CN201873599U - Drying and upgrading device for coal slim and sludge - Google Patents
Drying and upgrading device for coal slim and sludge Download PDFInfo
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- CN201873599U CN201873599U CN2010205699683U CN201020569968U CN201873599U CN 201873599 U CN201873599 U CN 201873599U CN 2010205699683 U CN2010205699683 U CN 2010205699683U CN 201020569968 U CN201020569968 U CN 201020569968U CN 201873599 U CN201873599 U CN 201873599U
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Abstract
A drying and upgrading device for coal slim and sludge mainly comprises a flue gas producer, a feeder, a drying tube, a material scattering device, a cyclone separator, a fine particle conveying device, a finished product conveying device, a dust collector and a draft fan, wherein a drying medium produced by the flue gas producer and a to-be-dried high-moisture material fed in by the feeder respectively enter the material scattering device and the drying tube, the high-moisture material is scattered and dried preliminarily in the material scattering device and is dried deeply and separated pneumatically in the drying tube, particles with sizes below an upper design limit are carried by air flow into the separator, coal particles with sizes above the upper design limit fall into the scattering device to be scattered again, then finished products collected by the separator are conveyed to a coal yard or other places via the conveying device, and exhaust gas discharged by the separator is treated by the dust collector prior to being discharged into atmosphere via the draft fan. The drying and upgrading device has the advantages of better drying effect, reliability in operation, simplicity and compact structure.
Description
Technical field
The utility model relates to the drying and upgrading technical field, is specifically related to a kind of coal slime, drying sludge device for improving quality.
Background technology
Coal separation is produced will be accompanied by a large amount of primary slimes and secondary slime, and higher because of moisture, the product sales resistance can only be stacked in vacant lot, not only easily causes the wasting of resources, and easily causes environmental pollution.Even after reclaiming through pressure filter, coal slime filter cake fine size, moisture height, viscosity is big, quality is low, be difficult to realize efficient industrial application, and be main outlet to sell civilianly.
At present, power industry only has minority circulating fluidized bed (CFB) boiler can directly adopt the mode of mixing burning to carry out the utilization of press filtration coal slime, mixes and burns the share basic controlling at total below 30% of fuel quantity.This utilizes mode not only to need powerful coal slime pumping system, and coal slime that need press filtration is good is added moisture again and is reached the requirement of coal slime pumping system to guarantee its moisture, with domestic certain 1025t/h CFB boiler is example, the coal slime moisture that coal separating plant supplies with is between 22%～26%, carry requirement in order to satisfy the coal slime pumping system, coal slime must be added about moisture to 30%, thereby cause heat loss due to exhaust gas to increase, reduce boiler thermal output, reduced the utility value of coal slime.
At present, in the actual production, a large amount of washing coal slimes can only adopt the modes such as commercial coal of mixing after the washing to handle, owing to contain large quantity of moisture in the coal slime, calorific value is low, has reduced the quality and the economic worth of finished market product coal.
Along with the development of China's municipal sewage treatment, the output of mud is rapid ascendant trend in recent years, has produced the high-moisture mud of enormous amount, owing to contain hazardous and noxious substances such as various pathogenic agent, heavy metal, must carry out treatment and disposal.And increasingly serious land resources has also proposed very high requirement to the time and the space of sludge treatment.
The advantage of sludge incineration is to reduce largely the volume of mud, decomposes the poisonous organic matter in the mud, can recycle the heat energy that sludge incineration produces, and meets China's sustainable development path, but need carry out drying treatment before the burning of mud.
Therefore, after high-moisture material drying upgradings such as coal slime, the mud processing, be convenient to realize that it effectively utilizes, improves commercial value, reduces floor space, reduces environmental pollution, for enterprise increases economic benefit.
At present, using comparatively extensively, the coal slime drying installation is the coal slime roller drying device.This device mainly by thermal source, break up device, belt feeder, charger, revolving cylinder, belt discharging machine, induced draft fan, dumper and power distribution cabinet and constitute, its ultimate principle is the rotation by cylinder, make coal slime in slow moving process by the elevated temperature heat flue gas drying.The coal slime roller drying device is comparatively simple, and technology is comparatively ripe, but also has open defect such as comprise that low, the single cover system processing power of heat transfer coefficient is limited, finished product granularity poor quality, floor space are big.
Summary of the invention
In order to overcome the shortcoming of above-mentioned prior art, the purpose of this utility model provides a kind of coal slime, drying sludge device for improving quality, has that drying effect is better, reliable, system is simple, the characteristics of compact construction.
To achieve these goals, the technical solution of the utility model is achieved in that
A kind of coal slime, the drying sludge device for improving quality, comprise drying tube 3, the lower end of drying tube 3 or side lower part are connected with the outlet that material is broken up device 4, the outlet of drying tube 3 is connected with the import of separator 9, it is characterized in that, below the outlet of drying tube 3, middle part or upper position place that material is broken up the above drying tube 3 of the outlet of device 4 dispose high moisture material import to be dried, the gas approach that material is broken up device 4 is arranged in material and breaks up the middle part of device 4 or bottom and be connected with the exhanst gas outlet of flue gas producer 5, the tail gas outlet of separator 9 is connected with the import of fly-ash separator 12, the product outlet of separator 9 is connected with finished conveying device 11, the fine particle outlet of fly-ash separator 12 is connected with fine particle e Foerderanlage 10, and the tail gas outlet of fly-ash separator 12 is connected with atmosphere through induced draft fan 13.
Be positioned under the high moisture material import to be dried in the said drying tube 3, material breaks up position on the device 4 and disposes that material is broken up device 14 in advance or grid enters the raw meal particle size that material is broken up device 4 with control.
Said flue gas producer 5 can be a coal furnace, also can be gas furnace, and coal furnace can be chain furnace, fluid bed furnace or coal-powder boiler.Said hot flue gas producer 5 can dispose separately, also can utilize existing boiler, and as station boiler, as hot flue gas producer, the hot flue gas by in position extracting suitable temp is as drying medium.
Said material is broken up device 4 and can be adopted wind formula impact breaker, cross wind formula plate-hammer crusher, blower mill or similar simplification device.
Said drying tube 3 has the pneumatic separation effect simultaneously, and may command is carried the grain graininess and the degree of drying of the dry finished product that leaves drying tube by drying medium.Drying medium speed in the said drying tube 3 is at 5～25m/s.Said drying tube 3 cross sections are circular, square or irregularly shaped, and different heights place cross-sectional shape can change, with the troubled water that changes descending wet stock and up drying air stream and the sorting situation of large granular materials.
Principle of work of the present utility model is: 200～850 ℃ of high-temperature flue gas that adopt that flue gas producer 5 produces or air are as drying medium, top or bottom that drying medium is broken up device 4 by material feed, coal slime, mud are fed by the middle part of drying tube 3 or the high moisture material import to be dried on top, when coal slime, mud were broken, break up in material is broken up device 4, the medium that is dried was predrying; Drying medium carry secretly break up with predrying after enter drying tube 3 than fine particle and carry out further drying, wherein particle diameter is no more than particle that the design upper limit requires and is carried by air-flow and enter in the separator 9, and particle diameter falls into material greater than the particle of the design upper limit and breaks up device 4 and broken up once more; Send into coal yard or other place by the finished product that separator 9 is collected through finished conveying device 11, the tail gas of being discharged by separator 9 enters atmosphere by induced draft fan 13 after fly-ash separator 12 is handled, the fine particle that fly-ash separator 12 produces is sent into coal yard or other place through fine particle e Foerderanlage 10.
High moisture material import to be dried is arranged in middle part or the top in the drying tube 3, therefore, feeding high moisture material falls into material and breaks up in device 4 processes because of action of gravity is descending, being adverse current with hot flow of flue gas direction flows to, make to enter material and break up the wet stock of device 4 and carry out preliminarily dried and sorting, break up the working load of device and sticking stifled possibility takes place to alleviate material.Drying tube 3 outlets can be provided with inertial separator, to strengthen the sorting control to discharging-material size.
The utlity model has following advantage:
1, adopts the convection drying mode, flue gas and high moisture material heat and mass to be dried are strong, both can accelerate moisture diffusion speed in the high moisture material to be dried, and can significantly improve the processing power of single complete equipment and system again, single complete equipment can realize that processing power is substantially more than 150t/h;
2, adopt material to break up the mode of device and drying tube combination layout, efficiently solve the antiseized stifled problem in the high moisture material drying process;
3, adopting the spatial altitude direction is main decoration form, and whole process system floor space is little;
4, by the particular design of pneumatic separation and inertial separation and drying tube, can realize effective control to the finished product granularity, guarantee the quality of drying and upgrading product;
5, by selecting and controlling the drying medium initial temperature and high-effective dust-removing equipment is set, can guarantee finally to enter atmospheric weary gas and satisfy country and local environmental emission standard, free from environmental pollution.
6, systemic resistance is little, and power consumption is low.
Description of drawings
Fig. 1 is the structural representation of embodiment 1 of the present utility model.
Fig. 2 is the structural representation of embodiment 2 of the present utility model.
Fig. 3 is the structural representation of embodiment 3 of the present utility model.
Fig. 4 is the variable section structure synoptic diagram of drying tube 3 among Fig. 2.
Fig. 5 is the structural representation that material is broken up device 14 in advance among Fig. 2, wherein, (a) is vertical view; (b) be the A-A sectional view.
Embodiment
Below in conjunction with drawings and Examples the utility model is done more detailed description.
Referring to Fig. 1, the drying tube of this embodiment 13 adopts the uniform cross section structures, and high moisture material import to be dried is configured in the middle part of the above drying tube 3 of the outlet that outlet is following, material is broken up device 4 of drying tube 3, realizes the middle part feed; High moisture material import to be dried is connected with the discharge port of feeding machine 2, the opening for feed of feeding machine 2 is connected with feed bin 1, feeding machine 2 is the coal slime peeler, the gas approach that material is broken up device 4 is arranged in material and breaks up the bottom of device 4 and be connected with the exhanst gas outlet of flue gas producer 5, adopt material to break up the mode that device 4 bottoms feed flue gas, flue gas producer 5 is a chain furnace.In addition, among Fig. 1,6 is fan; 7 is feeder; 8 is coal bunker; 9 is cyclonic separator; Fly-ash separator 12 is a sack cleaner.
Referring to Fig. 2, the drying tube of this embodiment 23 adopts variable section structures, and high moisture material import to be dried is configured in the top of the above drying tube 3 of the outlet that outlet is following, material is broken up device 4 of drying tube 3, realizes the top feed; High moisture material import to be dried is connected with the discharge port of feeding machine 2, the opening for feed of feeding machine 2 is connected with feed bin 1, feeding machine 2 is the coal slime crusher, the gas approach that material is broken up device 4 is arranged in material and breaks up the top of device 4 and be connected with the exhanst gas outlet of flue gas producer 5, adopt material to break up the mode that device 4 tops feed flue gas, flue gas producer 5 is a chain furnace.In addition, among Fig. 2,6 is fan; 7 is feeder; 8 is coal bunker; Separator 9 is a cyclonic separator; Fly-ash separator 12 is a sack cleaner; 14 break up device in advance for the material that material breaks up on the device 4 that is positioned at that is configured in the drying tube 3.
Referring to Fig. 3, the drying tube of this embodiment 33 adopts the uniform cross section structures, and high moisture material import to be dried is configured in the middle part of the above drying tube 3 of the outlet that outlet is following, material is broken up device 4 of drying tube 3, realizes the middle part feed; High moisture material import to be dried is connected with the discharge port of feeding machine 2, the opening for feed of feeding machine 2 is connected with feed bin 1, feeding machine 2 is the coal slime peeler, the gas approach that material is broken up device 4 is arranged in material and breaks up the bottom of device 4 and be connected with the exhanst gas outlet of flue gas producer 5, adopt material to break up the mode that device 4 bottoms feed flue gas, flue gas producer 5 is a fluidized-bed flue gas producer.In addition, among Fig. 3,6 is fan; 7 is feeder; 8 is coal bunker; Separator 9 is an inertial separator; Fly-ash separator 12 is a sack cleaner.
The coal slime filter cake that moisture after the press filtration is about 30%, apparent size is about 400mm is sent into feeding machine 2 through belt and is broken into granularity and is not more than the coal slime cluster of grains of 50mm and sends into drying tube 3; Under the effect of gravity, bulk coal slime cluster of grains falls to entering that material is broken up device 14 in advance, material is broken up device 4 or directly entered material and breaks up device 4, and the fine particle coal slime rises with flue gas; Being lower than about 470 ℃ flue gas that the flue gas producer of 3000kCal/kg burning inferior coal produces by thermal value breaks up after the middle part of device 4 or bottom feed from material, to fall into the large coal particles walk drying that material is broken up device 4 from drying tube 3, in this process, finish breaing up of coal slime group, the coal slime granularity is met the demands; The fine particle coal slime that meets the demands rises with flue gas and enters drying tube 3, further enter after the drying separator 9 of drying tube 3 outlets separated after, be delivered to finished goods warehouse through finished conveying device 11; The low-temperature flue gas of being discharged by separator 9 is discharged into atmosphere by induced draft fan 13 after fly-ash separator 12 dust removal process; The fine particle that fly-ash separator 12 produces is sent into coal yard or other place through fine particle e Foerderanlage 10.
Referring to Fig. 4, the cross section of drying tube 3 is a variable section structure.
Referring to Fig. 5, it is a pulverizer that material is broken up device 14 in advance.
Claims (6)
1. coal slime, the drying sludge device for improving quality, comprise drying tube (3), the lower end of drying tube (3) or side lower part are connected with the outlet that material is broken up device (4), the outlet of drying tube (3) is connected with the import of separator (9), it is characterized in that, below the outlet of drying tube (3), middle part or upper position place that material is broken up the above drying tube (3) of the outlet of device (4) dispose high moisture material import to be dried, the gas approach that material is broken up device (4) is arranged in material and breaks up the middle part of device (4) or bottom and be connected with the exhanst gas outlet of flue gas producer (5), the tail gas outlet of separator (9) is connected with the import of fly-ash separator (12), the product outlet of separator (9) is connected with finished conveying device (11), the fine particle outlet of fly-ash separator (12) is connected with fine particle e Foerderanlage (10), and the tail gas outlet of fly-ash separator (12) is connected with atmosphere through induced draft fan (13).
2. device according to claim 1 is characterized in that, is positioned under the high moisture material import to be dried in the said drying tube (3), material breaks up position on the device (4) and dispose material and break up device (14) or grid in advance.
3. device according to claim 1 is characterized in that, said drying tube (3) cross section is circular, square, and different heights place cross-sectional shape is identical or different.
4. device according to claim 1 is characterized in that, said flue gas producer (5) is a coal furnace, or gas furnace, and coal furnace can be chain furnace, fluid bed furnace or coal-powder boiler.
5. device according to claim 1 is characterized in that, it was wind formula impact crusher that said material is broken up device (4), cross wind formula hammering crusher, blower mill.
6. device according to claim 1 is characterized in that, said hot flue gas producer (5) is separately configuration, or utilizes existing boiler as hot flue gas producer, and the hot flue gas by extracting suitable temp is as drying medium.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205699683U CN201873599U (en) | 2010-10-20 | 2010-10-20 | Drying and upgrading device for coal slim and sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205699683U CN201873599U (en) | 2010-10-20 | 2010-10-20 | Drying and upgrading device for coal slim and sludge |
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| Publication Number | Publication Date |
|---|---|
| CN201873599U true CN201873599U (en) | 2011-06-22 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010205699683U Expired - Lifetime CN201873599U (en) | 2010-10-20 | 2010-10-20 | Drying and upgrading device for coal slim and sludge |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104150737A (en) * | 2014-07-30 | 2014-11-19 | 沈阳航空航天大学 | Single-shaft self-cleaning/dispersion sludge drier and method thereof |
| CN107309056A (en) * | 2017-08-10 | 2017-11-03 | 长兴捷明机械有限公司 | A kind of cement material grinding system |
| CN111649334A (en) * | 2020-06-29 | 2020-09-11 | 华能国际电力股份有限公司 | Novel sludge drying and incinerating system and method |
| CN111735057A (en) * | 2020-06-29 | 2020-10-02 | 华能国际电力股份有限公司 | Rapid entrained flow bed sludge drying and incineration simple device and method |
-
2010
- 2010-10-20 CN CN2010205699683U patent/CN201873599U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104150737A (en) * | 2014-07-30 | 2014-11-19 | 沈阳航空航天大学 | Single-shaft self-cleaning/dispersion sludge drier and method thereof |
| CN104150737B (en) * | 2014-07-30 | 2015-11-18 | 沈阳航空航天大学 | Sludge drier and method thereof are broken up in a kind of single shaft self-stip |
| CN107309056A (en) * | 2017-08-10 | 2017-11-03 | 长兴捷明机械有限公司 | A kind of cement material grinding system |
| CN111649334A (en) * | 2020-06-29 | 2020-09-11 | 华能国际电力股份有限公司 | Novel sludge drying and incinerating system and method |
| CN111735057A (en) * | 2020-06-29 | 2020-10-02 | 华能国际电力股份有限公司 | Rapid entrained flow bed sludge drying and incineration simple device and method |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20110622 |