CN103768937B - The dust-proof Benitration reactor of a kind of FCC regenerated flue gas - Google Patents
The dust-proof Benitration reactor of a kind of FCC regenerated flue gas Download PDFInfo
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- CN103768937B CN103768937B CN201210408264.1A CN201210408264A CN103768937B CN 103768937 B CN103768937 B CN 103768937B CN 201210408264 A CN201210408264 A CN 201210408264A CN 103768937 B CN103768937 B CN 103768937B
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Abstract
The present invention relates to the dust-proof Benitration reactor of a kind of FCC regenerated flue gas, described dust-proof Benitration reactor comprises mixed flue gas air inlet section, denitration section and purifying smoke exhaust section, denitration section is provided with denitration unit, wherein: ash disposal section is set between mixed flue gas air inlet section and denitration section, in ash disposal section, dust block board is set, arrange ash silo in denitration section, the center line of ash silo overlaps with the center line of reactor, and the lower end of ash silo connects removing ash pipeline.Benitration reactor of the present invention by arranging dust block board in reactor, make mixed flue gas enter denitration unit before just effectively remove flue dust in mixed flue gas, prevent the catalyst duct in flue dust blocking denitration unit, improve denitration efficiency and denitration effect, by arranging drainage grid and flow straightening grid, the laminar flow state making the flue gas in Benitration reactor keep stable, improves denitration efficiency further.
Description
Technical field
The present invention relates to the controlling device of refinery FCC regenerated flue gas, particularly relate to refinery FCC regenerated flue gas SCR SCR denitration process unit.
Background technology
The whole world enters the NO of air every year
xtotal amount about reaches 5,000 ten thousand tons, 2008, China NO
xdischarge capacity has reached 2,000 ten thousand tons, becomes the first in the world large discharge state.Control if do not take measures, expect the year two thousand twenty, NO
xdischarge capacity will reach 3,000 ten thousand tons, and China the Eleventh Five-Year Plan period cuts down the effort of sulfur dioxide 10%, also will because of NO
xthe remarkable rising of discharge capacity and all offsetting.At present, China is by NO
x" 12 " period overall control category is included in as the binding indicator.Be discharged into the NO in air
xmainly contain three sources: power plant's (accounting for 46%), vehicle exhaust (accounting for 49%) and oil-refining chemical factory (accounting for 5%).
In FCC technique, catalyst granules is repeatedly cycling between catalytic cracking reaction zone and catalyst regeneration zones, and at regeneration period, the coke from cracking reaction on catalyst granules is at high temperature removed by air oxidation, make the activity recovery of catalyst, and again utilize in cracking reaction.NO in FCC flue gas
xmainly from the burning of coke nitrogenous on catalyst, therefore all can there is NO in the FCC apparatus of all process nitrogen-containing materials
xemission problem.NO in FCC flue gas
xmeasure general Zhan Quan factory NO
x50% of discharge capacity is the maximum NO of oil plant
xemission source.In FCC raw material, nitrogen content is generally 0.05% ~ 0.35%, and in raw material nitrogen, about 45% enters fluid product, and about 10% enters gas products, and all the other enter in coke.Nitrogen in coke about has 10% ~ 30% to enter flue gas as NO, and all the other are then reduced to N by coke and CO
2discharge.
Current gas denitrifying technology mainly contains: the SCR method (selective catalytic reduction) of gas-phase reaction and SNCR method (SNCR method), liquid absorption method, solid absorption method, high energy electron active oxidation method etc.
SCR method is under catalyst action, utilize reducing agent optionally with the NO in flue gas
xreaction, generates the N of nonhazardous effect
2and H
2the technology of O, its reducing agent can be ammonia, ammoniacal liquor or urea, also can select CO or H
2, also can select Small molecular alkane.SCR technology, compared with other technologies, has denitration efficiency high, the advantages such as thermal discharge is little, technology maturation, is to apply maximum technology in current Flue Gas Denitrification Engineering both at home and abroad.
SNCR method is under the effect not having catalyst, and in the burner hearths of 900 ~ 1100 DEG C, spray into reducing agent (generally using ammonia, ammoniacal liquor or urea), the rapid pyrolysis of reducing agent is NH
3, with the NO in flue gas
xreaction generates N
2and H
2o, has certain O in burner hearth
2exist, the reducing agent sprayed into optionally with NO
xreaction, substantially not with O
2reaction.If FCC apparatus is equipped with CO boiler, SNCR can directly apply.Upstream ammonia being expelled to CO boiler makes NH
3with NO
xreact in CO boiler.NO in this method
xthe scope of removing is limited in 40 ~ 60%.It is worth noting, if the SO in FCC tail gas
xcontaining causing ammonium sulfate precipitation in CO boiler by height.
CN201524525U describes a kind of SCR equipment for denitrifying flue gas, it comprises catalytic reactor, ammonia/air mixer, ammonia injection barrier, air preheater, wherein one end of catalytic reactor is connect by economizer and boiler tube, the other end is connect by air preheater and dedusting organ pipe, one entrance and the dilution air pipe of described ammonia/air mixer connect, and another entry sequence pipe of described ammonia/air mixer is connected to ammonia dashpot, ammonia evaporator, liquefied ammonia storage tank.The weak point of this structure is, inside reactor smoke distribution is uneven, affects denitration efficiency, and produces the escaping of ammonia; Meanwhile, catalytic reactor is placed in boiler exterior, and floor space is large, and equipment investment is high.
CN201454505U describes a kind of SCR denitration reactor, and the flue gas after dedusting, desulfurization fully mixes with ammonia at gas approach place, then enters in Benitration reactor shell via reactor inlet, and mist passes through beds, NO
xwith NH
3react under catalyst action, reach the object of denitration.The weak point of this structure is, flue gas just directly enters reactor without buffering, causes smoke distribution in reactor uneven, affects denitration efficiency, and produce the escaping of ammonia.
Summary of the invention
Not enough for prior art, the invention provides a kind of flue gas denitration reactor, be intended to solve inside reactor smoke distribution in prior art uneven, affect denitration efficiency, and produce the problem of the escaping of ammonia.
The invention provides the dust-proof Benitration reactor of a kind of FCC regenerated flue gas, described dust-proof Benitration reactor comprises mixed flue gas air inlet section, denitration section and purifying smoke exhaust section, described denitration section is provided with denitration unit, and denitration unit comprises hanging beam, steam sootblower, catalyst module and catalyst support beam; Wherein: between mixed flue gas air inlet section and denitration section, arrange ash disposal section, in ash disposal section, arrange dust block board, arrange ash silo in denitration section, the center line of ash silo overlaps with the center line of reactor, and the lower end of ash silo connects removing ash pipeline.
According to dust-proof Benitration reactor of the present invention, described dust block board is the sloping baffle of multi-layer intercrossed layout, baffle plate is inner near ash silo one end, opposite side is outer end, the outer end of baffle plate is higher than the inner, the inner of baffle plate is saw-tooth-type structures, and each layer baffle plate, along wall of reactor to center position, highly successively reduces.The lowermost layer baffle plate of described dust block board is connected with the upper end of ash silo, and the superiors' baffle plate of described dust block board is connected with ash disposal section inner wall sealing.Described dust block board is except the superiors' baffle plate, and all the other baffle plate outer ends can be sawtooth pattern.Every layer of baffle plate of described dust block board can be formed by one piece of baffle plate or be made up of some pieces of baffle plates, can have certain interval between baffle plate.Mixed flue gas passage is provided with between the adjacent two layers baffle plate of described dust block board.
According to dust-proof Benitration reactor of the present invention, arrange one or more denitration unit in described denitration section, described two or more denitration unit are uniformly distributed, by ash silo is separated on reactor water plane section.
According to dust-proof Benitration reactor of the present invention, described baffle plate the inner is zigzag structure, and the area that flows through of baffle plate porch flue gas is increased, and mixed flue gas gas prompt drop is low, and the ability of carrying dust reduces, and dust cannot carry and be trapped on baffle plate by mixed flue gas; On the other hand, baffle plate the inner is set to zigzag structure, also has certain flow-disturbing effect to mixed flue gas, promotes that flue dust is separated with mixed flue gas further.Adjacent two layers baffle plate is staggered, the inner of lower floor's baffle plate and outer end respectively compared with the inner of upper strata baffle plate and outer end closer to reactor center line, there is the region that partly overlaps in the projection of adjacent two layers baffle plate, mixed flue gas can be made on dust block board to produce baffling, be conducive to removing the flue dust in flue gas, and can prevent flue dust from directly dropping on catalyst module without lower one deck baffle plate falls into ash silo.Described each layer baffle plate successively reduces along wall of reactor to center position and is obliquely installed in ash disposal section, and the angle of inclination of baffle plate is arranged according to the angle of repose of flue dust, and inclination angle scope is 5 ° ~ 45 °, preferably 10 ° ~ 25 °.
According to dust-proof Benitration reactor of the present invention, be provided with ash silo in described denitration section, for collecting the dust in mixed flue gas, ash silo lower end is connected with removing ash pipeline, arranges ash discharge frequency according to the dustiness of flue gas; Removing ash pipeline is in tilted layout, and arranges the inclination angle of removing ash pipeline according to the angle of repose of flue dust, and inclination angle scope is 5 ° ~ 45 °, preferably 10 ° ~ 25 °.
According to dust-proof Benitration reactor of the present invention, preferably drainage grid is set between ash disposal section and denitration unit, flow straightening grid is set between denitration unit and purifying smoke exhaust section.By arranging drainage grid and flow straightening grid, can make to keep stable laminar flow state by the mixed flue gas in whole denitration unit, ensureing denitration efficiency and preventing the escaping of ammonia, simultaneously, can ensure that flue gas flows vertically through catalyst duct, reduce system pressure drop, prevent from causing damage to catalyst.Described flow straightening grid and drainage grid can adopt structure well known to those skilled in the art.
According to Benitration reactor of the present invention, described Benitration reactor is reducing reactor, and wherein said ash disposal section adopts expanding structure, can increase reactor inlet sectional area on the one hand, reduces flue gas flow rate, and promotion mixed flue gas is separated with flue dust; The sectional area of denitration unit can be increased on the other hand, when same catalyst consumption, reduce boiler height, economy system construction investment.Described purifying smoke exhaust section adopts undergauge structure, ensures that reactor gateway cross-sectional sizes is consistent, is convenient to form integral structure with CO boiler.
According to Benitration reactor of the present invention, described reactor can also comprise spray ammonia element, and described spray ammonia element can be arranged at mixed flue gas entrance, and described spray ammonia element can adopt structure well known to those skilled in the art.
Compared with prior art, Benitration reactor tool of the present invention has the following advantages:
(1) dust-proof Benitration reactor of the present invention is by arranging zigzag structure baffle plate, and the area that flows through of baffle plate porch flue gas is increased, and mixed flue gas gas prompt drop is low, and the ability of carrying dust reduces, and dust cannot carry and be trapped on baffle plate by mixed flue gas; On the other hand, baffle plate the inner is set to zigzag structure, flow-disturbing effect is to a certain degree had to mixed flue gas, further promotion flue dust is separated with mixed flue gas, just effectively can remove the flue dust in mixed flue gas, prevented the catalyst duct in flue dust blocking denitration unit before mixed flue gas enters denitration unit, improve denitration efficiency and denitration effect, meanwhile, can reduce and blow grey frequency, improve plant running stability.
(2) in dust-proof Benitration reactor of the present invention, drainage grid is set between ash disposal section and denitration unit, between denitration unit and purifying smoke exhaust section, flow straightening grid is set, can ensure that the mixed flue gas in whole Benitration reactor keeps stable laminar flow state, ensure denitration efficiency and prevent the escaping of ammonia, meanwhile, can ensure that flue gas flows vertically through catalyst duct, reduce system pressure drop, prevent from causing damage to catalyst.
(3) dust-proof Benitration reactor of the present invention is reducing reactor, and wherein said ash disposal section adopts expanding structure, can increase reactor inlet sectional area on the one hand, reduces flue gas flow rate, and promotion mixed flue gas is separated with flue dust; The sectional area of denitration unit can be increased on the other hand, when same catalyst consumption, reduce boiler height, economy system construction investment.Described ash discharge section adopts undergauge structure, ensures that reactor gateway cross-sectional sizes is consistent, is convenient to form integral structure with CO boiler.
Accompanying drawing explanation
Fig. 1 is the structural representation of the dust-proof Benitration reactor of the present invention.
Fig. 2 is the present invention's dust-proof Benitration reactor dust block board operating diagram.
Fig. 3 is the present invention's dust-proof Benitration reactor dust block board structural representation.
Detailed description of the invention
Concrete scheme of the present invention and occupation mode is further illustrated below in conjunction with accompanying drawing.
As shown in Figure 1, the invention provides the dust-proof Benitration reactor of a kind of FCC regenerated flue gas, described reactor comprises mixed flue gas air inlet section 1, denitration section 3 and purifying smoke exhaust section 4, wherein, denitration unit 6 is provided with in denitration section 3, denitration unit 6 is disposed with hanging beam 9 from top to bottom, soot blower 10, catalyst module 11 and catalyst support beam 12, described Benitration reactor arranges ash disposal section 2 between mixed flue gas air inlet section 1 and denitration section 3, dust block board 5 is set in ash disposal section 2, ash silo 7 is set in denitration section 3, the center line of ash silo overlaps with the center line of reactor, the lower end of ash silo 7 connects removing ash pipeline 8.Described dust block board 5 is the sloping baffle of multi-layer intercrossed layout, and the outer end of baffle plate is higher than the inner, and inclination angle scope is arranged according to the angle of repose of flue dust, and inclination angle ranges preferably from 10 ° ~ 25 °.The inner of baffle plate is sawtooth pattern, and from wall of reactor to center position, the height of baffle plate successively reduces.The lowermost layer baffle plate of described dust block board 5 is connected with the upper end of ash silo 7, and the superiors' baffle plate of described dust block board 5 is connected with ash disposal section 2 inner wall sealing.The multi-layer intercrossed arrangement of described dust block board, leaves mixed flue gas passage between adjacent two layers baffle plate 5.The lower end of ash silo 7 is connected with removing ash pipeline 8, and removing ash pipeline 8 is in tilted layout, and arranges the inclination angle of removing ash pipeline according to the angle of repose of flue dust, and inclination angle ranges preferably from 10 ° ~ 25 °.Drainage grid 13 is set between below ash disposal section 2 and above denitration unit 6 and flow straightening grid 14 is set below denitration unit 6 and between purifying smoke exhaust section 4.In mixed flue gas air inlet section, spray ammonia element can also be set.
As shown in Figure 1, catalyst module 11 in use, by the hanging beam 9 arranged in Benitration reactor, hangs in Benitration reactor, and is placed on catalyst support beam 12, complete the installation of catalyst module 11 by Benitration reactor of the present invention.Mixed flue gas evenly flow into ash disposal section 2 from mixed flue gas air inlet section 1, described ash disposal section 2 adopts expanding structure, add reactor inlet sectional area, reduce flue gas flow rate, mixed flue gas is through being obliquely installed the zigzag structure baffle plate in ash disposal section 2, adjacent two layers baffle plate is staggered, the inner of lower floor's baffle plate and outer end respectively compared with the inner of upper strata baffle plate and outer end closer to reactor center line, there is the region that partly overlaps in the projection of adjacent two layers baffle plate, described each layer baffle plate the inner is zigzag structure, the area that flows through of baffle plate porch flue gas is increased, mixed flue gas gas prompt drop is low, the ability of carrying dust reduces, dust cannot carry and be trapped on baffle plate by mixed flue gas, and zigzag structure baffle plate has certain flow-disturbing effect to mixed flue gas, further promotion flue dust is separated with mixed flue gas, flue dust impinges upon on baffle plate, and successively fall into ash silo 7 along baffle plate under gravity, reach the object of dedusting, mixed flue gas produces baffling on dust block board 5, flue gas flow direction enters denitration unit 6 by the mixed flue gas passage between adjacent two layers baffle plate after there is continuous reverse deviation after drainage grid 13 drainage, beds 11 in denitration unit 6 carries out denitration process, removing NO
x, purifying smoke after denitration process is again after flow straightening grid 14 rectification, flow out denitration unit 6, the purifying smoke flowed out in two denitration unit, again the merga pass purifying smoke exhaust section 4 that converges discharges Benitration reactor, according to the dustiness in flue gas, in the setting ash discharge cycle, by the removing ash pipeline 8 tilted, the flue dust of ash silo 7 inner accumulated is discharged Benitration reactor.
Claims (12)
1. the dust-proof Benitration reactor of FCC regenerated flue gas, described dust-proof Benitration reactor comprises mixed flue gas air inlet section, denitration section and purifying smoke exhaust section, wherein said denitration section is provided with denitration unit, and denitration unit comprises hanging beam, soot blower, catalyst module and catalyst support beam, it is characterized in that: ash disposal section is set between mixed flue gas air inlet section and denitration section, in ash disposal section, dust block board is set, in denitration section, ash silo is set, the center line of ash silo overlaps with the center line of reactor, the lower end of ash silo connects removing ash pipeline, described dust block board is the sloping baffle of multi-layer intercrossed layout, the inner of lower floor's baffle plate and outer end respectively compared with the inner of upper strata baffle plate and outer end closer to reactor center line, there is the region that partly overlaps in the projection of adjacent two layers baffle plate, the outer end of baffle plate is higher than the inner, the inner of baffle plate is saw-tooth-type structures, from wall of reactor to the direction at center, the height of baffle plate successively reduces.
2. according to reactor according to claim 1, it is characterized in that, the lowermost layer baffle plate of described dust block board is connected with the upper end of ash silo, and the superiors' baffle plate of described dust block board is connected with ash disposal section inner wall sealing.
3. according to reactor according to claim 1, it is characterized in that: described dust block board all the other baffle plate outer ends except the superiors' baffle plate are sawtooth pattern.
4. according to reactor according to claim 1, it is characterized in that: every layer of baffle plate of described dust block board is made up of one piece of baffle plate.
5. according to reactor according to claim 1, it is characterized in that: every layer of baffle plate of described dust block board is made up of some pieces of baffle plates, has certain interval between baffle plate.
6. according to reactor according to claim 1, it is characterized in that: between the adjacent two layers baffle plate of described dust block board, be provided with mixed flue gas passage.
7. according to reactor according to claim 1, it is characterized in that: described dust block board inclination angle scope is 5 ° ~ 45 °.
8. according to reactor according to claim 1, it is characterized in that: described removing ash pipeline is obliquely installed, inclination angle scope is 5 ° ~ 45 °.
9. according to reactor according to claim 1, it is characterized in that, arrange one or more denitration unit in described denitration section, described plural denitration unit is uniformly distributed, by ash silo is separated on reactor water plane section.
10. according to reactor according to claim 1, it is characterized in that: between described ash disposal section and denitration unit, be provided with drainage grid, between described denitration unit and purifying smoke exhaust section, be provided with flow straightening grid.
11., according to reactor according to claim 1, is characterized in that: described Benitration reactor is reducing reactor, and described ash disposal section adopts expanding structure, and described purifying smoke exhaust section adopts undergauge structure.
12., according to reactor according to claim 1, is characterized in that: described Benitration reactor also comprises spray ammonia element, is arranged at ash disposal section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210408264.1A CN103768937B (en) | 2012-10-24 | 2012-10-24 | The dust-proof Benitration reactor of a kind of FCC regenerated flue gas |
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|---|---|---|---|
| CN201210408264.1A CN103768937B (en) | 2012-10-24 | 2012-10-24 | The dust-proof Benitration reactor of a kind of FCC regenerated flue gas |
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| CN103768937B true CN103768937B (en) | 2015-08-12 |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105833643B (en) * | 2016-04-28 | 2018-03-06 | 中国计量大学 | A kind of puffed rice ash collection system in coal-fired boiler tail gas |
| CN108310972B (en) * | 2018-03-21 | 2023-01-31 | 中冶京诚工程技术有限公司 | Multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof |
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| CN1895744A (en) * | 2006-06-26 | 2007-01-17 | 马春强 | Dusted composite SCR smoke denitration and its denitrating catalytic reactor |
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| CN102179156A (en) * | 2011-05-06 | 2011-09-14 | 东南大学 | Smoke denitration device for preventing catalyst from being plugged by popcorn ash |
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Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52148470A (en) * | 1976-06-04 | 1977-12-09 | Kawasaki Heavy Ind Ltd | Apparatus for dust collection and denitration |
-
2012
- 2012-10-24 CN CN201210408264.1A patent/CN103768937B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2274094Y (en) * | 1996-01-16 | 1998-02-11 | 陶以成 | Smoke isolation purifier |
| CN1895744A (en) * | 2006-06-26 | 2007-01-17 | 马春强 | Dusted composite SCR smoke denitration and its denitrating catalytic reactor |
| CN201676639U (en) * | 2010-05-11 | 2010-12-22 | 浙江蓝天求是环保集团有限公司 | Ammonia gas injection device for fire coal flue gas SCR denitration technology |
| CN201791476U (en) * | 2010-05-21 | 2011-04-13 | 中国神华能源股份有限公司 | Flue gas denitration device |
| CN102179156A (en) * | 2011-05-06 | 2011-09-14 | 东南大学 | Smoke denitration device for preventing catalyst from being plugged by popcorn ash |
| CN102688629A (en) * | 2012-06-04 | 2012-09-26 | 东方电气集团东方锅炉股份有限公司 | SCR (selective catalytic reduction) denitration dedusting device |
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