CN103776013B - There is the CO boiler of dusting function - Google Patents

There is the CO boiler of dusting function Download PDF

Info

Publication number
CN103776013B
CN103776013B CN201210408167.2A CN201210408167A CN103776013B CN 103776013 B CN103776013 B CN 103776013B CN 201210408167 A CN201210408167 A CN 201210408167A CN 103776013 B CN103776013 B CN 103776013B
Authority
CN
China
Prior art keywords
flue
boiler
ammonia
block board
plate
Prior art date
Application number
CN201210408167.2A
Other languages
Chinese (zh)
Other versions
CN103776013A (en
Inventor
彭德强
王岩
陈新
姜阳
刘志禹
李欣
王明星
Original Assignee
中国石油化工股份有限公司
中国石油化工股份有限公司抚顺石油化工研究院
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 中国石油化工股份有限公司, 中国石油化工股份有限公司抚顺石油化工研究院 filed Critical 中国石油化工股份有限公司
Priority to CN201210408167.2A priority Critical patent/CN103776013B/en
Publication of CN103776013A publication Critical patent/CN103776013A/en
Application granted granted Critical
Publication of CN103776013B publication Critical patent/CN103776013B/en

Links

Abstract

The invention discloses a kind of CO boiler with dusting function.Described CO boiler comprises the first vertical flue, horizontal flue and the second vertical flue, first vertical flue is provided with combustion chamber, combustion chamber is provided with dust block board, in combustion chamber, the walling of flue arranged outside in contiguous second vertical flue direction has the ash-storing bin of external hanging type, the first vertical flue has ash discharging hole and communicates with ash-storing bin; Described dust block board is the baffle arrangement of multi-layer intercrossed layout, and dust block board is obliquely installed, and its outer end is higher than the inner.The dust block board arranged in CO boiler of the present invention, can remove most of flue dust contained in flue gas, can solve the equipment erosion problem because flue dust causes to greatest extent, optimizes flue gas treating process, reduces energy consumption, and investment reduction.

Description

There is the CO boiler of dusting function

Technical field

The present invention relates to a kind of CO waste heat boiler of oil plant catalytic cracking (FCC) regenerated flue gas, particularly a kind of CO boiler with ash disposal and denitration function.

Background technology

Nitrogen oxide (NOx) is one of primary pollution source of atmosphere pollution.Nitrogen oxide comprises multiple compounds as nitrous oxide (N 2o), nitric oxide (NO), nitrogen dioxide (NO 2), nitrogen trioxide (N 2o 3), dinitrogen tetroxide (N 2o 4) and dinitrogen pentoxide (N 2o 5) etc.Except nitrogen dioxide, the equal extremely unstable of other nitrogen oxide, meet light, wet or thermal change becomes nitrogen dioxide and nitric oxide, nitric oxide becomes nitrogen dioxide again.Therefore, what contact in occupational environment is that several admixture of gas is often called the smoke of gunpowder (gas), is mainly nitric oxide and nitrogen dioxide, and based on nitrogen dioxide.NOx has toxicity in various degree, is the major reason forming photochemical fog and acid rain based on the NOx of nitric oxide and nitrogen dioxide.NOx in vehicle exhaust and hydrocarbon to react the toxic smog formed through Ultraviolet radiation, are called photochemical fog.In addition, the water in NOx and air reacts the composition that the nitric acid that generates and nitrous acid are acid rain.The harm of NOx to human body is mainly manifested in infringement respiratory tract.

The NOx be discharged in air mainly contains three sources: power plant's (accounting for 46%), vehicle exhaust (accounting for 49%) and oil-refining chemical factory (accounting for 5%).Oil plant is one of main nitrogen oxide (NOx) emission source.50% of NOx amount in FCC flue gas general Zhan Quan factory NOx discharge is the maximum NOx emission source of oil plant.Current FCC gas denitrifying technology mainly comprises: the selective catalytic reduction (SCR method) of gas-phase reaction and SNCR method (SNCR method), liquid absorption method, solid absorption method and high energy electron active oxidation method etc.

Selective catalytic reduction (SCR method) is under catalyst action, utilizes reducing agent selectively to react with the NOx in flue gas, and 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, react with the NOx in flue gas and generate nitrogen and water, in burner hearth, have certain oxygen to exist, the reducing agent sprayed into optionally with NOx, substantially not with oxygen reaction.If FCC apparatus is equipped with CO boiler, SNCR can directly apply.Upstream ammonia being expelled to CO boiler makes NH 3react in CO boiler with NOx.NOx in this method removes scope and is limited in 40-60%.The SOx content height in FCC tail gas it is worth noting, if can cause ammonium sulfate precipitation in CO boiler.NSCR refers to that NOx in source of the gas is under uniform temperature and catalyst action, is reduced agent and is reduced to N 2, simultaneously reducing agent also with the O in source of the gas 2reaction generates H 2o and CO 2, in this denitrification process, reaction need by means of the catalytic action of catalyst, and reducing agent and NOx and O 2all react, non-selectivity, therefore be called non-selective catalytic reduction.

1986, the SCR device that first set is applied on FCC flue gas in the world put into operation.By 2005, have nearly 20 cover SCR device abroad for the treatment of the NOx in FCC flue gas, domestic also do not have commercial Application at present.In the 20 cover SCR method FCC equipment for denitrifying flue gas applied, 1 cover has run 16 years, and 9 covers have run 10 years, and catalyst the longest service life is 12 years.Reactor all adopts and falls flow operation, the height of NOx clearance as requested, adopts single or many operations.

CN1895744A discloses a kind of high dirt composite SCR smoke denitrating technique and denitration catalyst reaction unit, and ammonia nitrogen gaseous mixture enters hydrogen-catalyst reactor top air chamber through deflector, then enters in catalyst layer downwards and be reduced into N 2and H 2o, the flue gas after denitration, by heat exchange, dedusting and desulfurization, is finally discharged from chimney, in the ash bucket that the dust being adsorbed on catalyst surface falls into bottom hydrogen-catalyst reactor in the effect of dust arrester, the row for the treatment of.The weak point of this structure is, meeting blocking catalyst duct, employing is oppositely blown ash and the dust in duct can not be blown off completely.Meanwhile, when catalyst strength is not enough, broken catalyst can block Benitration reactor, causes flue gas to circulate not smooth, and then affects upstream and downstream unit normal run.

CN201454505U discloses 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, when processing high cloud of dust gas, soot blower can only clear up the dust stratification on beds surface, and flue gas just directly enters reactor without buffering, and the dust meeting blocking catalyst duct contained in flue gas, has a strong impact on denitration efficiency.Meanwhile, when catalyst strength is not enough, broken catalyst can block Benitration reactor, causes flue gas to circulate not smooth, and then affects upstream and downstream unit normal run.

Summary of the invention

The technical problem to be solved in the present invention is to provide a kind of CO boiler with dusting function, to be intended to solve in prior art smoke content in CO boiler smoke too high and cause heat-obtaining section efficiency to reduce and the problem of equipment corrosion.

The invention provides a kind of CO boiler with dusting function, described CO boiler comprises flue, combustion chamber, steam drum, evaporator section and economizer section, described flue comprises the first vertical flue, horizontal flue and the second vertical flue, combustion chamber is provided with in the first vertical flue, steam drum is provided with in horizontal flue, evaporator section and economizer section is provided with in second vertical flue, it is characterized in that, dust block board is provided with in described combustion chamber, in combustion chamber, the walling of flue arranged outside in contiguous second vertical flue direction has the ash-storing bin of external hanging type, first vertical flue has ash discharging hole communicate with ash-storing bin, described dust block board is the baffle arrangement of multi-layer intercrossed layout, and dust block board is obliquely installed, and its outer end is higher than the inner.

Of the present invention have in the CO boiler of dusting function, described dust block board is the sloping baffle of multi-layer intercrossed layout, baffle plate is inner near ash-storing bin one end, opposite side is outer end, the outer end of baffle plate is higher than the inner, except orlop baffle plate, the inner of all the other baffle plates is sawtooth pattern, successively reduces along the first vertical walling of flue to ash-storing bin direction height.The lowermost layer baffle plate of described dust block board is inner to be connected with edge under ash discharging hole, and the superiors' baffle plate of described dust block board and the first vertical walling of flue are tightly connected.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 combination, can have certain interval or gapless between some pieces of baffle plates.Mixed flue gas passage is provided with between adjacent two layers baffle plate.

Of the present invention have in the CO boiler of dusting function, and described baffle plate the inner is zigzag, and the relative circulation area of baffle plate entrance is increased, and the gas prompt drop of flue gas is low, and dust cannot be carried by flue gas and be trapped on baffle plate; On the other hand, baffle plate is set to zigzag, has pointed structures, has certain flow-disturbing effect to mixed flue gas, can promote that flue dust is separated with mixed flue gas further.Adjacent two layers baffle plate is staggered, there is certain overlapping region, makes flue gas produce baffling on dust block board, is conducive to removing the flue dust in flue gas, and can prevent flue dust to fall back the first vertical flue without lower one deck baffle plate, affects ash disposal efficiency.Described baffle plate successively reduces along the first vertical walling of flue to ash-storing bin direction, is obliquely installed in the turning junction of the first vertical flue and horizontal flue.Baffle plate outer end is higher than the inner, and angle of inclination is arranged according to the angle of repose of flue dust, and inclination angle scope is generally 5 ° ~ 45 °, preferably 10 ° ~ 25 °.

According to the CO boiler with dusting function of the present invention, ammonia-gas spraying device and Benitration reactor can also be set in the second vertical flue.Described Benitration reactor is arranged between evaporator section and economizer section, forms vertical linearity integral structure with the second vertical flue.Benitration reactor generally includes some denitration unit, and each denitration unit generally includes hanging beam, steam sootblower, catalyst module and catalyst support beam.The principle of CO boiler is first by the CO in burning removing flue gas, then by each heat-obtaining section Mist heat recovering.SCR reaction needed is carried out at about 350 DEG C, also not heat release of neither absorbing heat in course of reaction.Therefore between evaporator section and economizer section, arrange Benitration reactor, the temperature field that can be formed by CO boiler combustion and heat-obtaining, the temperature spot reacted at suitable SCR carries out SCR reaction, the NO in removing flue gas x, do not affect boiler heat-obtaining, and heat be fully used, thus reach energy-conservation object.

Described ammonia-gas spraying device can be arranged at the top of evaporator section, also can be arranged between evaporator section and Benitration reactor, preferably ammonia-gas spraying device is arranged on the top of evaporator section.

Steam drum described in CO boiler of the present invention and evaporator section all adopt structure well known in the art, general employing pipe heat exchanger structure.Because described evaporator section is generally the pipe heat exchanger of multiple row tube bank interlaced arrangement, it is highly generally 3 ~ 5 meters, be provided with some parallel heat exchanger tubes in every tubulation bundle, adopt end to end serpentine configuration to arrange between adjacent heat exchange tubes, heat exchanger tube is finned pipe.Evaporator section generally comprises at least two group heat exchangers, its height of about 8 meters of generally having an appointment along the second vertical flue.Ammonia-gas spraying device is arranged on evaporator section upper inlet place, the finned tube that can make full use of on evaporator section heat exchanger forms turbulent element, utilizes evaporator section about 8 meters of high blending spaces simultaneously, strengthens the mixed effect of ammonia and flue gas.

Of the present invention have in the CO boiler of dusting function, and described ammonia-gas spraying device can adopt structure well known to those skilled in the art, as adopted ammonia-spraying grid, or can adopt blender disclosed in CN201988343U.In CO boiler of the present invention, in order to increase the mixed effect of flue gas and ammonia further, saving the extra space increasing mixed ammonia grid simultaneously, recommending the ammonia-gas spraying device adopting following structure.Described ammonia-gas spraying device comprises spray ammonia house steward, spray ammonia arm and spray ammonia element, and spray ammonia arm arranges some, and spray ammonia arm one end is connected with spray ammonia house steward, and the other end is enclosed construction; Described spray ammonia element comprises nozzle, anemostat and spatter plate, and the lower surface of spray ammonia arm is connected with described spray ammonia element by nozzle.Described anemostat comprises contraction section, trunnion and expansion segment, and jet expansion stretches in anemostat contraction section, spatters the below that plate is arranged at expansion segment.

In CO boiler of the present invention, the outlet of described nozzle lower end preferably adopts undergauge structure.The angle of throat of described anemostat contraction section is generally 10 ° ~ 60 °, preferably 15 ° ~ 30 °.The length of described trunnion is generally 1 ~ 4 times of throat pipe diameter, preferably 1 ~ 3 times.The angle of flare of described expansion segment for being generally 7 ° ~ 30 °, preferably 10 ° ~ 20 °.

In CO boiler of the present invention, described in spatter plate and be at least two-layer, plate is provided with sieve aperture, described in spatter packing free ratio be 10% ~ 60%, preferably 30% ~ 50%.Described plate shape of spattering can be circular, square, rectangle, preferably consistent with outlet, anemostat lower end shape.Described sieve aperture shape can be circle, triangle or square, circular.Describedly spatter the aperture of sieve aperture on plate and be generally 3 ~ 8mm, preferred aperture 4 ~ 6mm, sieve aperture can adopt equilateral triangle to arrange or square arrangement, and adjacent to spatter sieve aperture between plate staggered.Described nozzle, anemostat and spatter the dead in line of plate, spattering the distance that plate and expansion segment export horizontal cross-section can be generally 30% ~ 150% of length of throat, preferably 80% ~ 120%.

Compared with prior art, the CO boiler that the present invention has a dusting function has following characteristics:

1, of the present invention have in the CO boiler of dusting function, and dust block board is arranged in combustion chamber, under the prerequisite not affecting boiler thermal output, realize the collection of flue dust and outer row, prevent flue dust from entering in Benitration reactor and boiler heat-obtaining section, reduce and blow grey frequency, improve boiler thermal output, simultaneously, the dust pelletizing system in follow-up desulfurization process can also be simplified, solve the equipment erosion problem because flue dust causes, optimize flue gas treating process, reduce energy consumption, investment reduction.

2, the CO boiler that the present invention has a dusting function can also comprise ammonia-gas spraying device and Benitration reactor simultaneously, thus becomes the CO boiler with ash disposal and denitration function.Before ammonia-gas spraying device is arranged on evaporator section, the finned tube on evaporator section heat exchanger is utilized to form turbulent element on the one hand; The space of evaporator section about about 8 meters height can be made full use of on the other hand, for flue gas and ammonia provide the larger blending space of longer mixing Distance geometry, strengthen ammonia and flue gas mixture homogeneity, solve the problem that mixing distance short-range missile causes ammonia and flue gas mixed effect difference; Improve the mixed effect of ammonia and flue gas, contribute to equally improving denitration efficiency and preventing the escaping of ammonia.

3, the CO boiler with dusting function of the present invention, Benitration reactor and CO boiler form integral structure, by the finned tube of evaporator section heat exchanger, do not need additionally to arrange mixed ammonia flow straightening grid, namely Benitration reactor inside smoke can be made to be evenly distributed, fluid stable, and ensure that flue gas flows vertically through catalyst duct, prevent from causing damage to catalyst, reduce system pressure drop; Stable laminar flow state can also be provided for economizer section simultaneously, ensure the thermal efficiency of evaporator section and economizer section.

4, the described CO boiler with dusting function, the efficient ammonia-gas spraying device of preferred employing, the wherein said plate that spatters is at least two-layer, ground floor spatters plate sectional area and is greater than expansion segment lower end discharge area, mist is made to form solid-cone range of distribution after spattering plate, and produce larger dispersion territory, increase mist be not inhaled into anemostat flue gas mix probability again, flue gas is mixed more abundant with ammonia, ensure that within the scope of whole reactor cross section, ammonia is uniformly distributed, give full play to catalyst performance, improve denitration efficiency and prevent the escaping of ammonia, reduce the space required for mixing, reduce investment outlay.Described gas jet arms parallel is arranged in flue, and nozzle, along the intensive layout in flue cross section, makes each anemostat suction areas overlap, and ensures being uniformly distributed of gas.By being arranged on the efficient spray ammonia element before Benitration reactor, ensureing being uniformly distributed of ammonia within the scope of whole reactor cross section, giving full play to catalyst performance, ensure denitration efficiency and prevent the escaping of ammonia.

Accompanying drawing explanation

Fig. 1 is the structural representation that the present invention has the CO boiler of dusting function.

Fig. 2 is structure and the operating diagram of dust block board.

Fig. 3 is ammonia-gas spraying device front view of the present invention.

Fig. 4 is spray ammonia element front view of the present invention.

Detailed description of the invention

Concrete scheme and the occupation mode of Benitration reactor of the present invention is further illustrated below in conjunction with accompanying drawing.

As shown in Figure 1, the CO boiler that the present invention has dusting function comprises flue 1, combustion chamber 2, steam drum 3, evaporator section 5, economizer section 7 and dust block board 24, described flue comprises the first vertical flue 8, horizontal flue 9 and the second vertical flue 10, described horizontal flue 9 two ends respectively flue 8 vertical with first are communicated with the top of the second vertical flue 10, combustion chamber 2 is arranged in the first vertical flue 8, steam drum 3 is arranged in horizontal flue 9, and evaporator section 5 and economizer section 7 are arranged in the second vertical flue 10.In the combustion chamber 2 of the first vertical flue 8, be provided with dust block board 24, in combustion chamber 2, the walling of flue arranged outside in contiguous second vertical flue 10 direction has and the vertical flue 8 of ash-storing bin 25, first of external hanging type has ash discharging hole communicates with ash-storing bin 25.Described dust block board 24 is the sloping baffle of multi-layer intercrossed layout, and baffle plate 24 is inner near ash-storing bin 25 one end, and opposite side is outer end, and the outer end of baffle plate 24 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 °.Except orlop baffle plate, the inner of all the other baffle plates is sawtooth pattern, successively reduces along the first vertical walling of flue to ash-storing bin 25 direction height.The lowermost layer baffle plate of described dust block board 24 is inner to be connected with edge under ash discharging hole, and the superiors' baffle plate of described dust block board 24 is connected with the first vertical flue 8 inner wall sealing.Described dust block board 24 is except the superiors' baffle plate, and the outer end of all the other baffle plates is preferably sawtooth pattern.Described dust block board 24, in multi-layer intercrossed arrangement, leaves mixed flue gas passage between adjacent two layers baffle plate.

The present invention has in the CO boiler of dusting function, can also comprise ammonia-gas spraying device 4 and Benitration reactor 6 simultaneously, and described ammonia-gas spraying device 4 is arranged in the second vertical flue 10, and be positioned at above evaporator section 5, Benitration reactor 6 is between evaporator section 5 and economizer section 7.Benitration reactor 6 comprises hanging beam 11, steam sootblower 12, catalyst module 13 and catalyst support beam 14.

In use, the hanging beam 11 first by arranging in Benitration reactor 6, hangs in catalyst module 13 in Benitration reactor 6, is placed on catalyst support beam 14, complete the installation of catalyst module 13 the CO boiler with dusting function provided by the invention.Flue gas is Thorough combustion in combustion chamber 2 first, CO in removing flue gas, flue gas is through the dust block board 24 be inclined in combustion chamber 2, adjacent two layers baffle plate is staggered, there is certain overlapping region, because baffle plate one or both ends are zigzag, make the long-pending increase of dust block board entrance section, relative circulation area increases, mixed flue gas gas prompt drop is low, dust cannot carry and be trapped on baffle plate by mixed flue gas, and saw-tooth shaped baffles 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-storing bin 25 by ash discharging hole along baffle plate under gravity, reach the object of dedusting, mixed flue gas produces baffling on dust block board 24, flue gas flow direction passes through the mixed flue gas passage between adjacent two layers baffle plate after there is continuous reverse deviation after, heat-obtaining is carried out again by the steam drum 3 of CO boiler 1, the ammonia that flue gas after steam drum heat-obtaining and ammonia-gas spraying device 4 spray into mixes, and the finned tube in evaporator section on heat exchanger forms turbulent element, strengthens ammonia and flue gas mixed effect.Described evaporator section has the height of about 8 meters along the second flue on the other hand, and for flue gas and ammonia provide larger blending space, mixed flue-gas temperature, at about 350 DEG C, enters Benitration reactor 6 and carries out reduction reaction removing NO x; Flue gas after denitration process enters economizer section 7 and continues heat-obtaining, after completing net quantity of heat removal process, and can discharging directly into atmosphere or enter desulfurizer.When in flue gas, dust content increases, during blocking catalyst duct, start steam sootblower 12 and carry out blowing ash.

Of the present invention have in the CO boiler of dusting function, the ammonia-spraying grid that ammonia-gas spraying device 4 can adopt this area conventional.The present invention recommends the ammonia-gas spraying device adopting following structure.Described ammonia-gas spraying device 4 comprises spray ammonia house steward 15, spray ammonia arm 16 and spray ammonia element 17, and described spray ammonia arm 16 arranges some, and one end of spray ammonia arm 16 is connected with spray ammonia house steward 15, and the other end is enclosed construction; Described spray ammonia element 17 comprises nozzle 18, anemostat 19 and spatter plate 20, and the lower surface of spray ammonia arm 16 is connected with described spray ammonia element 17 by nozzle 18.Described anemostat 19 comprises contraction section 21, trunnion 22 and expansion segment 23 from top to bottom successively, nozzle 18 lower end outlet stretches in anemostat contraction section 21, described in spatter the below that plate 20 is arranged at expansion segment 23.Wherein, contraction section angle of throat is 15 ° ~ 30 °, the expansion segment angle of flare 10 ° ~ 20 °, and length of throat is 1 ~ 3 times of throat pipe diameter; The described plate 4 that spatters can be three layers, and plate is provided with sieve aperture, ground floor spatters the lower end discharge area that plate sectional area is greater than expansion segment 7, all the other two-layer plate sectional areas that spatter reduce gradually, the described packing free ratio that spatters is 30% ~ 50%, the aperture spattering sieve aperture on plate is 4 ~ 6mm, and adopt equilateral triangle arrangement or square arrangement, adjacent to spatter sieve aperture between plate staggered.

Ammonia-gas spraying device 4 of the present invention in use, ammonia enters spray ammonia arm 16 through spray ammonia house steward 15, anemostat contraction section 21 is sprayed into by the nozzle 18 on spray ammonia arm 10, and accelerate in contraction section 21, form negative pressuren zone, produce swabbing action and suck most of flue gas near contraction section 21 entrance, mist enters anemostat expansion segment 23 through trunnion 22, and slow down in expansion segment 23, realize the first stage mixing of two kinds of gases; Mist is spattering the generation splash of plate 20 place, utilization is spattered plate 20 pairs of simulation model for mixing gases flows and is formed obstruction, mist is made to form solid-cone range of distribution after spattering plate 20, increase mist be not inhaled into anemostat 19 flue gas mix probability again, and produce larger dispersion territory, realize mist to mix with the second stage not being inhaled into anemostat 19 flue gas, reach good mixed effect.

Claims (10)

1. one kind has the CO boiler of dusting function, described CO boiler comprises flue, combustion chamber, steam drum, evaporator section and economizer section, described flue comprises the first vertical flue, horizontal flue and the second vertical flue, combustion chamber is provided with in the first vertical flue, steam drum is provided with in horizontal flue, evaporator section and economizer section is provided with in second vertical flue, it is characterized in that, described combustion chamber medium dip is provided with dust block board, in combustion chamber, the walling of flue arranged outside in contiguous second vertical flue direction has the ash-storing bin of external hanging type, first vertical flue has ash discharging hole communicate with ash-storing bin, described dust block board is the baffle plate of multi-layer intercrossed layout, and dust block board successively reduces along the first vertical walling of flue to ash-storing bin direction height, and except orlop baffle plate, the inner of all the other baffle plates is sawtooth pattern.
2. according to CO boiler according to claim 1, it is characterized in that, the inclination angle of dust block board is greater than the angle of repose of contained flue dust in flue gas.
3. according to CO boiler according to claim 1, it is characterized in that, described dust block board is except the superiors' baffle plate, and all the other baffle plate outer ends can be sawtooth pattern.
4. according to CO boiler according to claim 1, it is characterized in that, every layer of baffle plate of described dust block board is formed by one piece of baffle plate or is made up of some pieces of baffle combination, has certain interval or gapless between some pieces of baffle plates.
5. according to CO boiler according to claim 1, it is characterized in that, in the second vertical flue, ammonia-gas spraying device and Benitration reactor are also set, described Benitration reactor is arranged between evaporator section and economizer section, Benitration reactor comprises some denitration unit, and each denitration unit includes hanging beam, steam sootblower, catalyst module and catalyst support beam.
6. according to CO boiler according to claim 5, it is characterized in that, described ammonia-gas spraying device is arranged at the top of evaporator section, or is arranged between evaporator section and Benitration reactor.
7. according to the CO boiler described in claim 5 or 6, it is characterized in that, described ammonia-gas spraying device comprises spray ammonia house steward, spray ammonia arm and spray ammonia element, and spray ammonia arm arranges some, and spray ammonia arm one end is connected with spray ammonia house steward, and the other end is enclosed construction; Described spray ammonia element comprises nozzle, anemostat and spatter plate, and the lower surface of spray ammonia arm is connected with described spray ammonia element by nozzle; Described anemostat comprises contraction section, trunnion and expansion segment, and jet expansion stretches in anemostat contraction section, spatters the below that plate is arranged at expansion segment.
8. according to CO boiler according to claim 7, it is characterized in that, the angle of throat of described contraction section is 10 ° ~ 60 °, and the length of described trunnion is 1 ~ 4 times of throat pipe diameter, and the angle of flare of described expansion segment is 7 ° ~ 30 °.
9. according to CO boiler according to claim 7, it is characterized in that, the described plate that spatters is at least two-layer, and plate is provided with sieve aperture, described in spatter packing free ratio be 10% ~ 60%, described nozzle, anemostat and spatter the dead in line of plate.
10., according to CO boiler according to claim 7, it is characterized in that, described in spatter plate shape consistent with outlet, anemostat lower end shape.
CN201210408167.2A 2012-10-24 2012-10-24 There is the CO boiler of dusting function CN103776013B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201210408167.2A CN103776013B (en) 2012-10-24 2012-10-24 There is the CO boiler of dusting function

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201210408167.2A CN103776013B (en) 2012-10-24 2012-10-24 There is the CO boiler of dusting function

Publications (2)

Publication Number Publication Date
CN103776013A CN103776013A (en) 2014-05-07
CN103776013B true CN103776013B (en) 2016-03-02

Family

ID=50568565

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201210408167.2A CN103776013B (en) 2012-10-24 2012-10-24 There is the CO boiler of dusting function

Country Status (1)

Country Link
CN (1) CN103776013B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104084040A (en) * 2014-08-01 2014-10-08 哈尔滨工业大学 Deflector set in SCR (selective catalytic reduction) flue gas denitrification reactor
CN106000140A (en) * 2016-07-08 2016-10-12 大唐环境产业集团股份有限公司 Ammonia-air mixing device for flue gas denitration
CN106166455B (en) * 2016-08-10 2020-01-07 大唐环境产业集团股份有限公司 Denitration ammonia pretreatment systems
CN106139946B (en) * 2016-08-10 2020-01-07 大唐环境产业集团股份有限公司 Denitration ammonia air mixing device

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2062412U (en) * 1989-03-30 1990-09-19 东北电力学院 Anti-abrasive device for boiler coal saver
US6095095A (en) * 1998-12-07 2000-08-01 The Bacock & Wilcox Company Circulating fluidized bed reactor with floored internal primary particle separator
CN201394414Y (en) * 2009-05-09 2010-02-03 江苏中科节能环保技术有限公司 Injection ammonia-spray mixing mechanism of SCR reaction device
CN201754031U (en) * 2010-09-30 2011-03-02 天壕节能科技股份有限公司 Glass furnace waste heat boiler with denitration joint
CN102512954A (en) * 2011-12-23 2012-06-27 东方电气集团东方锅炉股份有限公司 Heat recovery steam generator flue gas denitration apparatus
CN102537980A (en) * 2012-01-16 2012-07-04 哈尔滨工业大学 High-temperature melting treatment system and method for sludge

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2062412U (en) * 1989-03-30 1990-09-19 东北电力学院 Anti-abrasive device for boiler coal saver
US6095095A (en) * 1998-12-07 2000-08-01 The Bacock & Wilcox Company Circulating fluidized bed reactor with floored internal primary particle separator
CN201394414Y (en) * 2009-05-09 2010-02-03 江苏中科节能环保技术有限公司 Injection ammonia-spray mixing mechanism of SCR reaction device
CN201754031U (en) * 2010-09-30 2011-03-02 天壕节能科技股份有限公司 Glass furnace waste heat boiler with denitration joint
CN102512954A (en) * 2011-12-23 2012-06-27 东方电气集团东方锅炉股份有限公司 Heat recovery steam generator flue gas denitration apparatus
CN102537980A (en) * 2012-01-16 2012-07-04 哈尔滨工业大学 High-temperature melting treatment system and method for sludge

Also Published As

Publication number Publication date
CN103776013A (en) 2014-05-07

Similar Documents

Publication Publication Date Title
US8480984B2 (en) Biomass boiler SCR NOx and CO reduction system
CN103990365B (en) The flue gas purifying method of a kind of ozone/hydrogen peroxide induced radical and system
CA2501995C (en) Method for treating emissions
US7776297B2 (en) Multi-stage heat absorbing reactor and process for SCR or NOx and for oxidation of elemental mercury
CN100496676C (en) Wet ammonia flue gas cleaning technology simultaneously removing various pollutant and system thereof
US20050118084A1 (en) Multi-stage heat absorbing reactor and process for SCR of NOx and for oxidation of elemental mercury
CN106659971A (en) Method and apparatus for removing contaminants from exhaust gases
CN101219329B (en) Flue gas denitrating technique with preposed whirlwind beforehand dust removal SCR
CN103212284A (en) Method and device for combined removal of nitric oxide and sulfide in flue gas
CN105688622B (en) Use the flue gas desulfurization and denitration method and device of the double adsorption towers of series connection
CN201380039Y (en) Double-tower flue gas desulphurization device
CN203437036U (en) Sintering fume desulfurization and denitrification device
CN104226479A (en) Efficient wet type electric dedusting and purifying device and method for smoke obtained after wet desulphurization
CN105080332B (en) Agglomerates of sintered pellets reclamation system and process
CN104043325B (en) The flue gas purifying method of a kind of ozone activation persulfate and device
JP2009240908A (en) Wet two step flue gas desulfurization apparatus and operation method of wet two step flue gas desulfurization apparatus
CN103585885B (en) Low-temperature denitration catalyst module and cement kiln low-temperature selective catalytic reduction denitration system
WO2005028082A1 (en) A dry flue gas cleaning process and its system for simultaneously desulfurization and denitrating
CN101601965B (en) Ammonia-spraying grid device for SCR-method flue gas denitrification, and SCR-method flue gas denitrification process
CN103506002B (en) Two-period form Two-way Cycle spraying filler composite absorption tower
CN103768903B (en) A kind of FCC apparatus regenerated flue gas denitrating technique
EP3137745B1 (en) Compact selective catalytic reduction system for nitrogen oxide reduction in the oxygen-rich exhaust of 500 to 4500 kw internal combustion engines
TW201118316A (en) System and method for protection of SCR catalyst
CN204891568U (en) Distributed SOx/NOx control device of boiler flue gas integration
CA2501997C (en) Emission treatment system

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model