CN109340743A - A kind of duff grain circulating fluidized bed boiler - Google Patents
A kind of duff grain circulating fluidized bed boiler Download PDFInfo
- Publication number
- CN109340743A CN109340743A CN201811149691.6A CN201811149691A CN109340743A CN 109340743 A CN109340743 A CN 109340743A CN 201811149691 A CN201811149691 A CN 201811149691A CN 109340743 A CN109340743 A CN 109340743A
- Authority
- CN
- China
- Prior art keywords
- fluidized bed
- circulating fluidized
- bed boiler
- section
- boiler according
- 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.)
- Granted
Links
- 238000002347 injection Methods 0.000 claims abstract description 67
- 239000007924 injection Substances 0.000 claims abstract description 67
- 239000002245 particle Substances 0.000 claims abstract description 32
- 239000003245 coal Substances 0.000 claims abstract description 30
- 235000019738 Limestone Nutrition 0.000 claims abstract description 10
- 239000006028 limestone Substances 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims description 67
- 238000002485 combustion reaction Methods 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 18
- 239000002826 coolant Substances 0.000 claims description 14
- 230000001154 acute effect Effects 0.000 claims description 9
- 230000002441 reversible effect Effects 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 6
- 239000004744 fabric Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 241000237858 Gastropoda Species 0.000 claims 1
- 238000005452 bending Methods 0.000 claims 1
- 235000019504 cigarettes Nutrition 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 12
- 238000006477 desulfuration reaction Methods 0.000 abstract description 10
- 238000010438 heat treatment Methods 0.000 abstract description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 230000023556 desulfurization Effects 0.000 abstract description 5
- 239000003500 flue dust Substances 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 27
- 239000003546 flue gas Substances 0.000 description 27
- 239000000428 dust Substances 0.000 description 22
- 239000002956 ash Substances 0.000 description 12
- 239000000463 material Substances 0.000 description 12
- 230000007423 decrease Effects 0.000 description 9
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 7
- 229910052698 phosphorus Inorganic materials 0.000 description 7
- 239000011574 phosphorus Substances 0.000 description 7
- 230000009467 reduction Effects 0.000 description 7
- 238000005299 abrasion Methods 0.000 description 6
- 230000033001 locomotion Effects 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 239000002893 slag Substances 0.000 description 5
- 238000009826 distribution Methods 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 230000003134 recirculating effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000000149 penetrating effect Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000010079 rubber tapping Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 241000937378 Everettia interior Species 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 210000000038 chest Anatomy 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011044 inertial separation Methods 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000003340 mental effect Effects 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C11/00—Accessories, e.g. safety or control devices, not otherwise provided for, e.g. regulators, valves in inlet or overflow ducting
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L9/00—Passages or apertures for delivering secondary air for completing combustion of fuel
-
- 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 duff grain circulating fluidized bed boiler, including burner hearth, primary air system, secondary air system, separator and back-end ductwork, the circulating fluidized bed boiler, which uses, shunts cyclone separator, cyclone separator is shunted in particular by multistage injection, its separative efficiency can be significantly increased, unburned carbon in flue dust can significantly reduce, again by to coal partial size, limestone particle size, the reconstruct of one Secondary Air parameter and structure, this equipment is run under high underload all has burning, desulfurization and nitric efficiency are high, blast cap and heating surface wear are small in furnace, one, the Secondary Air performance that low energy consumption.
Description
Technical field
The invention belongs to field of boilers, are related to a kind of circulating fluidized bed boiler more particularly to a kind of duff grain circulating combustion
Circulating Fluidized Bed Boiler Equipment.
Background technique
Circulating fluidized bed boiler is developed from bubbling bed boiler, has more than 40 years history, it is with fluidization gas
Based on fixed double phase flow is theoretical, by adding separator, the circulating combustion of solid particle is realized, the biography of upper furnace is strengthened
Heat cancels pipe laying and increases substantially efficiency of combustion, elimination is buried while keeping bubbling bed boiler burning colm advantage
Pipe abrasion, and realize desulfuration in furnace denitrogenation, and be rapidly developed.But compared with current most widely used pulverized-coal fired boiler, still
It is low that there are efficiencies of combustion, and burner hearth internal heating surface serious wear, first and second fan energy consumption is big and desulfuration in furnace nitric efficiency is inclined
The problems such as low.
Separator is the important device in circulating fluidized bed boiler, its performance has weight to the performance of circulating fluidized bed boiler
The influence wanted.Initially use inertia separator has not been had to due to low separation efficiency, and circulating fluidized bed boiler is all adopted at present
Use high temperature cyclone separator.
Cyclone separator is the difference using gas-solid specific gravity, and the centrifugal force generated by working medium rotary motion is by solid from gas
The technology separated in body.Influence Cyclone efficiency factor be dust flow in cyclone separator suffered by from
The interaction of mental and physical efforts, gravity and drag force, when centrifugal force and gravity are greater than drag force, dust is separated, otherwise dust is carried
Cyclone separator out.
Cyclone separator is made of cylinder, cone, air inlet section, exhaust pipe and ash tube etc..The advantages of cyclone separator is
Structure is simple, small in size, movement-less part, and operation is easy to maintenance, and the pressure loss is medium, and power consumption is little；The disadvantage is that dedusting
Inefficient, efficiency of dust collection is lower when underload.
The course of work of cyclone separator is when dusty gas enters cyclone separator by tangential admission mouth, and air-flow generates
Circle rotation movement, swirling eddy the overwhelming majority along wall from cylinder twist downwardly toward cone flow, commonly referred to as this
For outer rotational gas flow.
When the outward turning gas of rotation decline reaches cone, drawn close due to the contraction of cone to deduster center.According to " rotation
Torque " invariance principle, tangential velocity are continuously improved, and centrifugal force suffered by grit is also constantly reinforced.When air-flow reaches cyclonic separation
In the middle part of device when a certain position, i.e., with same direction of rotation by lower counter steer, continuing the flowing of spinning property, i.e. interior rotational airflow.
Dusty gas generates centrifugal force in rotary course, and the grit that relative density is greater than gas is got rid of to wall.Grit
Outer swirling eddy and enter ash tube under the action of gravity near wall.Final purification gas and a part are taken by interior rotational airflow
The grit of band through exhaust pipe discharge pipe outside.
It is flowed from another small portion of gas that air inlet section flows into cyclone separator top cover, then on the outside of exhaust pipe downwards
Flowing, when reaching exhaust pipe lower end, that is, counter steer on, with rising central gas stream together from exhaust pipe discharge.It is distributed in this
Also companion is pulled away grit in partial air-flow.The air-flow of this part is referred to as short-circuit flow.It is attached that dust-exhausting port is fallen by separation
Close dust enters interior rotational airflow cocurrent air inlet-outlet pipe again and is referred to as dust back-mixing." short-circuit flow " and row under exhaust pipe near mouth
" dust back-mixing " near dirt mouth is two most important factors for influencing the Effiency of whirlwind Separator.
Particle is separated with gas in cyclone separator depends primarily on centrifugal force, centrifugal force and rotation speed square at
Direct ratio is inversely proportional with radius of turn；The escape of particle depends on drag force, and the viscosity of gas is produced in the solid particle wherein moved
Raw drag force makes its escape, and the size of drag force depends on gas viscosity and air velocity, the main influence of dust escape capability because
Element is radial velocity and moves radially distance.
The separative efficiency of ordinary cyclones separator increases with tangential increasing for rotation speed, but depositing due to short-circuit flow
, when tangential velocity be greater than 25m/s when, the intensity of short-circuit flow also increases, and causes the increment of separative efficiency very low, resistance is rapid
Increase.Therefore ordinary cyclones separator maximum tangential velocity is all selected as 25m/s or so, and centrifugal force field is with cyclone dust collectors cylinder
The increase of body diameter and reduce, separative efficiency also decreases.
Since circulating fluidized bed boiler exhaust gas volumn is huge, though high-temperature separator is using parallel arrangement, single diameter
Reach several meters of size, this makes its separative efficiency lower, by dimensionally-optimised, separate critical incising control and only reaches d99 ≈
100 μm or so, 20 μm of d50 ≈ or so.In order to guarantee that circulating fluidized bed boiler reaches high magnification Matter Transfer, boiler coal feeding partial size
Generally 0-8mm, the inner flue gas of the stove rate of climb are needed up to 5m/s or so, and between 0-700 μm, this causes to follow recycle stock partial size
The coarse granule of ring material is to burner hearth internal heating surface serious wear；Particle size of fly ash is thick and carbon content is high, and efficiency of combustion is low；While in order to
Guarantee that slag phosphorus content is low, high charge level in furnace need to be maintained, in air side, primary air ratio is 50% or so, First air compartment pressure
For 11-13KPa；In fume side, in order to guarantee separative efficiency, isolation resistance 1.5-2KPa；This results in current recycle stream
The energy consumption for sending air-introduced machine of fluidized bed boiler is much larger than pulverized-coal fired boiler.Separator is low, and primary air ratio is high, also results in and follows
Circulation fluidized bed boiler desulfuration in furnace nitric efficiency is relatively low, and low-load performance is poor.
Summary of the invention
The purpose of the present invention is to provide a kind of duff grain circulating fluidized bed boiler, using cyclone separator is shunted, especially
It is that cyclone separator is shunted using multistage injection, since their separative efficiencies have significantly than cyclone separator used at present
Improve, unburned carbon in flue dust can significantly reduce, then by to coal partial size, limestone particle size, a Secondary Air parameter and structure weight
Structure, running duff grain circulating fluidized bed boiler under high underload all has burning, desulfurization and nitric efficiency height, blast cap in furnace
It is small with heating surface wear, the primary and secondary air performance that low energy consumption.
In order to achieve the above object, solution of the invention is:
A kind of duff grain circulating fluidized bed boiler, including burner hearth, primary air system, secondary air system, separator and tail portion
Flue, the separator of the circulating fluidized bed boiler are to shunt cyclone separator, shunt cyclone separator include cylinder, cone,
Air inlet section, separation panel tracheae and ash tube.
The shunting separator of the circulating fluidized bed boiler is that multistage injection shunts cyclone separator, and multistage injection shunts rotation
Wind separator includes cylinder, cone, air inlet section, separation panel tracheae, ash tube and multistage injection unit, the multistage injection unit
Including pipeline and nozzle, the path that the nozzle is decayed along air-flow flowing and air-flow tangential velocity is in multistage arrangement, the pipe
For connecting nozzle and providing high pressure gas, the high-speed jet that the high pressure gas is ejected by the nozzle is tangential along air-flow in road
Flow direction sprays, formation injection air, and the angle of the circle tangent line of jet direction and cylinder is 20 ° -60 °.Wherein, the circle refers to
Using body centre as several concentric circles in the center of circle on the cross section of cylinder.
In the description of the present invention, " multistage " is meant that two-stage or two-stage or more, unless otherwise specifically defined.
Further, " multistage arrangement " of the present invention, which refers to, arranges institute along the path multiple spot of air-flow flowing and the decaying of air-flow tangential velocity
State nozzle, and the flow type pump with injection flow that nozzle not at the same level sprays is set as needed, can be identical or different, such as become larger or
It gradually becomes smaller.
Preferably, the nozzle is arranged on the cylinder and/or cone by multistage；It is further preferred that the nozzle
It is arranged on the cylinder and/or cone and in the air inlet section by multistage.
It is preferably 5-20 that the air inlet section for shunting separator, which is tangential or volute air-inlet, the depth-width ratio of air inlet,.It is described
The cross-sectional area of Membrane Separator Cylinder for CFB Boiler and the cross-sectional area of air inlet section outlet are shunted than being preferably 5-22.
It is described shunt separator separation panel tracheae can shunt gas, wherein can shunt gas pipeline section be referred to as shunt
Section, the tube body of the separation panel tracheae along cylinder to the direction of cone include straight section and cone section；The separation panel tracheae straight section
Diameter and the cylinder diameter than be preferably 0.5-0.7.
The shunting circulation area of the separation panel tracheae and the cross-sectional area of separation panel tracheae straight section are than being preferably 0.6-
3.6；Further, when the circulating fluidized bed boiler does not have multistage injection unit, the shunting circulation of the separation panel tracheae
The cross-sectional area of area and separation panel tracheae straight section is than being preferably 0.6-2.7；When the circulating fluidized bed boiler has multistage
When injection unit, the shunting circulation area of the separation panel tracheae is preferably with the cross-sectional area ratio of separation panel tracheae straight section
0.9-3.6。
Several shunting slits, the tangential velocity direction in the direction for shunting slit and air-flow are disposed on the tube body
In reverse directional acute angle, the angle of reverse directional acute angle is preferably 20 ° -50 °, so that splitting streams is flowed through the slit and generates U-turn, point
The length-width ratio for flowing slit is preferably 2-4.
Being disposed in the present invention and shunting the multiple exhaust pipeline section of slit is shunting section.
Preferably, the slit step-by-step arrangement that shunts is in the straight section of separation panel tracheae and cone section, especially proximate to cone
Straight section and cone section.
Preferably, several tube body circumferential arrangements for shunting slit by several elongated thin slices along separation panel tracheae form；
Boss is arranged in the both ends that slit is shunted at each section, and several elongated thin slices shunt slit, elongate thin by the fixed composition of boss
Piece can be made of sheet metal or potsherd, can fix elongated thin slice by the way that several oblique slots are arranged on boss.Boss can be with
It is multistage arrangement, boss cross-sectional profile can be circular arc, rectangle, trapezoidal or triangle etc..
In the preferred embodiment of the present invention, it is described shunt cyclone separator separation panel tracheae by upper tube body,
Multistage boss, connecting rod, elongated thin slice and lower mouth composition, upper tube body is straight pipe, multistage boss, connecting rod, elongated thin slice group
At the lower tube body for being changed into taper by straight, connecting rod is for connecting boss at different levels.
Further, the upper tube body in above embodiment is made by cooling down tube panel, and boss is made of header and convex body, even
Extension bar is made of connecting tube, can flow cooling medium in cooling tube panel, connecting tube and header, cooling medium can be water,
Steam water interface, steam or air etc..
Cone one end connector drum of the separator, other end connection plus cone and ash tube.
The connecting tube includes cooling medium general pipeline, and cooling medium general pipeline is bent from adding pyramid side to enter separator
It is arranged later along the longitudinal center line of the separator.
Optionally, the shunting section of the separation panel tracheae is arranged in below the air inlet section.
Optionally, the shunting section of the separation panel tracheae is partly or entirely arranged in the range of the air inlet section inlet height
It is interior.
In the preferred embodiment of the present invention, the multistage injection shunts the separation panel tracheae of cyclone separator
Shunting section is arranged in below air inlet section, and the nozzle multistage in multistage injection unit is arranged in the air inlet section before the shunting section
And/or on the cylinder and/or cone in region corresponding to cylinder and shunting section and shunting section.
In another preferred embodiment of the invention, the multistage injection shunts the separation panel tracheae of cyclone separator
Shunting section is partly or entirely arranged in the range of its air inlet section inlet height, and the nozzle multistage in multistage injection unit is arranged in
On the cylinder and/or cone in region corresponding to air inlet section entrance and shunting section.
The duff grain circulating fluidized bed boiler is 0-3mm to coal particle diameter, is preferably 0- to coal particle diameter
1mm。
The duff grain circulating fluidized bed boiler to coal particle diameter be 0-3mm when, primary air ratio 20%-30%,
When being preferably 0-1mm to coal particle diameter, primary air ratio 15%-25%.
The limestone particle diameter that the duff grain circulating fluidized bed boiler uses is 0-0.1mm.
The secondary air system of the duff grain circulating fluidized bed boiler arranges that upper section is multilayer in two sections, before every layer
Wall cross hedge is arranged afterwards, and lower section is one or more layers, and each layer also arrange by front-back wall cross hedge, upper section secondary air system bottom
Height between blast cap is 3-10 meters
By adopting the above scheme, the beneficial effects of the present invention are: shunting rotation due to being provided in the equipment
Wind separator shunts cyclone separator in particular by multistage injection, and separative efficiency can get and increase substantially, when underload,
Separative efficiency does not reduce, and is 0-3mm or 0-1mm, limestone particle size 0-0.1mm, secondary air separating two sections cloth to coal partial size
It sets, strengthens fractional combustion, primary air ratio is greatly lowered, and first and second wind pressure significantly reduces, so that duff grain recirculating fluidized bed
Boiler plant all has burning, desulfurization and nitric efficiency high in high underload, and furnace internal heating surface wears small, primary and secondary air energy consumption
It is low, the big performance of load regulation rate.
It is described further below with reference to technical effect of the attached drawing to design of the invention, specific structure and generation, with
It is fully understood from the purpose of the present invention, feature and effect.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of duff grain Circulating Fluidized Bed Boiler Equipment in the embodiment of the present invention；
Fig. 2 is the structural schematic diagram that multistage injection shunts cyclone separator in the embodiment of the present invention；
Fig. 3 is the A-A view of embodiment illustrated in fig. 2；
Fig. 4 is the B-B view of embodiment illustrated in fig. 2；
Fig. 5 is the elongated thin slice of embodiment illustrated in fig. 2 and a kind of partial enlargement C view of connection type of boss；
Fig. 6 is the nozzle of embodiment illustrated in fig. 2 and the partial enlargement D view of cylinder connection type；
Fig. 7 is the structural schematic diagram that another multistage injection shunts cyclone separator in the embodiment of the present invention；
Fig. 8 is the E-E view of embodiment illustrated in fig. 7；
Fig. 9 is the F-F view of embodiment illustrated in fig. 7.
In attached drawing: 1, coal grain storehouse；2, drum；3, down-comer；4, burner hearth；5, burner hearth flow of flue gas direction；6, upper section is secondary
Wind；7, duff grain delivery pipe；8, lower section Secondary Air；9, air compartment；10, separator gas inlet direction；11, separator air inlet section；
12, separator injection unit；13, separator exhanst gas outlet direction；14, separation panel tracheae；15, cylinder；16, cone；17, it plus bores
Body；18, ash tube；19, material returning device；20, First air approach axis；21, back-end ductwork；22, tail flue gas flow direction；23,
Smoke evacuation export direction；24, high pressure blower；25, injection air general pipeline；26, injection air Way in；27, cooling medium Way in；
28, cooling tube panel；29, boss；30, injection air is in charge of；31, elongated thin slice；32, injection air export direction；33, nozzle；34, even
Adapter tube b；35, linkage section header；36, connecting tube a；37, lower mouth；38, cooling medium general pipeline；39, cooling tube；40, fin；41,
Ring baffle；42, screw.
Specific embodiment
The embodiment of the present invention is described below in detail, examples of the embodiments are shown in the accompanying drawings, wherein from beginning to end
Same or similar label indicates same or similar element or element with the same or similar functions.Below with reference to attached
The embodiment of figure description is exemplary, it is intended to is used to explain the present invention, and is not considered as limiting the invention.
In the description of the present invention, it is to be understood that, term " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" height ", " thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom" "inner", "outside",
The orientation or positional relationship of the instructions such as " clockwise ", " counterclockwise " be based on the orientation or positional relationship shown in the drawings, be only for
Convenient for the description present invention and simplify description, rather than the device or element of indication or suggestion meaning there must be specific side
Position is constructed and operated in a specific orientation, therefore is not considered as limiting the invention.
In the present invention unless specifically defined or limited otherwise, the terms such as term " connected ", " connection ", " fixation " are answered
It is interpreted broadly, for example, it may be being fixedly connected, may be a detachable connection, or be integrally connected；It can be mechanical connect
It connects, is also possible to be electrically connected；It can be directly connected, can also can be in two elements indirectly connected through an intermediary
The connection in portion.For the ordinary skill in the art, it can understand as the case may be above-mentioned term in the present invention
Concrete meaning.
As shown in Figure 1, coal grain enters burner hearth 4 by duff grain delivery pipe 7 from coal grain storehouse 1, First air passes through wind from air compartment 9
Cap enters burner hearth 4, and Secondary Air enters burner hearth 4 along burner hearth two sections of multilayers of height in the top of blast cap, and flue gas passes through furnace from bottom to top
Thorax 4 enters cyclone separator, then flows out cyclone separator by separation panel tracheae 14 and enter back-end ductwork, in back-end ductwork 21
It can arrange the various heating surfaces such as superheater, economizer and air preheater, the soot particle that cyclone separator separates is by falling ash
Pipe 18 and material returning device 19 enter burner hearth 4, participate in circulating combustion.
Circulating fluidized bed boiler is 0-8mm to coal partial size at present, and the inner flue gas of the stove rate of climb is in 5m/s or so, according to stream
For state theory of gas-solid two-phase it is found that at this moment 0-700 μm of fine grained can be carried flake hearth-tapping by flue gas, the tail-off time of coal grain is same
Coal grain diameter is directly proportional, be greater than 700 μm of particle substantial dwell times in furnace, can abundant after-flame, finally in the form of slag exclude
Burner hearth, slag phosphorus content are generally less than 1%, and the fine grained overwhelming majority that flue gas is carried along into separator is separated, as circulation
Material returns to burner hearth and participates in burning again, flees from the fine grained of separator as flying dust and takes boiler out of by flue gas, recycle stock with
Particle size of fly ash distribution is related with critical incising control d99 is separated, and present 100 μm of cyclone separator of circulating fluidized bed boiler d99 ≈
Left and right, the partial size of recycle stock are mainly distributed as 100-600 μm, and the particle diameter distribution of flying dust is 0-100 μm, due to partial size in flying dust
Tail-off time needed for 40 μm or so of particle and the practical residence time difference maximum in furnace, therefore its phosphorus content highest, flying dust are whole
The phosphorus content of body reaches 5-25%, and much higher than the unburned carbon in flue dust of coal-powder boiler, the separative efficiency for improving separator can be effectively reduced
Particle size of fly ash reduces its phosphorus content, improves boiler combustion efficiency.
Coal grain enters circulating fluidized bed boiler and participates in fluidisation and circulating combustion, due to burning, explosion and abrasion,
Particle will gradually become smaller.Big to coal diameter, to guarantee slag after-flame, bed material needs are more, and primary air ratio is big, and primary air pressure is high,
In addition blast cap abrasion is big；Coal particle size is small, it is desirable that separator is high, and it is low otherwise to will lead to circulating ratio, flying marking
Amount is high.
Raising separator, which can reduce, gives coal diameter, reduces primary air ratio and primary wind pressure, mitigates blast cap abrasion,
Improve boiler combustion efficiency.It additionally by the reduction of primary air ratio, can also strengthen fractional combustion, reduce the discharge of NOx.
The cyclone diameter that circulating fluidized bed boiler now uses at present is 1-10 meter, and there are large scale short-circuit flow and powder
Dirt air-teturning mixed phenomenon causes separative efficiency that can not further increase.
As shown in Figure 2 and Figure 4, it shunts cyclone separator and is different from ordinary cyclones separator in the flow field of Diverging area, no
There are outer rotational gas flow and interior rotational airflow, air-flow does strong rotary motion between cylinder 15 and separation panel tracheae 14, shunts gas
Stream is in reverse directional acute angle in the tangential velocity direction of the slit direction and air-flow that flow through separation panel tracheae 14, does U-turn movement,
Acute angle is smaller, and the angle of turn of splitting streams is bigger, and separating effect is better, but the circulation area that will cause slit reduces, resistance
Increase, thus reverse directional acute angle angle is preferably 20 ° -50 °, the length-width ratio of narrow-gap channel is bigger, and the guiding of splitting streams turning is made
With better, be conducive to gas solid separation, but narrow-gap channel two sidewalls projection overlapping portion is also bigger, easily cause channel knot ash blocking,
To prevent from tying grey blocking, thus shunting slit length-width ratio is preferably 2-4, shunts the setting of slit so that splitting streams uniformly divide
Cloth, therefore short-circuit flow is eliminated, dust is successively rotated and inertial separation.The Diverging area of separation panel tracheae 14 can the row of being arranged in
Along cylinder on the straight section in the direction of cone and cone section, the mouth 37 under the arrangement of its lower end is not split tracheae for flowing through
Air-flow.
The air inlet section 11 for shunting cyclone separator is that tangential or volute air-inlet, the reduction of air scoop width can increase shunting gas
Flow path improves separative efficiency to moving distance, but will increase the height of cylinder 15, thus the depth-width ratio of air inlet is preferably 5-
20。
The cross-sectional area for shunting cyclone separator cylinder 15 is bigger, accessible gas flow is more or separative efficiency more
Height, but cost is more expensive；11 exit cross-section area of separator air inlet section is smaller, and air-flow enters that separator flow velocity is higher, and resistance is got over
Greatly, separative efficiency is higher.The cross-sectional area of Membrane Separator Cylinder for CFB Boiler 15 and the ratio of 11 exit cross-section area of separator air inlet section
It can be 5-22.
The shunting circulation area for shunting cyclone separator separation panel tracheae 14 is bigger, and isolation resistance is smaller, using injection
When, influence of the injection for separator is more obvious, and separative efficiency is significantly improved with the increase of injection volume, is shunted
The shunting circulation area of exhaust pipe 14 and the cross-sectional area ratio of separation panel tracheae straight section can be 0.6-3.6.Of the invention one
In kind preferred embodiment, the circulating fluidized bed boiler does not have multistage injection unit, shunts circulation area and separation panel
The cross-sectional area ratio of tracheae straight section is 0.6-2.7；In another preferred embodiment of the invention, the recirculating fluidized bed
Boiler has multistage injection unit, and the cross-sectional area ratio for shunting circulation area and separation panel tracheae straight section is 0.9-3.6.
The diameter and shunting circulation area of 14 top straight section of separation panel tracheae increase, and can be effectively reduced the resistance of separator
Power, but because splitting streams move radially the reduction of distance, will cause the decline of separative efficiency, thus 14 straight section of separation panel tracheae
The diameter of diameter and cylinder 15 is than being preferably 0.5-0.7.
In the case where shunting cyclone separator, its flow field of the lower section of mouth 37 is almost the same with ordinary cyclones separator, due to shunting
The most of air-flows of region have processed, the diameter and flow of lower mouth 37 all greatly reduce, therefore its ability for carrying dust also reduces.
Cyclone separator is shunted on the path of airflow diversion, rotation speed decays rapidly with the increase for shunting tolerance, this will
Cause the flow rotation speed in Diverging area latter end too small, separative efficiency is also with a sharp decline.Shunting cyclone separator can
It keeps the rotation speed for shunting end less low by improving initial flow rotation speed, reduces lower 37 diameter of mouth, make it
It is whole that there is very high separative efficiency, but this will necessarily cause its resistance high, and the flow rotation energy consumption for shunting leading portion largely meets with
To waste.In addition with the reduction of load, the decline of flow rotation speed, separative efficiency will also be greatly lowered therewith.
The tangential entry flow velocity for shunting cyclone separator can be 30-100m/s, and separator diameter is bigger, tangential entry flow velocity
Ying Yuegao, to maintain higher separative efficiency.
As illustrated in fig. 1 and 2, it is to be additionally arranged multistage in above-mentioned shunting cyclone separator that multistage injection, which shunts cyclone separator,
Injection unit 12.Multistage injection unit 12 by injection air general pipeline 25, injection air be in charge of 30 and nozzle 33 form, high pressure blower 24 will
Injection air is sent into injection air general pipeline 25, enters back into injection air and is in charge of 30 and nozzle 33, injection air be in charge of 30 and nozzle 33 along gas
The path multistage arrangement of stream flowing and the decaying of air-flow tangential velocity, the high-speed jet that high pressure gas is ejected by nozzle 33 is along gas
Tangential flow direction is flowed to spray, multistage injection air is in charge of the principle that 30 can distribute according to bypass flow etc. than ratio to arrange, this
Injection energy consumption can be reduced.The angle of jet direction and circle tangent line is too small to be directly washed into cylinder 15, too big to inject separation panel
Tracheae 14, in order to improve the utilization rate of injection air-flow, injection more participates in high speed close to the low speed flow of separation panel tracheae 14 and revolves
Turn, as shown in figure 3, its angle α is 20 ° -60 °；Because swirling eddy is that from top to bottom, the vertical direction component velocity of jet stream should be the same as rotation
The axial velocity for turning air-flow is almost the same, and horizontal sextant angle is slightly downward, its angle β as shown in Figure 6 is 0 ° -30 °.
It is arranged in the air-flow that the nozzle 33 above Diverging area is sprayed, is opened in underload, when ensuring underload
The initial tangential velocity of air-flow is consistently higher than setting value, and it is very high that this can keep cyclone separator all to have within the scope of full load
Separative efficiency.Multistage injection air air hose 30 and nozzle 33 are arranged on the path of air-flow tangential velocity decaying, what nozzle 33 sprayed
High-speed jet can significantly reduce the decaying of the tangential rotation speed of Diverging area, by calculating it is found that lower in injection energy consumption
Under the conditions of, can making injection Diverging area, swirling eddy obtains tangential velocity not less than setting numerical value everywhere, that is, can guarantee shunting zone
The separating property in domain reaches very high separative efficiency under conditions of lower initial tangential velocity.The small part after shunting
Swirling eddy enters separation panel tracheae 14 by lower mouth 37, and isolated mechanism is consistent with cyclone separator, due to radial velocity
Reduction and lower port diameter reduction, cyclonic separation efficiency herein can increase substantially than the cyclone separator not shunted.Institute
Very high separation can integrally be can get under the conditions of the moderate injection energy consumption of resistance is lower by shunting cyclone separator with multistage injection
Efficiency.
The tangential entry flow velocity that multistage injection shunts cyclone separator can be 25-70m/s, and injection air injection flow velocity can be
80-300m/s, their flow velocity is higher, and the separative efficiency that multistage injection shunts cyclone separator is also higher.
As shown in Fig. 2, flue gas tangentially enters cyclone separator cylinder 15 by separator air inlet section 11, air-flow is in cylinder 15
Downward rotary motion is done between separation panel tracheae 14, the splitting streams close to separation panel tracheae 14 are again through slit U-turn
Exhaust pipe, the centrifugal force separate that dust is rotated and turned are flowed into, air-flow passes through multistage boss 29 in downward movement, close
The low speed rotation air-flow of separation panel tracheae 14 is transported in high-speed rotating primary air by boss 29, this makes every level shunt flue gas
Separative efficiency be improved.Boss 29 can be multistage arrangement, and 29 cross-sectional profile of boss can be circular arc, rectangle, trapezoidal
Or triangle etc..Connecting rod and elongated thin slice 31 are arranged between each boss 29, form multi-stage diffluence structure.Separation panel tracheae 14
Diverging area can be arranged in exhaust pipe straight section and cone section on, its lower end arrangement under mouth 37, be not split for flowing through
Air-flow.Fig. 3 is the A-A view of embodiment illustrated in fig. 2, and Fig. 4 is the B-B view of embodiment illustrated in fig. 2, and Fig. 5 is shown in Fig. 2
The partial enlargement C view of embodiment, Fig. 6 are the partial enlargement D view of embodiment illustrated in fig. 2.
Shunting multicyclone apparatus can be used for handling high-temperature flue gas.When handling 800 DEG C or more of high-temperature flue gas, into
Gas section 11, cylinder 15, cone 16 and ash tube 18 can add thermal insulation material to add structure of refractory form using steel shell, can also be with
Add the structure type of castable refractory using thermal insulation material plus cooling tube panel.
The exhaust pipe in cyclone separator of circulating fluidized bed boiler is all made of metal material at present, in processing high temperature
When flue gas, have the shortcomings that price and service life are short.In order to improve separation panel tracheae 14 rigidity and service life in a high temperauture environment,
And cost is reduced, the present embodiment Fig. 2 illustrates separation panel tracheae 14 structure cooling using medium.Cooling medium is from cooling medium
General pipeline 38 enters linkage section header 35 by connecting tube a36, then enters next linkage section header 35 by connecting tube b34, according to
Secondary to be connected to the last one linkage section header 35, the last one linkage section header 35 is connected with cooling tube panel 28, cooling tube panel
28 are made of cooling tube 39 and the welding of fin 40, are disposed with connecting tube b34 and elongated thin slice 31 between each linkage section header 35,
Boss 29 is made in header 35 and convex body welding, has numerous oblique slots on convex body 29, in elongated 31 insertion groove of thin slice, uses ring baffle
41 and screw 42 be fixed, elongated thin slice 31 as shown in Figure 4 with swirling eddy direction in reverse directional acute angle arrange, adjacent two length of a film
What is formed between shape thin slice 31 is used to shunt swirling eddy, elongated thin slice with swirling eddy direction in the slit in reverse directional acute angle direction
31 can be made of metal resistant to high temperature or ceramics.Since connecting tube, header and tube panel have cooling medium flowing cooling, in high temperature
It also can guarantee good rigidity and service life in flue gas using carbon steel, 31 stress very little of elongate thin, material high temperature resistant, so using
The cooling separation panel tracheae of medium has the advantages that high temperature resistant, low cost and service life are long.Cooling medium can be water, steam or vapour
Aqueous mixtures.
The air inlet section for shunting cyclone separator can be tangential admission or volute air-inlet channel, and volute air-inlet can make cylinder
Interior tangential rotation speed is more uniform, is conducive to improve shunting efficiency.
The connection of cone lower part plus cone and the ash tube for shunting cyclone separator, add cone to can reduce the anti-of cone lower part
Intensity of flow reduces back mixing, improves separative efficiency.
Shunt cyclone separator 16 lower part of cone connection plus cone 17 and ash tube 18, cooling medium general pipeline 38 from add cone
17 side of body enters separator turning and is connected by connecting tube and linkage section header 35 with cooling tube 39 along longitudinal center line, arranges
Cooling medium general pipeline 38 on separator longitudinal center line can effectively maintain the central symmetry of swirling eddy, prevent residual rotation gas
Stream is wagged the tail.
Embodiment shown in Fig. 2 is that the Diverging area of separation panel tracheae 14 is arranged in the lower section of tangential admission section 11, this
So that the swirling eddy of 11 lower section of air inlet section is relatively uniform in the tangential velocity of circumferencial direction, separative efficiency is higher.Using multistage
When injection, jet nozzle arrangement is easy.But it is longer that it will cause cylinder, and manufacturing cost increases.Shunt the height of cyclone separator
Greatly, separative efficiency is high, but cost is big, and the ratio between the shunting cyclone separator height of this structure type and barrel diameter can be 3.5-5.
Embodiment shown in Fig. 7 is that the shunting section of separation panel tracheae 14 is partly or entirely arranged in its 11 import of air inlet section
In the range of height, this, which can reduce cylinder 15 and 14 length of separation panel tracheae, reduces cost.When using multistage injection, multistage injection
33 hierarchical arrangement of nozzle in unit on the cylinder 15 and centrum 16 of 14 Diverging area of 11 import of air inlet section and separation panel tracheae,
Each section swirling eddy can also be made to be uniformly distributed in the tangential velocity of circumferencial direction by multistage injection.The shunting of this structure type
The ratio between cyclone separator height and barrel diameter can be 3-4.5.Fig. 8 is the E-E view of embodiment illustrated in fig. 7, and Fig. 9 is Fig. 7 institute
Show the F-F view of embodiment.
Circulating fluidized bed boiler separator diameter reaches 1-10 meters, can be by improving gas inlet using cyclone separator is shunted
Flow velocity, separating critical incising control can be easy to reach 50 μm of d99 ≈ or so, 10 μm of d50 ≈ or so of numerical value；Drawn using multistage
Penetrate shunt cyclone separator reach above-mentioned separative efficiency, inlet velocity can be greatly lowered, i.e., resistance can sharp fall, together
When also ensuring underload separative efficiency do not reduce.
Since the present invention is using cyclone separator is shunted, cyclone separator is shunted in particular by multistage injection, separation is faced
Boundary's incising control can reduce by more than 50 than cyclone separator, and the efficiency of combustion of circulating fluidized bed boiler is significantly mentioned
It is high.
On the basis of this, it will be reduced to 0-3mm from current 0-8mm to coal partial size, and guarantee what slag phosphorus content did not improved
Under the conditions of, bed material thickness can be reduced at double, and one time wind resistance can also reduce at double, due to the drop of burner hearth bottom combustion share
Low, primary air ratio can be reduced to 20%-30% from 50%, i.e. the energy consumption of primary air fan can be greatly lowered.Secondary wind pressure determines
The flow velocity of overfire air jet, flow velocity is higher, and penetration power and stirring capacity are stronger, can stir evenly high concentration gas-solid mixture,
To the reduction of coal partial size, internal circulating load in material can be reduced, reduces burner hearth recycle stock concentration, so required secondary wind wind speed
I.e. wind pressure can also reduce.
Wear rate in furnace everywhere, 3 powers with particle speed, the first power of square of particle diameter, concentration are directly proportional.
Since bed material attenuates, fluidising air velocity is reduced, and the abrasion of blast cap can be greatly reduced.
Secondary Air divides two sections to arrange along furnace height, and upper section Secondary Air 6 is multi-tier arrangement, every layer of front-back wall cross-pair
Punching arrangement；Lower section Secondary Air 8 is one or more layers arrangement, and every layer also front-back wall cross hedge is arranged, to guarantee that air distribution is uniform, is made
It is uniform to obtain flue-gas temperature in burner hearth.There are certain spaces between 8 top of 6 bottom of upper section Secondary Air and lower section Secondary Air, upper
Since flue gas flow rate is lower in section Secondary Air 6 space below, material can form strong interior circulation, and the coarse granule in furnace can stay
In burner hearth bottom, 6 bottom of upper section Secondary Air is protected with the water-cooling wall of lower hearth surrounding with wear-resistant castable, burner hearth upper section Secondary Air
Although 6 or more space flue gas flow rate is higher, recycle stock is thinner, and the amount recycled in material is smaller, close to furnace wall cooling
Sinking flow velocity it is lower, the abrasion of surrounding water-cooling wall and heating surface can be greatly reduced in furnace.In order to which coarse granule is stayed in furnace
Bottom reduces the dust concentration of upper furnace as far as possible, and 6 wind rate of upper section Secondary Air is 50% or so, and 8 wind rate of lower section Secondary Air is 25%
Left and right, First air wind rate are 25% or so, and the height between 6 bottom of upper section Secondary Air and blast cap is 3-10 meters.At this moment under burner hearth
The flue gas rate of climb in portion is 2.5m/s or so, and flue gas carries flake hearth-tapping fine grained partial size and is reduced to 0-400 μm or so, is such as shunted
50 μm or so of cyclone separator d99 ≈, the partial size of recycle stock is mainly distributed as 50-350 μm, and the particle diameter distribution of flying dust is 0-50
μm.Although the particle that burner hearth enters separator is thinner, the amount recycled in upper furnace material is smaller, and granule density is lower, due to
The fine grained tail-off time is short, the completely available guarantee of residing time in furnace required for flying dust after-flame, therefore the partial size of flying dust is thin
And phosphorus content is low, boiler combustion efficiency is high, and the heating surface wear being arranged in boiler back end ductwork 21 is light.
The water-cooling wall of burner hearth bottom surrounding is protected with wear-resistant castable, and i.e. abrasionproof is kept the temperature again for it.Wear-resistant castable and blast cap
Between height be 3-12 meter, due to the heat output very little in this region, in underload, smoke temperature herein be convenient to control exists
900 DEG C or so.It is specified negative in boiler since multistage injection shunting cyclone separator separative efficiency within the scope of full load is all very high
When lotus, the upflow velocity of flue gas can be 2-6m/s in burner hearth, and boiler capacity hour selects low value, high level is selected when boiler capacity is big,
When 30% load of boiler, since upper furnace heat output is big, flue-gas temperature is low, but duff grain is in lower furnace portion high-temperature flue gas region
The one-pass residence time still up to 4 seconds or more, can satisfy the after-flame needs of flying dust completely.
The factors such as desulphurization in circulating fluidized bed boiler efficiency and Ca/S ratio, flue-gas temperature and limestone particle size are related.Mesh
Preceding circulating fluid bed boiler desulfurization limestone particle size is generally 0-1mm, the shunting cyclone separator separation used due to the present invention
Efficiency is very high, therefore its limestone particle size can be adjusted to 0-0.1mm, and the specific surface area of lime stone significantly improves, desulfuration in furnace
Efficiency can increase substantially.
In circulating fluid bed boiler in nitric efficiency and flue-gas temperature, a Secondary Air ratio and furnace excess air coefficient etc. because
It is known as pass, a Secondary Air is than smaller, and the efficiency of fractional combustion denitrogenation is higher, and excess air coefficient is smaller in furnace, the production quantity of NOx
It is lower.Primary air ratio of the present invention can be 25% or so, and two layers of secondary air separating arrangement, lower layer's secondary air ratio is 25% or so, upper layer
Secondary air ratio is 50% or so, and shunting flue-gas temperature in cyclone separator is 880 DEG C or so, the Secondary Air burner hearth below on upper layer
It is inside gasification, and combustion, the not generation of NOx substantially, upper layer Secondary Air is multistage penetrating burner hearth, enhances fractional combustion, draws at a high speed
Penetrating wind not only can be improved separative efficiency, but also play after-flame wind action, and excess air coefficient can be controlled in very low in furnace
Numerical value, so NOx emission concentration of the invention is greatly reduced than current circulating fluidized bed boiler.
Cyclone inlet flue gas flow rate and injection air air quantity and wind speed are shunted by improving, further increases it
Separative efficiency will more optimizedly be reduced to 0-1mm to coal partial size, and at this moment First air wind rate can drop to 15%-25%, one or two wind pressure
It can also further decrease, a secondary air fan energy consumption also further decreases therewith, more significant, the NOx emission concentration of fractional combustion
Lower, circulating ratio and recycle stock partial size further decrease in furnace, wear everywhere in furnace gentlier, low-load performance is obtained into one
Step is promoted.
Cyclone separator is shunted using multistage injection, in boiler at low load, is entered since separator can be improved by injection
The tangential velocity of mouth and shunting section, separator can guarantee and not reduce, so boiler combustion efficiency and desulfuration efficiency
It can not decline；Fractional combustion can still be strengthened, and nitric efficiency is still very high in furnace.
Under conditions of separator flue gas resistance increases few, cyclone separator in the prior art and shunting of the invention
Cyclone separator, multistage injection shunt the separation efficiency comparative of cyclone separator, and the results are shown in Table 1:
Table 1
| Boiler capacity: t/h | 2 | 75 | 1000 |
| Separator diameter: m | 0.9 | 3.2 | 9.6 |
| Cyclone separator d99: μm | 50 | 85 | 130 |
| Shunt cyclone separator d99: μm | 30 | 50 | 80 |
| Multistage injection shunts cyclone separator d99: μm | 22 | 35 | 55 |
Circulating fluidized bed boiler (CFB) in the prior art and injection of the invention shunt duff grain circulating fluidized bed boiler
(BCFB) calculated performance comparing result is as shown in table 2:
Table 2
It is above-mentioned to coal partial size and First air wind rate be for bituminous coal, since different types of coal combustion characteristics is widely different,
To different coals, above-mentioned parameter should be made the appropriate adjustments.Anthracitic accordingly to reduce to coal partial size, primary air ratio increases accordingly；
Lignite is increased accordingly to coal partial size, and primary air ratio accordingly reduces.
Cyclone separator is shunted when separation bonds strong dust, acoustic wave ash ejector can be used, shock wave soot blower, pulse are blown
Grey device or steam sootblower are cleared up slit is shunted.
In summary, duff grain circulating fluidized bed boiler of the invention shunts cyclone separator due to using, especially
Cyclone separator is shunted using multistage injection, separative efficiency can be significantly increased, and unburned carbon in flue dust can significantly reduce,
Pass through the reconstruct to coal partial size, limestone particle size, a Secondary Air parameter and structure is given, duff grain recirculating fluidized bed of the invention again
Boiler, running under high underload all has burning, desulfurization and nitric efficiency high, and blast cap and heating surface wear are small in furnace, and one or two
The low performance of secondary fan energy consumption.
This hair can be understood and applied the above description of the embodiments is intended to facilitate those skilled in the art
It is bright.Person skilled in the art obviously easily can make various modifications to these embodiments, and described herein
General Principle is applied in other embodiments without having to go through creative labor.Therefore, the present invention is not limited to implementations here
Example, those skilled in the art's announcement according to the present invention, improvement and modification made without departing from the scope of the present invention all should be
Within protection scope of the present invention.
Claims (28)
1. a kind of duff grain circulating fluidized bed boiler, including burner hearth, primary air system, secondary air system, separator and tail portion cigarette
Road, it is characterised in that: the separator is to shunt cyclone separator, and the shunting cyclone separator includes cylinder, cone, air inlet
Section, separation panel tracheae and ash tube.
2. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the separator is multistage injection
Shunt cyclone separator, including cylinder, cone, air inlet section, separation panel tracheae, ash tube and multistage injection unit, the multistage
Injection unit includes pipeline and nozzle, and the nozzle is in multistage cloth along the path that air-flow flowing and air-flow tangential velocity decay
It sets, for the pipeline for connecting nozzle and providing high pressure gas, the high pressure gas is suitable by the high-speed jet that the nozzle ejects
Air-flow tangential flow direction spray, the angle of the circle tangent line of jet direction and cylinder is 20 ° -60 °.
3. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the air inlet section is tangential or snail
Shell air inlet, the depth-width ratio of air inlet are 5-20.
4. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the cross-sectional area of the cylinder
Cross-sectional area ratio with air inlet section outlet is 5-22.
5. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the separation panel tracheae is along cylinder
Body to the direction of cone include straight section and cone section.
6. duff grain circulating fluidized bed boiler according to claim 5, it is characterised in that: the shunting of the separation panel tracheae
The cross-sectional area ratio of circulation area and separation panel tracheae straight section is 0.6-3.6.
7. duff grain circulating fluidized bed boiler according to claim 5, it is characterised in that: the separation panel tracheae straight section
The diameter ratio of diameter and the cylinder is 0.5-0.7.
8. duff grain circulating fluidized bed boiler according to claim 5, it is characterised in that: in the pipe of the separation panel tracheae
Several shunting slits are disposed on body, the direction of the shunting slit and the tangential velocity direction of air-flow are in reverse directional acute angle.
9. duff grain circulating fluidized bed boiler according to claim 8, it is characterised in that: the angle of the reverse directional acute angle is
20°-50°。
10. duff grain circulating fluidized bed boiler according to claim 8, it is characterised in that: the length and width for shunting slit
Than for 2-4.
11. duff grain circulating fluidized bed boiler according to claim 8, it is characterised in that: the shunting slit is segmented cloth
The straight section and cone section in the separation panel tracheae are set, several shunting slits are by several elongated thin slices along the pipe of separation panel tracheae
Boss is arranged in body circumferential arrangement composition, the both ends that slit is shunted at each section, and several elongated thin slices are formed by the way that boss is fixed
Shunt slit.
12. duff grain circulating fluidized bed boiler according to claim 11, it is characterised in that: be arranged on the boss several
Oblique slot fixes the elongated thin slice.
13. duff grain circulating fluidized bed boiler according to claim 11 or 12, it is characterised in that: the boss is multistage
Arrangement.
14. duff grain circulating fluidized bed boiler according to claim 11 or 12, it is characterised in that: the boss cross section
Shape is circular arc, rectangle, trapezoidal or triangle.
15. duff grain circulating fluidized bed boiler according to claim 8, it is characterised in that: the separation panel tracheae is by upper
Tube body, multistage boss, connecting rod, elongated thin slice and lower mouth composition, the upper tube body are straight pipe, the multistage boss, described
Connecting rod, the elongated thin slice composition are changed into the lower tube body of taper by straight, and the connecting rod is for connecting boss at different levels.
16. duff grain circulating fluidized bed boiler according to claim 15, it is characterised in that: the upper tube body is by cooling tube
Screen is made, and the boss is made of header and convex body, and the connecting rod is made of connecting tube, in cooling tube panel, connecting tube sum aggregate
Cooling medium can be flowed in case.
17. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: described cone one end connects institute
State cylinder, other end connection plus cone and the ash tube.
18. duff grain circulating fluidized bed boiler according to claim 17, it is characterised in that: the connecting tube includes cold
But medium general pipeline, cooling medium general pipeline enter the separator from described plus pyramid side, along the separator after bending
Longitudinal center line arrangement.
19. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: point of the separation panel tracheae
Stream section is arranged in below the air inlet section.
20. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: point of the separation panel tracheae
Stream section is partly or entirely arranged in the range of the air inlet section inlet height.
21. duff grain circulating fluidized bed boiler according to claim 2, it is characterised in that: point of the separation panel tracheae
Stream section is arranged in below the air inlet section, and the nozzle multistage in the multistage injection unit is arranged in front of the shunting section
Air inlet section and/or cylinder and shunting section corresponding to region cylinder and/or cone on.
22. duff grain circulating fluidized bed boiler according to claim 2, it is characterised in that: point of the separation panel tracheae
Stream section is partly or entirely arranged in the range of the air inlet section inlet height, and the nozzle in the multistage injection unit is more
Grade is arranged in cylinder and/or the cone in region corresponding to the air inlet section import and the shunting section.
23. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the fluidized-bed combustion boiler is given
Coal particle diameter is 0-3mm.
24. duff grain circulating fluidized bed boiler according to claim 22, it is characterised in that: the one of the fluidized-bed combustion boiler
Secondary wind rate is 20%-30%.
25. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the fluidized-bed combustion boiler is given
Coal particle diameter is 0-1mm.
26. duff grain circulating fluidized bed boiler according to claim 24, it is characterised in that: the one of the fluidized-bed combustion boiler
Secondary wind rate is 15%-25%.
27. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the fluidized-bed combustion boiler uses
Limestone particle diameter be 0-0.1mm.
28. duff grain circulating fluidized bed boiler according to claim 1, it is characterised in that: the secondary air system is presented
Lower two sections of arrangements, upper section are multilayer, and every layer of front-back wall cross hedge arrangement, lower section is one or more layers, and each layer also hand over by front-back wall
The arrangement that liquidates is pitched, the height between upper section secondary air system bottom and blast cap is 3-10 meters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811149691.6A CN109340743B (en) | 2018-09-29 | 2018-09-29 | Fine coal particle circulating fluidized bed boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811149691.6A CN109340743B (en) | 2018-09-29 | 2018-09-29 | Fine coal particle circulating fluidized bed boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109340743A true CN109340743A (en) | 2019-02-15 |
| CN109340743B CN109340743B (en) | 2020-03-17 |
Family
ID=65307594
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811149691.6A Expired - Fee Related CN109340743B (en) | 2018-09-29 | 2018-09-29 | Fine coal particle circulating fluidized bed boiler |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109340743B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110145736A (en) * | 2019-06-21 | 2019-08-20 | 烟台龙源电力技术股份有限公司 | The adjusting method of cyclone separator, circulating fluidized bed boiler and the Effiency of whirlwind Separator |
| CN110184090A (en) * | 2019-05-05 | 2019-08-30 | 江苏世博设计研究院有限公司 | Desulfurizer and method in a kind of coal boiler |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1244447A (en) * | 1998-08-07 | 2000-02-16 | 彪万热斗株式会社 | Cyclone separator and filter thereof |
| CN2711540Y (en) * | 2004-06-12 | 2005-07-20 | 唐山信德锅炉制造有限公司 | Low circulation multiplying factor low smoke speed intermediate temperature separation circulating fluidized bed boiler |
| CN1817437A (en) * | 2004-10-22 | 2006-08-16 | 阿尔斯通技术有限公司 | Method and device for adjustment solid cycle quantity of circulating fluidized bed reaction system |
| CN204276175U (en) * | 2014-10-31 | 2015-04-22 | 陕西煤业化工技术研究院有限责任公司 | Dry laminating air swirl separator |
| US20180238620A1 (en) * | 2017-02-22 | 2018-08-23 | Larry Baxter | Air-Sparged Hydrocyclone For Cryogenic Gas Vapor Separation |
-
2018
- 2018-09-29 CN CN201811149691.6A patent/CN109340743B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1244447A (en) * | 1998-08-07 | 2000-02-16 | 彪万热斗株式会社 | Cyclone separator and filter thereof |
| CN2711540Y (en) * | 2004-06-12 | 2005-07-20 | 唐山信德锅炉制造有限公司 | Low circulation multiplying factor low smoke speed intermediate temperature separation circulating fluidized bed boiler |
| CN1817437A (en) * | 2004-10-22 | 2006-08-16 | 阿尔斯通技术有限公司 | Method and device for adjustment solid cycle quantity of circulating fluidized bed reaction system |
| CN204276175U (en) * | 2014-10-31 | 2015-04-22 | 陕西煤业化工技术研究院有限责任公司 | Dry laminating air swirl separator |
| US20180238620A1 (en) * | 2017-02-22 | 2018-08-23 | Larry Baxter | Air-Sparged Hydrocyclone For Cryogenic Gas Vapor Separation |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110184090A (en) * | 2019-05-05 | 2019-08-30 | 江苏世博设计研究院有限公司 | Desulfurizer and method in a kind of coal boiler |
| CN110145736A (en) * | 2019-06-21 | 2019-08-20 | 烟台龙源电力技术股份有限公司 | The adjusting method of cyclone separator, circulating fluidized bed boiler and the Effiency of whirlwind Separator |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109340743B (en) | 2020-03-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102062395B (en) | Gas and solid separator of recirculating fluidized bed boiler and boiler containing same | |
| CN109332016A (en) | A kind of multistage injection shunting cyclone separator | |
| CN1125948C (en) | Combustion apparatus with cross-section variable circulating fluidized bed | |
| CN105090980B (en) | A kind of spiral-flow type fluidized bed combustion device | |
| CN101832550A (en) | Swirl pulverized-coal burner based on multi-level pulverized-coal concentration | |
| CN109340743A (en) | A kind of duff grain circulating fluidized bed boiler | |
| CN206247319U (en) | A kind of eddy flow boiler combustion system for tertiary air separate | |
| CN206504320U (en) | The energy-efficient Circulating Fluidized Bed Boiler of low nitrogen | |
| CN108954298A (en) | A kind of circulating fluidized bed boiler low nitrogen burning exhaust system and its remodeling method | |
| CN208976077U (en) | A kind of tubular cyclones | |
| CN109595548A (en) | Deep or light back-mixing formula vortex burner | |
| CN103953923B (en) | A kind of coal sorting feeder | |
| CN101033848A (en) | Flow equalizing low-resistance dust dedusting system | |
| CN202884900U (en) | Pulverized coal firing boiler with wall-attaching secondary air and latticework burnout air | |
| CN207308133U (en) | A kind of axial swirler and system for being suitable for gas-solid two phases | |
| CN104100968B (en) | A kind of cyclone separator of circulating fluidized bed boiler with integral inclined central tube | |
| CN109225689A (en) | A kind of tubular cyclones | |
| CN202762559U (en) | Scroll cyclone dust collector | |
| CN211801696U (en) | Multistage combined weak vortex low-resistance cyclone preheating system | |
| CN104235834B (en) | CFBB high-temperature separator | |
| CN203810397U (en) | Coal spreading device | |
| CN211801693U (en) | High-efficiency low-resistance cyclone cylinder | |
| CN207196473U (en) | CFB boiler with the effect of certain abrasionproof | |
| CN108800118B (en) | A kind of CFB Slag waste-heat recovery device | |
| GB2061773A (en) | Particle separators |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20200317 |