CN202605937U - System for reducing discharge of ultrafine particles in ash-laden gas - Google Patents
System for reducing discharge of ultrafine particles in ash-laden gas Download PDFInfo
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- CN202605937U CN202605937U CN 201220100938 CN201220100938U CN202605937U CN 202605937 U CN202605937 U CN 202605937U CN 201220100938 CN201220100938 CN 201220100938 CN 201220100938 U CN201220100938 U CN 201220100938U CN 202605937 U CN202605937 U CN 202605937U
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Abstract
The utility model provides a method and a system for reducing discharge of ultrafine particles in ash-laden gas, achieves particle growth or agglomeration to further control discharge of the ultrafine particles through prilling of a smoke fluidized bed and belongs to the technical fields of environmental pollution prevention and clean coal. The ash-laden gas flows through a vertically-arranged fluidized bed prilling reactor, smoke carried by exhaust gas in the fluidized bed prilling reactor serves as raw material particles, the exhaust gas serves as a fluidizing agent, prilling growth of the smoke particles is achieved by spraying feed liquid, grew particles fall into an ash bucket at the bottom of the fluidized bed prilling reactor, and then surplus ash-laden gas enters a conventional dust-cleaning apparatus for dust cleaning. The system can obviously improve capability of the conventional dust-cleaning apparatus to capture the ultrafine particles, has advantages of being less in floor space, less in investment, low in operation cost, free of transformation of the existing dust-cleaning apparatus and the like, and has important significant on effect increasing transformation of the dust-cleaning apparatus.
Description
Technical field
The utility model belongs to environmental pollution prevention and control and clean coal technology field, and particularly a kind of ash-laden gas reduces discharging the system of superfine particulate matter.
Background technology
Contain a large amount of superfine particulate matters in the coal-fired flue-gas, research shows, accounts for 33% by what fire coal generated in the overall suspended pellet in the urban air, and wherein superfine particulate matter accounts for 35%.According to China Environmental Monitoring General Station two-year superfine particulate matter monitoring has been carried out in domestic four cities and shown that the superfine particulate matter discharging year of China, average daily concentration is severe overweight all.
The capital equipment of gas cleaning is the deduster of various types, and industry is at present gone up widely used deduster and mainly contained mechanical collector, electrostatic precipitator and filtration dust catcher etc.Although the said equipment efficiency of dust collection has reached very high level---efficiency of dust collection reaches more than 95%; Even more than 99%; But they are but very low to the arresting efficiency of the superfine particulate matters such as PM2.5 of One's name is legion in the flue dust, cause a large amount of superfine particulate matters to be drained in the atmosphere, cause environmental pollution.
Mechanical collector has gravity settling chamber, inertial dust separator, cyclone dust collectors.Mechanical collector is because it is simple in structure, cheap, convenient for maintenance management and suitable face width and generally used at each industrial circle; Because separating mechanism mainly utilizes gravitational settling and particle inertial separation; So handling meal dirt particle, mechanical collector has no problem; And for micron order and sub-micron grade particle, its separating power is very low.
Electrostatic precipitator is charged to dust under the high voltage situation, and charged particle is hunted down under the electric field force effect.The electrostatic precipitation effect is not only relevant with grain diameter, but also relevant with the ratio resistance of particle, hangs down the removing that all is unfavorable for particle than too high in resistance with crossing.Although the efficiency of dust collection of electrostatic precipitation is higher,,, electrostatic precipitator can not be removed effectively to it owing to can not make it effectively charged for micron-sized superfine particulate matter.
Filtration dust catcher is with particle separating process from air-flow by means of porous media; Fiberfill layer (filter cloth, filter paper, metal wool, sack cleaner etc.) or stratum granulosum (slag, quartz sand, active carbon etc.) purify the filtration mechanism that all belongs to same to gas.But the filtration dust catcher pressure loss is bigger, and the filtrate corrosion resistance is poor, needs cleaned at regular intervals and replacing, and maintenance cost is higher, uses few in China.
Mechanical collector, electrostatic precipitator and filtration dust catcher; They all have separately pluses and minuses and application scenario, and to the dust granules more than the 50 μ m, the efficiency of dust collection of these cleaners is all higher; But they are to the superfine particulate matter of 0.01～10 μ m---the particle diameter of these superfine particulate matters is very little; And mass concentration accounts for overall share seldom, but quantity is very big, and elimination efficiency is all very low.Therefore, the discharging of superfine particulate matter be fundamentally controlled, new control method must be sought.
So-called granulation is meant material is processed the shot-like particle easy to use or the operation of trickle article shaped.Fluidized bed prilling is to utilize blowing of fluidized-bed layer bottom air-flow to make powder keep the fluidized state that suspends; Again spraying in the bed after water or the atomizing of other binding agent; Powder rolls through fluidisation and is agglomerated into the method for larger particles gradually, in industries such as food, medicine, chemical industry, seed treatment, has obtained at present using preferably.The fluidized bed prilling technology can be accomplished mixing, granulation, dry run in an equipment.In the granulation process, interparticle adhesion has five kinds of forms: 1) gravitation between solids; 2) but interfacial tension and capillary force that free flowing liquid produces; 3) cohesive force that produces of flowable liquids not; 4) solid bridge between particle; 5) the particle room machine is inlayed etc.
Through to the understanding of fluidized bed prilling and to influencing the analysis of particle agglomeration factor, can think that fluid bed realizes that as reactor the ultra-fine grain granulation is grown up and then removed is possible.
The utility model content
The purpose of the utility model is to overcome the deficiency that above-mentioned technology exists; Provide a kind of ash-laden gas to reduce discharging the system of superfine particulate matter; After realizing that through flue dust fluidized bed prilling technology particle is grown up or reunited, carry out dedusting again, thereby reduce the superfine particulate matter concentration of emission of conventional deduster.
The utility model is realized through following mode:
A kind of ash-laden gas reduces discharging the superfine particulate matter method and uses system; It comprises fluidized-bed reactor, and fluidized-bed reactor is vertically to be provided with, and its underpart is connected with gas approach; Air inlet place at fluidized-bed reactor is provided with the smoke distribution device, in fluidized-bed reactor, is provided with feed liquid atomizing device; The outlet of fluidized-bed reactor is connected with cleaner.
Said fluidized-bed reactor cross sectional shape is square or cylindrical.
Said feed liquid atomizing device comprises the feed liquid atomizer that places in the fluidized-bed reactor, and this feed liquid atomizer is connected with the slurries pipeline, and the slurries pipeline is connected with slush pump, and slush pump is connected with agitator.
Said feed liquid atomizer also is connected with air compressor.
Said cleaner is dust removal with machine device or electrostatic precipitator or is filtering dust-arrester.
Said fluidized-bed reactor bottom is provided with ash bucket.
A kind of ash-laden gas reduces discharging the method for superfine particulate matter; The ash-laden gas fluidized bed prilling reactor vertically set up of flowing through earlier, the flue dust that in the fluidized bed prilling reactor, carries with flue gas is a feed particles, is fluidizing agent with the flue gas; Through spraying into the form of feed liquid; The granulation of realization soot dust granule is grown up, and the particle after growing up falls into the ash bucket of fluidized bed prilling reactor bottom, and the residue ash-laden gas then gets into conventional cleaner again and carries out dedusting.
Said granulation growth process is: in fluid bed, spray into feed liquid; Flue gas upwards gets into fluid bed by the bottom through the smoke distribution device; With drip collision by the feed liquid of feed liquid atomizing device ejection, the conventional cleaner dedusting that flue gas is upwards flowed through and got into downstream after the fluid bed main body after the granulation.
The fluidizing velocity of said fluidized bed prilling reactor is 5～20m/s.
Said feed liquid is that water or concentration are concentration less than 15% white lime slurries, and the amount that sprays into makes flue gas relative humidity not surpass 80%.
The utility model mainly is to have utilized the granulation principle to carry out the purification of flue gas; It not only relies on the dedusting of electric cleaner or mechanical dust collector etc.; But fluidization is effectively combined with granulating technique, realize that in fluidized-bed reactor agglomeration of particles grows up, the particle after growing up will overcome the holder power that flue gas rises and fall into the ash bucket bottom the fluidized-bed reactor; Realize main catharsis, remaining ash-laden gas then can be through conventional cleaner dedusting.
The advantage of the utility model is embodied in:
1) with fluidized bed prilling process and conventional cleaner series operation, increased substantially the removal efficiency of existing cleaner to superfine particulate matter;
2) the fluidized bed prilling structure of reactor is simple, and is easy and simple to handle, and the reunion feed liquid is water or the white lime slurries that are easy to get, and small investment, operating cost are low;
3) utilize the method for the utility model, conventional cleaner need not be transformed its structure, just can reduce the superfine particulate matter concentration of emission of each pollution sources.
4) whole system is simple in structure, and fault rate is low, safeguards very convenient.
Description of drawings
Fig. 1 utilizes water to carry out the sketch map of the ash-laden gas reduction of discharging superfine particulate matter of granulation.
Fig. 2 utilizes the white lime slurries to carry out the sketch map of the ash-laden gas reduction of discharging superfine particulate matter of granulation.
Among the figure, 1 is the smoke distribution device, and 2 is the feed liquid atomizer, and 3 is fluidized-bed reactor, and 4 is flue; 5 is electrostatic precipitator, and 6 is air-introduced machine, and 7 is tank or agitator, and 8 is slush pump; 9 is the slurries pipeline, and 10 is air compressor, and 11 is ash bucket, and 12 is gas approach.
The specific embodiment
Below in conjunction with accompanying drawing and embodiment the utility model is done further explanation.
Embodiment 1:
Ash-laden gas is upwards got in the fluidized-bed reactor 3 through smoke distribution device 1 by gas approach 12.Simultaneously; Slush pump 8 is taken out current from tank 7 through pipeline 8; Send in the feed liquid atomizer 2 of fluidized-bed reactor 3 inside, water is atomized, superfine particulate matter passes through chain reunion, surface adhesion or dressing mode etc. by drop or particle capture; Thereby make dust granules realize that in fluidized-bed reactor 3 fluidization granulation grows up, larger particles falls in the ash bucket 11.
In granulation process, often to add a certain amount of binding agent, particle mainly leans on the bridging action of the binding agent granulating that bonds each other.In the present embodiment, the binding agent of employing is a water.Evenly be injected to after the water atomization on the dust granules in the fluid bed, at first, drop makes the particle of collision contact moistening and accumulate in and form particle core, i.e. ultra-fine grain aggregate around own; Simultaneously, drop adheres to a large amount of fine particle and drying and consolidating at the surface deposition of particle core, and forming larger particles is the aggregate of carrier; Along with the continuation deposition of drop, aggregate is nuclear with the centrophyten, adheres to layer by layer and forms the dressing structure.
In the fluidized bed prilling process, the size of fluidizing velocity has determined the granular size after the granulation, can distribute and the different fluidizing velocity of other demands of different selection according to smoke granularity.
The flue gas of accomplishing granulation process carries dust through carrying out dedusting in the flue 4 entering electrostatic precipitator 5, and flue gas after being purified is sent into smoke stack emission through air-introduced machine 6.
Embodiment 2:
Utilize the white lime slurries to reduce discharging superfine particulate matter technology as the ash-laden gas that binding agent carries out granulation.
Ash-laden gas is upwards got in the fluidized-bed reactor 3 through smoke distribution device 1 by gas approach 12.Water is mixed with a certain amount of hydrated lime in powder; In agitator 7, process concentration of slurry and be 1～15% lime slurry; Slush pump 8 is taken out from the lime slurry of agitator 7 pipeline 8 of flowing through; Send in the feed liquid atomizer 2 of fluidized-bed reactor 3 inside, by the compressed air from air compressor 10 it is atomized, superfine particulate matter passes through chain reunion, surface adhesion or dressing mode etc. by drop or particle capture; Thereby make dust granules realize that in fluidized-bed reactor 3 fluidization granulation grows up, larger particles falls in the ash bucket 10.
In the present embodiment, the binding agent of employing is the lime slurry with certain viscosity.Evenly be injected in the fluid bed after the lime slurry atomizing, each lime white drop forms " seed grain ", at first, " seed grain " make the particle of contact moistening and accumulate in own around, form the cluster of grains aggressiveness; Simultaneously, be dropped on " seed grain " surface by the lime slurry that continues to spray into again and produce bridging action, make between " seed grain ", mutually combine between " seed grain " and the fluid bed endoparticle, grow up bigger particle gradually.After the drying, intergranular liquid is built bridge and is become the solid bridge formation, formation porous, the particle that specific area is bigger.
The flue gas of accomplishing granulation process carries dust through carrying out dedusting in the flue 4 entering electrostatic precipitator 5, and flue gas after being purified is sent into smoke stack emission through air-introduced machine 6.
Claims (6)
1. an ash-laden gas reduces discharging the system of superfine particulate matter; It is characterized in that it comprises fluidized-bed reactor, fluidized-bed reactor is vertically to be provided with; Its underpart is connected with gas approach; Air inlet place at fluidized-bed reactor is provided with the smoke distribution device, in fluidized-bed reactor, is provided with feed liquid atomizing device; The outlet of fluidized-bed reactor is connected with conventional cleaner; The flue dust that carries with flue gas in the fluidized bed prilling reactor is a feed particles; With the flue gas is fluidizing agent; Through the feed liquid that sprays into the soot dust granule granulation is grown up; Particle after growing up falls into the ash bucket of fluidized bed prilling reactor bottom, and the residue ash-laden gas then gets into conventional cleaner again and carries out dedusting.
2. the system of claim 1 is characterized in that, said fluidized-bed reactor cross sectional shape is square or cylindrical.
3. the system of claim 1 is characterized in that, said feed liquid atomizing device comprises that as for the feed liquid atomizer in the fluidized-bed reactor, this feed liquid atomizer is connected with the slurries pipeline, and the slurries pipeline is connected with slush pump, and slush pump is connected with agitator.
4. the system of claim 1 is characterized in that, said feed liquid atomizer also is connected with air compressor.
5. the system of claim 1 is characterized in that, said cleaner is dust removal with machine device or electrostatic precipitator or is filtering dust-arrester.
6. the system of claim 1 is characterized in that, said fluidized-bed reactor bottom is provided with ash bucket.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220100938 CN202605937U (en) | 2012-03-16 | 2012-03-16 | System for reducing discharge of ultrafine particles in ash-laden gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220100938 CN202605937U (en) | 2012-03-16 | 2012-03-16 | System for reducing discharge of ultrafine particles in ash-laden gas |
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| CN202605937U true CN202605937U (en) | 2012-12-19 |
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| CN 201220100938 Expired - Fee Related CN202605937U (en) | 2012-03-16 | 2012-03-16 | System for reducing discharge of ultrafine particles in ash-laden gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102527184A (en) * | 2012-03-16 | 2012-07-04 | 山东大学 | Method and system for discharge reduction of superfine particulate matters in dusty flue gas |
| CN104307279A (en) * | 2014-11-12 | 2015-01-28 | 广西天源生物之本环保科技有限公司 | Wet dust removal and waste heat recovery device |
| CN111804107A (en) * | 2020-07-21 | 2020-10-23 | 常德市正邦建筑装饰材料有限公司 | Negative pressure dust removal system for iron oxide pigment production line |
-
2012
- 2012-03-16 CN CN 201220100938 patent/CN202605937U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102527184A (en) * | 2012-03-16 | 2012-07-04 | 山东大学 | Method and system for discharge reduction of superfine particulate matters in dusty flue gas |
| CN104307279A (en) * | 2014-11-12 | 2015-01-28 | 广西天源生物之本环保科技有限公司 | Wet dust removal and waste heat recovery device |
| CN111804107A (en) * | 2020-07-21 | 2020-10-23 | 常德市正邦建筑装饰材料有限公司 | Negative pressure dust removal system for iron oxide pigment production line |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20121219 Termination date: 20200316 |
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| CF01 | Termination of patent right due to non-payment of annual fee |