CN212841544U - Pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler - Google Patents
Pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler Download PDFInfo
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- CN212841544U CN212841544U CN202021787372.0U CN202021787372U CN212841544U CN 212841544 U CN212841544 U CN 212841544U CN 202021787372 U CN202021787372 U CN 202021787372U CN 212841544 U CN212841544 U CN 212841544U
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Abstract
A pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler is characterized in that an isobaric air chamber is arranged below a hearth and is communicated with the isobaric air chamber through an air distribution plate, a high-position buried pipe is arranged above the air distribution plate, a feed inlet is arranged on one side of the lower portion of the hearth, a first-stage water-cooling groove-shaped separator and a second-stage water-cooling groove-shaped separator are sequentially arranged at a flue gas outlet on the upper portion of the hearth, the second-stage water-cooling groove-shaped separator is connected with a material return port of the hearth through a first-stage U-shaped material return device, a flue gas channel is arranged at a flue gas outlet of the second-stage water-cooling groove-shaped separator, a selective multi-pipe separator. The utility model discloses the device can realize that 700-fired 1600kcal/kg low heating value fuel is fired to purity, and combustion efficiency is high, and accommodation range is big, and the bed fluidization is even stable moreover, and excess air factor is little, and furnace diaphragm type wall does not have wearing and tearing, NOXLow emission (< 200 mg/m)3) And the SNCR and the SCR can reach ultra-low emission conveniently.
Description
Technical Field
The utility model relates to a fluidized bed boiler especially relates to a pure tertiary separation fluidized bed boiler of low heat value gangue that fires.
Background
The coal gangue is a waste in coal mine production, and the calorific value is low. Along with the improvement of the innovation of mining and washing technologies, the heat value of coal gangue produced by coal mines and coal washing plants is lower and lower, and the low calorific value is mostly lower than 1400 kcal/kg; the boiler which is purely fired with the low-calorific-value coal gangue fuel is used for supplying heat and generating electricity (a large amount of generated ash and slag are also used as building materials in the cement industry), so that great economic and environmental benefits can be generated.
The heat value of coal gangue burned by a rapid circulating fluidized bed boiler of a coal gangue power plant is over 1800kcal/kg (actually, the coal gangue is mixed with middlings according to a certain proportion), and the cost is high. The pure combustion low-calorific value coal gangue rapid circulating fluidized bed boiler causes too large amount of return materials due to high-rate circulation, and often causes flameout of a main bed.
The pure combustion low-calorific value coal gangue fuel can be prepared by adopting a low-speed bed, and some users adopt a double-bed staged combustion technology, but the structure and the operation are complex; also, users have tried low hearths and cyclone separators, because the hearths are short and the burning time is short, the operation can be basically stabilized only by increasing the number of cycles, but the main bed temperature is often low or flameout is often caused because the amount of returned materials is still large. Taking a 40-ton boiler burning 1030kcal/kg coal gangue as an example, the ash content of the fuel reaches 71.986%, the total amount of ash generated by burning reaches 17.8 tons/hour, and the increase of the circulation times for improving the efficiency is not feasible.
Small changes in the calorific value of the coal gangue can cause a large fluctuation range, such as 900kcal/kg to 1400kcal/kg, and 500kcal/kg, the relative range of the 500kcal/kg fluctuation reaches 55% (likewise, the boiler, the variation range of the coal used for burning is only 10% from 5000kcal/kg to 5500 kcal/kg), and the operation adjustment of the designed boiler is difficult due to the change of the calorific value of the fuel.
The low-speed bed causes the original NO emission due to the large bed area, the heavy bed material and the large wind quantity operationXAt 400mg/m3Above, the smoke reaches the standard and is discharged in an ultralow way, and the environmental protection operating cost is high.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that overcome the above-mentioned defect that prior art exists, provide a combustion efficiency height, reduce NOXA pure combustion coal gangue three-stage separation fluidized bed boiler with low heat value (700-.
The utility model provides a technical scheme that its technical problem adopted is: a pure-combustion low-calorific-value (700-1600 kcal/kg) coal gangue three-stage separation fluidized bed boiler comprises a hearth, wherein an isobaric air chamber is arranged below the hearth and is communicated with the isobaric air chamber through an air distribution plate, a high-position buried pipe is arranged above the air distribution plate, a feed inlet is arranged on one side of the lower part of the hearth, a return port is arranged on the other side of the lower part of the hearth, a slag discharge pipe is arranged at the position, close to the return port, of the lower part of the hearth, a primary water-cooling trough type separator and a secondary water-cooling trough type separator are sequentially arranged at a flue gas outlet at the upper part of the hearth, the secondary water-cooling trough type separator is connected with the return port of the hearth through a primary U-shaped return device, a flue gas channel is arranged at the flue gas outlet of the secondary water-cooling trough type separator, a selective multi-pipe separator is arranged in the, and the second fly ash outlet of the selective multi-pipe separator is connected with an ash storehouse.
Further, the wind distribution plate is provided with directional wind caps in ten rows close to the front wall. So as to facilitate the diffusion of the bed material to the rear without accumulation. Furthermore, the diameter of the blast caps on the air distribution plate is 30-50mm, the diameter of the ventilation holes on the blast caps is 4.5-5mm, and the distance between the adjacent blast caps is 70-75 mm.
Further, a high-temperature superheater, a low-temperature superheater, a high-temperature economizer, a medium-temperature economizer and an air preheater are sequentially arranged in the flue gas channel.
Furthermore, a middle ash storage bin and pneumatic conveying equipment are arranged on a pipeline connecting a second fly ash outlet of the selective multi-pipe separator and the ash storage bin.
Furthermore, a flow regulating valve is arranged on a pipeline connecting the first fly ash outlet of the selective multi-pipe separator and the second-level U-shaped material returning device. For different fuel heating values, the return amount is adjusted through the flow regulating valve and the secondary U-shaped return feeder, and the requirement of the boiler combustion efficiency is met.
Furthermore, the primary water-cooling groove-shaped separator is a groove formed by a heating surface pipe and hook-shaped fins welded on the heating surface pipe, and anti-abrasion flat steel is welded in the groove. The fly ash separated by the primary water-cooling trough type separator flows downwards along the rear wall and returns to the lower part of the hearth. Belonging to the furnace internal circulation.
Further, the second-stage water-cooling groove-shaped separator is a groove-shaped formed by pressing a heat-resistant alloy steel plate.
Furthermore, the selective multi-pipe separator is used for exhausting gas downwards, and the spiral component in the selective multi-pipe separator is of a building block structure, wherein the spiral blade can be taken out and replaced after the furnace is shut down. And arranging a selective multi-pipe separator at a position of about 500 ℃ behind the high-temperature economizer, and returning part or all of the materials to the hearth through a flow regulating valve and a secondary U-shaped material returning device when the calorific value of the fuel is more than 1200kcal/kg or the carbon content of the fly ash is more than 4-5% by sampling. The separation efficiency of the selective multi-pipe separator reaches 95 percent, and the separation efficiency is adjusted by replacing different helical blades. The selective multi-pipe separator is equivalent to a dust remover in the furnace at the same time, thereby reducing the abrasion of the heated surface at the tail part and reducing the load of a cloth bag at the tail part.
Preferably, the size of the section of the hearth is small at the bottom and large at the top, the flow velocity of flue gas is 2.5-4.0m/s, the flow path of the flue gas is 6-8s, the hearth is of a full-film wall structure, and a burning guarding belt is completely laid on the fire facing surface below a flue gas outlet. The water wall is not abraded due to the isolation of the guard burning zone.
Preferably, the high-position buried pipe is positioned at the position of 650-800mm of the height in the hearth. The lower edge of the feed inlet is positioned at the position of 1900-2200mm of the inner height of the hearth.
The furnace chamber circulating combustion system of the utility model has high combustion efficiency for low-heat value gangue fuel and no abrasion of water-cooled wall; the slag discharge pipe close to the material return port is selected, so that the retention time of coarse bed materials can be prolonged in the combustion process, and the fly ash circulation quantity of the boiler can be adjusted in an auxiliary mode. Has the following advantages: firstly, the flow of the hearth is prolonged to 6-8s, which is improved by 50% compared with the common boiler, and the requirement that the fine ash which passes through the hearth at one time and is not separated and returned by the separator is basically burnt out is met; secondly, strengthening the internal circulation of the furnace: the efficiency of the primary water-cooling trough-type separator is 40-60%, and the separated fly ash flows downwards along the rear wall and returns to the lower part of the hearth, belonging to the in-furnace circulation; thirdly, the external circulation multiplying power is reduced, the efficiency of the secondary water-cooling groove type separator is 60-85%, and the external circulation multiplying power is relatively low; fourthly, the temperature of the upper part of the hearth is uniform and not reduced at 850-920 ℃.
Through three-stage separation and material return, the carbon-containing fine ash at the upper part of the hearth has high concentration, and the temperature at the upper part is ensured to be uniform and not reduced at 850-; in the operation process, 0-30% of tail flue gas is added into the air chamber, so that not only is the uniform and stable fluidization in the bed maintained, but also the excess air coefficient is controlled, and the oxygen deficiency and uniform and stable combustion at the lower part inhibit NOXGeneration of (1); the high-concentration red-hot carbon particles at the upper part of the hearth form NOXThe reduction reaction reduces NOXAnd (5) discharging.
The utility model disclosesThe device can realize pure combustion of 700-1600kcal/kg low-heat-value fuel, has high combustion efficiency, large adjustment range, uniform and stable in-bed fluidization, small excess air coefficient, NO abrasion of the membrane wall of the hearth and NO NOXLow emission (< 200 mg/m)3) And the SNCR and the SCR can reach ultra-low emission conveniently.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention;
FIG. 2 is a view taken along line A-A of FIG. 1;
fig. 3 is a view from B-B in fig. 1.
In the figure: 1. the device comprises a hearth, 2 parts of an isobaric air chamber, 3 parts of a small hood air distribution plate, 4 parts of a slag discharge pipe, 5 parts of a directional hood, 6 parts of a high-position buried pipe, 7 parts of a feed inlet, 8 parts of a primary water-cooling trough type separator, 9 parts of a secondary water-cooling trough type separator, 10 parts of a primary U-shaped return feeder, 11 parts of an anti-abrasion flat steel, 12 parts of a high-temperature superheater, 13 parts of a low-temperature superheater, 14 parts of a high-temperature economizer, 15 parts of a selective multi-pipe separator, 1501 parts of a first fly ash outlet, 1502 parts of a second fly ash outlet, 16 parts of a helical blade, 17 parts of a secondary U-shaped return feeder, 18 parts of a flow regulating valve, 19 parts of a medium-temperature economizer, 20 parts of the low-temperature economizer, 21 parts of an air preheater.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
As shown in figure 1, the present embodiment comprises a hearth 1, wherein an isobaric air chamber 2 is arranged below the hearth 1 and is communicated with the isobaric air chamber 2 through a small hood air distribution plate 3, and a high-level buried pipe 6 and a feeding hole 7 are arranged above the hearth. The small wind cap wind distribution plate 3 is provided with a directional wind cap 5 close to the front wall 10 and a slag pipe 4 close to the material returning port. A first-stage water-cooling groove type separator 8 and a second-stage groove type separator 9 are sequentially arranged at a smoke gas outlet of the hearth 1. The second-stage groove type separator 9 is connected to a hearth material returning port through a first-stage U-shaped material returning device 10. The smoke outlet of the secondary trough type separator 9 is sequentially connected with a high-temperature superheater 12, a low-temperature superheater 13, a high-temperature economizer 14, a selective multi-pipe separator 15, a medium-temperature economizer 19, a low-temperature economizer 20 and an air preheater 21, and then the smoke enters tail environment-friendly treatment equipment to be discharged after reaching the standard. The first fly ash outlet 1501 of the selective multi-pipe separator 15 is connected with the material returning port 7 of the furnace 1 through a secondary U-shaped material returning device 17, and the second fly ash outlet 1502 of the selective multi-pipe separator 15 sends fly ash to an ash silo (not shown in the figure).
The section size of the hearth 1 is small at the bottom and large at the top, the flow velocity of flue gas is 3m/s, the flow of the flue gas is 6-8s, the hearth 1 is of a full-film wall structure, a burning-preventive belt is completely laid on the fire surface of the hearth 1 below a flue gas outlet, and the water-cooled wall of the hearth 1 is not abraded due to the isolation of the burning-preventive belt.
The diameter of the blast cap of the small blast cap air distribution plate 3 is 50mm, the area of the small blast cap air distribution plate is about 20 percent larger than that of 3000kcal/kg fuel, the diameter of the ventilation hole on the blast cap is 5mm, and the distance between the adjacent blast caps is 70 mm. The small wind cap wind distribution plate 3 is close to the front wall and is provided with ten rows of directional wind caps 5. A slag discharge pipe 4 is arranged at the position, close to the material return port, of the small blast cap air distribution plate 3. The fluidized air of the air distribution plate 3 is tail flue gas mixed with 20% of fresh air.
The high-position buried pipe 6 is positioned at the position with the height of 700mm in the hearth 1. The lower edge of the feed inlet 7 is positioned at the position of 2000mm of the inner height of the hearth 1.
As shown in FIG. 2, the primary water-cooled trough-type separator 8 is a trough-type separator composed of a heating surface pipe and hook-shaped fins welded on the heating surface pipe, and an anti-abrasion flat steel 11 is welded in the trough.
As shown in FIG. 3, the two-stage water-cooled tank-type separator 9 is a heat-resistant alloy steel plate pressed into a tank-type.
The selective multi-pipe separator 5 is used for exhausting gas downwards, the spiral component in the selective multi-pipe separator is of a building block structure, and the spiral blades 16 in the spiral component can be taken out and replaced after the furnace is shut down. Or different structures are replaced according to the requirements of the coal types, such as adjusting the number of blades, single helix, double helix, triple helix, climbing angle and the like.
The utility model discloses the working process is as follows:
850-1400kcal/kg coal gangue fuel is added into a dense phase zone at the lower part of a hearth from a feed inlet, fresh air is mixed with 20 percent of tail flue gas to carry out fluidized boiling combustion, and coarse particles larger than 2mm are combusted in the dense phase zone. The fine particles are blown into a dilute phase zone at the upper part of the hearth, and are combusted for 6-8s, and then are discharged from the hearth 1, and a part (40-60%) of the fine particles are intercepted by a first-stage water-cooling trough type separator and fall to a dense phase zone along a rear wall for circulating combustion. The coarse particles which are not intercepted fall after passing through the secondary groove type separator, are basically separated (60-85 percent) and are sent back to the hearth 1 through a material returning mechanism for circulating combustion.
For fuels below 1200kcal/kg, because of low carbon content and combustion time of 6-8s, the smaller particles can be substantially burned out and are not intercepted by the primary and secondary water-cooled trough separators and enter the tail heating surface. For fuels greater than 1200kcal/kg, the smaller particles may be unburnt and not intercepted, entering the tail heating surface, although the burning time is 6-8s, because the carbon content is higher. Because a selective multi-pipe separator (separation efficiency is up to 95%) is arranged at a position of about 500 ℃ behind the high-temperature economizer 14, when the carbon content of the fly ash is found to be more than 4-5% by sampling, the fly ash is partially or completely returned to the hearth through the flow regulating valve and the secondary U-shaped return feeder. The selective multi-tube separator 15 (the separation efficiency can be adjusted by replacing different helical blades) is equivalent to a dust remover in a furnace, and reduces the abrasion of a tail heating surface and the load of a tail cloth bag.
By adding 20% tail flue gas into the isobaric air chamber 2, the in-bed fluidization is maintained to be uniform and stable, the excess air coefficient is controlled, and the NO is inhibited by oxygen deficiency and uniform and stable combustion at the lower partXGeneration of (1); through three-stage separation and material return, the carbon-containing fine ash at the upper part of the hearth has high concentration, the upper temperature of 850-XThe reduction reaction reduces NOXAnd (5) discharging.
Application example 1:
by using the technology, when a 40-ton power generation boiler is installed in a coal gangue power plant, and the calorific value of coal gangue is 1000-; when the calorific value of coal gangue is 1200-1400kcal/kg in actual operation, the material is partially returned by the selective multi-tube separator (less than 50 percent). The boiler combustion is stable, all parameters meet the design requirements, the bed temperature can be stabilized at 850-920 ℃, the carbon content of fly ash is 1-3%, the carbon content of slag is 0.5-2%, the smoke discharge temperature is 140 ℃, NO is originally discharged without smoke fluidizationXAt 250mg/m3The fume is added to fluidize the raw materialsInitial emission of NOXAt 150mg/m3The following.
Various modifications and variations of the present invention may be made by those skilled in the art, and they are within the scope of the present invention provided they are within the scope of the claims and their equivalents.
What is not described in detail in the specification is prior art that is well known to those skilled in the art.
Claims (8)
1. The utility model provides a pure tertiary separation fluidized bed boiler of low heat value gangue, includes furnace, the below of furnace is equipped with isobaric air chamber, isobaric air chamber passes through the grid plate and communicates with isobaric air chamber its characterized in that: the top of air distributor is equipped with high-order buried pipe, furnace's lower part one side is equipped with the feed inlet, and the opposite side is equipped with the return material mouth, furnace's lower part is equipped with the slagging-off pipe being close to return material mouth department, and the exit of flue gas on furnace upper portion is equipped with one-level water-cooling cell type separator and second grade water-cooling cell type separator in proper order, second grade water-cooling cell type separator passes through one-level U type returning charge ware and is connected with furnace's return material mouth, the exit of flue gas of second grade water-cooling cell type separator is equipped with the flue gas passageway, be equipped with the selectivity multi-tube separator in the flue gas passageway, the first flying dust export of selectivity multi-tube separator is connected with furnace's return material mouth through second grade U type returning charge.
2. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in claim 1, characterized in that: the wind distribution plate is provided with directional wind caps at ten rows close to the front wall.
3. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in claim 2, characterized in that: the diameter of the blast caps on the air distribution plate is 30-50mm, the diameter of the ventilation holes on the blast caps is 4.5-5mm, and the distance between the adjacent blast caps is 70-75 mm.
4. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in any one of claims 1 to 3, characterized in that: and a high-temperature superheater, a low-temperature superheater, a high-temperature economizer, a medium-temperature economizer and an air preheater are sequentially arranged in the flue gas channel.
5. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in any one of claims 1 to 3, characterized in that: the pipeline connecting the second fly ash outlet of the selective multi-pipe separator and the ash storehouse is provided with an intermediate ash storage storehouse and pneumatic conveying equipment.
6. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in any one of claims 1 to 3, characterized in that: and a flow regulating valve is arranged on a pipeline connecting the first fly ash outlet of the selective multi-pipe separator and the second-level U-shaped material returning device.
7. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in claim 1, characterized in that: the primary water-cooling groove-shaped separator is a groove-shaped structure formed by a heating surface pipe and hook-shaped fins welded on the heating surface pipe, and anti-abrasion flat steel is welded in the groove.
8. The pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler as claimed in claim 1, characterized in that: the second-stage water-cooling groove-shaped separator is a groove-shaped formed by pressing a heat-resistant alloy steel plate.
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| CN202021787372.0U CN212841544U (en) | 2020-08-25 | 2020-08-25 | Pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler |
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| CN202021787372.0U CN212841544U (en) | 2020-08-25 | 2020-08-25 | Pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111853764A (en) * | 2020-08-25 | 2020-10-30 | 湖南湘慧达新能源科技发展有限公司 | Pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111853764A (en) * | 2020-08-25 | 2020-10-30 | 湖南湘慧达新能源科技发展有限公司 | Pure-combustion low-calorific-value coal gangue three-stage separation fluidized bed boiler |
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Effective date of registration: 20210705 Address after: Room 306, office building, 418 Fenglin Third Road, Changsha hi tech Development Zone, Hunan 410000 Patentee after: Hunan Daqian Huizhi New Energy Technology Co., Ltd Patentee after: Wu Xianzhong Address before: 410006 room card-1318, room 307, building a, Lugu business center, No. 199, Lulong Road, high tech Development Zone, Changsha City, Hunan Province (cluster registration) Patentee before: Hunan Xianghuida New Energy Technology Development Co.,Ltd. Patentee before: Wu Xianzhong |
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