CN205461778U - Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously - Google Patents

Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously Download PDF

Info

Publication number
CN205461778U
CN205461778U CN201620126472.6U CN201620126472U CN205461778U CN 205461778 U CN205461778 U CN 205461778U CN 201620126472 U CN201620126472 U CN 201620126472U CN 205461778 U CN205461778 U CN 205461778U
Authority
CN
China
Prior art keywords
flue gas
fluidisation
connects
denitrifying
flue
Prior art date
Legal status (The legal status 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 status listed.)
Expired - Fee Related
Application number
CN201620126472.6U
Other languages
Chinese (zh)
Inventor
刁经中
赵钰慧
黄灵芝
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Bolang Environmental Engineering & Technology Co., Ltd.
Original Assignee
Beijing Bolang Eco - Environmental Science And Technology Co Ltd
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 Beijing Bolang Eco - Environmental Science And Technology Co Ltd filed Critical Beijing Bolang Eco - Environmental Science And Technology Co Ltd
Priority to CN201620126472.6U priority Critical patent/CN205461778U/en
Application granted granted Critical
Publication of CN205461778U publication Critical patent/CN205461778U/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

The utility model discloses a semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously is provided with the SOx/NOx control reactor, bag collector is connected to the reactor, the reactor includes the reacting chamber at middle part, and the reacting chamber lower part is provided with imported flue, and upper portion is provided with exhaust pass, be provided with upper and lower two -layer hydraulic in the reacting chamber, for reaction sequence humidification and cooling, in the top of upper hydraulic, be provided with cyclone in the reacting chamber exit, particulate matter behind the cracking reaction in the flue gas air current.

Description

A kind of semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device
Technical field
This utility model relates to a kind of semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device, is specifically related to reactor and sack cleaner, it is adaptable to garbage incinerating power plant, the smoke eliminator of Industrial Stoves.
Background technology
Semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device is currently in the research and development starting stage.Most fluidized bed fume purifying devices can only desulfurization, it is impossible to denitration simultaneously.
There are three big technical barriers in the key core equipment reactor of existing recirculating fluidized bed flue gas and desulfurizing and denitrifying device: 1. flue gas flow field, " rich oxygen type " highly active absorbent flow field and in order to can be with " rich oxygen type " highly active absorbent increase humidity of simultaneous SO_2 and NO removal, the humidification activation water smoke flow field improving its reactivity is the most uneven, even serious bias current or local eddy currents;2. desulphurization denitration product glues wall, conglomeration, the bed that collapses, stifled tower have generation more, causes whole system to be difficult to long-period stable operation;3. exiting flue gas dustiness is the highest by (800~1000g/Nm3), causing the sack cleaner overload at rear portion, resistance drop quickly raises.
The normally used other visual plant pulsed sack cleaner of this technology, there is also three big technical barriers: 1. the breakage rate in advance of filter bag is high;2. the leak detection work of filter bag damage is the most difficult;3. it is difficult to shut down process damaged filter bag at once.
Utility model content
For problems of the prior art, this utility model provides a kind of semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device, these difficult problems in prior art can be solved well, it is achieved the industrialization of " rich oxygen type " highly active absorbent CFB method flue gas and desulfurizing and denitrifying, commercial application.
The purpose of this utility model is achieved through the following technical solutions:
A kind of semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device, it is provided with desulfurization and denitrification reaction device, described reactor connects sack cleaner, described reactor includes the reative cell at middle part, reative cell bottom is provided with inlet flue duct, top is provided with exhaust pass, is provided with upper and lower two-layer hydraulic spray nozzle in described reative cell, for course of reaction humidification and cooling;Above upper water atomizing nozzle, reative cell exit is provided with cyclone separator, the particulate matter in flue gas stream after separating reaction.
Further, being provided with 3 deflectors not waiting arc in the inlet flue duct of described reactor, reative cell bottom is provided with some groups of Laval nozzle formula flue gases and absorbent accelerator, and flue gas stream is in described accelerator enters reative cell;
It is provided with " rich oxygen type " highly active absorbent entrance above inlet flue duct on body, connects " rich oxygen type " highly active absorbent feed bin;
It is provided with dust outlet below inlet flue duct on body, connects flue ash bucket.
Further, described cyclone separator is circumferentially provided with spiral-guide tooth, and flue gas stream is guided by cyclone separator and utilizes centrifugal force to carry out particulate separation, and described reative cell arranges 6 air intake passages and connects cyclone separator.
Further, described cyclone separator bottom is provided with circulating ash down-comer, and circulating ash down-comer is configured with air conveying booster, and the upper port of circulating ash down-comer is horn mouth, and the lower port of circulating ash down-comer is arranged at described reative cell inlet flue duct.
Further, described lower layer of water atomizing nozzle is provided with 6, and described upper water atomizing nozzle is provided with 3, the injection direction of upper and lower two-layer hydraulic spray nozzle the most upward, the high pressure fine water-spray system of described hydraulic spray nozzle coupled reaction outdoor.
Further, the exhaust pass of described reactor is divided into two branch roads, a branch road to connect described sack cleaner, sack cleaner connects air-introduced machine, another branch road connects described air-introduced machine, this branch road is provided with stop valve as alternate channel, and described air-introduced machine connects chimney.
Further, being provided with filtering cabin in described sack cleaner, be lifted with some groups of filter bags in filtering cabin, filtering cabin top is provided with blowback storehouse, and filtering cabin bottom is provided with fluidisation Lower Hold, and the particulate matter after filtration discharges described sack cleaner through fluidisation Lower Hold.
Further, being provided with stop valve at the inlet flue duct of described sack cleaner, be additionally provided with cold blast sliding valve, inlet flue duct connects active charcoal feed bin;
The entrance point of described sack cleaner is horn-like, is provided with some groups of multiaperture-type flue gas stream distribution grids, the particulate matter in flue gas after separating reaction in loudspeaker cylinder, and the particulate matter after separation enters described fluidisation Lower Hold.
Further, described fluidisation Lower Hold is sharp bottom boat shape, in fluidisation Lower Hold, bracing frame is provided with fluidisation cloth, is provided with fluidisation airduct below fluidisation cloth, and fluidisation airduct connects roots blower;
Fluidize in Lower Hold described in corresponding every fluidisation airduct and be additionally provided with impingement baffle;
Pneumatic ash transmitting system outside the connection of described fluidisation Lower Hold, pneumatic ash transmitting system connects ash storehouse by pipeline.
Further, arranging marsupial cage in described filter bag, often group filter bag is all lifted on porous card, is blowback storehouse above described card;
Being provided with the soot blower system positioning walking line by line on described card, described soot blower system connects the clean gas pipeline at air-introduced machine rear by pipeline, introduces clean gas to often organizing filter bag soot blowing;Top, blowback storehouse is additionally provided with spraying system of promptly lowering the temperature.
The semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device using said structure to arrange has the advantage that
This utility model is rational in infrastructure, flue gas flow field, " rich oxygen type " highly active absorbent flow field and can increase humidity with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal to give, improve the humidification activation water smoke flow field of its reactivity, the most uniform for regulating and controlling the water smoke flow field of flue-gas temperature.
" rich oxygen type " highly active absorbent short distance Rapid Circulation in reactor, it is achieved high-efficiency desulfurization denitration.
Flexible flue-gas temperature, effectively prevents equipment corrosion, prevents desulphurization denitration product from gluing wall, conglomeration, the bed that collapses, stifled tower.
Exiting flue gas dustiness greatly reduces, the circulating fluid bed reactor of circulating flue gas simultaneous SO_2 and NO removal in lower resistance single tube.
Use the static deashing locellus orientation blowback bag type collector of walking simultaneously.Its principle, structure are the simplest;Owing to using purifying smoke minute-pressure reverse gas cleaning technology, compared with traditional pulsed sack cleaner, its soot cleaning system is not in use by the complicated air machinery such as roots blower, air accumulator, pulse valve, and number of devices reduces~70%, it is achieved non-oxidation, without the temperature difference, idle deashing;Use oblate filter bag and bag cage, on the premise of filter area is identical, the minimizing of filter bag quantity~50%;Resistance power consumption can reduce~15%;There is device on-load, until the most not shutting down switching maintenance, changing the ability of whole filter bag;Can effectively extend life-span of the filter bag, corrosion-resistant, high temperature resistant, the cheap filtrate such as glass, basalt fibre Nomex can be used safely, it is ensured that equipment safety, stable operation.
This utility model have employed " rich oxygen type " highly active absorbent, can realize CFB(recirculating fluidized bed) method flue gas and desulfurizing and denitrifying.This technical matters is simple, do not have SCR(SCR) the complicated spray ammonia system of gas denitrifying technology, there is no SCR denitration reaction unit, reduced investment, take up an area little, operating cost is low, non-secondary pollution (non-wastewater discharge), desulfuration efficiency up to 95.5%, denitration efficiency is up to 64.8%, equipment does not corrodes, available general carbon steel manufacture, meeting China's actual conditions, prospect is the most considerable.
Accompanying drawing explanation
Fig. 1 is the structural representation for this utility model semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device;
Fig. 2 is the structural representation of circulating fluid bed reactor of circulating flue gas simultaneous SO_2 and NO removal in the lower resistance single tube that this utility model uses;
Fig. 3 is the structural representation of the static deashing locellus orientation blowback bag type collector of walking that this utility model uses.
In figure: 1, high-pressure hydraulic pump;2, flue ash bucket;3, inlet flue duct;4, " rich oxygen type " highly active absorbent feed bin;
5, reactor;5-1, absorbent entrance;5-2, accelerator;5-3, reactor shell diffuser;5-4, lower layer of water atomizing nozzle;5-5, circulating ash down-comer;5-6, upper water atomizing nozzle;5-7, reative cell;5-8, air conveying booster;5-9, air intake passage;5-10, cyclone separator;5-11, exhaust pass;
6, activated carbon feed bin;7, bypass flue;
8, sack cleaner;8-1, inlet flue duct;8-2, stop valve;8-3, cold blast sliding valve;8-4, import loudspeaker;8-5, flue gas stream distribution grid;8-6, card;8-7, filter bag;8-8, casing;8-9, promptly lower the temperature spraying system;8-10, neat stress exhaust pass;8-11, stop valve;8-12, purifying smoke return flue;8-13, desulphurization denitration product exit;8-14, impingement baffle;8-15, fluidisation airduct;8-16, fluidisation cloth;8-17, fluidisation Lower Hold housing;
9, fluidisation Lower Hold;10, soot blower system;11, Hui Ku;12, chimney;13, air-introduced machine;14, ash-transmission system;15, fluidized wind system.
Detailed description of the invention
By further illustrating the technological means and effect that this utility model taked by reaching predetermined technique purpose, below in conjunction with accompanying drawing and preferred embodiment, structure of the present utility model, workflow are described in detail as follows.
(1) it is one of embodiment of the present utility model as shown in Figure 1, Figure 2, Figure 3 shows, in this embodiment, simultaneous SO_2 and NO removal device is provided with desulfurization and denitrification reaction device 5, and reactor 5 connects sack cleaner 8, and reactor 5 includes the reative cell 5-7 at middle part, reative cell 5-7 bottom is provided with inlet flue duct 3, top is provided with exhaust pass 5-11, in reative cell 5-7, is provided with upper and lower two-layer hydraulic spray nozzle, lower layer of water atomizing nozzle 5-4 is course of reaction humidification, and upper water atomizing nozzle 5-6 is flue gas stream cooling;Above upper water atomizing nozzle 5-6, reative cell 5-7 exit is provided with cyclone separator 5-10, the particulate matter in flue gas stream after separating reaction.
As in figure 2 it is shown, be provided with 3 deflectors not waiting arc in the inlet flue duct 3 of reactor 5, reative cell 5-7 bottom is provided with some groups of Laval nozzle formula flue gases and absorbent accelerator 5-2, and flue gas stream is in accelerator 5-2 enters reative cell 5-7.
It is provided with " rich oxygen type " highly active absorbent entrance 5-1 above inlet flue duct 3 on body, connects " rich oxygen type " highly active absorbent feed bin 4." rich oxygen type " highly active absorbent feed bin 4 includes the parts such as roof scrubber, pressure relief valve, feed bin, gasification board, frequency conversion motor and star-shape feeding valve.
Rich oxygen type " highly active absorbent can use the absorbent type disclosed in Chinese invention patent " method and device of removing sulfur, nitrate and mercury simultaneously from boiler flue gas " (application number 200610102077.5).
It is provided with dust outlet below inlet flue duct 3 on body, connects flue ash bucket 2.
Cyclone separator 5-10 is circumferentially provided with spiral-guide tooth, and flue gas stream is guided by cyclone separator 5-10 and utilizes centrifugal force to carry out particulate separation, and reative cell 5-7 arranges 6 air intake passage 5-9 and connects cyclone separator.
Cyclone separator 5-10 bottom is provided with circulating ash down-comer 5-5, air conveying booster 5-8 it is configured with on circulating ash down-comer 5-5, the upper port of circulating ash down-comer 5-5 is horn mouth, and the lower port of circulating ash down-comer 5-5 is arranged at reative cell 5-7 inlet flue duct 3.
Lower layer of water atomizing nozzle 5-4 is provided with 6, and upper water atomizing nozzle 5-6 is provided with 3, the injection direction of upper and lower two-layer hydraulic spray nozzle the most upward, the high pressure fine water-spray system outside hydraulic spray nozzle coupled reaction room 5-7.High pressure fine water-spray system includes the parts such as water tank, piping filter, high-pressure hydraulic pump, regulation valve, effusion meter.
The exhaust pass of reactor 5 is divided into two branch roads, a branch road to connect sack cleaner 8, and sack cleaner 8 connects air-introduced machine 13, and another branch road connects air-introduced machine 13, this branch road is provided with stop valve and connects chimney 12 as alternate channel, air-introduced machine 13.
Above-mentioned stop valve can use two veneer soft edge stop valves.Air-introduced machine 13, is whole system flue gas, " rich oxygen type " highly active absorbent and the power source of desulphurization denitration product flowing.
Being provided with filtering cabin in sack cleaner 8, be lifted with some groups of filter bag 8-7 in filtering cabin, filtering cabin top is provided with blowback storehouse, and filtering cabin bottom is provided with fluidisation Lower Hold 9, and the particulate matter after filtration discharges sack cleaner 8 through fluidisation Lower Hold 9.
Being provided with stop valve 8-2 at the inlet flue duct of sack cleaner 8, be additionally provided with cold blast sliding valve 8-3, inlet flue duct connects active charcoal feed bin 6.Activated carbon feed bin 6 includes feed bin, gasification board, frequency conversion motor and star-shape feeding valve.Stop valve 8-2 can use veneer soft edge stop valve.
The entrance point of sack cleaner 8 is horn-like, is provided with some groups of multiaperture-type flue gas stream distribution grid 8-5, the particulate matter in flue gas after separating reaction in loudspeaker cylinder, and the particulate matter after separation enters fluidisation Lower Hold 9.
Fluidisation Lower Hold 9, in sharp bottom boat shape, is provided with fluidisation cloth 8-16 by bracing frame in fluidisation Lower Hold 9, is provided with fluidisation airduct 8-15, fluidisation airduct 8-15 and connects roots blower below fluidisation cloth 8-16.Fluidisation Lower Hold fluidized wind system containing roots blower, the parts such as including roots blower, air preheater and fluidized wind pipeline.
Corresponding every fluidisation airduct 8-15 fluidisation Lower Hold 9 is additionally provided with impingement baffle 8-14.
Fluidisation Lower Hold 9 connects the pneumatic ash transmitting system 14 of outside, and pneumatic ash transmitting system 14 connects ash storehouse 11 by pipeline.
Containing the pneumatic ash transmitting system of storehouse pump, the parts such as including feed pipe, inlet valve, storehouse pump case, level-sensing device, compressed air inlet pipe, intake valve, fluidized disk, discharge nozzle, outlet valve.
Ash storehouse 11, the parts such as including top, storehouse cleaner unit, pressure relief valve, feed bin, radar level gauge, gasification board, frequency conversion motor and star-shape feeding valve, push-pull valve, wetting stirrer, dry ash bulk machine.
Arranging marsupial cage in filter bag 8-7, often group filter bag 8-7 is all lifted on porous card 8-6, is blowback storehouse above card 8-6.Filter bag 8-7 and bag cage are all in oblateness.
Being provided with the soot blower system 10 positioning walking line by line on card 8-6, soot blower system 10 connects the clean gas pipeline at air-introduced machine 13 rear by pipeline, introduces clean gas to often organizing filter bag 8-7 soot blowing;Top, blowback storehouse is additionally provided with urgent cooling spraying system 8-9.
This utility model uses the truthful data of Practical Project, through rigorous technology Calculation, and uses Fluent software to carry out multiphase flow flow field analysis to be verified, effect is very good.
(2) the more detailed structure of this utility model and work process are described as follows.
Seeing Fig. 1, the circulating fluid bed reactor of circulating flue gas simultaneous SO_2 and NO removal in the core reaction equipment lower resistance single tube that this utility model uses, its unique texture is: with the streamlined inlet flue duct of direct current of 3 Unequal distance circular blast baffles;6 Laval nozzle formula flue gas accelerators;Humidity can be increased with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal to give, improve its reactivity and be provided with 6 high-pressure fine water mist nozzles of ground floor;It is provided with 3 high-pressure fine water mist nozzles of the second layer to regulate and control flue-gas temperature;There is the single flow cyclone separator of 4 tangential entries;There is the circulating ash down-comer being positioned at reactor axis of 6 outlets with air conveying booster and lower end;And the ring smoke outlet being made up of top angle cylinder, concentric circular tubular flat-top cover and downward-sloping flue.
The static deashing locellus orientation blowback bag type collector of another visual plant walking that this utility model uses, its unique texture is: use oblate filter bag and bag cage, gas approach and the employing of neat stress exhaust pass to be similar to the veneer soft edge stop valve of zero air leak rate of air curtain, deashing device is utilization backflow neat stress, can position the purifying smoke minute-pressure reverse gas cleaning system of walking, the ship shape ash bucket operated steadily and fluidisation Lower Hold line by line.
See Fig. 2, burning power plant boiler or the exiting flue gas of Industrial Stoves, enter the streamlined inlet flue duct of reactor direct current 3 with 3 Unequal distance circular blast baffles, fresh can be with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal through absorbent entrance, enter the Reactor inlet flue with 3 Unequal distance circular blast baffles, through 3 Unequal distance circular blast baffles together with former flue gas, continue up, by 6 Laval nozzle formula flue gases and absorbent accelerator, enter reactor main reaction region.
The particulate matter that in former flue gas, volume is bigger, heavier lodges in the Reactor inlet flue ash bucket with star-shaped dust-discharging valve and push-pull valve, periodically discharges;Carry fresh can be with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal and the former flue gas of a large amount of circulating ash, through 6 Laval nozzle formula flue gases and absorbent accelerator, moment flue gas flow rate is enhanced more than 3 times, and even dispersion is in the main reaction region total space.
It is arranged on above 6 Laval nozzle formula flue gases and absorbent accelerator diffuser, 6 can increase humidity with " rich oxygen type " high-efficiency absorbent of simultaneous SO_2 and NO removal to give, improve 6 high-pressure fine water mist nozzles of ground floor of its reactivity, the heavy pressure fine spray of 1~10 μm ejected, can be at flash evapn so that humidity can be increased with " rich oxygen type " highly active absorbent surface of simultaneous SO_2 and NO removal, improve its reactivity, make flue gas lower the temperature rapidly, and with the sour gas SO in flue gas3、SO2, strong collision, mixing, mass transfer, the heat transfer such as NOx, HCl, HF, there is ion reaction, reach the purpose of desulphurization denitration.
Solid phase particles thing in main reaction region constantly collides, and can be stripped with the powdery salts reaction product that the reaction on " rich oxygen type " highly active absorbent surface of simultaneous SO_2 and NO removal with sour gas generates, moves upward with flue gas;The cluster of grains that volume is bigger is difficult to rise with flue gas, and assembles landing and enter inlet flue duct ash bucket, discharges through star-shaped dust-discharging valve and push-pull valve.
The flue gas being basically completed desulfurization and denitrification reaction continues up flowing, mix with the heavy pressure fine spray of 1~10 μm ejected for regulating and controlling 3 high-pressure fine water mist nozzles 21 of the second layer of flue-gas temperature, proceed desulfurization and denitrification reaction, so this position is also known as side reaction district, regulate and control flue-gas temperature simultaneously, temperature controlled higher than flue gas dew point temperature 15 DEG C~about 20 DEG C by the way of regulation injection flow rate, to ensure that carbon steel equipment does not corrodes.
The flue gas being complete desulfurization and denitrification reaction continues up flowing, by having the intake channel of the single flow cyclone separator flue gas of 4 tangential entries, enters the single flow cyclone separator with 4 tangential entries.With desulphurization denitration product and react the most completely can be with the flue gas of " rich oxygen type " highly active absorbent powder body of simultaneous SO_2 and NO removal, annular space between single flow cyclone separator inner barrel and the central row trachea with 4 tangential entries, the screw that specification rotates up, major part bigger, the heavier particulate matter of particle diameter throws away from inner barrel top by centrifugal force, glide and deposit to have the single flow cyclone separator cone end of 4 tangential entries, flow into the circulating ash down-comer being positioned at reactor axis.They are positioned at the circulating ash down-comer smooth outflow downwards of reactor axis by acting on of deadweight and air conveying booster, flow out by being positioned at 6 outlets bottom the circulating ash down-comer 20 of reactor axis.Brought into 6 Laval nozzle formula flue gases and absorbent accelerator by swiftly flowing former flue gas immediately, flow up, repeatedly participate in desulfurization and denitrification reaction.
See Fig. 1, desulphurization denitration flue gas through a gas solid separation flows out from reactor head, enter the static deashing locellus orientation blowback bag type collector of walking, before entering the static deashing locellus orientation blowback bag type collector of walking, can be with the absorbent charcoal powder body of Adsorption of Heavy Metals and dioxin by the star-like feed valve of activated carbon bin bottom frequency control, inject the static deashing locellus orientation blowback bag type collector inlet flue duct of walking, complete in sack cleaner heavy metal in flue gas and the absorption of dioxin and remove.
See Fig. 3, with desulphurization denitration product and the flue gas of absorbent charcoal powder body, by inlet flue duct, veneer soft edge stop valve, enter import loudspeaker.Flue gas is in import loudspeaker, through the obstruct of multiaperture-type airflow-distribution board, redistribution, and carries out second time gas solid separation.The powder body being separated falls directly into bottom the static deashing locellus orientation blowback bag type collector of walking above the gasification cloth of ship shape ash bucket and fluidisation Lower Hold.
Entering the static deashing locellus orientation blowback bag type collector casing of walking with remaining desulphurization denitration product, heavy metal, the flue gas of dioxin dust, through the filtration of oblate filter bag, i.e. third time gas solid separation, the dust of more than 99.9% is separated.Owing to filter bag by the deadweight of bag cage and closely cooperates, filter bag being stretched, tensioning, bag cage uses high density skeletal support, and when filtering, filter bag keeps straight with depression, and dust adhesive force is little.When flue dust deadweight is more than attachment frictional force, dust can automatic landing more than 50%.
When starting the purifying smoke minute-pressure reverse gas cleaning system that can position walking line by line, the neat stress returning flue from neat stress blows in oblate filter bag 33, owing to deashing pressure only has 0.03Mpa, filter bag be in again stretch, tense situation, during deashing, filter bag is without obvious action, it is achieved that static deashing.The flying dust separated by filter bag is slipped to above the gasification cloth of ship shape ash bucket and fluidisation Lower Hold.Hot-fluid wind-transformation bottom fluidisation storehouse is blowed to desulphurization denitration product exit, enters the air-transport system containing storehouse pump, delivers to ash storehouse.Purify flue gas up to standard to be discharged by veneer soft edge stop valve, neat stress exhaust pass, drain into air by air-introduced machine, chimney.
(3) the utility model has the advantage of:
A. this utility model can be with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal owing to have employed:
1) CFB method flue gas and desulfurizing and denitrifying can be realized.
2) technique is simple, does not has the spray ammonia system of SCR equipment for denitrifying flue gas and technical sophistication, safe and reliable to operation.
3) appliance arrangement quantity is few, take up an area little, reduced investment.
4) economizing on water, economize on electricity, operating cost is low.
5) non-secondary pollution, non-wastewater discharge.
6) equipment does not corrodes, available general carbon steel manufacture.
7) desulfuration efficiency up to 95.5%, denitration efficiency is up to 64.8%.
B. the circulating fluid bed reactor of circulating flue gas simultaneous SO_2 and NO removal in the lower resistance single tube that this utility model uses:
1) with the streamlined inlet flue duct of reactor direct current of 3 Unequal distance circular blast baffles: meet the natural streamline of flow of flue gas, form inequality at bend deflector cut section and cross stream, effectively reduce lateral eddy current, prevent flue gas bias current, it is achieved the steady flow that flue gas is evenly distributed in reactor;Fluid resistance is little;This structure is better than the bilateral air intake structure of Wulff company of Germany, is better than the air intake structure of two 135 ° of knuckle elbows of single flow of LLAG company of Germany, the most domestic traditional unilateral perpendicular quadrature air intake structure.
2) 6 Laval nozzle formula flue gases and absorbent accelerator: using Laval nozzle, the length of its aditus laryngis high regime is far smaller than the length of domestic and international CFB method venturi aditus laryngis high regime, and therefore its resistance drop is substantially reduced.Carry fresh can be with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal and the former flue gas of a large amount of circulating ash, through 6 Laval nozzle formula flue gases and absorbent accelerator, moment flow velocity is enhanced more than 3 times, and they enter main reaction region together.The kinetic energy of flue gas can be effectively improved, realize the flue gas acceleration to solid particulate matter, guarantee to be uniformly suspended within flue gas with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal, make gas-particle two-phase be sufficiently mixed, collide, rub, mass transfer, conduct heat, react.
3) 6 high-pressure fine water mist nozzles of the ground floor of main reaction region, and 3 high-pressure fine water mist nozzles of the second layer in side reaction district: use high-pressure fine water mist nozzle, water smoke continuous uniform, mist particle diameter is little, usually 1~10 μm, minimum up to nanoscale, specific surface area substantially exceeds general water smoke, droplet speed is high, density is big, can evaporate rapidly, absorbs heat, lower the temperature;" rich oxygen type " high-efficiency absorbent allowing to simultaneous SO_2 and NO removal increases humidity, improves its reactivity;And greatly increase can be with " rich oxygen type " highly active absorbent of simultaneous SO_2 and NO removal and SO2、SO3, the water film surface of the sour gas such as NOx, HCL, HF contact amass, under gaseous state, liquid and the vapor state between gas-liquid, make SO2、SO3, the sour gas such as NOx, HCL, HF, through absorbing, be humidified, condense, rub, colliding, mass transfer, heat transfer, ion reaction, thus reach the purpose of efficient deacidification.Owing to uniform flue gas and absorbent flow field enclose uniform spray vaporization flow field, the wet wall effect caused because of local water spray excess can be prevented effectively from, it is to avoid viscous wall, fouling, conglomeration, the bed that collapses, stifled tower phenomenon occur, it is ensured that device is stable, long-term operation.
4) there is the single flow cyclone separator of 4 tangential entries: its gas approach passage is made up of 4 tangential entries, its inner barrel is a kind of conic tube, its center exhaustor is circular cylinder, bottom is provided with a umbrella shape getter section, the outer wall of central row trachea cylinder is welded with 3 the spiral stream guidance fins rotated up, the centrifugal force of flue gas flow rate and particulate matter can be effectively improved, be conducive to improving gas-solid disngaging efficiency.
5) the circulating ash down-comer of reactor axis it is positioned at: owing to air conveying booster, by multiple compressed airs that the most tiltedly tangential small-hole enters, circulating ash powder body can be promoted to flow downward smoothly.Circulating ash down-comer outlet at bottom is 6, is respectively aligned to 6 Laval nozzle formula flue gases and the orientation of absorbent accelerator.Circulating ash down-comer bottom is in flue gas high velocity, and high velocity smoke portability circulating ash continues up, and enters 6 Laval nozzle formula flue gases and absorbent accelerator smoothly.
6) the ring exit flue of reactor head it is positioned at: the flue gas that desulphurization denitration and rough dusting have purified, by the annular space between angle cylinder and concentric circular tubular flat-top cover, beneficially in reactor, flue gas flow field is uniform, and hoop resistance drop is uniform.
C. the walking static state deashing locellus orientation blowback bag type collector that this utility model uses:
1) its principle, structure are the simplest.
2) owing to using the purifying smoke minute-pressure reverse gas cleaning system that can position walking line by line, compared with traditional pulsed sack cleaner, its soot cleaning system is not in use by the air machinery of the complexity such as roots blower, air accumulator, pulse valve, number of devices reduces about 70%, it is achieved non-oxidation, without the temperature difference, idle deashing.
3) using oblate filter bag and bag cage, on the premise of filter area is identical, filter bag quantity reduces about 50%.
4) resistance power consumption can reduce about 15%.
5) there is device on-load, until the most not shutting down switching maintenance, changing the ability of whole filter bag.
6) can effectively extend life-span of the filter bag, corrosion-resistant, high temperature resistant, the cheap filtrate such as glass, basalt fibre Nomex can be used safely, it is ensured that equipment safety, stable operation.
Described above simply to illustrate that this utility model, it is understood that this utility model is not limited to above example, meets the various variants of this utility model thought all within protection domain of the present utility model.

Claims (10)

1. a semidry-method recirculating fluidized bed flue gas and desulfurizing and denitrifying device, it is provided with desulfurization and denitrification reaction device, described reactor connects sack cleaner, described reactor includes the reative cell at middle part, reative cell bottom is provided with inlet flue duct, and top is provided with exhaust pass, it is characterised in that, described reative cell is provided with upper and lower two-layer hydraulic spray nozzle, for course of reaction humidification and cooling;Above upper water atomizing nozzle, reative cell exit is provided with cyclone separator, the particulate matter in flue gas stream after separating reaction.
2. desulfuring and denitrifying apparatus as claimed in claim 1, it is characterized in that, being provided with 3 deflectors not waiting arc in the inlet flue duct of described reactor, reative cell bottom is provided with some groups of Laval nozzle formula flue gases and absorbent accelerator, and flue gas stream is in described accelerator enters reative cell;
It is provided with " rich oxygen type " highly active absorbent entrance above inlet flue duct on body, connects " rich oxygen type " highly active absorbent feed bin;
It is provided with dust outlet below inlet flue duct on body, connects flue ash bucket.
3. desulfuring and denitrifying apparatus as claimed in claim 1, it is characterized in that, described cyclone separator is circumferentially provided with spiral-guide tooth, and flue gas stream is guided by cyclone separator and utilizes centrifugal force to carry out particulate separation, and described reative cell arranges 6 air intake passages and connects cyclone separator.
4. desulfuring and denitrifying apparatus as claimed in claim 1, it is characterized in that, described cyclone separator bottom is provided with circulating ash down-comer, air conveying booster it is configured with on circulating ash down-comer, the upper port of circulating ash down-comer is horn mouth, and the lower port of circulating ash down-comer is arranged at described reative cell inlet flue duct.
5. desulfuring and denitrifying apparatus as claimed in claim 1, it is characterized in that, described lower layer of water atomizing nozzle is provided with 6, and described upper water atomizing nozzle is provided with 3, the injection direction of two-layer hydraulic spray nozzle is the most up and down, the high pressure fine water-spray system of described hydraulic spray nozzle coupled reaction outdoor.
6. desulfuring and denitrifying apparatus as claimed in claim 1, it is characterized in that, the exhaust pass of described reactor is divided into two branch roads, article one, branch road connects described sack cleaner, sack cleaner connects air-introduced machine, another branch road connects described air-introduced machine, this branch road is provided with stop valve as alternate channel, and described air-introduced machine connects chimney.
7. desulfuring and denitrifying apparatus as claimed in claim 6, it is characterized in that, described sack cleaner is provided with filtering cabin, filtering cabin is lifted with some groups of filter bags, filtering cabin top is provided with blowback storehouse, filtering cabin bottom is provided with fluidisation Lower Hold, and the particulate matter after filtration discharges described sack cleaner through fluidisation Lower Hold.
8. desulfuring and denitrifying apparatus as claimed in claim 6, it is characterised in that being provided with stop valve at the inlet flue duct of described sack cleaner, be additionally provided with cold blast sliding valve, inlet flue duct connects active charcoal feed bin;
The entrance point of described sack cleaner is horn-like, is provided with some groups of multiaperture-type flue gas stream distribution grids, the particulate matter in flue gas after separating reaction in loudspeaker cylinder, and the particulate matter after separation enters described fluidisation Lower Hold.
9. desulfuring and denitrifying apparatus as claimed in claim 7, it is characterised in that described fluidisation Lower Hold is sharp bottom boat shape, is provided with fluidisation cloth by bracing frame in fluidisation Lower Hold, is provided with fluidisation airduct below fluidisation cloth, and fluidisation airduct connects roots blower;
Fluidize in Lower Hold described in corresponding every fluidisation airduct and be additionally provided with impingement baffle;
Pneumatic ash transmitting system outside the connection of described fluidisation Lower Hold, pneumatic ash transmitting system connects ash storehouse by pipeline.
10. desulfuring and denitrifying apparatus as claimed in claim 7, it is characterised in that arranging marsupial cage in described filter bag, often group filter bag is all lifted on porous card, is blowback storehouse above described card;
Being provided with the soot blower system positioning walking line by line on described card, described soot blower system connects the clean gas pipeline at air-introduced machine rear by pipeline, introduces clean gas to often organizing filter bag soot blowing;Top, blowback storehouse is additionally provided with spraying system of promptly lowering the temperature.
CN201620126472.6U 2016-02-18 2016-02-18 Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously Expired - Fee Related CN205461778U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201620126472.6U CN205461778U (en) 2016-02-18 2016-02-18 Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201620126472.6U CN205461778U (en) 2016-02-18 2016-02-18 Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously

Publications (1)

Publication Number Publication Date
CN205461778U true CN205461778U (en) 2016-08-17

Family

ID=56677872

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201620126472.6U Expired - Fee Related CN205461778U (en) 2016-02-18 2016-02-18 Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously

Country Status (1)

Country Link
CN (1) CN205461778U (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110117011A (en) * 2019-06-10 2019-08-13 新疆鑫力环保科技有限公司 A kind of method that physical method prepares active carbon
WO2019228545A1 (en) * 2018-05-31 2019-12-05 郑州市天之蓝环保科技有限公司 Industrial flue gas treatment system

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019228545A1 (en) * 2018-05-31 2019-12-05 郑州市天之蓝环保科技有限公司 Industrial flue gas treatment system
CN110117011A (en) * 2019-06-10 2019-08-13 新疆鑫力环保科技有限公司 A kind of method that physical method prepares active carbon

Similar Documents

Publication Publication Date Title
CN103203170B (en) Flue-gas cleaner
CN201684540U (en) Cleaning tower for smoke generated from aerodynamic turbulence
CN100525885C (en) Turbine type pressure charging acceleration fuel gas desulfurization gas wash tower
CN101799169B (en) Device for guiding airflow to impact liquid level in tangential direction for forming moisture-containing airflow
CN205461778U (en) Semidry method circulating fluidized bed flue gas is SOx/NOx control device simultaneously
CN107261781A (en) A kind of desulphurization denitration dust pelletizing system
CN205461770U (en) Quick circulation of coaxial short distance is semidry method gas cleaning equipment of desorption pollutant in coordination
CN201783300U (en) Fume elimination, dust removal and desulfuration integrated device
CN102266718A (en) Semi dry process flue gas desulfurization method of circulating fluidized bed based on circulation, and apparatus thereof
CN203916431U (en) A kind of gaseous oxidation is in conjunction with the flue gas combined desulfurization and denitration device of wet absorption
CN201609640U (en) Tail water body structure for guiding airflow to tangentially impact liquid level to form moist airflow
CN202191838U (en) Flue gas disposing device of coal-fired industrial boiler
CN203030186U (en) Short-range quick-circulation semi-dry method smoke desulfurization reactor
CN104437069A (en) Desulfurization and dust-removal device and desulfurization and dust-removal method of membrane separation circulating fluidized bed
CN204469531U (en) Membrane separation circulating fluid bed desulfation dust-extraction device
CN201030287Y (en) Cyclone boiler flue gas desulfurization dust cleaning apparatus
CN101357299A (en) Desulfurization reaction tower of circulating fluid bed
CN102423593A (en) Method for simultaneously dedusting, desulphurizing and denitrating boiler flue gas in coal-fired industry
CN102512901B (en) Composite dust-removing and collaborative desulfurization and denitration device capable of wetting flue gas
CN203400626U (en) Circulating fluidized bed reactor with low-resistance single-tube internal circulation, and function of simultaneous desulfurization and denitrification for smoke
CN206152622U (en) Domestic waste torrent recirculated flue gas purifier
KR101231923B1 (en) Semi-dry flue gas de-sulfurization apparatus and circulating fluidized bed combustion device
CN203342648U (en) Circulating fluid bed reactor realizing single-pipe internal circulating of absorbent and simultaneous desulfuration and denitration of smoke
CN107469610A (en) A kind of coal burning flue gas desulfurization low-temperature denitration device
CN202427313U (en) Smoke humidification composite type dust-removing and synergistic desulfurization and denitration device

Legal Events

Date Code Title Description
GR01 Patent grant
C14 Grant of patent or utility model
TR01 Transfer of patent right

Effective date of registration: 20170323

Address after: 100085 Beijing city Haidian District Xueqing Road No. 9 Ebizal building block B room 1010

Patentee after: Beijing Bolang Environmental Engineering & Technology Co., Ltd.

Address before: 100085 Beijing city Haidian District Xueqing Road No. 9 Ebizal building block B room 1010

Patentee before: Beijing Bolang Eco - Environmental Science AND Technology Co., Ltd.

TR01 Transfer of patent right
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20160817

Termination date: 20200218

CF01 Termination of patent right due to non-payment of annual fee