CN104056549B - A kind of fluidization gas furnace kiln flue gas SCR denitration system - Google Patents
A kind of fluidization gas furnace kiln flue gas SCR denitration system Download PDFInfo
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- CN104056549B CN104056549B CN201410316964.7A CN201410316964A CN104056549B CN 104056549 B CN104056549 B CN 104056549B CN 201410316964 A CN201410316964 A CN 201410316964A CN 104056549 B CN104056549 B CN 104056549B
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Abstract
The invention provides a kind of fluidization gas furnace kiln flue gas SCR denitration system, comprise reative cell, be positioned at mixing chamber below reative cell; Be provided with air distribution plate between reative cell and mixing chamber, on air distribution plate, the form arrangement of equilateral triangle pressed by blast cap, and it is the blast cap aperture of 5 ° ~ 15 ° that blast cap neck is provided with the angle of level cross-sectionn; Air distribution plate upper surface is furnished with catalyst granules, the ceramic particle of its carrier to be particle diameter be 0.1 ~ 5mm, and applicator is SCR denitration active material; The piling height of catalyst granules is 2-6 times of blast cap height.In the technology of the present invention, catalyst granules specific area is large, the mixed airflow that catalyst granules is upwards flowed and self gravitation double action, constantly circulate up and down and seethe, make catalyst granules in fluid mapper process with the contact of flue gas/ammonia gas mixture body with mix comparatively compared with conventional art more strongly, more abundant, catalytic effect is better, and denitration efficiency reaches more than 99%.
Description
Technical field
The present invention relates to flue gas pollutant Treatment process field, especially, relate to a kind of fluidization gas furnace kiln flue gas SCR denitration system.
Background technology
Current, high with denitration efficiency, the selective plurality of advantages such as good, stable of the gas denitrifying technology based on SCR (SelectiveCatalystReduction, SCR) and being used widely.The principle of this technology is namely under the condition having catalyst, and (nitrogen oxide comprises NO and NO to the NOx in flue gas
2) with the NH that sprays into
3there is chemical reaction and generate harmless N in (ammonia)
2and H
20, chemical equation is as follows:
But the SCR system of current domestic operation exists following problem to be waited to solve always:
(1) specific surface area of catalyst is little.
The catalyst that engineering is applied, according to the difference of version mainly contain honeycomb fashion, flat, corrugated three kinds.The catalyst of these three kinds of versions in running because needing to consider the fluid resistance loss of flue gas, reaction time, the factor such as whether catalyst duct blocks, the degree of wear of catalyst body the aperture size of catalyst is chosen comparatively large, cause the less (350 ~ 850m of monolith specific area
2/ m
3), and being the technical requirement reaching denitrating flue gas, this arranges the number of plies with regard to needs extra increase catalyst, and then makes device structure complicated, cost increase.
(2) catalyst amount cannot regulate in real time.
For improving the in-site installation speed of catalyst and the convenience of maintenance, catalyst many employings modularization that engineering is applied is installed, namely combined by some catalyst elements and add that outside framework forms a catalyst module, the catalyst major defect of this arrangement form works as fuel quality, when load conditions etc. change and cause exhaust gas volumn or smoke components to change, the consumption of catalyst can not timely adjustment, cause the unnecessary dissipation of partially catalyzed agent, the concentration value of NOx in exiting flue gas is caused to fluctuate by a relatively large margin up and down, the catalyst of this kind of arrangement form to load variations in good time should not be strong.
(3) Benitration reactor volume is large, high material consumption.
Current, in the SCR system of commercial Application, the layout number of plies of catalyst presses 2+1 mode arrangement, namely installs 2 layers reserved 1 layer, and consider that running a period of time rear catalyst must change and maintenance etc., is all reserved with certain height and position for maintainer's turnover between each layer catalyst.The arrangement mode of catalyst adds that the reserved height space between each layer catalyst makes the bulky of whole Benitration reactor, and consumption of materials is huge.Moreover, this cause because Benitration reactor is bulky this technology of application to old stove carry out denitration engineered time, the use of denitrification apparatus to be limited because of the place space constraints of stove.
(4) catalyst activity when denitrating system normally runs is difficult to realize normalization and maintains.
At present, by regenerated liquid, its activity is recovered for the offline mode that adopts main on the Catalyat Engideering of activity reduction.Though regenerated offline mode is the mode that application is more at present, when which is run, there are two obvious technological deficiencies: one is need to force blowing out, will affect normal operation and the production of enterprise; Two are unloadings of catalyst, long-distance transport, factory's activation and the process of reloading waste time and energy, substantially prolongs the regeneration duration of catalyst.In addition, the on-line regeneration technology about flue gas SCR decaying catalyst is still in the initial stage of fumbling, rarely has report both at home and abroad.Because the regenerated offline mode of decaying catalyst just must can take out after blowing out, activate, this operator scheme makes denitrating system be difficult to realize the normalization when normal operation and maintains the catalytic activity of catalyst.
Therefore, for the series of problems that active service SCR denitration system exists, the SCR system of inventing a kind of new structure to reduce SCR denitration system operating cost, increase specific surface area of catalyst, realize catalyst amount real-time, tunable etc. to improving the operational efficiency of SCR denitration system, the discharge of decreasing pollution thing has important practical significance.
Summary of the invention
The object of the invention is to provide a kind of fluidization gas furnace kiln flue gas SCR denitration system, and to solve, specific surface area of catalyst is little, Benitration reactor volume is large, catalyst amount can not regulate in real time, catalytic activity is difficult to realize the technical problems such as normalization maintenance in reative cell.
For achieving the above object, the invention provides a kind of fluidization gas furnace kiln flue gas SCR denitration system, comprise reative cell, be positioned at mixing chamber below reative cell;
Be provided with air distribution plate between described reative cell and described mixing chamber, described air distribution plate comprises card and is arranged on the some blast caps on card, and the form arrangement of equilateral triangle pressed by adjacent blast cap, and the length of side of described equilateral triangle is 1.3 ~ 1.7 times of blast cap diameter;
Blast cap is the warhead shape object that hemisphere face is combined with cylinder, and upper end hemisphere face is closed, and lower end cylinder arranges through hole and inserts in the jack on card, and described through hole bottom communicates with mixing chamber; The neck of blast cap is provided with blast cap aperture, and the axis of blast cap aperture and the angle of level cross-sectionn are 5 ° ~ 15 °;
Described air distribution plate upper surface is provided with catalyst granules, the ceramic particle of the carrier of described catalyst granules to be particle diameter be 0.1 ~ 5mm, and the applicator on carrier is SCR denitration active material; Described SCR denitration active material comprises V
2o
5, WO
3, MoO
3;
The piling height of catalyst granules is 2-6 times of described blast cap height.
Preferably, described reative cell sidewall is provided with particle and supplements mouth, the vertical range that described particle supplements mouth and air distribution plate is 100 ~ 500mm.
Preferably, the angle of the described particle axis and level cross-sectionn that supplement mouth is 30 ° ~ 60 °.
Preferably, described reative cell sidewall is provided with particle scavenge port, described particle scavenge port is positioned at air distribution plate sustained height, and the axis of described particle scavenge port and the angle of level cross-sectionn are 30 ° ~ 60 °.
Preferably, the exhanst gas outlet of described reative cell is provided with flue gas NOx checkout gear.
Preferably, also comprise smoke inlet pipeline in mixing chamber front end, in described smoke inlet pipeline, be provided with ammonia-spraying grid; Described ammonia-spraying grid is made up of ammonia mother pipe and several points of gamete pipes, and a point gamete tube side-by-side is connected on ammonia mother pipe, and every root divides on gamete pipe and is respectively arranged with flow control valve and several nozzle.
Preferably, described smoke inlet install pipeline has booster fan.
Preferably, the little hole number of blast cap on single blast cap is 4-8.
Preferably, particle scavenge port and particle supplement the quantity of mouth is 4 ~ 10.
The present invention has following beneficial effect:
The particle diameter that the present invention selects physicochemical properties more stable be the ceramic particle of 0.1 ~ 5mm as catalyst carrier, and real time on-line monitoring, the adjust structure of catalyst are set, reach following advantage:
(1) specific surface area of catalyst is large, flue gas/ammonia gas mixture body and catalyst exposure with mix strongly, denitration efficiency is high.
Catalyst during present system uses selects particle diameter to be that the ceramic particle of 0.1 ~ 5mm is as catalyst carrier, the coating of SCR denitration active material is obtained on the carrier particles, its specific surface area of catalyst is 5 ~ 36 times of active service conventional cellular catalyst, being 8 ~ 54 times of the corrugated catalyst of active service, is 11 ~ 70 times of the flat catalyst of active service.
In addition, in conventional art, catalyst maintains static, and has contacted chemical reaction when flue gas/ammonia gas mixture body passes the stationary conduit in catalyst with catalyst wall; In the technology of the present invention, not only specific surface area of catalyst strengthens, and the mixed airflow that upwards flowed in reative cell of catalyst and self gravitation double action, constantly circulate up and down and seethe, make catalyst in fluid mapper process with the contact of flue gas/ammonia gas mixture body and mixing all comparatively compared with conventional art more strongly, more abundant, catalytic effect is better, and in flue gas, that the speed of chemical reduction reaction occurs is faster for NOx, denitration efficiency is higher, and denitration efficiency can reach more than 99%.
(2) catalyst amount is few, and Benitration reactor volume is little, equipment manufacturing cost and operation expense low.
Research shows, when the cross-sectional area of present system and traditional SCR denitration system is with size, under the abundant fluidisation of catalyst granules in present system in reative cell (during as particle voids rate >=0.98) state, under administering equal exhaust gas volumn operating mode, when catalyst granules piling height in present system in reative cell only needs 2/3 ~ 4/5 of the catalyst monolayers height reaching traditional SCR denitration system, the denitration efficiency of equal extent can be reached, now, the volume of whole Benitration reactor is only 1/3 ~ 1/5 of traditional SCR denitration reactor, material consumption is only 1/4 ~ 1/10 of traditional SCR denitration reactor, because the reduction of catalyst amount and Benitration reactor volume makes the equipment manufacturing cost of present system be only about 1/3 of traditional SCR denitration system.
In addition, as the ceramic particle of catalyst carrier, its wide material sources, and have good high temperature resistant, corrosion-resistant and thermal shock resistance, can effectively overcome conventional cellular or corrugated plate dst catalyst is subject to the technical barrier such as mechanical damage, channel blockage in running.Catalyst granules after inactivation its mechanical strength after regenerated liquid regeneration can not decline still can drop into and recycle, and its equipment dependability and service life are far above existing catalytic unit.
Moreover, consider from the structural configuration angle of whole furnace kiln system, because Benitration reactor volume in present system is little, device spatial volume is little, traditional structure can be adapted to and arrange that the denitration of compacter old stove is engineered.Meanwhile, for the spatial volume that also significantly can reduce whole system during newly-built stove application present system, save occupation area of equipment, reduce device space complexity.
(3) catalyst amount real-time, tunable, fuel, load adaptability are wide, can the normalization of the indoor catalytic activity of realization response maintain.
In present system, when the fuel quality, load condition etc. of stove change cause that in exhaust gas volumn, flue gas, NOx content changes time, in the NOx checkout gear that can arrange according to exhanst gas outlet, the data fed back open particle scavenge port on reative cell sidewall or particle supplements mouth to regulate catalyst granules accumulating amount in reative cell fast, the real-time adjustment of catalyst granules accumulating amount is equivalent to the catalysis area that have adjusted catalyst in real time, to adapt to the change of exhaust gas volumn and flue gas quality.The real-time, tunable of catalyst amount makes present system to the change strong adaptability of stove load condition and fuel quality, and fuel tolerance is wide, and load adaptability is wide.
Present system is after operation a period of time, and in reative cell, the catalyst granules of inactivation is discharged fast by particle scavenge port, supplements mouth simultaneously supplement highly active fresh catalyst particles in time by particle.In reative cell, the discharge of decaying catalyst and the supplementary of fresh catalyst can realize the continued operation when shutdown system does not normally run, and supplement to have with discharge process speed fast, save time, the feature such as laborsaving, easy to operate, this characteristic can make the normalization realizing catalyst activity in reative cell maintain.
(4) flue gas/ammonia mixes, and grain fluidized uniformity degree is high.
In present system, ammonia-spraying grid is set in the smoke inlet pipeline of mixing chamber front end, card equidistantly arranges blast cap by the form of equilateral triangle, even circumference arranges blast cap aperture in blast cap neck cross section, flue gas/ammonia gas mixture body can be impelled evenly to send forth and to enter reative cell, realize the even fluidizing of catalyst granules, make the contact of flue gas/ammonia gas mixture body and catalyst granules and mix all more abundant.The all mixed technology of flue gas/ammonia in present system and uniform particles fluidization technique can not only strengthen catalytic effect, improve denitration efficiency, also can reduce the ammonia caused because flue gas/ammonia mixing is uneven, mist/catalyst granules contact is insufficient to escape, alleviate the impact of ammonia escape environmental pollution.
Fluidization SCR denitration system of the present invention is the important breakthrough of the Theory and technology to existing traditional flue gas denitrification system, there is unrivaled technology and economy advantage, and will important technical be brought to change to the design of gas fired-boiler, gas burning kiln etc., manufacture and operation, having broad application prospects in industrial equipment tail gas denitration technology field, is the important technology support to going deep into promotion and implementation energy-saving and emission-reduction strategy.
Except object described above, feature and advantage, the present invention also has other object, feature and advantage.Below with reference to figure, the present invention is further detailed explanation.
Accompanying drawing explanation
The accompanying drawing forming a application's part is used to provide a further understanding of the present invention, and schematic description and description of the present invention, for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 is the system architecture schematic diagram of the preferred embodiment of the present invention;
Fig. 2 is the air distribution plate of the preferred embodiment of the present invention and the assembly structure schematic diagram of blast cap;
Marginal data: 1-reative cell, 2-mixing chamber, 3-ammonia-spraying grid, 4-smoke inlet pipeline, 5-exhanst gas outlet, 6-catalyst granules, 7-blast cap, 8-air distribution plate, 9-blast cap aperture, 10-particle scavenge port, 11-particle supplements mouth, 12-booster fan, 13-ammonia mother pipe, 14-divides gamete pipe, 15-NOx checkout gear.
Detailed description of the invention
Below in conjunction with accompanying drawing, embodiments of the invention are described in detail, but the multitude of different ways that the present invention can limit according to claim and cover is implemented.
See Fig. 1, present system docks primarily of reative cell 1 and mixing chamber about 2 arranges composition.Be arranged in reative cell 1 bottom of top and be provided with air distribution plate 8 between reative cell 1 and mixing chamber 2, air distribution plate 8 is piled up catalyst granules 6.
For controlling the quality and quantity of catalyst granules 6 in real time, the sidewall of reative cell 1 can be provided with particle scavenge port 10 and particle supplements mouth 11.Particle scavenge port 10 is arranged on the bottom of reative cell, is positioned at air distribution plate sustained height; Particle supplements mouth 11 and is arranged on position higher than the bed bed of material.Preferably, particle supplements the side-walls that mouth 11 is arranged on 100 ~ 500mm on a bed depth direction.The axis of particle scavenge port and the angle α of level cross-sectionn, particle supplement the axis of mouth and the angle β of level cross-sectionn can be all 30 ° ~ 60 °, and particle smooth, continuous print can be filled into and discharge.Particle scavenge port 10 and particle supplement mouth 11 and can be evenly arranged 4 ~ 10 along on reative cell cross section.
Reative cell 1 upper end is provided with exhanst gas outlet 5, and mixing chamber 2 front end be arranged in below reative cell is provided with smoke inlet pipeline 4, is respectively arranged with booster fan 12 and ammonia-spraying grid 3 in smoke inlet pipeline 4.Described ammonia-spraying grid 3 is made up of the female pipe 13 of an ammonia and several points of gamete pipes 14, and a point gamete pipe 14 is connected on the female pipe 13 of ammonia side by side.Every root divides on gamete pipe 14 and is provided with a flow control valve and several nozzle, and ammonia is entered in smoke inlet pipeline by nozzle and mixes with flue gas.Ammonia-spraying grid 3 spray into that a position is chosen, minute gamete pipe quantity is chosen and the design of nozzle, layout, choosing of quantity can adopt computational fluid dynamics method (CFD) to determine according to on-site actual situations.
Fig. 2 is the air distributor structure schematic diagram of present system.The effect of air distribution plate 8 is supported the static bed of material and distributes mist uniformly, mist is sent forth equably by the blast cap 7 on air distribution plate 8 to be entered in reative cell, to ensure the even fluidizing of catalyst granules, realize flue gas/ammonia gas mixture body and fully contact with catalyst granules.
Air distribution plate 8 in present system is made up of blast cap 7 and card.Card is the porous flat plate be made up of steel plate or cast iron plate, is used for fixing blast cap, makes to arrange by the form of equilateral triangle between blast cap and blast cap.The leg-of-mutton length of side can be 1.3 ~ 1.7 times of blast cap diameter, and the gas that adjacent blast cap is sent forth out influences each other less, and takes into account card area utilization ratio.
Blast cap 7 can be the warhead shape object that semi-sphere is combined with cylinder, and upper end sphere is closed, and lower end cylinder arranges through hole and vertically inserts in the jack on card, and described through hole communicates with mixing chamber down.
Blast cap aperture 9 can be provided with at blast cap 7 neck, the axis of blast cap aperture 9 and the angle γ of level cross-sectionn are 5 ° ~ 15 °, be make the mist sent forth out from blast cap aperture have tangential velocity on the one hand, be conducive to having draged blast cap aperture on air distribution plate and make it fluidisation with the accumulation catalyst granules of lower part; On the other hand, the inclined design that the summary of blast cap aperture is downward adds the stroke of mist in reative cell, extends the time of staying of mist in reative cell, and be conducive to mist and catalyst exposure more abundant, catalytic effect is better.
Blast cap aperture 9 can evenly arrange 4 ~ 8 along blast cap neck cross section, does not affect the realization of the present embodiment.
Flue gas in mixing chamber/ammonia gas mixture body is evenly sent forth and entered in reative cell is realized by two processes.First, mist carries out at card place for the first time " shunting ", makes mist flow into each blast cap from the lower port of each blast cap respectively.Secondly, after mist upwards flow to neck in blast cap, namely laterally to send forth at a high speed to all directions with the high velocity air of tiny, high degree of dispersion and strong disturbance in a large number from some blast cap apertures and come, uniform distribution enters the mist of reative cell again.
The catalyst of present system on the ceramic particle that particle diameter is 0.1 ~ 5mm, applies active material obtain, and the applicator on carrier is SCR denitration active material; Described SCR denitration active material comprises V
2o
5, WO
3, MoO
3.
The voidage of the catalyst granules in fluidized state in reative cell should be greater than 0.98, is conducive to the surface area fully utilizing catalyst granules completely like this, the area that increase mist and catalyst exposure react, and improves denitration efficiency.Theoretically, under uniform particles fluidized state, when the material bed height after fluidisation reach initial pile amass 2 times of material bed height time, now intergranular space rate is just 1.When the piling height of catalyst granules is the 2-6 times of described blast cap height, the catalyst granules voidage more easily realized under fluidized state is greater than 0.98.
When using present system, first by SCR denitration active material (V
2o
5, WO
3, MoO
3deng) be coated in the upper obtained catalyst granules of catalyst carrier (ceramic particle), then catalyst granules is deposited on the air distribution plate of reative cell, forms catalyst granules bed; Stove back-end ductwork exiting flue gas and ammonia pass into mixing chamber after Homogeneous phase mixing through smoke inlet and ammonia-spraying grid respectively in flue, flue gas in mixing chamber/ammonia gas mixture body blows particle when sending the bed entering and piled up by catalyst granules forth at a high speed by air distribution plate and upwards does turbulent motion, form " fluidisation " phenomenon, in fluid mapper process, flue gas/ammonia gas mixture body and catalyst granules fully contact and chemical reaction occurs complete denitrating flue gas process.The catalyst granules moved upward is under self gravitation effect, will stop moving upward after mixed air-flow brings to certain altitude falls after rise on air distribution plate gradually, still contact with mixed airflow in falling process, still can realize the generation that catalysis promotes denitration chemical reaction.The particle fallen after rise to a certain height again can be driven by the air-flow upwards flowed again and move upward, and moves to a certain height again because self gravitation effect moves downward, so constantly circulates up and down and seethe, complete the catalysis of catalyst granules.Complete the exhanst gas outlet of the reacted flue gas of denitration chemistry through reative cell top to flow out, so far complete denitrating flue gas process.
After running present system a period of time, catalyst granules on air distribution plate because of the factors such as particle in fluid mapper process and intergranular friction, collision cause that its surface active ingredient runs off, activity decrease be not enough to satisfied normal chemical reaction require time, go out the catalyst particles of activity decrease by particle scavenge port quick drain, supplement mouth by particle simultaneously and supplement highly active fresh catalyst particles in time.
In present system running, when stove load condition, fuel quality etc. change cause exhaust gas volumn to change time, by opening particle scavenge port on reative cell sidewall fast or particle supplements mouth to regulate the accumulating amount of catalyst granules on air distribution plate to adapt to the change of exhaust gas volumn.Such as, the exhanst gas outlet 5 of reative cell is provided with flue gas NOx checkout gear 15, the data feedback that described flue gas NOx checkout gear 15 records is to adjusting device, thus mouth 11 is supplemented to particle scavenge port 10 or particle regulate, the quantity of catalyst granules 6 then can be regulated according to the Real-Time Monitoring result of flue gas NOx checkout gear 15, convenient to operation.
The real-time, tunable of catalyst amount is equivalent to the catalysis area that have adjusted catalyst in running in real time, is the important breakthrough of active service catalyst technology.Can regulating in real time of catalyst amount makes the change adaptability of present system to stove load condition and fuel quality wider.
The present invention passes through Ceramics particle as catalyst carrier, specific area significantly improves, simultaneously by spaced set blast cap, blast cap neck is the blast cap aperture that arranges of circumference evenly, impels flue gas/ammonia gas mixture body evenly to send forth and enters reative cell, the indoor catalyst granules of realization response even fluidizing, make the contact of flue gas/ammonia gas mixture body and catalyst granules with mix more abundant, catalyst catalytic performance is better, and denitration efficiency is higher, and in flue gas, NOx removal efficiency is higher.Under the condition not adopting other added technique measure, the denitration efficiency of present system can reach more than 99%, compared with current active service tradition SCR denitration system, has effectively administered more NOx.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (9)
1. a fluidization gas furnace kiln flue gas SCR denitration system, is characterized in that, comprises reative cell, is positioned at mixing chamber below reative cell;
Be provided with air distribution plate between described reative cell and described mixing chamber, described air distribution plate comprises card and is arranged on the some blast caps on card, and the form arrangement of equilateral triangle pressed by adjacent blast cap, and the length of side of described equilateral triangle is 1.3 ~ 1.7 times of blast cap diameter;
Blast cap is the warhead shape object that hemisphere face is combined with cylinder, and upper end hemisphere face is closed, and lower end cylinder arranges through hole and inserts in the jack on card, and described through hole bottom communicates with mixing chamber; The neck of blast cap is provided with blast cap aperture, and the axis of blast cap aperture and the angle of level cross-sectionn are 5 ° ~ 15 °;
Described air distribution plate upper surface is furnished with catalyst granules, the ceramic particle of the carrier of described catalyst granules to be particle diameter be 0.1 ~ 5mm, and the applicator on carrier is SCR denitration active material; Described SCR denitration active material comprises V
2o
5, WO
3, MoO
3;
The piling height of catalyst granules is 2-6 times of described blast cap height, and the voidage of the catalyst granules in fluidized state in reative cell is greater than 0.98.
2. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 1, it is characterized in that, described reative cell sidewall is provided with particle and supplements mouth, the vertical range that described particle supplements mouth and air distribution plate is 100 ~ 500mm.
3. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 2, is characterized in that, the angle of axis and level cross-sectionn that described particle supplements mouth is 30 ° ~ 60 °.
4. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 1, it is characterized in that, described reative cell sidewall is provided with particle scavenge port, described particle scavenge port is positioned at air distribution plate sustained height, and the axis of described particle scavenge port and the angle of level cross-sectionn are 30 ° ~ 60 °.
5. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to any one of Claims 1-4, it is characterized in that, the exhanst gas outlet of described reative cell is provided with flue gas NOx checkout gear.
6. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 1, is characterized in that, also comprise smoke inlet pipeline in mixing chamber front end, be provided with ammonia-spraying grid in described smoke inlet pipeline; Described ammonia-spraying grid is made up of ammonia mother pipe and several points of gamete pipes, and a point gamete tube side-by-side is connected on ammonia mother pipe, and every root divides on gamete pipe and is respectively arranged with flow control valve and several nozzle.
7. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 6, it is characterized in that, described smoke inlet install pipeline has booster fan.
8. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 1, is characterized in that, the little hole number of the blast cap on single blast cap is 4-8.
9. a kind of fluidization gas furnace kiln flue gas SCR denitration system according to claim 1, it is characterized in that, the quantity that particle scavenge port and particle supplement mouth is 4 ~ 10.
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| CN106669419A (en) * | 2015-11-11 | 2017-05-17 | 中国石油化工股份有限公司 | Denitration method for FCC (Fluid Catalytic Cracking) device regenerated fume |
| CN109351149B (en) * | 2018-12-11 | 2023-08-22 | 青岛双瑞海洋环境工程股份有限公司 | Ship exhaust gas desulfurization and denitrification system |
| CN113441188A (en) * | 2021-06-11 | 2021-09-28 | 中科合成油技术有限公司 | Pre-sulfurization method of inferior and/or heavy oil slurry bed hydrogenation iron-based catalyst |
| CN113797751A (en) * | 2021-10-28 | 2021-12-17 | 上海大学 | Regulation and control catalyst self-transfer strengthened low-temperature flue gas NH3-SCR denitration method and device |
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| CN102614779B (en) * | 2012-04-28 | 2013-09-11 | 湖南大学 | Dedusting-denitrating integrated device |
| CN202909626U (en) * | 2012-11-05 | 2013-05-01 | 航天环境工程有限公司 | Catalytic fluidized bed flue gas denitration reaction device |
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