CN1041646A - Composite circulation fluidizing bed boiler - Google Patents
Composite circulation fluidizing bed boiler Download PDFInfo
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- CN1041646A CN1041646A CN89107888A CN89107888A CN1041646A CN 1041646 A CN1041646 A CN 1041646A CN 89107888 A CN89107888 A CN 89107888A CN 89107888 A CN89107888 A CN 89107888A CN 1041646 A CN1041646 A CN 1041646A
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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
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
- F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
- F22B31/0084—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed with recirculation of separated solids or with cooling of the bed particles outside the combustion bed
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
- F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
- F22B31/0084—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed with recirculation of separated solids or with cooling of the bed particles outside the combustion bed
- F22B31/0092—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed with recirculation of separated solids or with cooling of the bed particles outside the combustion bed with a fluidized heat exchange bed and a fluidized combustion bed separated by a partition, the bed particles circulating around or through that partition
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Invalid Beds And Related Equipment (AREA)
- Laminated Bodies (AREA)
Abstract
The present invention is a kind of composite circulation fluidizing bed boiler, its fluid bed is divided into main chamber and heat recovery chamber, the flowing velocity of the flow media in the main chamber is big, the flowing velocity of the flow media in the heat recovery chamber is little, make up this two kinds of different flowing velocities, make the flow media in the main chamber form the circular flow that circles round, and between main chamber and heat recovery chamber, form the circular flow of flow media, and the decline mobile layer that in heat recovery chamber, forms flow media.Carry out the heat recovery of waste gas in free space and downstream thereof, EGT enters cyclone dust collectors after descending, and the particulate that contains charcoal that captures in cyclone dust collectors send the decline mobile layer of the flow media that adds main chamber and/or heat recovery chamber again.
Description
The present invention relates to the inner loop fluidized-bed combustion boiler, this boiler can reclaim heat from the heat transfer component of circular flow and free space and side during with combustibles such as the body refuse of the various coals of fluidized bed combustion of the so-called sliding-type that circles round, low grade coal, coal washing, petroleum coke rocks.
In recent years, coal shows one's promises as the alternative energy source of oil, still, because coal acts as a fuel on physical property and chemical property all than oil difference, so in order to enlarge the scope of application of coal, people are just promoting the technology of the utilization of coal in the processing of accelerate development coal, conveying etc.; Aspect combustion technology, boiler and fluidized-bed combustion boiler to the combustion particle coal dust being are also are being researched and developed always energetically, but because these combustion technologies are from the generation aspect of efficiency of combustion, reduction nitrogen oxide and sulfur oxide, kind to coal is also restricted, but also the significant disadvantages such as control difficulty when existing coal supply system complexity, load variations, particularly for medium and small boiler, the problems referred to above are more obvious.
In addition, for fluidized-bed combustion boiler, different according to the layout of its heat transfer component and the mode of how considering the unburned particle that flies upward away from fluidized bed is burnt can have following two kinds of forms:
(1) non-circulating type fluidized-bed combustion boiler (fluidized-bed combustion boiler or the boiling type fluidized-bed combustion boiler that also can be called existing form).
(2) circulating fluid bed boiler.
The non-circulating type fluidized-bed combustion boiler disposes heat-transfer pipe in fluidized bed, directly contact by means of its mobile medium of burnt fuel under high temperature, carry out heat exchange with very high heat transfer efficiency, circulating fluid bed boiler then is to use the part (solid circle particle) of tiny unburned powder and ash content or flow media to introduce in the independent heat-exchanging part that is provided with that separates with the combustion chamber together along with the air-flow of burning gases, unburned particle is burnt away, and the solid circle particle that has passed through heat exchange is turned back in the combustion chamber, owing to carry out the circulation of solids by this way, so be referred to as circulating.
According to Fig. 4 and Fig. 5 non-circulating type fluidized-bed combustion boiler and circulating fluid bed boiler are described below.
Fig. 4 represents the non-circulating type fluidized-bed combustion boiler, the air that the fluidisation of being come by not shown air blast force feed is used through dispersion plates 72 and be blown into 71 li in boiler, forms fluidized bed 73 from air chamber 74, fuel (for example coal dust) just infeeds fluidized bed 73, burns.And in fluidized bed 73 and at the waste gas outlet of free space, partly be provided with heat- transfer pipe 76 and 77 to reclaim heat.
Lower slightly the waste gas of temperature flows into convection heat transfer' heat-transfer by convection part 78 from the waste gas outlet of free space, further reclaim heat after, contained trickle particle in the recovery waste gas cyclone dust collectors 29 in is discharged to the outside of steam generator system then.The ash content that is reclaimed in convection heat transfer' heat-transfer by convection part, except a part pumps out from pipeline 81, with the ash content that from pipeline 80, pumps out, be discharged to outside the outside of steam generator system through piping 82, some then gets back to fluidized bed 73 by air chamber 74 or fuel supply port 75, burns again.
Fig. 5 represents circulating fluid bed boiler, the air that the fluidisation of being come by not shown air blast force feed is used by air chamber 104, is blown in the boiler 101 through dispersion plate 102, make to infeed coal dust in the stove, that contain the lime of using as desulfurizing agent as required and be fluidized state, and make it burning.
Different with the non-circulating type fluidized-bed combustion boiler, because the jet velocity of the air that the fluidisation that process dispersion plate 102 is blown into is used is higher than the final velocity of fluidized particle, so particle is more violent with mixing of gas, particle is upwards blown afloat with gas, forms fluidized bed and shunting layer in the gamut of combustion furnace from the bottom up successively.Particle and gas have exchanged after a part of heat with water cooled furnace wall 107 halfway, enter cyclone dust collectors 108.After burning gases flow out, carry out heat exchange in the convection heat transfer' heat-transfer by convection part 109 on being arranged on the rear portion flue again from cyclone dust collectors 108.
On the other hand, the particle that is trapped in cyclone dust collectors 108 returns the combustion chamber except a part heavily again through passage 113, in order to control the temperature in the stove, some particle enters external heat exchanger 115 through path 114, after cooling, return the combustion chamber again, a part wherein is a coal ash, then discharges outside the steam generator system.This particle is the characteristics of circulating fluid bed boiler by the circulation of combustion chamber.The particle of circulation mainly is lime stone and added burning of coal ashes and the unburned coal ash etc. that add as desulfurizing agent.
In this fluidized-bed combustion boiler, since its combustion system, the selectable wide range of the combustible that is burnt, and still, on the other hand, also the someone has pointed out its shortcoming.
The shortcoming of boiling type fluidized-bed combustion boiler is its load characteristic, the fuel feed system complexity, and the heat-transfer pipe in the fluidized bed is wear-resisting etc.
Though everybody thinks that circulating fluid bed boiler can solve these intrinsic problems, but make the circulatory system of the cyclonic separation gas that comprises combustion gas keep suitable temperature, also have some key problem in technology that need solve, in addition, the conveying of solid circle particle also has problems, and if be used for medium small boiler, design of miniization also is a difficult point.
The inventor is in order to address the above problem, through long-term constantly research, finally found and to have improved efficiency of combustion, reduce nitrogen oxide, and the technical scheme that makes the boiler miniaturization, Here it is inner loop fluidized-bed combustion boiler, it causes the stream that circles round by means of different fluidizing velocities in fluidized bed inside, and, utilize the circular flow of this flow media between stream formation and the heat recovery chamber that circles round, the free space part above fluidized bed and the downstream of free space part are provided with the heat recovery component of evaporation tube and so on, and will introduce cyclone dust collectors through the low temperature waste gas after the recuperation of heat, the decline mobile layer that the particle that is captured in these cyclone dust collectors is sent back to fluid bed top flow media goes then.In addition, because the stream that circles round has been arranged, even the ratio height of coal dust in the flammable mixture, also can completing combustion, to the grade of coal without limits.Can use silica sand as flow media in addition, and, it and lime stone are mixed use, can also obtain reducing the effect of sulfur oxide.Integrate, the existing problem of coal fired boiler has just all found the way that solves up to now.
That is to say, the invention is characterized in:
First, this part of fluidized bed is divided into main chamber and heat recovery chamber with a big dividing plate, bottom at main chamber, at least be provided with two kinds of air chambers, the air chamber and air chamber that promptly have very big fluidizing velocity with less fluidizing velocity, by means of this different fluidizing velocity of combination, make the flow media generation in the main chamber loop back eddy flow, and, between main chamber and heat recovery chamber, form the recuperation of heat circular flow of a flow media, be that this is a kind of inner loop fluidized-bed combustion boiler, it is in the heat recovery chamber bottom, and in main chamber a side opposite with heat recovery chamber, be provided with and have the less air chamber of fluidizing velocity, its waste gas is introduced cyclone dust collectors, and the decline mobile layer of the particle that is captured being sent back to main chamber or heat recovery chamber in cyclone dust collectors goes.
Particle entrapment is not necessarily used cyclone dust collectors, also can send the particle that is captured back to the decline mobile layer behind the particle entrapment with cloth envelop collector etc.Owing to the particle that captures is sent back to the beginning part of decline mobile layer, unburnt ingredient (charcoal) in the particle that captures just is diffused into fluidized bed inside equably, make to be reducing atmosphere in the whole fluidized bed, so just reduced from the nitrogen oxide of fluidized bed freedom of entry space segment.
Making carbon granule turn back to the resulting effect of decline mobile layer is, if charcoal turns back to fluidized bed, because charcoal is graininess, just fly upward at once, almost the time of in fluidized bed, not being detained, can not give full play to the burning of charcoal itself and the catalyst function of reduction nitrogen oxide, and when making charcoal get back to the decline mobile layer, even it has very trickle particle, it can spread in this one deck in sedimentation, so carbon granule just can play one's part to the full, extremely significant effect is arranged to reducing nitrogen oxide in this one deck that produces nitrogen oxide because of coal combustion.
The reaction of this minimizing nitrogen oxide has two kinds:
Any reaction is all relevant with charcoal, can think, its oxidation reaction performance and effect of catalyst make it possess the function that reduces nitrogen oxide.
Second function is that heat-transfer pipe has been arranged in the free space part above fluidized bed or the downstream of free space part, mainly relies on convection heat transfer' heat-transfer by convection to carry out the recovery of heat.
Convection heat transfer' heat-transfer by convection parts in the past all partly separate independent the setting with free space, the present invention is in order to reach the purpose of miniaturization, on the basis of the volume that guarantees the necessary free space part of second-time burning, the downstream of top in free space or free space part is provided with the convection heat transfer' heat-transfer by convection parts
*So, except the dust around the former boiler is handled and the recirculation of carbon granule etc. become easy, the temperature that enters the gas of cyclone dust collectors also has only 250 °～400 ℃, make cyclone dust collectors not need to use and cast out next interior lining panel, can make of steel, realize lightweight and miniaturization.
The 3rd feature is, owing to convection heat transfer' heat-transfer by convection partly is arranged on the top of free space, perhaps make the furnace wall of boiler with water cooled pipeline, in order to prevent to descend, attach the heat-insulating material that refractory material is done to convection heat transfer' heat-transfer by convection parts or water cooled furnace wall in a side of combustion chamber owing to radiation effect makes the temperature of free space internal combustion gas.Adopt such measure, just can receive the temperature of keeping burning gases, reduce the effect of CO.
* original text is " free space ", and is obstructed, and doubting is " convection heat transfer' heat-transfer by convection parts " mistake, so change.
-translator
When the convection heat transfer' heat-transfer by convection parts being arranged on the downstream of free space part, just just passable as long as on the water cooled furnace wall that constitutes the free space part, attach refractory thermal insulating material.
That is to say that the present invention is the composite circulation fluidizing bed boiler that is combined by three circulations, these three circulations are: the circular flow that circles round of main chamber; The recuperation of heat circulation of the flow media that carries out between main chamber and the heat recovery chamber; The outer loop that the decline mobile layer that makes unburned carbon granule return the flow media in main chamber or the heat recovery chamber in addition goes (carbon granule subcycle).
Be simple declaration below to accompanying drawing.
Fig. 1, Fig. 2 and Fig. 3 are respectively the schematic diagrames that is provided with the dissimilar composite circulation fluidizing bed boiler of the present invention of heat-transfer pipe of evaporation tube and so on free space top; Fig. 4 is the schematic diagram of fluidized boiler in the past; Fig. 6 represents the relation of flow media internal circulating load in the fluidization air amount of tilt clapboard bottom and the heat recovery chamber; Fig. 7 represents the air quantity of diffused air of heat recovery chamber and the relation of decline mobile layer sinking speed; Fig. 8 represents the mass velocity of general fluidizing gas and the relation of complex heat transfer coefficient; Fig. 9 represents the air quantity of diffused air of inner loop type heat recovery chamber and the relation of complex heat transfer coefficient; Figure 10 represents the mass velocity of fluidizing gas and the relation of the heat-transfer pipe rate of wear; To be the present invention in the downstream of free space part be furnished with Figure 11 partly becomes the schematic diagram of composite circulation fluidizing bed boiler of the heat transfer tube group of as a whole evaporation tube and so on free space; Figure 12 is the profile along Figure 11 A-A line; Figure 13 also is the profile that is equivalent to along the composite circulation fluidizing bed boiler of Figure 11 A-A line, but this boiler the downstream of free space part be furnished with partly form the heat transfer tube group of evaporation tube and so on of an integral body with free space in, go back the bigger particle that handlebar captured and send the mechanism that goes in the left and right heat recovery chamber that is arranged in the main chamber two ends back in the part of this heat transfer tube group; Figure 14 tiny contains carbon granule to what captured in the cyclone dust collectors and the above-mentioned particle that is captured is sent the embodiment that fluid bed partly goes back to handling machineries such as conveyers in heat transfer tube group.
Describe the present invention with reference to the accompanying drawings in detail.
Among Fig. 1, be provided with the dispersion plate 2 of the air that fluidisation that air blast 16 force feeds come uses in the bottom of boiler body 1, the both sides of the edge of dispersion plate 2 central authorities are high, make the bottom of boiler body be spill.
Like this, the air that the fluidisation of being come by air blast 16 force feeds is used is through air chamber 12,13,14, spray upward from air dispersion plate 2, the fluidisation that ejects from central air chamber 13 is with the mass velocity of air, be enough to make the flow media in the boiler body to form fluidized bed, just in the 4-20Gmf scope, be preferably in the scope of 6-12Gmf, and from the air chamber 12 of both sides, 14 fluidisations that eject are littler than the former with the mass velocity of air, generally be taken in the scope of 0-3Gmf, the mass velocity of 12 injection airs of air chamber that is furnished with heat recovery chamber 4 bottoms of heat-transfer pipe 5 is good with 0-2Gmf, and the mass velocity that forms the air that the air chamber 14 of main chamber 3 bottoms sprayed is good with 1-2Gmf.
The result, in main chamber 3 inside, because the fluidisation that ejects from air chamber 13 is big with the mass velocity of air from the fluidisation that air chamber 12,14 ejects with the mass-velocity ratio of air, so top at air chamber 13, air and flow media are the jet state, and the motion upward sharp from fluidized bed inside is in case spray from the surface of fluidized bed, i.e. diffusion towards periphery, and flow media just drops on the fluidized bed surface on air chamber 12,14 tops.
On the other hand, in the fluidized bed on air chamber 13 tops, for the space of fill flow moving medium after moving upward, two lateral movements get fluidized bed slowly, the flow media of the fluidized bed of air chamber 12,14 tops bottom just, just to middle body, promptly move on the top of air chamber 13.So in fluidized bed, middle body forms rapid upwelling, peripheral part then forms the mobile layer that descends slowly.
Be provided with vertical dividing plate 18 in the fluidized bed above air chamber 12,13 intersections, 5 tops that are arranged in air chamber 12 of heat-transfer pipe in the back side and the fluidized bed between the water-cooling wall of dividing plate 18, thereby have formed heat recovery chamber.The height of dividing plate 18 can allow the flow media of 4 li of heat recovery chamber return the opening 19 that goes in the main chamber except making that flow media can enter the heat recovery chamber 4 in motion process above air chamber 13, also should having between the dispersion plate of dividing plate 18 and bottom surface.Therefore, flow media is in the combustion chamber after the rapid rising of jet-like, in the fluidized bed diffusion into the surface, cross dividing plate 18 and enter heat recovery chamber, that causes along with the air that utilizes air chamber 12 to be blown into again flows and decline gradually slowly, during this period, carries out heat exchange by heat-transfer pipe 5.
The amount of flow media sedimentation circulation in heat recovery chamber can be used the air quantity that spreads from air chamber 12, and control with the air quantity of air from the liquidation that air chamber 13 sprays in main chamber in heat recovery chamber 4.That is, if the air capacity that the fluidisation that blows out from air chamber 13 is used increases, then the amount of the flow media of sedimentation circulation also increases.In addition, as shown in Figure 7, when when changing in the scope of air quantity at 0～1Gmf of the indoor diffusion of recuperation of heat, the amount of the flow media of sedimentation almost changes with it with being directly proportional in the heat recovery chamber, when the air quantity that spreads in the heat recovery chamber during, then almost invariable greater than 1Gmf.
The amount of this invariable flow media roughly with the amount G of the flow media that enters heat recovery chamber 4
1Equate, so the amount of the flow media of sedimentation correspondingly also is G in the heat recovery chamber
1By means of regulating above-mentioned two kinds of air quantity, can control the amount of the flow media of sedimentation in the heat recovery chamber 4.
On the other hand, when from the flow media of sedimentation, carrying out the recovery of heat by heat-transfer pipe 5, when the air quantity that spreads in heat recovery chamber 4 from air chamber 12 changes between 0～2Gmf, the variation of its heat transfer coefficient as shown in Figure 9, roughly linearly variation, so, can control the heat of recovery and the fluidized bed temperature in the main chamber 3 as required by means of the air quantity that changes diffusion.
Promptly, when the amount of the fluidization air in air chamber 13 enters main chamber 3 is constant, as increase the air quantity of 4 li diffusions of heat recovery chamber, when then increasing with the internal circulating load of flow media, heat transfer coefficient also increases, because these two effects that multiplied together caused increase considerably with regard to the heat that makes recovery.Reclaim this a part of that a part of balance mutually that increases with the interior heat that produces of main chamber that increases in the heat, so just can make the temperature maintenance of fluidized bed invariable.
In addition, three times of the rate of wear that it is generally acknowledged heat-transfer pipe in the fluidized bed and fluidizing velocity are directly proportional, so the relation of the mass velocity of fluidizing gas and the heat-transfer pipe rate of wear as shown in figure 10.That is, as to establish the diffusion air quantity that is blown into heat recovery chamber be 0～3Gmf, and (preferably 0～2Gmf), then the wearing and tearing of heat-transfer pipe are few, can improve its life-span.
On the other hand, simultaneously partly infeed coal as fuel to the beginning of 3 li decline mobile layers in the combustion chamber.So just can make the fuel circulation of in the fluidized bed of high temperature, circling round, even the high coal of combustible ratio also can completing combustion, and can carry out the burning of high load capacity, so except can making the boiler miniaturization, to the kind of coal also without limits, therefore, made contribution for applying of boiler.
Waste gas enters cyclone dust collectors 7 after discharging from boiler.The particle that in cyclone separator, is captured, by the dual baffle plate 8 in the bottom in the boiler shown in Figure 1, the coal that infeeds abreast enters hopper 10 together, by means of feeding screw 11, send into after the mixing in the decline mobile layer of main chamber, unburned part (charcoal) in the particle of capture is burnt away, and help to reduce nitrogen oxide.Certainly, the particle that is captured in the cyclone separator can not mix with coal in advance yet, but before being transported to main chamber separately, and circulates in the mobile layer by means of circling round after entering the decline mobile layer of main chamber and mix.
On the other hand, on free space top, be provided with convection heat transfer' heat-transfer by convection parts 6, carry out the recovery of heat, and the function with economizer, evaporation tube for the ignition temperature in the free space can keep constant, preferably remains on 900 ℃, in case of necessity, can be at the heat-insulating material 17 of the bottom of convection heat transfer' heat-transfer by convection parts 6 and combustion chamber one side attaching refractory material of water cooled furnace wall and so on.On the convection heat transfer' heat-transfer by convection parts, can wrap it with heat-insulating material near each root heat-transfer pipe of free space, but, in this case, female mediocre superfluous words should be taken into account the circulation that does not hinder waste gas when the spacing of determining between the heat-transfer pipe.
Like this, owing to added heat-insulating material 17, the bottom of free space part just can remain on the condition of high temperature, and the air for second-time burning that is blown into from the air intlet 20 of free space just can play the effect of minimizing CO.
Fig. 2 is an alternative embodiment of the invention.
The structure of boiler identical with shown in Fig. 1 basically among Fig. 2, the course of work is also identical.Main difference is that the bottom that separates the dividing plate 38 of main chamber 23 and heat recovery chamber 24 tilts, in order that be blocked in the big air-flow of fluidizing velocity that main chamber is upwards sprayed by air chamber 33, and this part air-flow is turned, flow to the top of the little air chamber of fluidizing velocity 34, the angle that tilts is for becoming 10～60 degree angles, preferably 25～45 degree with horizontal plane.In addition, the projected length 1 of the horizontal direction of dividing plate sloping portion on furnace bottom accounts for 1/6～1/2 of this furnace hearth level direction length L, and preferably 1/4～1/2.
The fluidized bed of boiler body 21 bottoms is divided into heat recovery chamber 24 and main chamber 23 with aforementioned barriers, is provided with the air dispersion plate 22 that fluidisation is used in main chamber 23 bottoms.
In addition, the middle body of the air dispersion plate 22 that fluidisation is used is low, and that side height relative with heat recovery chamber.And two kinds of air chambers 33,34 are arranged at the bottom of dispersion plate 22.
The mass velocity of the air that the fluidisation that ejects from the air chamber 33 of central authorities is used must be the sufficiently high speed that can form the fluidized bed of flow media in main chamber, i.e. 4～20Gmf, preferably in the scope of 6～12Gmf, and the air quality speed of using from the fluidisation that air chamber 34 ejects is littler than the former, in the scope of 0～3Gmf, at this moment, flow media on air chamber 34 is not to carry out fierce moving up and down, but is forming the mobile layer that descends in the flow regime slowly.This mobile layer below expand and come, move to air chamber 33 above the time, be subjected to the effect of the very big fluidization air of the mass velocity that ejects from air chamber 33 and upwards blow afloat.So, since the flow media of mobile layer bottom some be blown away, mobile layer just depends on deadweight to descend.On the other hand, the flow media that the fluidisation that is sprayed by air chamber 33 upwards blows afloat with the jet power of air has changed the direction of motion because of hitting on the dividing plate that tilts, and major part drops on mobile layer top, is that the mobile layer that descends replenishes flow media.The result that this process is carried out continuously, the mobile layer of slow decline has just been formed at the top of air chamber 34, and as a complete unit, then the flow media in the main chamber 23 has formed circumnutation stream.On the other hand, the air that the fluidisation that is sprayed by air chamber 33 is used upwards blows afloat, and again because of tilt clapboard 38 changes a part in the flow media of direction, crosses the top of tilt clapboard 38 and enters heat recovery chamber 24.Enter the flow media in the heat recovery chamber 24, form the mobile layer that descends slowly by means of the air that is blown into from diffused air device 32.
When the reduction of speed degree was slow instantly, the flow media that enters heat recovery chamber formed the angle of repose on the top of heat recovery chamber, and its redundance then falls back in the main chamber from the top of tilt clapboard 38.
In heat recovery chamber,,, then, flow back into main chamber from opening portion 39 Yi Bian carry out heat exchange by heat-transfer pipe 25 Yi Bian flow media descends lentamente.
The sedimentation internal circulating load of flow media and the heat of recovery are the same with the embodiment shown in Fig. 1 in the heat recovery chamber, can control with the diffusion air quantity that is blown in the heat recovery chamber.Boiler as shown in Figure 2 is to be controlled by blow into the air capacity of coming from diffused air device 32, and its mass velocity is preferably in the scope of 0～2Gmf between 0～3Gmf.
On the other hand, waste gas just enters cyclone dust collectors 27 after discharging from boiler.The particle that in cyclone dust collectors 27, is captured, by double-deck baffle plate 28, enter hopper 30 with the coal that infeeds abreast, by means of feeding screw 31, send into the decline mobile layer of main chamber 23 after the mixing, be the top of air chamber 34, the unburned part (charcoal) in the particle of capture burns away, and helps to reduce nitrogen oxide.
The particle that is captured in cyclone separator 27 also can be used and the different feeding device shown in Fig. 2, do not infeed together with coal, but infeed separately, nor one establishes a capital and uses feeding screw, also can use the air carrying method.
On the other hand,, be provided with convection heat transfer' heat-transfer by convection parts 26, carry out the recovery of heat on free space top.In order to keep ignition temperature in the free space on 900 ℃ of constant optimum temperatures, as required, except attaching in the combustion chamber of convection heat transfer' heat-transfer by convection parts 26 bottoms and water cooled furnace wall one side the heat-insulating material 37 of refractory material and so on, also be provided with the air intlet 40 that second-time burning is used, it has the effect that reduces CO and so on.
Fig. 3 is another embodiment of the present invention.It is that the heat recovery chamber among the embodiment shown in Figure 2 is respectively established one Face to face basically on the position of symmetry, makes an integral body altogether.The result, the air chamber 53 that the air quality speed that ejects is little is arranged in the position of central authorities, the air chamber 52,54 that mass velocity is big then is arranged on the position of both sides, so the flow media that the air that is ejected by air chamber 52,54 blows afloat stream because of hit tilt clapboard 58,58 ' above the change flow direction, fall middle body, form the decline mobile layer, and arrive the top of air chamber 53, about here being divided into two strands, blown again.Therefore, in the fluidized bed of main chamber, exist the stream that circles round of two bursts of symmetries.
Coal and with the particle that cyclone dust collectors captured then infeed central authorities the decline mobile layer.
Among Fig. 3, the feed position is in main chamber, and * represents with mark, and the direction of feed is the direction vertical with paper.In the example of Fig. 3, infeed after being mixed with feeding screw 51 by particle that cyclone dust collectors captured and coal, but also can be different from the example shown in the figure, the particle of coal and capture infeeds respectively, perhaps also can adopt the air input method.
On the other hand, the air that is ejected by air chamber 52,54 and the flow media stream that causes is because of tilt clapboard 58,58 ' when changing flow direction, wherein some crosses dividing plate, entered heat recovery chamber 44,44 '.
The sedimentation internal circulating load of the flow media in the heat recovery chamber can be by controlling with the air quantity of the diffused air of air- diffuser 60,60 same shown in Fig. 2 ' introduced.
Flow media is by after the heat-transfer pipe 45,45 ' carry out exchange heat, by opening portion 59,59 ' flow back in the main chamber.
On the other hand, be provided with convection heat transfer' heat-transfer by convection parts 46 on free space top, carry out the recovery of heat, in order to keep the ignition temperature in the free space constant, preferably 900 ℃, as required, except attaching in the combustion chamber of convection heat transfer' heat-transfer by convection parts 46 and water cooled furnace wall one side the heat-insulating material of refractory material and so on, also be provided with the air intlet 61 that second-time burning is used, can reduce CO effectively.
Below, to Figure 14, illustrate that the present invention becomes as a whole heat transfer tube group waste gas to be carried out other embodiment of heat recovery by means of the downstream that is arranged on free space and with free space with reference to Figure 11.
To be the present invention carry out the profilograph of embodiment of a kind of composite circulation fluidizing bed boiler of heat recovery by means of the downstream that is arranged on free space and with the heat transfer tube group that free space becomes one to Figure 11 to waste gas, and Figure 12 is along the profile of A-A line among Figure 11.In Figure 11 and Figure 12, label 201 is boiler bodies, label 202 is air divergent nozzles that fluidisation is used, the 203rd, main chamber, 204,204 ' be heat recovery chamber, 205,205 ' be heat-transfer pipe, the 207th, cyclone dust collectors, the 208th, revolving valve, the 209th, fuel supply pipe, the 210th, hopper, the 211st, the feeding screw that fuel supplying is used, 212,213 and 214 is air chambers, 218,218 ' be dividing plate, 219,219 ' be the backflow part of heat recovery chamber bottom, the 220th, the auxiliary air inlet tube, the 229th, waste gas outlet, the 230th, dry drum, the 231st, drum, the 232nd, the convection heat transfer' heat-transfer by convection chamber, 233,234 and 235 is the dividing plates in the convection heat transfer' heat-transfer by convection chamber, the 236th, and evaporation tube, the 237th, water wall, the 238th, the bottom of convection heat transfer' heat-transfer by convection chamber, the 239th, conveying worm, the 240th, the blast pipe of convection heat transfer' heat-transfer by convection chamber, 242,242 ', 243,243 ' be and the different air-diffuser of pattern shown in Fig. 2 and Fig. 3.
The main chamber of Figure 11 and Figure 12, the effect of heat recovery chamber, fully with identical to the explanation that Fig. 3 did, be with the boiler difference shown in Fig. 3, in the boiler among Figure 11 and Figure 12, the heat transfer tube group that reclaims heat from waste gas is not arranged on the free space part, and is arranged on the downstream of free space and becomes as a whole convection heat transfer' heat-transfer by convection part with free space.
That is to say, the waste gas of discharging from the waste gas outlet 229 of free space part enters the object heat transfer chamber 232 that has the evaporation tube group that is arranged between dry drum 230 and the drum 231, by means of the effect that is arranged in the indoor dividing plate of convection heat transfer' heat-transfer by convection, waste gas along the direction of arrow indication in the process of convection heat transfer' heat-transfer by convection chamber downstream flow, carry out exchange heat with the water in the evaporation tube group, be cooled to after 250～400 ℃, enter cyclone dust collectors 207 through blast pipe 240, after having captured the fine particle that contains charcoal at cyclone dust collectors, enter atmosphere.Drop into afterwards with from dog-house 209 through revolving valve 208 by the fine particle that contains charcoal that cyclone dust collectors captured, infeed through hopper 210 and feeding screw 211 boiler coal and so on fuel together, send back to from same inlet directly over the decline mobile layer of fluid bed of combustion chamber 203.
On the other hand, the flow media that the diameter that is separated in convection heat transfer' heat-transfer by convection part 232 is bigger, desulfurizing agent and contain the particle of charcoal, then aggregation is in the V-shape of convection heat transfer' heat-transfer by convection part bottom bottom, sent back to directly over the fuel of main chamber 203 infeeds the decline mobile layer of the relative side of side by conveying worm 239.
As Figure 11 and shown in Figure 12, when convection heat transfer' heat-transfer by convection partly being arranged on the downstream of free space part, as shown in figure 11, because it is opposite from the flow direction that free space flows into the convection heat transfer' heat-transfer by convection part with waste gas to be blown into the direction of auxiliary air, make and in free space, caused the stream that circles round, effectively oxygen and waste gas are mixed, very big effect is arranged for reducing CO.
Below with reference to Figure 13 an alternative embodiment of the invention is described.
Figure 13 is equivalent to the such profile of Figure 12, except label 238 ' and 239 ' also be that same label is represented same parts the V font bottom and conveying worm of expression convection heat transfer' heat-transfer by convection part.
In this embodiment, only be provided with two V font bottoms 238,238 ' (W font bottom) in bottom, convection heat transfer' heat-transfer by convection chamber, and V font bottom 238,238 ' middle aggregation bigger contain carbon granule be with two conveying worms 239,239 ' send back to flow media in the heat recovery chamber that is arranged on the both sides, combustion chamber decline mobile layer 204,204 ' directly over this 2 point of going, different with the boiler shown in Figure 11 and Figure 12.
Figure 14 is another embodiment of the present invention.
Label 241 expression conduits among Figure 14, other label are all identical with label meaning among Figure 11.
Embodiment among Figure 14 and the embodiment difference shown in Figure 11 only are, the fine particle that contains charcoal that is captured by cyclone dust collectors 207 by the top of the feeding screw 239 of conduit 241 input convection heat transfer' heat-transfer by convection parts 232 bottoms after and in the convection heat transfer' heat-transfer by convection part, captured bigger contain carbon granule send back to together main chamber the decline mobile layer directly over.
Claims (14)
1, a kind of composite circulation fluidizing bed boiler, it is that the fluid bed of boiler partly is divided into main chamber and heat recovery chamber, at least dispose two kinds of air chambers in the main chamber bottom, a kind of air chamber makes flow media have big fluidizing velocity, a kind of air chamber makes flow media have little fluidizing velocity, by means of making up the air that ejects from these two kinds of air chambers with different fluidizing velocities, make the flow media in the main chamber produce the circular flow that circles round, and, between main chamber and heat recovery chamber, form a kind of like this inner loop fluidized-bed combustion boiler of the circular flow of flow media, it is characterized in that, carry out the heat recovery of waste gas, after the cooling exhaust of the exit of boiler, waste gas is introduced cyclone dust collectors, and the particle that will be captured in these cyclone dust collectors sends above-mentioned main chamber or heat recovery chamber back to, send back to the little decline mobile layer of opening fluidizing velocity in fluidized bed of particle of capture directly over, in the mobile layer that perhaps descends.
2, composite circulation fluidizing bed boiler as claimed in claim 1, it is characterized in that, the dividing plate that separates above-mentioned main chamber and heat recovery chamber is made inclination, in order that in main chamber, eject the big air chamber of mass velocity above stop the air-flow that makes progress that ejects from this air chamber, and this a part of air-flow is turned, flow to the top of the little air chamber of liquidation air quality speed.
3, composite circulation fluidizing bed boiler as claimed in claim 1 or 2 is characterized in that the decline mobile layer supply desulfurizing agent to main chamber.
4, as each described composite circulation fluidizing bed boiler in the claim 1,2,3, it is characterized in that, waste gas is cooled to 250 °～400 ℃ introduces cyclone dust collectors afterwards.
5, as each described composite circulation fluidizing bed boiler in the claim 1,2,3,4, it is characterized in that, reclaim the heat of waste gas by the heat transfer tube group in the free space part that is arranged on the fluidized bed top.
6, as each described composite circulation fluidizing bed boiler in the claim 1,2,3,4, it is characterized in that, partly become as a whole heat transfer tube group to reclaim the heat of waste gas by the downstream that is arranged on free space part and with free space.
7, composite circulation fluidizing bed boiler as claimed in claim 6, it is characterized in that, by being arranged on free space portion downstream side and partly becoming the bigger flow media of the diameter that part captured at as a whole heat transfer tube group place with free space, desulfurizing agent and carbon granule, send back to the conveying machinery of conveying worm and so on fluidized bed in the main chamber the decline mobile layer directly over or among the decline mobile layer.
8, composite circulation fluidizing bed boiler as claimed in claim 6, it is characterized in that, partly become the bigger flow media of the diameter that part captured at as a whole heat transfer tube group place by the downstream that is arranged on free space part and with free space, desulfurizing agent and carbon granule, send back to the conveying machinery of conveying worm and so on flow media in the heat recovery chamber the decline mobile layer directly over or among the decline mobile layer.
9, composite circulation fluidizing bed boiler as claimed in claim 8 is characterized in that, the flow media that diameter is bigger, desulfurizing agent and carbon granule send back in two heat recovery chamber that are arranged on the main chamber left and right sides.
10, as each described composite circulation fluidizing bed boiler in the claim 7,8,9, it is characterized in that, by the particle that contains tiny carbon granule that cyclone dust collectors captured, by the above-mentioned particle that part captured that becomes as a whole heat transfer tube group place with free space, all use the conveying machinery of conveying worm and so on to send fluid bed part or heat recovery section back to.
11, as each described composite circulation fluidizing bed boiler in the claim 1 to 10, it is characterized in that, have by means of being blown into flow direction and flowing to the opposite auxiliary air of exhaust gas flow direction of convection heat transfer' heat-transfer by convection part from free space, make the structure that in the free space part, produces the gyration airflow of waste gas.
12, a kind of composite circulation fluidizing bed boiler, it is that the fluid bed of fluidized-bed combustion boiler is divided into main chamber and heat recovery chamber, in the main chamber bottom, be provided with and make flow media have big flowing velocity and make flow media have two kinds of air chambers of little flowing velocity, by means of the air that makes up the friction speed that from these two kinds of air chambers, ejects, make the flow media in the main chamber produce the circular flow that circles round, and, between main chamber and heat recovery chamber, form a kind of like this inner loop fluidized-bed combustion boiler of the circular flow of flow media, it is characterized in that, in its structure, be arranged on the downstream of the free space part of main chamber in addition, and partly become as a whole convection heat transfer' heat-transfer by convection parts with free space, and, in free space part be provided with dry drum above the convection heat transfer' heat-transfer by convection parts, below the convection heat transfer' heat-transfer by convection parts, be provided with drum, draw the pipeline of the water wall that constitutes main chamber from the free space top partly of this dry drum, to in the convection heat transfer' heat-transfer by convection part, the evaporation tube that reclaims its heat when making waste gas cooling then is arranged between dry drum and the drum, and have with the particle that is captured in the convection heat transfer' heat-transfer by convection part send back to back the flow media flowing velocity is little in main chamber or the heat recovery chamber decline mobile layer directly over or device among the decline mobile layer.
13, composite circulation fluidizing bed boiler as claimed in claim 12, it is characterized in that, it also has the particle aggregation that the V font bottom that is arranged in drum below is captured, with the conveying worm that is located at V font bottom these particles are sent back to flow media in main chamber or the heat recovery chamber the decline mobile layer directly over or the device that goes among the decline mobile layer.
14, composite circulation fluidizing bed boiler as claimed in claim 12, it is characterized in that, it also has being arranged in the particle aggregation that W font bottom, drum below is captured, with two conveying worms that are arranged on W font bottom these particles are sent back to flow media in main chamber or the heat recovery chamber the decline mobile layer directly over or the device that goes among the decline mobile layer.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP215135/88 | 1988-08-31 | ||
| JP21513588 | 1988-08-31 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1041646A true CN1041646A (en) | 1990-04-25 |
| CN1017469B CN1017469B (en) | 1992-07-15 |
Family
ID=16667285
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89107888A Expired CN1017469B (en) | 1988-08-31 | 1989-08-31 | Composite circulation fluidizing bed boiler |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0431163B1 (en) |
| KR (1) | KR100229691B1 (en) |
| CN (1) | CN1017469B (en) |
| AT (1) | ATE131271T1 (en) |
| AU (1) | AU4199889A (en) |
| CA (1) | CA1332685C (en) |
| DE (1) | DE68925033T2 (en) |
| MY (1) | MY104683A (en) |
| WO (1) | WO1990002293A1 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100417862C (en) * | 2005-12-09 | 2008-09-10 | 清华大学 | Horizontal circulating fluidized bed burning equipment and its circulating burning method |
| CN103090397A (en) * | 2013-01-16 | 2013-05-08 | 河南科技大学 | Sludge and coal fluidized bed co-firing reactor |
| CN104136842A (en) * | 2012-02-13 | 2014-11-05 | 荏原环境工程有限公司 | In-bed heat transfer tube for fluidized bed boiler |
| CN104279548A (en) * | 2013-07-12 | 2015-01-14 | 李雨田 | Energy-collecting heat exchange environment-friendly boiler |
| CN105444160A (en) * | 2014-08-29 | 2016-03-30 | 中国科学院工程热物理研究所 | Circulating fluidized bed fine ash burning apparatus |
| CN106196124A (en) * | 2016-08-23 | 2016-12-07 | 苏州泰盛新绿节能环保科技有限公司 | A kind of coal-burning boiler assembly reducing smoke evacuation oxygen content |
| 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 |
| CN114353049A (en) * | 2021-12-25 | 2022-04-15 | 江苏中科重工股份有限公司 | Method and equipment for recycling steam-water heat of boiler drain flash tank |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2116745C (en) * | 1993-03-03 | 2007-05-15 | Shuichi Nagato | Pressurized internal circulating fluidized-bed boiler |
| FI122040B (en) * | 2009-11-10 | 2011-07-29 | Foster Wheeler Energia Oy | Process and arrangement for feeding fuel into a boiler with circulating fluidized beds |
| JP5992322B2 (en) * | 2012-12-28 | 2016-09-14 | 住友重機械工業株式会社 | Circulating fluidized bed boiler |
| FI126744B (en) | 2013-05-14 | 2017-04-28 | Valmet Technologies Oy | Arrangement and method of fluidization boiler |
| JP7079627B2 (en) * | 2018-03-13 | 2022-06-02 | 荏原環境プラント株式会社 | Fluidized bed heat recovery device |
| EP3957909B1 (en) | 2020-08-20 | 2024-06-26 | Steinmüller Engineering GmbH | Asymmetric fluidized-bed furnace for combustion of materials and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1517166A1 (en) * | 1963-12-03 | 1969-05-14 | Container Corp | Process for treating a waste liquor containing organic and inorganic substances |
| DE2449798C2 (en) * | 1974-10-19 | 1982-10-07 | Thyssen Industrie Ag, 4300 Essen | Fluidized bed furnace for the incineration of partially dewatered sludge |
| US4253425A (en) * | 1979-01-31 | 1981-03-03 | Foster Wheeler Energy Corporation | Internal dust recirculation system for a fluidized bed heat exchanger |
| JPS57139205A (en) * | 1981-02-23 | 1982-08-28 | Babcock Hitachi Kk | Fluidized bed furnace |
| GB2151503B (en) * | 1981-12-15 | 1986-08-20 | William Benedict Johnson | Fluidized bed combustion apparatus and method of carrying out fluidized bed combustion |
| CH659876A5 (en) * | 1983-05-10 | 1987-02-27 | Sulzer Ag | Fluid bed firing. |
| JPS62141408A (en) * | 1985-12-13 | 1987-06-24 | Mitsubishi Heavy Ind Ltd | Circulation type fluidized bed combustor |
| CA1285375C (en) * | 1986-01-21 | 1991-07-02 | Takahiro Ohshita | Thermal reactor |
| JPS63143409A (en) * | 1986-12-03 | 1988-06-15 | Mitsubishi Heavy Ind Ltd | Fluidized bed boiler of circulation type |
-
1989
- 1989-08-30 AT AT89909857T patent/ATE131271T1/en not_active IP Right Cessation
- 1989-08-30 AU AU41998/89A patent/AU4199889A/en not_active Abandoned
- 1989-08-30 DE DE68925033T patent/DE68925033T2/en not_active Expired - Fee Related
- 1989-08-30 EP EP89909857A patent/EP0431163B1/en not_active Expired - Lifetime
- 1989-08-30 WO PCT/JP1989/000883 patent/WO1990002293A1/en active IP Right Grant
- 1989-08-31 CN CN89107888A patent/CN1017469B/en not_active Expired
- 1989-08-31 CA CA000610057A patent/CA1332685C/en not_active Expired - Fee Related
- 1989-11-30 MY MYPI89001666A patent/MY104683A/en unknown
- 1989-12-29 KR KR1019890702496A patent/KR100229691B1/en not_active IP Right Cessation
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100417862C (en) * | 2005-12-09 | 2008-09-10 | 清华大学 | Horizontal circulating fluidized bed burning equipment and its circulating burning method |
| CN104136842A (en) * | 2012-02-13 | 2014-11-05 | 荏原环境工程有限公司 | In-bed heat transfer tube for fluidized bed boiler |
| CN104136842B (en) * | 2012-02-13 | 2016-05-11 | 荏原环境工程有限公司 | Heat-transfer pipe in the layer of fluidized bed boiler |
| CN103090397A (en) * | 2013-01-16 | 2013-05-08 | 河南科技大学 | Sludge and coal fluidized bed co-firing reactor |
| CN104279548A (en) * | 2013-07-12 | 2015-01-14 | 李雨田 | Energy-collecting heat exchange environment-friendly boiler |
| CN105444160A (en) * | 2014-08-29 | 2016-03-30 | 中国科学院工程热物理研究所 | Circulating fluidized bed fine ash burning apparatus |
| CN105444160B (en) * | 2014-08-29 | 2019-01-08 | 中国科学院工程热物理研究所 | Recirculating fluidized bed fine ash burner |
| CN106196124A (en) * | 2016-08-23 | 2016-12-07 | 苏州泰盛新绿节能环保科技有限公司 | A kind of coal-burning boiler assembly reducing smoke evacuation oxygen content |
| 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 |
| CN110043895A (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 and its control method |
| CN114353049A (en) * | 2021-12-25 | 2022-04-15 | 江苏中科重工股份有限公司 | Method and equipment for recycling steam-water heat of boiler drain flash tank |
Also Published As
| Publication number | Publication date |
|---|---|
| AU4199889A (en) | 1990-03-23 |
| MY104683A (en) | 1994-05-31 |
| WO1990002293A1 (en) | 1990-03-08 |
| KR900700822A (en) | 1990-08-17 |
| CN1017469B (en) | 1992-07-15 |
| ATE131271T1 (en) | 1995-12-15 |
| CA1332685C (en) | 1994-10-25 |
| DE68925033T2 (en) | 1996-05-15 |
| EP0431163A1 (en) | 1991-06-12 |
| EP0431163A4 (en) | 1992-05-20 |
| EP0431163B1 (en) | 1995-12-06 |
| KR100229691B1 (en) | 1999-11-15 |
| DE68925033D1 (en) | 1996-01-18 |
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