection of gas flow rate and catalyst arrangement amount.Compare with the modularization catalyst, adopt the mobile catalyst pressure loss little, and catalyst granules can not adhere to dust and reduce activity or poison deactivation.

Description of drawings:

Fig. 1 ebullated bed Benitration reactor general structure front view;

Fig. 2 ebullated bed Benitration reactor structure rearview;

Fig. 3 ebullated bed Benitration reactor texture edge part sectioned view;

Fig. 4 Benitration reactor catalyst layer profile

Among the figure: 1, flue, 2, cone, 3, cylindrical shell, 4, reducing, 5, porous plate, 6, flange, 7, the catalyst discharge port, 8, catalyst charging hole, 9, check valve.

The specific embodiment:

According to Fig. 1, Fig. 2 and Fig. 3, Fig. 4, gas from bottom to top passes through in the reactor, forms the ebullated bed state with light granules, can not produce dust stratification or catalyst absorption dust and loses efficacy, and its structure mainly contains flue 1, cone 2, cylindrical shell 3 etc. and is welded to form.Be gas approach 1 at the reactor low side, before flue gas enters cylindrical shell, pass through first reducing 4, reducing 4 becomes 30 ° with flue 1 level; The mouth of pipe that gas goes out reducing has porous plate 5; Multiple tracks porous plate 5 is set in the cylindrical shell; In reducing 4 parts a flange 6 is set; What be connected with reducing 4 upper ends is cone 3,75 ° at cone 3 ground and horizontal plane, and upper diameter is greater than lower diameter; Cylindrical shell 3 partially catalyzed agent sections are equidistant, two windows are staggered up and down: catalyst charging hole 8, catalyst discharge port 7; Flue gas is discharged by the exhaust pass 1 of reactor top, and outlet cone 2 becomes 75 ° with horizontal plane; Exhaust pass diameter and facies superior pyramidis equal diameters; Check valve 9 is set in exhaust pass.Flue gas and lightweight catalyst granules form ebullated bed between each porous plate, can prevent dust to the absorption of catalyst granules or produce dust stratification, to improve denitrating flue gas efficient.Reactor is comprised of double-decker, and internal layer is heat-insulation layer, and skin is the steel structure layer.

Claims

1. catalyst bubbling bed Benitration reactor of light granules, comprise flue (1), cone (2), cylindrical shell (3), it is characterized in that: the flue (1) that is positioned at reactor bottom links to each other with reducing (4), reducing (4) links to each other with cylindrical shell (3) again, and last cylindrical shell (3) links to each other with the flue that is positioned at reactor head (1) again; Reducing (4) links to each other with parts up and down by cone (2) respectively, is provided with flange (6) in the reducing (4); The cylindrical shell moderate distance arranges the porous plate (5) that multiple tracks is used for placing the light granules catalyst, is arranged in catalyst charging hole (8) and the catalyst discharge port (7) that the porous plate position is staggered up and down and is arranged symmetrically with at cylindrical shell; The flue (1) that is positioned at reactor head is provided with check valve (9).

2. the catalyst bubbling bed Benitration reactor of a kind of light granules according to claim 1, it is characterized in that: the diameter of described reducing (4) is less than the diameter of flue (1) and cylindrical shell (3).

3. the catalyst bubbling bed Benitration reactor of a kind of light granules according to claim 1, it is characterized in that: described porous plate (5) is porous ceramic plate.

4. the catalyst bubbling bed Benitration reactor of a kind of light granules according to claim 1, it is characterized in that: described reactor has double-decker, and inside is heat-insulation layer, and the outside is the steel structure layer.