CN201526976U - Refuse-fired boiler for circulating fluidized bed - Google Patents
Refuse-fired boiler for circulating fluidized bed Download PDFInfo
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- CN201526976U CN201526976U CN2009202463553U CN200920246355U CN201526976U CN 201526976 U CN201526976 U CN 201526976U CN 2009202463553 U CN2009202463553 U CN 2009202463553U CN 200920246355 U CN200920246355 U CN 200920246355U CN 201526976 U CN201526976 U CN 201526976U
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- circulating fluid
- refuse incinerator
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Abstract
A refuse-fired boiler for circulating fluidized bed comprises a steel frame and a hearth body, a middle flue, a tail flue and a boiler drum, which are equipped on the steel frame. A flue gas separator and a feed back device are provided in the middle flue. The flue gas separator and the feed back device are respectively connected with the hearth body. The tail flue is connected with the flue gas separator. A steam-water system which is connected with the boiler drum is provided in the hearth body and the tail flue. The hearth body comprises the following components: an upper water hating wall hearth, a middle heat insulation hearth and a lower heat insulation hearth, wherein, the middle heat insulation hearth and the lower heat insulation hearth have hearth structures without heating surface for preventing the heat loss caused after refuse firing and using the heat for preheating and igniting the newly input refuse. The refuse-fired boiler for circulating fluidized bed reduces the operation cost of refuse-burning power plant and increases the suitability to the change of refuse quality.
Description
Technical field
The utility model relates to a kind of garbage power equipment, particularly a kind of refuse incinerator of circulating fluid bed.
Background technology
At present, along with the raising of quickening of urbanization process and living standards of the people, the life of urban resident garbage disposal has become an important content of environmental protection.The rubbish total amount that 655 in China in 2007 establishes the city, city promptly reaches 1.25 hundred million tons, and a lot of cities face " garbage-surrounded city ", and rubbish processing to be harmless has become one of of paramount importance environmental protection problem.
In three kinds of methods of rubbish processing to be harmless, waste incineration and generating electricity is press close to garbage disposal most innoxious, and therefore the processing mode of minimizing and resource three principles has begun in China developed.Wherein, adopt the equipment investment of refuse incinerator of circulating fluid bed few, be applicable to that refuse thermal value is lower, acidity and the bigger house refuse of moisture.But, the refuse incinerator of circulating fluid bed that China puts into operation at present, its burner hearth all is made of fin panel casing.Fin panel casing will absorb the heat in the stove, and the inner flue gas of the stove temperature is reduced, thus the preheating that has influence on rubbish catch fire, and do not reach dioxin and decompose the temperature that requires, thus all to drop into a certain proportion of coal, with the rubbish multifuel combustion to improve flue-gas temperature.The good calorific value height of rubbish quality can drop into some coals less, and rubbish calorific value of poor quality is low, will drop into some coals more.According to Tsing-Hua University's research, when rubbish was best in quality, the coal amount of input can not be less than 6% of whole fuel gross weight.Because the holding at high price of current China coal significantly improved the operating cost of refuse-burning plant, have in addition be in the loss edge.Application number is " 00108520.4 ", and name is called the disclosed garbage burning boiler of Chinese utility application file of " city house refuse internal circulating different weight fluidized-bed incineration boiler ", does not relate to the adiabatic problem of its combustion chamber; Application number is " 200410009082.2 ", name is called the disclosed CFBB of Chinese utility application of " a kind of CFBB that is used for burning domestic garbage ", reduce the fin panel casing heat absorption though in the combustion chamber, be provided with, guarantee the wall with refractory lining, refracto of combustion chamber internal combustion temperature, but structure and composition to this wall with refractory lining, refracto do not describe in detail, can't judge that from disclosed file how this wall with refractory lining, refracto realizes reducing the fin panel casing heat absorption, guarantees the function of combustion chamber internal combustion temperature.
The utility model content
Technical problem to be solved in the utility model provides a kind of shortcoming that overcomes prior art, do not need to add the combustion-supporting recirculating fluidized bed refuse-burning boilers of exotic fuels, to improve the adaptability that the rubbish quality is changed and to reduce the operating cost of refuse-burning plant.
To achieve these goals, the utility model provides a kind of refuse incinerator of circulating fluid bed, comprise the steel framework and be arranged on burner hearth body on the described steel framework, the middle part flue, back-end ductwork and drum, be provided with flue gas separation unit and feeding back device in the flue of described middle part, described flue gas separation unit is connected with described burner hearth body respectively with described feeding back device, described back-end ductwork is connected with described flue gas separation unit, be provided with boiler circuit in described burner hearth body and the described back-end ductwork, described boiler circuit is connected with described drum, wherein, described burner hearth body comprises:
The top water-evaporating furnace, it is provided with exhanst gas outlet, and described exhanst gas outlet is used for guiding flue gas into described flue gas separation unit;
The lower thermal barrier burner hearth, it is provided with garbage inlet, overfire air port and feed back inlet, and described feed back inlet is used to connect described feeding back device;
The middle part adiabatic furnace is used for connecting respectively described top water-evaporating furnace and described lower thermal barrier burner hearth;
Wherein, described middle part adiabatic furnace and described lower thermal barrier burner hearth are no heating surface chamber structure, are used to prevent that the heat that produces behind the incineration firing scatters and disappears, and drop into the preheating of rubbish and light described heat is used for the later stage.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, described no heating surface chamber structure comprises furnace wall and is installed in the pressure-bearing backplate of the outer surface of described furnace wall, described furnace wall comprises fire brick layer and builds outer field heat-insulation layer at described fire brick layer by laying bricks or stones.
Above-mentioned refuse incinerator of circulating fluid bed wherein, also is provided with multiple layer refractory brick support on the described furnace wall, described refractory brick support is fixed on the described pressure-bearing backplate.
Above-mentioned refuse incinerator of circulating fluid bed wherein, between described each layer refractory brick support, also is provided with the refractory brick drag hook, and described refractory brick drag hook is fixed on the described pressure-bearing backplate.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, the edge of described pressure-bearing backplate is provided with the two-way expansion joint that is used to seal, and described two-way expansion joint can absorb two-way expansion.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, described pressure-bearing backplate is the lattice structure of High-Strength Low-Alloy structural steel, the outer surface of described lattice structure adopts the low alloy steel plate hermetically-sealed construction.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, the longitudinal section of described lower thermal barrier burner hearth is wide at the top and narrow at the bottom trapezoidal, it is funnelform air distribution plate that the bottom port place of described lower thermal barrier burner hearth is provided with structure, described air distribution plate is provided with the deslagging mouth of pipe and many air drafts cap, and the described deslagging mouth of pipe is arranged on the centre of described many air drafts cap.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, described lower thermal barrier burner hearth bottom is connected with air compartment of water-cooled, air compartment of described water-cooled is provided with a wind inlet and is used to connect the burner interface that starts burner, and air compartment of described water-cooled is connected with described drum by pipeline.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, air compartment of described water-cooled comprise upper collecting chamber, next part case and be arranged at described upper collecting chamber and described next part case between fin panel casing, described upper collecting chamber, described next part case and described fin panel casing form the box-shaped air compartment jointly, and described air distribution plate is arranged in the described upper collecting chamber.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, air compartment of described water-cooled also is connected with scum pipe.
Above-mentioned refuse incinerator of circulating fluid bed wherein, is arranged at the air vent that the described deslagging mouth of pipe described blast cap on every side is provided with the center of pointing to described scum pipe.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, the angle of inclination of the funnel surface of described air distribution plate is 15 °～25 °.
Above-mentioned refuse incinerator of circulating fluid bed, wherein, be provided with convection bank in the described back-end ductwork, described convection bank is connected with described drum, described convection bank is the tube bank along the equidistant arrangement of described back-end ductwork width, and described tube bank becomes 10 °～15 ° angle in the horizontal direction with horizontal line.
Above-mentioned refuse incinerator of circulating fluid bed wherein, also is provided with urgent coal filling hole on the sidewall of described lower thermal barrier burner hearth, being used for the rubbish quality, interim when abominable especially to throw coal combustion-supporting.
Technique effect of the present utility model is: recirculating fluidized bed refuse-burning boilers of the present utility model, its burner hearth combustion zone that catches fire is built by laying bricks or stones by flame-proof thermal insulation material, the water-cooling wall heat sink that does not have regular circulation fluidized combustion garbage fired boiler, thereby improved the flue-gas temperature of the combustion zone that catches fire greatly, descend in the rubbish quality, when the rubbish calorific capacity reduces, still can fire burns, not needing to add other exotic fuels (such as coal) comes combustion-supporting, thereby reduced the operating cost of refuse-burning plant, increased the adaptability that the rubbish quality is changed.
Below in conjunction with the drawings and specific embodiments the utility model is described in detail, but not as to qualification of the present utility model.
Description of drawings
Fig. 1 refuse incinerator of circulating fluid bed structured flowchart of the present utility model;
Fig. 2 the utility model boiler circuit structured flowchart;
Fig. 3 a the utility model dust pelletizing system structured flowchart;
Fig. 3 b the utility model dreg removing system structured flowchart;
Fig. 4 the utility model air system structured flowchart;
Fig. 5 the utility model oozes drop liquid treating system structured flowchart;
Fig. 6 refuse incinerator of circulating fluid bed structural representation of the present utility model;
Air compartment structural representation of Fig. 7 water-cooled of the present utility model;
Fig. 8 furnace wall structure schematic diagram of the present utility model;
The A portion structure for amplifying schematic diagram of Fig. 9 Fig. 8;
The B portion structure for amplifying schematic diagram of Figure 10 Fig. 8;
Figure 11 a～Figure 11 e heterotypic fire brick structural representation of the present utility model;
Figure 12 the utility model cap structure schematic diagram;
Near special cap structure schematic diagram Figure 13 the utility model scum pipe;
Figure 14 the utility model scum pipe connection diagram.
Wherein, Reference numeral
An air compartment 2F2 of 1 water-cooled air supply pipe
1A upper collecting chamber 2F3,2F4 air vent
1B next part case 2G castable refractory
1C fin panel casing 2H refractory brick
1D air distribution plate 2M refractory brick drag hook
2 lower thermal barrier burner hearth 2N refractory brick supports
2A pressure-bearing backplate 3 middle part adiabatic furnaces
2B furnace wall 4 top water-evaporating furnaces
2C high-temperature-resistant thermal-insulation material 41 exhanst gas outlets
2D is common, and insulation material 5 starts burner
The two-way expansion joint 51 burner interfaces of 2E
6 wind inlets of 2F blast cap
2F1 crown 7 overfire air ports
8 garbage inlet 25A support girder steel
9 urgent coal filling hole 26 superheated steam outlets
10 ooze the drop liquid 27 corrugated expansion joints that enter the mouth
11 scum pipes, 100 burner hearth bodies
The 11A deslagging mouth of pipe 101 middle part flues
12 drums, 102 back-end ductworks
13 cyclone separators, 200 air systems
14 feeding back devices, 201 air preheaters
141 feed backs, 300 boiler circuits that enter the mouth
15 convection banks, 301 water-cooling systems
16 higher level's economizers, 302 superheaters
17 higher level's superheaters, 303 economizers
The 18 superheater 400a of subordinate dust pelletizing systems
19 desuperheats, 401 flue gas separation units
Coal 400b dreg removing system is economized by 20 subordinates
21 feed-water intakes, 500 soot blower systems
22 1 times wind air preheater 600 oozes the drop liquid treating system
23 secondary wind air preheaters, 601 cesspools
24 exhanst gas outlet ash buckets, 602 sewage pumps
25 steel frameworks
The specific embodiment
Below in conjunction with accompanying drawing structural principle of the present utility model and operation principle are done concrete description:
The utility model is that the solution refuse thermal value is low and fluctuation is big, poor combustion stability, the low dioxin that influences of combustion temperature in hearth decomposes, contain the strong problems such as sour gas of corrosivity in the flue gas, on the boiler overall structure, adopted the structural design that is different from the coal-fired fuel combination CFBB of conventional rubbish.
Referring to Fig. 1 and Fig. 6, Fig. 1 is a refuse incinerator of circulating fluid bed structured flowchart of the present utility model, and Fig. 6 is a refuse incinerator of circulating fluid bed structural representation of the present utility model.Refuse incinerator of circulating fluid bed of the present utility model, comprise steel framework 25 and be arranged on burner hearth body 100 on the described steel framework 25, middle part flue 101, back-end ductwork 102 and drum 12, be provided with flue gas separation unit 401 and feeding back device 14 in the described middle part flue 101, described flue gas separation unit 401 is connected with described burner hearth body 100 respectively with described feeding back device 14, described back-end ductwork 102 is connected with described flue gas separation unit 401, be provided with boiler circuit 300 in described burner hearth body 100 and the back-end ductwork 102, described burner hearth body 100 comprises: top water-evaporating furnace 4, its furnace wall is provided with the exhanst gas outlet 41 that is used for flue gas is guided into described flue gas separation unit 401, and described flue gas separation unit 401 is connected with described exhanst gas outlet 41; Lower thermal barrier burner hearth 2, its furnace wall 2B are provided with the garbage inlet 8 that is used to throw in rubbish, feed back inlet 141 and the overfire air port 7 that is used to connect described feeding back device 14; Be used to connect the middle part adiabatic furnace 3 of described top water-evaporating furnace 4 and described lower thermal barrier burner hearth 2.The bottom of described lower thermal barrier burner hearth 2 is connected with air compartment 1 of water-cooled, air compartment 1 of described water-cooled is provided with a wind inlet 6 and is used to connect the combustion chamber interface 51 that starts burner 5, the working medium heating surface of an air compartment 1 of described water-cooled is connected with described drum 12 by pipeline, is starting and can be with heat transferred working medium during operation guaranteeing; Air compartment 1 bottom of described water-cooled is connected with scum pipe 11; Wherein, described middle part adiabatic furnace 3 is used to prevent that with described lower thermal barrier burner hearth 2 heat that produces behind the incineration firing scatters and disappears, and newly drops into the preheating of rubbish and lights so that described heat is used for.Wherein, so-called adiabatic furnace is that the burner hearth combustion zone that catches fire is built by laying bricks or stones by flame-proof thermal insulation material, the water-cooling wall heat sink that does not have regular circulation fluidized bed garbage combustion boiler, thereby can improve the catch fire flue-gas temperature of combustion zone of burner hearth greatly, descend in the rubbish quality, when the rubbish calorific capacity reduces, still can fire burns, it is next combustion-supporting not need to add other exotic fuels, thereby reduces the operating cost of refuse-burning plant, increases the adaptability that the rubbish quality is changed.
Referring to Fig. 6, Fig. 6 is a refuse incinerator of circulating fluid bed structural representation of the present utility model.In the present embodiment, burner hearth body 100 tops are connected with flue gas separation unit 401, feeding back device 14 bottoms are connected with burner hearth body 100 bottoms, feeding back device 14 is positioned at the centre position with flue gas separation unit 401, flue gas separation unit 401 is connected with back-end ductwork 102, is furnished with convection bank 15, higher level's economizer 16, higher level's superheater 17, attemperator 19, subordinate's superheater 18, subordinate's economizer 20, wind air preheater 22, secondary wind air preheater 23 and an exhanst gas outlet ash bucket 24 in the back-end ductwork 102 from top to bottom successively.Above convection bank 15, higher level's economizer 16, higher level's superheater 17, subordinate's superheater 18, subordinate's economizer 20 be arranged as back-end surfaces.Be subjected to the wearing and tearing of soot particle in the flue gas for fear of back-end surfaces, control is flow through the average flue gas flow rate of back-end surfaces between 4～6m/s, usually, on tube bank plane perpendicular to flue gas flow direction, the area that the tube bank of flue cross-sectional area deduction occupies, be the circulation area of flue gas, exhaust gas volumn is certain, and circulation area is big more, and cigarette speed is low more, so increase the flue cross-sectional area or reduce the area that tube bank occupies, can reduce flue gas flow rate.The main employing increases the purpose that the flue cross-sectional area reaches reduction cigarette speed in the present embodiment, so the circulation basal area of this boiler back end ductwork 102 is than big by about 40% with the capacity boiler.
The longitudinal section of described lower thermal barrier burner hearth 2 is wide at the top and narrow at the bottom trapezoidal, and the longitudinal section of described middle part adiabatic furnace 3 and described top water-evaporating furnace 4 is a rectangle, is beneficial to flue gas and does at the uniform velocity to rise in burner hearth to flow with the burning of rubbish.Referring to Fig. 8, Fig. 9 and Figure 10, Fig. 8 is a furnace wall structure schematic diagram of the present utility model, and Fig. 9 is the A portion structure for amplifying schematic diagram of Fig. 8, and Figure 10 is the B portion structure for amplifying schematic diagram of Fig. 8.Described middle part adiabatic furnace 3 and described lower thermal barrier burner hearth 2 are furnace wall 2B and pressure-bearing backplate 2A co-ordinative construction, described furnace wall 2B comprises building by laying bricks or stones and is the refractory brick 2H of one and the outer field insulation material 2C that builds by laying bricks or stones at described refractory brick 2H, 2D, the side towards the fire of furnace wall 2B is built by laying bricks or stones with refractory brick 2H, described refractory brick 2H is heterotypic fire brick (referring to Figure 11 a～Figure 11 e), can engagedly avoid coming off after building by laying bricks or stones, described heterotypic fire brick can be high-alumina brick, half ganister brick or mullite brick, and build the insulation material 2C of adequate thickness by laying bricks or stones in the outside of heterotypic fire brick, 2D makes the hull-skin temperature of furnace wall be no more than 50 ℃.Insulation material is built high-temperature-resistant thermal-insulation material 2C by laying bricks or stones in a side of being close to refractory brick 2H, build common insulation material 2D again by laying bricks or stones in the high-temperature-resistant thermal-insulation material 2C outside, described insulation material can be alumino-silicate brick, pearlite brick or diatomite brick, in the common insulation material 2D outside is described pressure-bearing backplate 2A, be the outer surface that pressure-bearing backplate 2A is installed in described furnace wall 2B, described pressure-bearing backplate 2A is used to bear the weight of described furnace wall 2B and keeps the interior pressure of burner hearth.Described pressure-bearing backplate 2A is the lattice structure of High-Strength Low-Alloy structural steel, and the outer surface of described lattice structure seals with low alloy steel plate.The lower edge of described pressure-bearing backplate 2A is used for supporting, and top edge, left side edge and the right side edge of described pressure-bearing backplate 2A are provided with the expansion clearance.The edge of described pressure-bearing backplate 2A is provided with the two-way expansion joint 2E that can absorb two-way expansion, and described two-way expansion joint 2E is used for sealing.Described furnace wall 2B is along also being provided with multiple layer refractory brick support 2N on the short transverse, every layer of refractory brick support 2N becomes annular in the horizontal direction, in short transverse, every about about 2 meters, one deck furnace wall refractory brick support 2N is set, leave enough expansion clearances in refractory brick support 2N bottom, described refractory brick support 2N is fixed on the described pressure-bearing backplate 2A, between each layer of described each layer refractory brick support 2N, also be provided with the refractory brick drag hook 2M that is used to keep described furnace wall 2B surfacing, described refractory brick drag hook 2M is fixed on the described pressure-bearing backplate 2A.When building by laying bricks or stones, two-layer up and down fire-resistant brickwork joint will stagger, and forms " fourth " font brickwork joint structure, avoids occurring cross brickwork joint.Furnace wall supports refractory brick support 2N and refractory brick drag hook 2M is taken root on pressure-bearing backplate 2A, and except that the basecoat furnace wall, 2A bears furnace wall weight respectively by each several part pressure-bearing backplate, then by pressure-bearing backplate 2A with each weight transmitting to steel framework 25.
Top water-evaporating furnace 4 is the film water cold wall structure of steel pipe and band steel weldering system, and the upper collecting chamber of described fin panel casing is connected with described drum 12 respectively with the next part case of described fin panel casing.The outer surface of described fin panel casing is coated with insulation material, and described insulation material can be mineral wool, rock wool or mineral wool.The next part case of fin panel casing is connected with drum 12 usefulness downcomers, and upper collecting chamber is connected with drum 12 with the carbonated drink fairlead.Fin panel casing is divided into 3 water-flow circuits, and circulating ratio is all greater than 20.Fin panel casing is provided with fixed support at next part case place, makes fin panel casing begin upwards to expand from the next part case, makes the seam between fin panel casing and the adiabatic furnace brick wall keep very little, is easy to sealing.The outer surface of fin panel casing makes its hull-skin temperature less than 50 ℃ with insulation materials such as the thick mineral wool of 200mm, rock wool, mineral wools.The back wall of fin panel casing is provided with two outlets, guides flue gas into cyclone separator 13.In design during cyclone separator, at first to determine the size that enters the mouth, the size of inlet is decided by exhaust gas volumn of passing through and inlet flue gas speed.Exhaust gas volumn depends on the quantity of refuse of burning, and velocity of flue gas has the recommendation of certain limit as usual.After the size of inlet had been determined, other sizes of separator all were in proportion with inlet, and just the whole size dimension of separator can be decided.The exhaust gas volumn that separator passes through is big, and the inlet of separator is just big, and then the size of separator is big.The quantity of separator sees mainly whether whether the size of separator and the size of boiler are coordinated, mate.Present embodiment adopts two cyclone separators 13, and flue gas divides two outlets to enter two cyclone separators 13 simultaneously respectively by upper furnace, and cyclone separator 13 is coordinated with boiler like this, and the attaching parts size is also more suitable.In the present embodiment, the fin panel casing pipe adopts φ 51～φ 60 specifications, and material is 20G/GB5310, and the running temperature that the choosing of band steel width will make the band steel center line is less than 400 ℃, to avoid the high temperature corrosion district.When using general rubbish, burner hearth cross section flue gas flow rate is 3.7m/s in the time of 920 ℃.The furnace outlet temperature is 910 ℃, and material layer temperature is 930 ℃, and the furnace outlet excess air coefficient is taken as 1.4.Bed of material static height is got 600-800mm, and guaranteeing has enough heat storage capacities to keep smooth combustion.Cyclone separator 13 adopts two scroll casing type high-temperature heat insulation separators, and technology is reliably ripe, the separative efficiency height.The import flue gas flow rate is chosen for 20～25m/s, and the dipleg internal diameter is chosen for φ 600～φ 800mm.The refeed line internal diameter is φ 600～φ 800mm.Design material circulating ratio is 20, and material movement speed is about 0.3m/s in the dipleg column.
The operating pressure of emulsion zone is generally 8kpa in the stove, and pressure-bearing backplate 2A is by 1.5 times of furnace pressures, and promptly 12kpa designs, and pressure-bearing backplate 2A does not produce distortion during with the assurance operation.The lower edge of every pressure-bearing backplate 2A is supported on respectively on the upper collecting chamber 1A of a steel framework 25 or an air compartment 1 of water-cooled, leaves the expansion clearance between its excess-three edge and the steel framework 25.Between four edges of pressure-bearing backplate 2A and the adjacent structure with the two-way expansion joint 2E sealing that can absorb two-way expansion.
Because heat insulating construction is adopted in the middle and lower part of burner hearth, the heat that produces behind the incineration firing of previous input is not is not scattered and disappeared basically, can all be used for the later stage to drop into the preheating of rubbish and light, so can improve the adaptability of boiler greatly the rubbish mass change.Whole furnace height surpasses 23 meters, guarantees that the flowing time of flue gas in burner hearth surpasses 4 seconds, has fully satisfied the dioxin resolving time to be not less than 2 seconds requirement, and dioxin can be decomposed fully.Burner hearth adopts the air stage feeding system, and one time wind is sent into by the blast cap 2F on the air distribution plate 1D that is arranged in an air compartment 1 of water-cooled, accounts for about 60% of total blast volume, and a wind-warm syndrome degree is greatly between 260 ℃～300 ℃.The secondary air temperature degree between 190 ℃～240 ℃, is sent into by lower furnace portion overfire air port 7 greatly, under the jet-action of secondary wind, impels air fully to mix with unburnt combustible, reaches the purpose that makes the rubbish after-flame.The emulsion zone flue-gas temperature of lower furnace portion is greater than 900 ℃.
Referring to Fig. 2 and Fig. 6, Fig. 2 is the utility model boiler circuit structured flowchart, described boiler circuit 300 comprises water-cooling system 301, economizer 303, superheater 302 and drum 12, described water-cooling system 301, described superheater 302 and described economizer 303 are connected with drum 12 respectively, and the convection bank 15 in the described water-cooling system 301, described economizer 303 and described superheater 302 are arranged in the described back-end ductwork 102.In the present embodiment, described economizer 303 comprises higher level's economizer 16 and subordinate's economizer 20, described higher level's economizer 16 is used to reduce flue-gas temperature, can avoid the high-temperature region of flue gas to guarantee described superheater 302, make the entrance flue gas temperature of superheater 302 be not more than 580 ℃, to guarantee higher level's superheater 17, subordinate's superheater 18 can be avoided the high temperature corrosion zone of flue gas.The structure of higher level's economizer 16 is along the snakelike tube bank of the equidistant arrangement of flue width and adopts extended surface.Described subordinate economizer 20 is used for heated feed water and further reduces the temperature of described flue gas, and its structure is along the snakelike tube bank of the equidistant arrangement of flue width and adopts extended surface.Described superheater 302 comprises higher level's superheater 17 and subordinate's superheater 18, its structure is along the snakelike tube bank of the equidistant arrangement of flue width and adopts extended surface, also be provided with attemperator 19 between described higher level's superheater 17 and the described subordinate superheater 18, described attemperator 19 is connected with described subordinate superheater 18 with described higher level's superheater 17 respectively, described attemperator 19 can be convection-type desuperheater or spray attemperator, owing to limited superheater 302 entrance flue gas temperatures, made the tube wall temperature of superheater 302 can avoid the fume high-temperature corrosion region.Simultaneously, the superheater bank that is in the corrosion deathtrap adopts the steel that certain corrosion resistance is arranged, and is coated with enameling or anticorrosive paint in the part.Back-end surfaces 15,16,17,18,20 belong to the part of boiler circuit, and the operational process of boiler circuit 300 is as follows: the stove feedwater is come out from the feedwater console, enters the feed-water intake 21 of the inlet collection case of subordinate's economizer 20, water is heated to 170 ℃～190 ℃ at subordinate's economizer 20, and this moment, subordinate's economizer 20 interior refrigerant flow rates were controlled between 0.4～0.8m/s.Working medium is to flow at the tube interior of subordinate's economizer 20, if the flow of working medium is certain, then refrigerant flow rate depends on the size of ips of subordinate's economizer 20 and the number of tubes of subordinate's economizer 20 of flowing through simultaneously.By convention, the refrigerant flow rate in the economizer 303 can not be lower than 0.3m/s, can not be higher than 1.2m/s.Control refrigerant flow rate by the ips of control subordinate economizer 20 and the number of tubes of subordinate's economizer 20 in the present embodiment, refrigerant flow rate is met the requirements.After water comes out from the outlet collection case of subordinate's economizer 20, enter the inlet collection case of higher level's economizer 16 through tube connector.Water is heated to 270 ℃～290 ℃ at higher level's economizer 16, and this moment, higher level's economizer 16 interior refrigerant flow rates were controlled between 0.4～0.8m/s.Water enters drum 12 after coming out from higher level's economizer 16, is redistributed to water-cooling system 301 by drum 12.
Water-cooling system 301 is made up of three parts: top water-evaporating furnace 4, convection bank 15, air compartment 1 of water-cooled.The top water-evaporating furnace divides three closed circuits: each one of both walls, front-back wall share one.Air compartment 1 of convection bank 15 and water-cooled each has the independent loops loop.The layout of convection bank 15 is in order to replenish the deficiency of burner hearth evaporating heating surface, also to play the effect of the inlet flue gas temperature that reduces higher level's superheater 17 and subordinate's superheater 18 simultaneously.The effect of water-cooling system 301 is to absorb flue gas heat, and saturation water is evaporated to saturated vapor, and saturated vapor is introduced superheater through drum 12.After saturated vapor was introduced the inlet collection case of subordinate's superheater 18 by drum 12,18 tube banks were heated to 370 ℃～390 ℃ through subordinate's superheater, introduce attemperator 19 from the outlet collection case of subordinate's superheater 18 through tube connector again.Steam is through desuperheat, and temperature reduces.Steam behind the desuperheat is introduced the inlet collection case of higher level's superheater 17 through tube connector.After 17 tube banks of steam process higher level superheater are heated to 450 ℃, leave boiler and be sent to steam turbine power generation.
Referring to Fig. 7, Fig. 7 is air compartment structural representation of water-cooled of the present utility model.Air compartment 1 of described water-cooled comprises upper collecting chamber 1A, next part case 1B and be arranged at described upper collecting chamber 1A and described next part case 1B between fin panel casing 1C, described upper collecting chamber 1A, the common box-shaped air compartment that forms of described next part case 1B and described fin panel casing 1C, be provided with air distribution plate 1D in the described upper collecting chamber 1A, described air distribution plate 1D is a funnel-form, the bottom of this funnel-form air distribution plate 1D is provided with and is used for the deslagging mouth of pipe 11A that is connected with scum pipe 11, this deslagging mouth of pipe 11A is arranged on the centre position of air distribution plate 1D, described air distribution plate 1D is fin panel casing and fire-resistant casting material 2G co-ordinative construction, it is provided with blast cap 2F, this blast cap 2F is mushroom-shaped blast cap (referring to Figure 12) in the present embodiment, comprises crown 2F1, air supply pipe 2F2, air vent 2F3.Air compartment 1 of water-cooled be positioned at burner hearth under.Its upper collecting chamber 1A forms " mouth " type structure in the horizontal direction by large-sized heavy-wall tube φ 406 * 45 and equal tee, in this " mouth " type plane, be furnished with fin panel casing, form air distribution plate 1D, on air distribution plate 1D, be furnished with mushroom-shaped blast cap 2F, blast cap is arranged to funnel-form along furnace chamber width, the angle of inclination of four faces of funnel is about 20 °, and the lowest part of funnel is furnished with heavy caliber φ 400mm scum pipe 11, can discharge out of the furnace rapidly to guarantee bulk noncombustibles material.Arrange special blast cap (referring to Figure 13) around the scum pipe 11, because scum pipe 11 sizes of the present utility model are bigger, may there be the phenomenon of air capacity deficiency in scum pipe 11 tops, so designed this special blast cap, try hard to increase the air quantity to the supply of scum pipe 11 tops.Special blast cap is to have increased the air vent 2F4 that points to scum pipe 11 centers with the difference of general blast cap, has strengthened the latus rectum of air supply pipe 2F2 simultaneously, and this special blast cap can replenish the deficiency of scum pipe 11 top air capacities.
The next part case 1B of an air compartment 1 of water-cooled forms " mouth " type structure in the horizontal direction by more small-bore thick-walled pipe φ 219 * 20 and equal tee, is positioned at the below of upper collecting chamber 1A.Connect with fin panel casing 1C between the big small-bore thick-walled pipe of last next part case, form a box-shaped air compartment, the wall of air compartment is equipped with burner interface 51 and wind inlet 6 that starts burner 5, end wall is equipped with scum pipe 11 through ports, adopt between scum pipe 11 and the end wall and flexibly connect (referring to Figure 14), be that the interior air distribution plate 1D welding of air compartment of scum pipe 11 upper ends and water-cooled 1 upper collecting chamber 1A is fixing, scum pipe 11 expands downwards from the upper end, the air compartment 1 in scum pipe 11 lower ends and water-cooled is connected by ripple type expansion joint 27, absorb expansion by ripple type expansion joint 27, the expansion of scum pipe 11 is not restricted substantially, so be referred to as to flexibly connect.
Referring to Fig. 3 a, Fig. 3 b and Fig. 6, Fig. 3 a is the utility model dust pelletizing system structured flowchart, Fig. 3 b is the utility model dreg removing system structured flowchart, described dust pelletizing system 400a comprises exhanst gas outlet ash bucket 24, described dreg removing system 400b comprises scum pipe 11, air distribution plate 1D in air compartment 1 of described scum pipe 11 1 ends and described water-cooled is connected, and scum pipe 11 another ports of export connect deslagging treatment system (figure does not show), and described exhanst gas outlet ash bucket 24 is connected described back-end ductwork 102 ends.The described exhanst gas outlet ash bucket 24 of flue gas process after flue gas separation unit 401 separates causes the deduster (figure does not show) of smoke processing system, to remove the dust in the flue gas.In the present embodiment, described flue gas separation unit 401 is a cyclone separator 13, and this cyclone separator 13 is a scroll casing type high-temperature heat insulation separator.
Referring to Fig. 4 and Fig. 6, Fig. 4 is the utility model air system structured flowchart, described air system 200 comprises startup burner 5, a wind inlet 6, overfire air port 7 and air preheater 201, air compartment 1 of described startup burner 5 and described water-cooled is connected, described wind inlet 6 is arranged on the sidewall of an air compartment 1 of described water-cooled, described overfire air port 7 is arranged on the sidewall of described lower thermal barrier burner hearth 2, described air preheater 201 is arranged in the described back-end ductwork 102, with air and the reduction flue-gas temperature of utilizing the flue gas heating flame to use, described air preheater 201 is connected with described wind inlet 6 and described overfire air port 7 respectively.In the present embodiment, described air preheater 201 comprises wind air preheater 22 and secondary wind air preheater 23, a described wind air preheater 22 is connected with described wind inlet 6, and described secondary wind air preheater 23 is connected with described overfire air port 7.The purpose that air preheater 201 is arranged is the air of using with the flue gas heating flame, flue-gas temperature is even lower, to improve the efficient of boiler.Air preheater 201 is made up of horizontally disposed tube bank, by air, passes through flue gas outside the pipe in the pipe.Wind air preheater 22 and secondary wind air preheater 23 are arranged apart.One time the heated temperature of wind is higher, and between 260 ℃～300 ℃, air quantity accounts for 60% of total blast volume greatly greatly, sends into burner hearth through air compartment 1 of water-cooled by the blast cap 2F on the air distribution plate 1D, the preheating of rubbish is caught fire play main effect.The secondary air temperature degree is low, between 190 ℃～240 ℃, sends into burner hearth by lower thermal barrier burner hearth 2 both walls greatly, to the rubbish supplemental oxygen of having caught fire, increases the degree that burns of rubbish.The pipe of air preheater 201 is made of the seamed steel pipe or the thread groove tube of φ 51～φ 76 specifications.For preventing the flue gas low-temperature corrosion of air preheater 201, the inlet temperature of air is greater than 120 ℃, and the outlet temperature of flue gas is greater than 200 ℃, before cold air enters air preheater 201, be heated to greater than 120 ℃ through the supercooled air pretreatment system.
Air compartment of water-cooled below air distribution plate 1D 1 rear portion wall is equipped with two diesel oil and starts burner 5, the usefulness of boiler of feeding starting ignition.Ignition under bed can shorten the start-up time of boiler greatly, saves the starting fluid amount.Starting fluid can adopt light diesel fuel.The high-temperature flue gas that produces behind the oil firing is heated to furnace charge after 850 ℃, and beginning drops into rubbish gradually and reduce to throw oil mass gradually, when rubbish can be kept more than 850 ℃ furnace temperature separately, and startup burner 5 out of service.In order to make boiler can when the rubbish quality be abominable especially, still can burn and reach the requirement that dioxin decomposes, described air system 200 also comprises urgent coal filling hole 9, being used for the rubbish quality, interim when abominable especially to throw coal combustion-supporting, and this urgent coal filling hole 9 is arranged on the sidewall of lower thermal barrier burner hearth 2.
Referring to Fig. 1, refuse incinerator of circulating fluid bed of the present utility model, in the present embodiment, also comprise the soot blower system 500 that is arranged in the described back-end ductwork 102, be used to prevent described back-end ductwork 102 heating surface (comprising convection bank 15, higher level's economizer 16, higher level's superheater 17, subordinate's superheater 18, subordinate's economizer 20, wind air preheater 22, secondary wind air preheater 23) be stained with ash fouling.Described soot blower system can be acoustic wave ash ejector, high energy pulse soot blower or steam sootblower, is arranged in the centre of adjacent tubes group, carries out selective sootblowing, can effectively the ash of being stained with of outer tube surface be removed.
Referring to Fig. 1 and Fig. 5, Fig. 5 oozes drop liquid treating system structured flowchart for the utility model, and refuse incinerator of circulating fluid bed of the present utility model in the present embodiment, also comprises and oozes drop liquid treating system 600.In soot dumping process, the meeting liquid body exudate is called and oozes drop liquid.The described drop liquid treating system 600 that oozes comprises cesspool 601, sewage pump 602 and oozes drop liquid inlet 10, the described drop liquid inlet 10 that oozes is arranged on the described middle part adiabatic furnace 3, described cesspool 601 is used for storage and oozes drop liquid, described sewage pump 602 is used for the drop liquid that oozes of described cesspool 601 is squeezed in the burner hearth atomizing and burned by the described drop liquid inlet 10 that oozes, between described cesspool 601 and the described sewage pump 602 and described sewage pump 602 enter the mouth and be connected by pipeline between 10 with the described drop liquid that oozes.
Combustion process is as follows: rubbish is delivered to above the air distribution plate 1D of lower thermal barrier burner hearth 2 by garbage inlet 8 after, the fine particle flue gas that risen is carried to the upper furnace space under the fluidisation wind action, while the fire burns that flowing, and be full of whole burner hearth, bulky grain rolls in the lower furnace portion boiling, through the drying and forewarm ignition process, emit heat heating furnace charge and form the high concentration material pond that has amount of stored heat, for catching fire smoothly, back adding rubbish provides sufficient thermal source.Carried the granule fuel that flows to furnace outlet by flue gas, comprise not burning part, enter cyclone separator 13, under action of centrifugal force, separate, fall back in the column dipleg, form the powdery ash in column dipleg bottom and pile up column with flue gas in company with flue gas.The lower surface that this powdery ash is piled up column connects feeding back device 14, under the returning charge wind action, is in fluidized state, piles up under the piston action of column at the powdery ash, forces the medium that is in fluidized state on the feeding back device 14 to flow in burner hearth.After getting back to burner hearth, the ash particle that contains flammable matter is heated rapidly again again, once more fire burns, flow to furnace outlet.The rubbish circulating combustion repeatedly that comes to this is up to burning.
After boiler startup preparation finishes, on air distribution plate 1D, add the thick furnace charge of about 800mm, add the high thin furnace charge of about 1500mm, begin to start burner 5 igniting then at feeding back device 14 inlet standpipes.Along with starting the burner increase of 5 running times, the inner flue gas of the stove temperature raises gradually.When the inner flue gas of the stove temperature is elevated to more than 850 ℃, begin to drop into rubbish, along with the increase gradually of rubbish input amount, reduce the throwing oil mass that starts burner 5 synchronously, close startup burner 5 at last, boiler enters the running status of pure garbage fuel.In this process, the inner flue gas of the stove temperature can not be lower than 850 ℃, to satisfy the requirement that dioxin decomposes.Simultaneously,, open the feedback air of big feeding back device 14 gradually, progressively set up normal material circulation along with the input of rubbish.
The outlet parameter of this boiler working medium side superheated steam adopts 6.5Mpa, 450 ℃ sub-high pressure parameter.The superheated steam outlet parameter is high more, and the generated energy of ton steam is big more.After adopting above-mentioned parameter, press parameter in comparing, make the power benefit of refuse-burning plant, can increase about 30 yuan of/ton rubbish, increased the overall efficiency of refuse-burning plant.
Certainly; the utility model also can have other various embodiments; under the situation that does not deviate from the utility model spirit and essence thereof; those of ordinary skill in the art work as can make various corresponding changes and distortion according to the utility model, but these corresponding changes and distortion all should belong to the protection domain of the appended claim of the utility model.
Claims (14)
1. refuse incinerator of circulating fluid bed, comprise the steel framework and be arranged on burner hearth body, middle part flue, back-end ductwork and drum on the described steel framework, be provided with flue gas separation unit and feeding back device in the flue of described middle part, described flue gas separation unit is connected with described burner hearth body respectively with described feeding back device, described back-end ductwork is connected with described flue gas separation unit, be provided with boiler circuit in described burner hearth body and the described back-end ductwork, described boiler circuit is connected with described drum, it is characterized in that described burner hearth body comprises:
The top water-evaporating furnace, it is provided with exhanst gas outlet, and described exhanst gas outlet is used for guiding flue gas into described flue gas separation unit;
The lower thermal barrier burner hearth, it is provided with garbage inlet, overfire air port and feed back inlet, and described feed back inlet is used to connect described feeding back device;
The middle part adiabatic furnace is used for connecting respectively described top water-evaporating furnace and described lower thermal barrier burner hearth;
Wherein, described middle part adiabatic furnace and described lower thermal barrier burner hearth are no heating surface chamber structure, are used to prevent that the heat that produces behind the incineration firing scatters and disappears, and drop into the preheating of rubbish and light described heat is used for the later stage.
2. refuse incinerator of circulating fluid bed as claimed in claim 1, it is characterized in that, described no heating surface chamber structure comprises furnace wall and is installed in the pressure-bearing backplate of the outer surface of described furnace wall, and described furnace wall comprises fire brick layer and builds outer field heat-insulation layer at described fire brick layer by laying bricks or stones.
3. refuse incinerator of circulating fluid bed as claimed in claim 2 is characterized in that, also is provided with multiple layer refractory brick support on the described furnace wall, and described refractory brick support is fixed on the described pressure-bearing backplate.
4. refuse incinerator of circulating fluid bed as claimed in claim 3 is characterized in that, between described each layer refractory brick support, also is provided with the refractory brick drag hook, and described refractory brick drag hook is fixed on the described pressure-bearing backplate.
5. as claim 2,3 or 4 described refuse incinerator of circulating fluid bed, it is characterized in that the edge of described pressure-bearing backplate is provided with the two-way expansion joint that is used to seal, described two-way expansion joint can absorb two-way expansion.
6. as claim 2,3 or 4 described refuse incinerator of circulating fluid bed, it is characterized in that described pressure-bearing backplate is the lattice structure of High-Strength Low-Alloy structural steel, the outer surface of described lattice structure adopts the low alloy steel plate hermetically-sealed construction.
7. as claim 1,2,3 or 4 described refuse incinerator of circulating fluid bed, it is characterized in that, the longitudinal section of described lower thermal barrier burner hearth is wide at the top and narrow at the bottom trapezoidal, it is funnelform air distribution plate that the bottom port place of described lower thermal barrier burner hearth is provided with structure, described air distribution plate is provided with the deslagging mouth of pipe and many air drafts cap, and the described deslagging mouth of pipe is arranged on the centre of described many air drafts cap.
8. refuse incinerator of circulating fluid bed as claimed in claim 7, it is characterized in that, described lower thermal barrier burner hearth bottom is connected with air compartment of water-cooled, air compartment of described water-cooled is provided with a wind inlet and is used to connect the burner interface that starts burner, and the working medium heating surface of an air compartment of described water-cooled is connected with described drum by pipeline.
9. refuse incinerator of circulating fluid bed as claimed in claim 8, it is characterized in that, air compartment of described water-cooled comprise upper collecting chamber, next part case and be arranged at described upper collecting chamber and described next part case between fin panel casing, described upper collecting chamber, described next part case and described fin panel casing form the box-shaped air compartment jointly, and described air distribution plate is arranged in the described upper collecting chamber.
10. refuse incinerator of circulating fluid bed as claimed in claim 8 is characterized in that, air compartment of described water-cooled also is connected with scum pipe.
11. refuse incinerator of circulating fluid bed as claimed in claim 10 is characterized in that, is arranged at the air vent that the described deslagging mouth of pipe described blast cap on every side is provided with the center of pointing to described scum pipe.
12. refuse incinerator of circulating fluid bed as claimed in claim 7 is characterized in that, the angle of inclination of the funnel surface of described air distribution plate is 15 °～25 °.
13. as claim 1,2,3,4,8,9,10,11 or 12 described refuse incinerator of circulating fluid bed, it is characterized in that, be provided with convection bank in the described back-end ductwork, described convection bank is connected with described drum, described convection bank is the tube bank along the equidistant arrangement of described back-end ductwork width, and described tube bank becomes 10 °～15 ° angle in the horizontal direction with horizontal line.
14. as claim 1,2,3,4,8,9,10,11 or 12 described refuse incinerator of circulating fluid bed, it is characterized in that, also be provided with urgent coal filling hole on the sidewall of described lower thermal barrier burner hearth, being used for the rubbish quality, interim when abominable especially to throw coal combustion-supporting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202463553U CN201526976U (en) | 2009-10-21 | 2009-10-21 | Refuse-fired boiler for circulating fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202463553U CN201526976U (en) | 2009-10-21 | 2009-10-21 | Refuse-fired boiler for circulating fluidized bed |
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| CN201526976U true CN201526976U (en) | 2010-07-14 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101963356A (en) * | 2010-11-02 | 2011-02-02 | 深圳京基环保设备有限公司 | Combustion system of vertical incinerator for household refuse suitable for power generation and control method thereof |
| CN102180525A (en) * | 2011-03-17 | 2011-09-14 | 绍兴文理学院 | Flameless chemical looping combustion oxidizing furnace |
| CN102179215A (en) * | 2011-03-17 | 2011-09-14 | 绍兴文理学院 | Petroleum and natural gas flameless chemical looping combustion power system and process flow thereof |
| CN102180526A (en) * | 2011-03-17 | 2011-09-14 | 绍兴文理学院 | Flameless chemical-looping combustion reduction furnace |
| CN102042600B (en) * | 2009-10-21 | 2013-04-17 | 烟台鑫丰源电站设备有限公司 | Circulating fluidized bed refuse incineration boiler |
| CN106196031A (en) * | 2016-08-31 | 2016-12-07 | 自贡华西能源工业有限公司 | A kind of flue gas generation equipment of CFB |
| CN108662593A (en) * | 2018-05-19 | 2018-10-16 | 潘礼斌 | A kind of animal husbandry excrement burning heat supply clean utilization system |
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2009
- 2009-10-21 CN CN2009202463553U patent/CN201526976U/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102042600B (en) * | 2009-10-21 | 2013-04-17 | 烟台鑫丰源电站设备有限公司 | Circulating fluidized bed refuse incineration boiler |
| CN101963356A (en) * | 2010-11-02 | 2011-02-02 | 深圳京基环保设备有限公司 | Combustion system of vertical incinerator for household refuse suitable for power generation and control method thereof |
| CN102180525A (en) * | 2011-03-17 | 2011-09-14 | 绍兴文理学院 | Flameless chemical looping combustion oxidizing furnace |
| CN102179215A (en) * | 2011-03-17 | 2011-09-14 | 绍兴文理学院 | Petroleum and natural gas flameless chemical looping combustion power system and process flow thereof |
| CN102180526A (en) * | 2011-03-17 | 2011-09-14 | 绍兴文理学院 | Flameless chemical-looping combustion reduction furnace |
| CN102180525B (en) * | 2011-03-17 | 2013-10-30 | 绍兴文理学院 | Flameless chemical looping combustion oxidizing furnace |
| CN102180526B (en) * | 2011-03-17 | 2013-11-20 | 绍兴文理学院 | Flameless chemical-looping combustion reduction furnace |
| CN102179215B (en) * | 2011-03-17 | 2014-04-23 | 绍兴文理学院 | Petroleum and natural gas flameless chemical looping combustion power system and process flow thereof |
| CN106196031A (en) * | 2016-08-31 | 2016-12-07 | 自贡华西能源工业有限公司 | A kind of flue gas generation equipment of CFB |
| CN108662593A (en) * | 2018-05-19 | 2018-10-16 | 潘礼斌 | A kind of animal husbandry excrement burning heat supply clean utilization system |
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Granted publication date: 20100714 |