CN106979514A - A kind of sunken bed ballast group fluid bed and its application method for using super-low calorific value fuel - Google Patents
A kind of sunken bed ballast group fluid bed and its application method for using super-low calorific value fuel Download PDFInfo
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- CN106979514A CN106979514A CN201710390950.3A CN201710390950A CN106979514A CN 106979514 A CN106979514 A CN 106979514A CN 201710390950 A CN201710390950 A CN 201710390950A CN 106979514 A CN106979514 A CN 106979514A
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- 239000000446 fuel Substances 0.000 title claims abstract description 46
- 239000012530 fluid Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 33
- 238000002485 combustion reaction Methods 0.000 claims abstract description 20
- 238000009826 distribution Methods 0.000 claims abstract description 20
- 239000002355 dual-layer Substances 0.000 claims abstract description 8
- 239000000779 smoke Substances 0.000 claims abstract description 5
- 210000004916 vomit Anatomy 0.000 claims abstract description 4
- 230000008673 vomiting Effects 0.000 claims abstract description 4
- 239000003245 coal Substances 0.000 claims description 31
- 239000002245 particle Substances 0.000 claims description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 239000003546 flue gas Substances 0.000 claims description 15
- 239000003818 cinder Substances 0.000 claims description 11
- 239000000839 emulsion Substances 0.000 claims description 10
- 239000010802 sludge Substances 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 239000008187 granular material Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 210000000038 chest Anatomy 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 2
- 239000010410 layer Substances 0.000 claims 1
- 238000005243 fluidization Methods 0.000 abstract description 11
- 238000005299 abrasion Methods 0.000 abstract description 10
- 238000005303 weighing Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 239000002956 ash Substances 0.000 description 32
- 238000006722 reduction reaction Methods 0.000 description 9
- 238000006477 desulfuration reaction Methods 0.000 description 8
- 235000019738 Limestone Nutrition 0.000 description 7
- 239000006028 limestone Substances 0.000 description 7
- 230000001603 reducing effect Effects 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- RJIWZDNTCBHXAL-UHFFFAOYSA-N nitroxoline Chemical compound C1=CN=C2C(O)=CC=C([N+]([O-])=O)C2=C1 RJIWZDNTCBHXAL-UHFFFAOYSA-N 0.000 description 5
- 230000004224 protection Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 230000002349 favourable effect Effects 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 101000911390 Homo sapiens Coagulation factor VIII Proteins 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000010884 boiler slag Substances 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 102000057593 human F8 Human genes 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000000116 mitigating effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229940047431 recombinate Drugs 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/22—Fuel feeders specially adapted for fluidised bed combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2206/00—Fluidised bed combustion
- F23C2206/10—Circulating fluidised bed
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention discloses a kind of sunken bed ballast group fluid bed and its application method for using super-low calorific value fuel, including burner hearth, isobaric air compartment is provided with below burner hearth, and connected by small blast cap air distribution plate with isobaric air compartment, its top is provided with high-order pipe laying, its smoke outlet sets scroll casing separator, scroll casing separator is connected at burner hearth returning charge mouth by the U-shaped material returning device of selectivity, the U-shaped material returning device side of selectivity is additionally provided with vomit pipe, breaker is provided with the charging aperture of burner hearth, breaker outlet is provided with Dual-layer screen plate, the mesh aperture of Dual-layer screen plate is respectively 6mm and 4mm, the outlet of lower floor screen plate and lower section are connected in agitator by two belt feeders of weighing respectively, agitator outlet is to charging aperture.The present invention greatly improves spoil, clinker into grey performance, reduces fluidized air blower pressure head energy-conservation and reduces combustion chamber abrasion, the interior fluidisation of bed is uniform and stable, and excess air coefficient is small, NOXReduce.
Description
Technical field
The invention belongs to fluidized bed combustion equipment technical field, and in particular to a kind of sunken bed pressure for using super-low calorific value fuel
Recombinate fluid bed and its application method.
Background technology
Our national environmental protections are to Coal Clean combustion requirements more and more higher, and more than the 300 kilometers coals far transported are usually low
Grey cleaning high heating value coal：Coal washing, with the innovation and development of coal-washing technique, coal washery output to wash cash calorific value more and more lower, it is low
Position calorific capacity below 1000 kilocalories greatly/kilogram；The coal slime calorific value of coal washery output is also more and more lower simultaneously, the coal of 35% moisture
Mud low heat value less than 1500 kilocalories/kilogram.
Now the boiler of coal washing Gangue Power Plant use spoil calorific value all 1800 kilocalories/kilogram more than；Coal slime calorific value is all
2500 kilocalories/kilogram more than.This results in coal washery, and on the one hand the stacking that need to take over the land for use of substantial amounts of spoil, coal slime becomes waste, separately
On the one hand the spoil matched somebody with somebody, coal slime power plant use substantial amounts of middle coal (mixing burning spoil), environment are not only polluted, while wasting energy again
Source, adds the power generation and heat supply cost of enterprise.
Coal chemical industry and chemical fertilizer manufacturing enterprise produce substantial amounts of gas-making cinder, its calorific value it is general 1500 kilocalories/kilogram or so；
The chain clinker that northern a large amount of heating chain-grate boilers are produced, its calorific value it is general more than 1200 kilocalories/kilogram or so.Due to former
Boiler combustion technology can only be mixed with the raw coal of higher thermal value burning gas making slag, substantial amounts of chain clinker can only be used for pave the way, cause
A large amount of wastes of low-phase energy.
Papermaking and printing and dyeing enterprise produce a large amount of sludge, its calorific value it is general more than 600 kilocalories/kilogram or so, also compel to be essential
Handle.
Use low heat value fluidized-bed combustion boiler now, no matter bubbling bed or fast bed because emulsion zone bed particle is thicker
Run using high blast, excess air coefficient is big, low heat value spoil, clinker fuel are into grey poor performance, coal slime returning charge amount of burning
Main bed is caused very much to stop working greatly, so can not be using the operation of high rate cyclic material, raw emissions NOXIn 400-500mg/m3More than,
For flue gas qualified discharge, environmentally friendly operating cost remains high.
The super-low calorific value such as gangue, clinker, coal slime, sludge fuel is burnt down entirely in fluid bed internal combustion, and the steam of generation can be supplied
Heat, while producing substantial amounts of electric energy, produced lime-ash or cement industry building materials raw material can produce huge economic and society
Benefit.
Conventional fluidization bed combustor emulsion zone fluidised form design stationary state region is tri- kinds of 0-8mm, 0-10mm, 0-13mm, it is impossible to
Adapt to the abundant burning of low burn value fuel.
The content of the invention
The technical problem to be solved in the present invention is：There is provided a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel and
Its application method, it is 0-6mm to realize emulsion zone fuel particle diameter, improves spoil, clinker into grey performance, reduces fluidized air blower pressure head section
Combustion chamber abrasion and can be reduced, and fluidisation is uniform and stable in bed, and excess air coefficient is small, and anoxycausis inhibits NOXProduction
It is raw, fluidised bed material balance system is formed the circulation of thinner material, fine ash concentration is high, extend reducing atmosphere height,
Reduction reaction reduces NOXDischarge, particle mean size, which attenuates, can reduce limestone granularity, increasing specific surface area, strengthen taking off in stove
Sulphur efficiency, the equipment flue gas for combustion low calorie fuels is further administered, greatly the environmentally friendly operating cost of reduction flue gas qualified discharge, with
Solve problems of the prior art.
The technical scheme that the present invention takes is：A kind of sunken bed ballast group fluid bed for using super-low calorific value fuel, including stove
Isobaric air compartment is provided with below thorax, burner hearth, and is connected by small blast cap air distribution plate with isobaric air compartment, its top is provided with a high position and buried
Pipe, its smoke outlet sets scroll casing separator, and scroll casing separator is connected to burner hearth returning charge mouth by the U-shaped material returning device of selectivity
Place, the U-shaped material returning device side of selectivity, which is additionally provided with vomit pipe, the charging aperture of burner hearth, is provided with breaker, and breaker goes out
Mouth is provided with Dual-layer screen plate, and the mesh aperture of Dual-layer screen plate is respectively 6mm and 4mm, the outlet of lower floor's screen plate
And lower section is connected in agitator by two belt feeders of weighing respectively, the charging aperture of agitator outlet to burner hearth.
It is preferred that, above-mentioned upper strata screen plate outlet reclaims conveying device by belt and is connected to breaker entrance.
It is preferred that, above-mentioned high-order pipe laying is located in burner hearth at 670-785mm.
It is preferred that, above-mentioned scroll casing separator is using the entrance that has a down dip, and porch, which is set, lengthens accelerating sections, scroll casing separator upper end
Air exit in setting.
It is preferred that, above-mentioned U-shaped material returning device uses U-shaped returning charge valve, including two outlets, and one is connected to burner hearth returning charge mouth,
Another selective ash-removing mouth is connected to lime-ash cooling device and reclaims heat.
It is preferred that, air distribution plate is provided with returning charge mouth in above-mentioned burner hearth puts the cold cinder notch of fine ash.
It is preferred that, a diameter of 50mm of blast cap of above-mentioned small blast cap air distribution plate, air-permeating hole a diameter of 5mm on blast cap are adjacent
Spacing is 70mm between blast cap.
It is preferred that, above-mentioned burner hearth is using single backhaul large-diameter or three backhaul pyknics.
It is preferred that, a kind of above-mentioned application method for the sunken bed ballast group fluid bed for using super-low calorific value fuel, this method bag
Include：Air compartment is set to isobaric air compartment in burner hearth, and air compartment import medium is that natural air and the tail flue gas less than 30% proportion are mixed
With coal slime or sludge are added by roof of the furnace, and gangue or clinker ultra-low heat value fuel are added from burner hearth side feed opening and flowed
Change on the small blast cap air distribution plate in bed bottom, the particle diameter of ultra-low heat value fuel is controlled by the double-deck screen plate of breaker,
The a diameter of 0-6mm of grain, wherein particle diameter are less than 4mm accountings and are more than 80%, and particle diameter is that 4-6mm accountings are less than 20%, is added up to
100%, by controlling fluidized bed pressure, coarse granule burns in burner hearth emulsion zone, and fine grained enters the long flow burner hearth of top low flow velocity
Burning：Flow velocity 3-4m/s, long flow makes burning time 6-8s；Fine grained enters burner hearth outer spiral casing separator, warp after burner hearth
Have a down dip entrance and the lengthening accelerating sections of scroll casing separator are crossed, realizes that fine ash is separated, fine ash particle diameter d50=10-12 microns, fine ash separation
The laggard U-shaped material returning device of selectable, separates flying dust to control dilute-phase zone bed by the selective ash-removing mouth of the U-shaped material returning device of selectivity
Pressure and regulation fine ash circulating ratio, while fluidized bed air distribution plate rear portion sets selectivity to put grey cinder notch regulation bed pressure close to returning charge mouth
With auxiliary adjustment fine ash circulating ratio.
Beneficial effects of the present invention：Compared with prior art, effect of the invention is as follows：
（1）The present invention realizes particle diameter after the breaker with double-deck screen plate, crushing and screening are set at fuel feed inlet
For 0-6mm, and feed back proportioning less than 4mm and 4-6mm two kinds of particles respectively using two belt feeders of weighing, less than 4mm
Particle difference proportion with 4-6mm is, more than 80% and less than 20%, to greatly improve spoil, clinker into grey performance, not only reduce stream
Wind transmission compressing head saves and reduced combustion chamber abrasion, and fluidisation is uniform and stable in bed, using isobaric air compartment, and control air contains
Amount, excess air coefficient is small, and anoxycausis inhibits NOXGeneration, and using scroll casing separator and the U-shaped material returning device shape of selectivity
Into fluid bed balance system, the circulation of thinner material, recycle stock median d are controlled50=10-12 microns, average grain diameter 100
Micron, reduces combustor tail abrasion, and fine ash concentration is high, extends reducing atmosphere height, and reduction reaction reduces NOXRow
Put, particle mean size, which attenuates, can reduce limestone granularity, increasing specific surface area, strengthen desulfuration in furnace efficiency；For combustion low heat value combustion
The equipment flue gas of material is further administered, greatly the environmentally friendly operating cost of reduction flue gas qualified discharge；
（2）The present invention is adapted to use gangue, clinker, coal slime, sludge, and ultra-low heat value fuel is experimentally confirmed, and it is used
Expect gangue, clinker low heat valve be more than 800 kilocalories/kilogram, coal slime low heat valve be more than 1100 kilocalories/kilogram, sludge
（Mix burning）Low heat valve be more than 600 kilocalories/kilogram under conditions of, fluid unit not only reduce fluidized air blower pressure head energy-conservation and
Combustion chamber abrasion is reduced, and fluidisation is uniform in bed, operation steady in a long-term, high combustion efficiency, while solving afterbody well
The problem of abrasion, combustion apparatus raw emissions NOXIn 200mg/m3Hereinafter, low-volatility fuel raw emissions NOX is in 100mg/m3
Hereinafter, minimum discharge, NO can be accomplished by SCR, SNCR denitration processingxLess than 50mg/m3, using microlith lime stone desulfuration in furnace
Effect is good, and the environmentally friendly operating cost of enterprise's qualified discharge is substantially reduced；
（3）The present invention uses small blast cap air distribution plate, and blast cap quantity is more, exhaust vent is small, wind velocity is high, adds granularity small, it is ensured that
The uniformity of the goods fluid uniformity and temperature in bed, suppresses NOXYield；
（4）Emulsion zone bed pressure affluence degree depends on the weight of maximum fuel, and such as 8mm weight is 1.77 times of 6mm, 10mm weight
It is 2.77 times of 6mm, so the particle diameter 0-6mm of fuel, low with respect to bed pressure affluence degree needed for other fluid beds, air blast power consumption
It is few, select to put the cold cinder notch auxiliary adjustment boiler fly ash internal circulating load of fine ash close to returning charge mouth in combustion process；
（5）The structure of burner hearth uses the long flow of low flow velocity：Flow velocity 3-4m/s, long flow makes burning time 6-8s, and its heating surface is applied
Lid wall with refractory lining, refracto, the long burning time of chamber structure is not only favourable to being difficult to the ultra-low heat value fuel after-flame of after-flame, and on burner hearth
Portion's red-hot carbon granule of high concentration fine ash is formd to NOXStrong reducing property condition, reduction reaction greatly reduces NOXDischarge capacity.Average grain
Degree attenuates and can reduce limestone granularity, increasing specific surface area, strengthens desulfuration in furnace efficiency；
（6）The cold cinder notch of fine ash and the U-shaped material returning device of selectivity and stove are put close to returning charge mouth setting selectivity in burner hearth air distribution plate rear portion
The combination of thorax outer spiral casing separator, had not only realized and has efficiently separated but also reduce flying dust share；
（7）The U-shaped material returning device of selectivity is different from conventional boiler, because fuel phosphorus content itself is very low, unburned carbon in flue dust in flue gas
It is relatively also not high, to avoid substantial amounts of flying dust disposable with flue gas venting and the back-end surfaces that wear and tear, therefore, using selective U
Type material returning device, U-shaped device has two outlets, and one of them puts grey outlet for selectivity, and the ash of releasing enters lime-ash cooling device and returned
Receive heat.
Brief description of the drawings
Fig. 1 is three backhaul pyknic fluidized-bed structure schematic diagrames；
Fig. 2 is single backhaul large-diameter fluidized-bed structure schematic diagram；
Fig. 3 is structural representation at breaker；
Fig. 4 is the A-A cross-sectional views in Fig. 1.
Embodiment
Below in conjunction with the accompanying drawings and the present invention is described further specific embodiment.
Embodiment 1：As Figure 1-Figure 4, a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel, including burner hearth
1, the lower section of burner hearth 1 is provided with isobaric air compartment 2, and is connected by small blast cap air distribution plate 3 with isobaric air compartment 2, and its top is provided with height
Position pipe laying 4, its smoke outlet sets scroll casing separator 5, and scroll casing separator 5 is connected to burner hearth by the U-shaped material returning device 6 of selectivity
At returning charge mouth 7, the U-shaped side of material returning device 6 of selectivity, which is additionally provided with vomit pipe 8, the charging aperture 9 of burner hearth 1, is provided with breaker
10, the outlet of breaker 10 is provided with Dual-layer screen plate 11, the mesh aperture of Dual-layer screen plate 11 be respectively 6mm and
4mm, lower floor's screen plate 11 is exported and lower section is connected in agitator 13 by two belt feeders 12 of weighing respectively, agitator
13 outlets are to the charging aperture of burner hearth 1.
The present invention is a kind of complete sunken bed ballast for adapting to use the ultra-low heat value fuel such as gangue, clinker, coal slime, sludge
Group fluid bed, energy-conservation, stably, high efficiency, light abrasion, the environmentally friendly operating cost of enterprise's qualified discharge is low, and flue gas is further
Minimum discharge requirement is met after improvement.
The present invention changes conventional fluidization bed fluidised form design stationary state region, and the design of conventional fluidization bed combustor emulsion zone fluidised form is fixed
State region is tri- kinds of 0-8mm, 0-10mm, 0-13mm, and low heat value spoil, clinker fuel change the close phase of fluid bed into grey poor performance
It is 0-6mm after area's fluidised form design restructuring, improves spoil, clinker into grey performance, not only reduce fluidized air blower pressure head to reach section
Combustion chamber abrasion and can be reduced, and fluidisation is uniform and stable in bed, and excess air coefficient is small, and anoxycausis inhibits NOX production
It is raw.Two be restructuring material balance system, by improving separative efficiency of the burner hearth outer spiral casing separator to thinner material, makes fluid bed
Material balance system can form the circulation of thinner material.Conventional fluidization bed flying dust median d50=20 microns, improve separator pair
Flying dust median d after fine ash separative efficiency50=10-12 microns, 100 microns of average grain diameter.Particle mean size, which attenuates, can not only drop
Low limestone granularity, increasing specific surface area strengthens desulfuration in furnace efficiency.And because soot particle is thin, low speed flue gas can be carried more
Many materials realize that moderate multiplying factor recycle stock is run, and ash concentration is high on the contrary, extend reducing atmosphere height, and reduction reaction is reduced
NOXDischarge.Above-mentioned fluid bed can realize raw emissions NOXIn 200mg/m3Hereinafter, accomplish to surpass by SCR, SNCR denitration processing
Low emission：NOx is less than 50mg/m3, enterprise carry out flue gas further administer minimum discharge environmentally friendly operating cost it is low.
It is preferred that, the above-mentioned outlet of upper strata screen plate 11 reclaims conveying device by belt and is connected to the entrance of breaker 10,
Realize the recycle and reuse of bulky grain.
It is preferred that, above-mentioned high-order pipe laying 4 is located in burner hearth 1 at 670-785mm, by reducing bed particle diameter i.e. weight
And speed, impact kinetic energy is reduced to mitigate buried pipe abrasion.
It is preferred that, above-mentioned scroll casing separator 5 is using the entrance that has a down dip, and porch, which is set, lengthens accelerating sections 14, scroll casing separator 5
Upper end sets upper air exit.
It is preferred that, above-mentioned U-shaped material returning device 6 uses U-shaped returning charge valve, including two outlets, and one is connected to burner hearth returning charge mouth
7, another selective ash-removing mouth is connected to lime-ash cooling device and reclaims heat.
It is preferred that, air distribution plate is provided with returning charge mouth in above-mentioned burner hearth 1 puts the cold cinder notch of fine ash, puts the cold cinder notch of fine ash auxiliary
Help regulation boiler fly ash internal circulating load.
It is preferred that, a diameter of 50mm of blast cap of above-mentioned small blast cap air distribution plate 3, air-permeating hole a diameter of 5mm on blast cap are adjacent
Spacing is 70mm between blast cap.
It is preferred that, above-mentioned burner hearth 1 is using single backhaul large-diameter or three backhaul pyknics, and the structure of burner hearth is long using low flow velocity
Flow：Flow velocity 3-4m/s, long flow makes burning time 6-8s, its heating surface mulching wall with refractory lining, refracto, the long burning time of chamber structure
It is not only favourable to being difficult to the ultra-low heat value fuel after-flame of after-flame, and the red-hot carbon granule of upper furnace high concentration fine ash forms pair
NOX strong reducing property condition, reduction reaction greatly reduces DS NOx Est amount.Particle mean size, which attenuates, can reduce limestone granularity, carry
High-specific surface area, strengthens desulfuration in furnace efficiency.
Embodiment 2：A kind of application method for the sunken bed ballast group fluid bed for using super-low calorific value fuel, including above-mentioned one kind
The sunken bed ballast group fluid bed of super-low calorific value fuel is used, this method includes：Air compartment is set to isobaric air compartment in burner hearth, and air compartment enters
Mouth medium is that natural air and the tail flue gas less than 30% proportion are admixed, and coal slime or sludge are added by roof of the furnace, by gangue
Or clinker ultra-low heat value fuel is added on the small blast cap air distribution plate in fluid bed bottom from burner hearth side feed opening, ultra-low heat value fuel
Particle diameter is by the breaker with double-deck screen plate, and particle diameter is 0-6mm after crushing and screening, and wherein particle diameter is less than
4mm accountings are more than 80%, and particle diameter is that 4-6mm accountings are less than 20%, adds up to 100%, because reduction granularity is to being difficult to the pole of after-flame
Low calorie fuels after-flame is favourable, reduces its tail-off time, by controlling fluidized bed pressure, and coarse granule burns in burner hearth emulsion zone,
Fine grained enters the long flow hearth combustion of top low flow velocity：Flow velocity 3-4m/s, long flow makes burning time 6-8s；Fine grained passes through
Enter burner hearth outer spiral casing separator after burner hearth, by have a down dip entrance and the lengthening accelerating sections of scroll casing separator, realize that fine ash is separated,
Fine ash particle diameter d50=10-12 microns, fine ash separates the laggard U-shaped material returning device of selectable, by the selection of the U-shaped material returning device of selectivity
Property ash-removing mouth separation flying dust to control dilute-phase zone bed to press and regulation fine ash circulating ratio, while fluidized bed air distribution plate rear portion is close to returning
Material mouth sets selectivity to put grey cinder notch regulation bed pressure and auxiliary adjustment fine ash circulating ratio.
Mud, sludge are added by roof of the furnace, and the ultra-low heat value such as gangue, clinker fuel is added into the small blast cap in fluid bed bottom
On air distribution plate, the particle diameter 0-6mm of fuel：Wherein it is less than 4mm accountings and is more than 80%, 4-6mm accountings less than 20%；Due to using
Larger bed inner area and thinner fuel particle, can use can ensure fluidisation operation compared with sunken bed pressure affluence degree, fluidize elegance
With isobaric wind indoor fresh air+part tail flue gas；It can ensure in emulsion zone bed to be anoxycausis, reduce NOXYield.
Coarse granule is complete in emulsion zone burning, and its partial exothermic is received by high-order pipe laying, and fine grained enters the long stream of low flow velocity
Journey burner hearth：Flow velocity 3-4m/s, long flow makes burning time 6-8s, its heating surface mulching wall with refractory lining, refracto, the long flow combustion of chamber structure
The burning time is not only favourable to being difficult to the ultra-low heat value fuel after-flame of after-flame, and the red-hot carbon granule of upper furnace high concentration fine ash is formed
To NOXStrong reducing property condition, reduction reaction greatly reduces NOXDischarge capacity.Particle mean size, which attenuates, can reduce limestone particle
Degree, increasing specific surface area strengthens desulfuration in furnace efficiency.
Fine grained enters burner hearth outer spiral casing separator after burner hearth, adds because separator is lengthened using the entrance that has a down dip, band
Fast section spiral case separation, upper exhaust structure are high for the separator of the more conventional fluid bed of separative efficiency of superfine circulation bed；Ensure
Fine ash separation, particle diameter d50=10-12 microns, while mitigating back-end surfaces abrasion.The laggard selectable of fine ash separation is U-shaped to be returned
Glassware：The U-shaped material returning device of selectivity has two outlets, and one of them puts grey outlet, the U-shaped returning charge valve of selectivity and burner hearth for selectivity
The combination of outer spiral casing separator, had not only realized and has efficiently separated but also reduce flying dust share, and the ash of releasing enters lime-ash cooling device
Heat is reclaimed, while air distribution plate rear portion sets selectivity to put grey cinder notch regulation bed pressure and the circulation of auxiliary adjustment fine ash close to returning charge mouth
Multiplying power.
Experimental verification example：By taking six disk extreme misery paving coal washing spoil power plant as an example, 3 12MW generating sets of the factory, first wife 3
75t/h Wuxis boiler factory CFBB, crude fuel use in coal+coal slime, middle calorific value of coal 4000kcal/kg with
On, coal slime caloric value is in more than 2600kcal/kg.With the upgrading of coal cleaning process, gangue caloric value is reduced to 800-
1500kcal/kg, coal slime caloric value is reduced to 1100-1500kcal/kg, and boiler can not be run, 2015, will using above-mentioned technology
Wherein 2 boiler improvements are sent out into sunken bed ballast group fluid bed, actual motion gangue caloric value 800-1200kcal/kg, coal slime
Heat is 1100-1500kcal/kg, and boiler combustion is stable, and parameters all reach design requirement, and bed presses 5000-5800Pa
It is warm can stably at 850 °C -920 °C, unburned carbon in flue dust in 3-6%, boiler slag carbon content in 1-2%, exhaust gas temperature at 120-130 °C,
It is not added with flue gas fluidisation raw emissions NOXIn 130mg/m3Hereinafter, smoke adding air-flow raw emissions NOXIn 80mg/m3Hereinafter, boiler
Desulfuration in furnace is not used, and desulfurization by lime gypsum method is only used outside stove.
The foregoing is only a specific embodiment of the invention, but protection scope of the present invention is not limited thereto, any
Those familiar with the art the invention discloses technical scope in, change or replacement can be readily occurred in, should all be contained
Cover within protection scope of the present invention, therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (9)
1. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel, it is characterised in that：Including burner hearth（1）, burner hearth（1）Under
Side is provided with isobaric air compartment（2）, and pass through small blast cap air distribution plate（3）With isobaric air compartment（2）Connection, its top is provided with a high position and buried
Pipe（4）, its smoke outlet setting scroll casing separator（5）, scroll casing separator（5）Pass through the U-shaped material returning device of selectivity（6）It is connected to
Burner hearth returning charge mouth（7）Place, the U-shaped material returning device of selectivity（6）Side is additionally provided with vomit pipe（8）, burner hearth（1）It is provided with charging aperture
Breaker（10）, breaker（10）Outlet is provided with Dual-layer screen plate（11）, Dual-layer screen plate（11）Net
Hole aperture is respectively 6mm and 4mm, lower floor's screen plate（11）Outlet and lower section are weighed belt feeder by two respectively（12）Even
It is connected to agitator（13）It is interior, agitator（13）Outlet is to burner hearth（1）Charging aperture（9）.
2. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 1, it is characterised in that：On
Layer screen plate（11）Conveying device is reclaimed by belt and is connected to breaker in outlet（10）Entrance.
3. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 1, it is characterised in that：It is high
Position pipe laying（4）Positioned at burner hearth（1）At interior 670-785mm.
4. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 1, it is characterised in that：Snail
Shell separator（5）Using the entrance that has a down dip, porch, which is set, lengthens accelerating sections（14）, scroll casing separator（5）Upper end is vented on setting
Outlet.
5. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 1, it is characterised in that：U
Type material returning device（6）Using U-shaped returning charge valve, including two outlets, one is connected to burner hearth（1）Burner hearth returning charge mouth（7）, another
Selective ash-removing mouth is connected to lime-ash cooling device and reclaims heat.
6. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 5, it is characterised in that：Stove
Thorax（1）Interior air distribution plate is provided with returning charge mouth puts the cold cinder notch of fine ash.
7. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 5, it is characterised in that：It is small
Blast cap air distribution plate（3）The a diameter of 50mm of blast cap, a diameter of 5mm of air-permeating hole on blast cap, spacing is 70mm between adjacent blast cap.
8. a kind of sunken bed ballast group fluid bed for using super-low calorific value fuel according to claim 1, it is characterised in that：Stove
Thorax（1）Using single backhaul large-diameter or three backhaul pyknics.
9. according to a kind of user of any described sunken bed ballast group fluid beds for using super-low calorific value fuel of claim 1-8
Method, it is characterised in that：This method includes：Air compartment is set to isobaric air compartment in burner hearth, and air compartment import medium is natural air and small
Admixed in the tail flue gas of 30% proportion, coal slime or sludge adds by roof of the furnace, by gangue or clinker ultra-low heat value fuel from
Burner hearth side feed opening is added on the small blast cap air distribution plate in fluid bed bottom, and the particle diameter of ultra-low heat value fuel passes through breaker
Double-deck screen plate control, particle diameter is 0-6mm, wherein particle diameter be less than 4mm accountings be more than 80%, particle diameter is 4-
6mm accountings are less than 20%, add up to 100%, by controlling fluidized bed pressure, and coarse granule burns in burner hearth emulsion zone, and fine grained enters
The long flow hearth combustion of top low flow velocity：Flow velocity 3-4m/s, long flow makes burning time 6-8s；Fine grained enters after burner hearth
Burner hearth outer spiral casing separator, by have a down dip entrance and the lengthening accelerating sections of scroll casing separator, realizes that fine ash is separated, fine ash particle diameter d50
=10-12 microns, fine ash separates the laggard U-shaped material returning device of selectable, by the selective ash-removing mouth point of the U-shaped material returning device of selectivity
From flying dust to control dilute-phase zone bed to press and regulation fine ash circulating ratio, selected while fluidized bed air distribution plate rear portion is set close to returning charge mouth
Selecting property puts grey cinder notch regulation bed pressure and auxiliary adjustment fine ash circulating ratio.
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| CN107965773A (en) * | 2017-10-30 | 2018-04-27 | 贵州新能源开发投资股份有限公司 | A kind of fluid bed heating center for using low calorie fuels and its application method |
| CN110043894A (en) * | 2017-10-27 | 2019-07-23 | 湘潭锅炉有限责任公司 | A kind of quasi- eastern coal circulating fluidized bed boiler |
| CN110052156A (en) * | 2019-04-01 | 2019-07-26 | 浙江菲达环保科技股份有限公司 | A kind of Hg, SO based on active carbon and flying dust bubbling bed3Cooperation-removal device |
| CN111396864A (en) * | 2020-04-01 | 2020-07-10 | 太原锅炉集团有限公司 | Circulating fluidized bed boiler capable of realizing ultralow emission of nitrogen oxide and sulfur dioxide |
| CN114046497A (en) * | 2021-11-17 | 2022-02-15 | 广东绿壳新能源有限公司 | Circulating fluidized bed boiler capable of reducing NOX discharge amount |
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