CN106016254B - Recirculating fluidized bed coal slime feeding system and circulating fluidized bed boiler - Google Patents
Recirculating fluidized bed coal slime feeding system and circulating fluidized bed boiler Download PDFInfo
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- CN106016254B CN106016254B CN201610313129.7A CN201610313129A CN106016254B CN 106016254 B CN106016254 B CN 106016254B CN 201610313129 A CN201610313129 A CN 201610313129A CN 106016254 B CN106016254 B CN 106016254B
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- coal slime
- fluidized bed
- furnace
- coal
- circulating fluidized
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- 239000003245 coal Substances 0.000 title claims abstract description 124
- 230000003134 recirculating effect Effects 0.000 title abstract 3
- 239000003250 coal slurry Substances 0.000 claims abstract description 45
- 239000008187 granular material Substances 0.000 claims abstract description 17
- 238000002485 combustion reaction Methods 0.000 abstract description 28
- 239000002245 particle Substances 0.000 abstract description 21
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 230000007423 decrease Effects 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 239000007921 spray Substances 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000003915 air pollution Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/01—Fluidised bed combustion apparatus in a fluidised bed of catalytic particles
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/22—Fuel feeders specially adapted for fluidised bed combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2206/00—Fluidised bed combustion
- F23C2206/10—Circulating fluidised bed
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
Abstract
The invention discloses a kind of recirculating fluidized bed coal slime feeding system and circulating fluidized bed boiler, recirculating fluidized bed coal slime feeding system includes burner hearth (1), it is arranged on the side wall of burner hearth (1) and for by refeed line (2) that the particle of recycling is fed again into burner hearth (1) and being arranged on the side wall of burner hearth (1) and for by the coal slurry inlet pipe (3) in coal slime feeding burner hearth (1), the neighbouring refeed line (2) of the coal slurry inlet pipe (3) is set and positioned at the top of the refeed line (2), one end being connected with the side wall of the burner hearth (1) of the coal slurry inlet pipe (3) tilts down.Since upper furnace has the granule boundary laminar flow of decline, the high-temperature particle that burner hearth is recycled to by refeed line of high concentration is arranged at lower part, two strands of high-temperature particle streams impact the coal slime for newly entering burner hearth, so that newly it is brought rapidly up into the coal slime of burner hearth, shorten the heating time of coal slime, so that burning time extends, the efficiency of combustion of coal slime is lifted.
Description
Technical Field
The invention relates to the technical field of circulating fluidized bed combustion, in particular to a circulating fluidized bed coal slime feeding system and a circulating fluidized bed boiler.
Background
The coal slime is a byproduct in the coal washing process and has the characteristics of large moisture, high ash content, fine particles and high viscosity. Due to the lack of effective utilization technology, the coal slime is stacked in fixed places, and great environmental hidden danger exists. For example, the coal slime can cause pollution to water resources when losing in water; when the air is dried, dust can be generated, and air pollution is caused. In addition, the coal slime generally has the heat of 2500-5500 kilocalories, even exceeds some low-heat-mass power coal, and the random stacking of the coal slime causes great energy waste. Therefore, the development and utilization of the technology related to the coal slime treatment are of great significance to the environmental safety and the efficient utilization of coal.
Due to the high content of moisture and ash, and the low calorific value, the coal slime is not suitable for the combustion of the traditional pulverized coal furnace. In order to realize the comprehensive utilization of the coal slime in a large scale and high efficiency, the coal slime is widely applied to the combustion power generation of the circulating fluidized bed. The coal slime is heated, agglomerated and deposited in the fluidized bed, so that the fluidization quality is damaged, and the combustion is unstable. In order to control the stable combustion of the fluidized bed, various feeding modes of coal slurry in the circulating fluidized bed exist in the prior art, which are mainly divided into the following four modes: (1) feeding at the top; (2) feeding in the middle; (3) feeding by a material return valve (namely feeding by a material return pipe); (4) the dense phase zone atomizes the feed. Wherein, because the feed inlet is close to the furnace export, the coal slime is short in the one-time dwell time of furnace in the top feed mode, and combustion efficiency is low. When the middle feeding is adopted, the feeding system is simple in structure, high in mechanical failure rate and low in combustion efficiency of coal slime. The feeding port of the coal slime moves towards the bottom, and the one-time retention time of the coal slime in the hearth is prolonged, so that the combustion efficiency is highest under two modes of feeding by a material return valve and atomizing feeding by a dense-phase region. For the feeding mode of the return valve, when the boiler is in a starting or low-load stage, because the quantity of the circulating ash is less, the carrying capacity of the circulating ash to the coal slime is insufficient, the coal slime is bonded in the return valve, the coal slime cannot be fed under the low load of the boiler, and the feeding mode is not suitable for large-proportion mixed combustion. For the dense-phase region atomization feeding mode, the coal slime particles are caused by atomization wind to wash the nozzle of the spray gun, so that the spray gun is seriously abraded, and the service life of the spray gun is influenced.
In view of the above-mentioned shortcomings of the prior art, there is a need for a new type of circulating fluidized bed coal slurry feeding system.
Disclosure of Invention
The invention aims to provide a circulating fluidized bed coal slime feeding system which is high in coal slime combustion efficiency and wide in combustion adaptability.
In order to achieve the purpose, the invention provides a circulating fluidized bed coal slurry feeding system which comprises a hearth, a return pipe arranged on the side wall of the hearth and used for feeding recovered particles into the hearth again, and a coal slurry inlet pipe arranged on the side wall of the hearth and used for feeding coal slurry into the hearth, wherein the coal slurry inlet pipe is arranged close to the return pipe and above the return pipe, and one end of the coal slurry inlet pipe, connected with the side wall of the hearth, is inclined downwards.
Preferably, the furnace is tower-shaped.
Preferably, the axis of the coal slurry inlet pipe is coplanar with the central axis of the furnace.
Preferably, an included angle between the extension direction of the coal slime inlet pipe and the axial direction of the hearth is a, and a is more than or equal to 30 degrees and less than or equal to 60 degrees.
Preferably, the extension direction of the coal slime inlet pipe is parallel to the extension direction of the return pipe.
Preferably, one end of the coal slime inlet pipe connected with the side wall of the hearth and one end of the return pipe connected with the side wall of the hearth are located on the same bus of the hearth.
Preferably, the distance between one end of the coal slime inlet pipe connected with the side wall of the hearth and one end of the return pipe connected with the side wall of the hearth is H, and H is more than or equal to 0.5m and less than or equal to 1 m.
Preferably, the working pressure in the coal slurry inlet pipe is greater than the working pressure at the coal slurry inlet in the hearth.
Preferably, the working pressure at the coal slime inlet in the hearth is 6-8 KPa.
The invention also provides a circulating fluidized bed boiler which comprises the circulating fluidized bed coal slurry feeding system.
Above-mentioned technical scheme in the adjacent return pipe setting of coal slime inlet tube and be located the top of return pipe, because the position of coal slime inlet tube is low, the residence time of coal slime in furnace is long. And, because there is descending granule boundary laminar flow on furnace upper portion, the lower part has the high-temperature granule of high concentration by the circulation of return pipe to furnace, and two strands of high-temperature granule flows strike the coal slime of newly entering furnace for the coal slime of newly entering furnace heaies up rapidly, shortens the heat time of coal slime, thereby makes the combustion time extension, promotes the combustion efficiency of coal slime. The impact of the particle flow strengthens the capability of the coal slime entering the hearth to diffuse towards all directions of the hearth, the coal slime is uniformly distributed on the cross section of the hearth, and the phenomenon of insufficient local combustion is avoided. The coal slime inlet pipe and the return pipe are separately arranged, so that the problem of insufficient carrying capacity of the circulating ash on the coal slime when the circulating ash amount is less can be solved, and the feeding of the coal slime feeding system of the circulating fluidized bed is not influenced by the load of the operating condition, and the coal slime feeding system has good combustion adaptability. In addition, this kind of circulating fluidized bed coal slime feed system is direct at the lateral wall of furnace upper shed, need not additionally set up devices such as spray gun, can avoid the granule stream to stretching into furnace's spray gun etc. and cause wearing and tearing for this kind of circulating fluidized bed coal slime feed system has lower mechanical wear.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic structural diagram of a circulating fluidized bed coal slurry feeding system of the present invention.
Wherein,
1 hearth and 2 return pipes
3 coal slime inlet tube 4 connecting pipes
Primary air A and secondary air B
C fluidized wind and D loosened wind
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The invention provides a coal slime feeding system of a circulating fluidized bed, which comprises a hearth 1, a return pipe 2 arranged on the side wall of the hearth 1 and used for sending recycled particles into the hearth 1 again, and a coal slime inlet pipe 3 arranged on the side wall of the hearth 1 and used for sending coal slime into the hearth 1, wherein the coal slime inlet pipe 3 is arranged close to the return pipe 2 and above the return pipe 2, and one end of the coal slime inlet pipe 3 connected with the side wall of the hearth 1 is inclined downwards. Wherein, coal slime inlet tube 3 is close to return pipe 2 and sets up and is located return pipe 2's top, because the position of coal slime inlet tube 3 is low, and the coal slime dwell time in furnace 1 is long. And, because there is descending granule boundary layer flow in 1 upper portion of furnace, the lower part has the high-temperature granule of high concentration by returning pipe 2 circulation to furnace 1, and two strands of high-temperature granule flows strike the coal slime of newly entering furnace 1 for the coal slime of newly entering furnace 1 heaies up rapidly, shortens the heat time of coal slime, thereby makes the combustion time extension, promotes the combustion efficiency of coal slime. The impact of the particle flow strengthens the capability of the coal slime entering the hearth 1 to diffuse towards all directions of the hearth, the coal slime is uniformly distributed on the cross section of the hearth 1, and the phenomenon of insufficient local combustion is avoided. The coal slime inlet pipe 3 and the return pipe 2 are separately arranged, so that the problem of insufficient carrying capacity of the circulating ash on the coal slime when the circulating ash amount is less can be solved, and the feeding of the coal slime feeding system of the circulating fluidized bed is not influenced by the load of the operating working condition, and the coal slime feeding system has good combustion adaptability. In addition, this kind of circulating fluidized bed coal slime feed system is direct at the lateral wall of furnace 1 upper shed, need not additionally set up devices such as spray gun, can avoid the granule to cause wearing and tearing to the spray gun etc. that stretches into furnace 1 for this kind of circulating fluidized bed coal slime feed system has lower mechanical wear.
In the preferred embodiment, the furnace 1 is tower-shaped, and as shown in fig. 1, the black particles in the figure are bottom materials, the white particles are coal slime, and the bottom of the furnace 1 is provided with an upward-conveying primary air a and a secondary air B conveyed towards the return pipe 2 and the coal slime inlet pipe 3, so that the bottom materials and the coal slime in the furnace 1 can be stirred, and the bottom materials and the coal slime at the bottom of the furnace 1 can be fully mixed and diffused. Meanwhile, the free end (the end far away from the side wall of the hearth 1) of the return pipe 2 is connected with a connecting pipe 4, the connecting pipe 4 is connected with a discharge port of a cyclone separator (not shown), after flue gas in the hearth 1 enters the cyclone separator through a flue gas discharge port to be separated, separated particles can enter the hearth 1 through the connecting pipe 4 and the return pipe 2 in sequence to be combusted again, and therefore the combustion efficiency of coal slime is improved. In addition, the fluidizing air C and the loosening air D conveyed into the connecting pipe 4 can also improve the flowing speed of particles entering the hearth 1 from the return pipe 2, and high-temperature particle flow impacts the coal slime newly entering the hearth 1, so that the coal slime newly entering the hearth 1 is rapidly heated, the heating time of the coal slime is shortened, the combustion time is prolonged, and the combustion efficiency of the coal slime is improved.
Further, the axis of the coal slurry inlet pipe 3 is coplanar with the central axis of the hearth 1. The axis of the coal slurry inlet pipe 3 is the connecting line of all cross section centroids in the extending direction of the coal slurry inlet pipe 3. Because the extending direction of coal slime inlet tube 3 is towards furnace 1's center, can carry out the most abundant diffusion under the high temperature granule that circulates to furnace 1 by return pipe 2 of the granule boundary laminar flow and the high concentration of primary air A, overgrate air B, decline in the coal slime inlet tube 3 entering furnace 1 flows the effect to make the combustion efficiency maximize of coal slime.
As shown in fig. 1, the included angle between the extending direction of the coal slurry inlet pipe 3 and the axial direction of the furnace 1 is a, and the included angle a cannot be too small or too large. When the included angle a is too small, the coal slime entering the hearth 1 lacks transverse speed, and the capability of the coal slime diffusing to the cross section of the whole hearth is low, so that the coal slime is not uniformly distributed on the cross section of the hearth, and local combustion is insufficient. However, if the included angle a is too large, the coal slurry flow lacks a downward speed division, and most of the coal slurry particles are conveyed to a position far away from the return pipe 2, so that the collision chance between the particles returned by the return pipe 2 and the coal slurry particles newly entering the hearth 1 is reduced, and the temperature rise rate of the coal slurry particles is reduced. In a preferred embodiment, the angle a should be such that 30 DEG.ltoreq.a.ltoreq.60 deg.
In addition, the extending direction of the coal slime inlet pipe 3 and the extending direction of the return pipe 2 are preferably parallel to each other, so that the particles returned by the return pipe 2 and the coal slime particles newly entering the hearth 1 can be fully collided, and the heating rate of the coal slime particles is improved. And the end of the coal slime inlet pipe 3 connected with the side wall of the hearth 1 and the end of the return pipe 2 connected with the side wall of the hearth 1 are on the same bus of the hearth 1. Wherein, the generatrix rotates one circle around a specific axis to form a solid geometric figure, and the generatrix of the hearth 1 is also the same, and specifically the generatrix of the hearth 1 refers to a line which extends along the up-down direction on the side wall of the hearth 1 and can be coplanar with the central axis of the hearth 1. Let the one end that the lateral wall of the one end of coal slime inlet tube 3 and furnace 1 is connected with the lateral wall of furnace 1 with return pipe 2 on the same bus of furnace 1 to the abundant collision between the granule that is returned by return pipe 2 and the new coal slime granule that gets into furnace 1 can be guaranteed by the same, in order to promote the rate of rise of temperature of coal slime granule.
Further, as shown in fig. 1, the distance between one end of the coal slurry inlet pipe 3 connected with the side wall of the furnace 1 and one end of the return pipe 2 connected with the side wall of the furnace 1 is H, and the distance H cannot be too large or too small. When the distance H is too large, the impact of particle flow with the upward lower part is lacked, the coal slime entering the hearth 1 flows downward along the wall and is difficult to diffuse to the transverse section of the whole hearth 1, the gas flow of the dilute phase zone of the hearth 1 is not uniformly distributed along the section, the gas flow velocity of the wall surface area is lower than the gas velocity of the center of the bed layer, the peat concentration of the wall surface area is too high, so that oxygen is deficient near the wall surface, and the combustion of the coal slime is insufficient. However, when the distance H is too small, the coal slurry may enter the dense phase zone and agglomerate and settle downward after entering the furnace. When the coal slime block is in the dense-phase region, the coal slime block may be deposited to the wind caps of the primary wind A and the secondary wind B to block the wind caps, so that the furnace is fluidized unevenly. As a preferred embodiment, the distance H should correspond to 0.5 m.ltoreq.H.ltoreq.1 m.
In addition, the coal slime passes through the pressure pump and delivers to furnace 1, must guarantee that the operating pressure in the coal slime inlet tube 3 is greater than the operating pressure of the coal slime entrance (the coal slime gets into furnace department position) in furnace 1, perhaps must guarantee that pressure pump outlet pressure is greater than the operating pressure of the coal slime entrance in furnace 1 to prevent gas and the granule in furnace 1 to get into coal slime pipeline transport system, just so can guarantee that the feed of coal slime is smooth and easy. If gas and granule in furnace 1 get into coal slime pipeline, can hinder the normal transportation of coal slime, and cause the influence to furnace 1's fluidization stability. The working pressure at the coal slurry inlet in the hearth 1 is 6-8 KPa, so that the outlet pressure of the pressure pump is required to be slightly larger than the working pressure, and the outlet pressure of the pressure pump is larger than the pressure at the coal slurry inlet in the hearth 1 at the end, so that the arrangement of a connecting pipeline between the outlet of the pressure pump and the coal slurry inlet is determined.
In a word, through reasonable design coal slime inlet tube 3, can guarantee that the coal slime has higher combustion efficiency, the feed of coal slime not receive the control of circulation volume, and avoided the wearing and tearing of outstanding parts such as nozzle for circulating fluidized bed coal slime feed system can work reliably and stably.
In addition, the invention also provides a circulating fluidized bed boiler which comprises the circulating fluidized bed coal slime feeding system, the cyclone separator, the tail flue, the selective catalytic reduction system, the superheater, the reheater, the economizer, the air preheater and the like, wherein the selective catalytic reduction system, the superheater, the reheater, the economizer and the air preheater are arranged in the tail flue. Through reasonable design coal slime inlet tube 3, can guarantee that the coal slime has higher combustion efficiency and makes the feed of coal slime not receive the control of circulation volume in circulating fluidized bed boiler.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. The invention is not described in detail in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (10)
1. Circulating fluidized bed coal slime feed system, its characterized in that, circulating fluidized bed coal slime feed system include furnace (1), set up in just be used for sending the granule of retrieving into again on the lateral wall of furnace (1) return pipe (2) in furnace (1) with set up in just be used for sending into the coal slime on the lateral wall of furnace (1) coal slime inlet tube (3) in furnace (1), coal slime inlet tube (3) are close to return pipe (2) set up and are located the top of return pipe (2), the coal slime inlet tube (3) with the one end downward sloping that the lateral wall of furnace (1) is connected.
2. A circulating fluidized bed coal slurry feeding system according to claim 1, characterized in that the furnace (1) is tower shaped.
3. A circulating fluidized bed coal slurry feeding system according to claim 2, characterized in that the axis of the coal slurry inlet pipe (3) is coplanar with the central axis of the furnace (1).
4. A circulating fluidized bed coal slurry feeding system according to claim 3, characterized in that the included angle between the extension direction of the coal slurry inlet pipe (3) and the axial direction of the furnace (1) is a, and a is more than or equal to 30 degrees and less than or equal to 60 degrees.
5. A circulating fluidized bed coal slurry feeding system according to claim 2, characterized in that the extension direction of the coal slurry inlet pipe (3) is parallel to the extension direction of the return pipe (2).
6. A circulating fluidized bed coal slurry feeding system according to claim 5, characterized in that the end of the coal slurry inlet pipe (3) connected to the side wall of the furnace (1) and the end of the return pipe (2) connected to the side wall of the furnace (1) are on the same bus of the furnace (1).
7. A circulating fluidized bed coal slurry feeding system according to claim 6, characterized in that the distance between the end of the coal slurry inlet pipe (3) connected with the side wall of the furnace (1) and the end of the return pipe (2) connected with the side wall of the furnace (1) is H, and H is more than or equal to 0.5m and less than or equal to 1 m.
8. A circulating fluidized bed coal slurry feeding system according to claim 1, characterized in that the working pressure in the coal slurry inlet pipe (3) is higher than the working pressure at the coal slurry inlet in the furnace (1).
9. A circulating fluidized bed coal slurry feeding system according to claim 8, characterized in that the working pressure at the coal slurry inlet in the furnace (1) is 6-8 KPa.
10. Circulating fluidized bed boiler, characterized in that it comprises a circulating fluidized bed coal slurry feeding system according to any one of claims 1 to 9.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201610313129.7A CN106016254B (en) | 2016-05-12 | 2016-05-12 | Recirculating fluidized bed coal slime feeding system and circulating fluidized bed boiler |
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| CN201610313129.7A CN106016254B (en) | 2016-05-12 | 2016-05-12 | Recirculating fluidized bed coal slime feeding system and circulating fluidized bed boiler |
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| CN106016254B true CN106016254B (en) | 2018-05-01 |
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| CN201610313129.7A Active CN106016254B (en) | 2016-05-12 | 2016-05-12 | Recirculating fluidized bed coal slime feeding system and circulating fluidized bed boiler |
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| CN109000221A (en) * | 2018-07-16 | 2018-12-14 | 大连亿斯德制冷设备有限公司 | A kind of coal slime processing method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101387404A (en) * | 2008-10-29 | 2009-03-18 | 中国科学院工程热物理研究所 | Wet sludge drying, incinerating and treating device |
| CN201697119U (en) * | 2010-07-07 | 2011-01-05 | 樊起国 | Feeding device for adding coal slurry for burning of fluidized bed boiler |
| CN202955686U (en) * | 2012-11-11 | 2013-05-29 | 山东诚信达锅炉技术有限公司 | Circulating fluidized bed boiler |
| CN205592940U (en) * | 2016-05-12 | 2016-09-21 | 中国神华能源股份有限公司 | Circulating fluidized bed coal slime feed system and circulating fluidized bed boiler |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3913229B2 (en) * | 2004-04-14 | 2007-05-09 | 三菱重工業株式会社 | Circulating fluid furnace |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101387404A (en) * | 2008-10-29 | 2009-03-18 | 中国科学院工程热物理研究所 | Wet sludge drying, incinerating and treating device |
| CN201697119U (en) * | 2010-07-07 | 2011-01-05 | 樊起国 | Feeding device for adding coal slurry for burning of fluidized bed boiler |
| CN202955686U (en) * | 2012-11-11 | 2013-05-29 | 山东诚信达锅炉技术有限公司 | Circulating fluidized bed boiler |
| CN205592940U (en) * | 2016-05-12 | 2016-09-21 | 中国神华能源股份有限公司 | Circulating fluidized bed coal slime feed system and circulating fluidized bed boiler |
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