CN214881080U - A steam fluidized heating sludge drying system - Google Patents
A steam fluidized heating sludge drying system Download PDFInfo
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- CN214881080U CN214881080U CN202120926884.9U CN202120926884U CN214881080U CN 214881080 U CN214881080 U CN 214881080U CN 202120926884 U CN202120926884 U CN 202120926884U CN 214881080 U CN214881080 U CN 214881080U
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Abstract
一种蒸汽流化加热的污泥干化系统，包括依次连接的鼓泡床污泥干化器、旋风式净化器和蒸汽再生器，所述鼓泡床污泥干化器从入口至出口方向隔成至少两个上部连通的空间，每个空间的下方均设有布风室，旋风式净化器的排渣管插入到第一个空间的床料层下方，所述蒸汽再生器包括主工作室、疏水箱和副水箱，疏水箱、副水箱位于主工作室的两侧，所述的主作室内从上至下间隔布置多个热交换面，所述主工作室通过管道与每个布风室连接。本实用新型有效的解决了垃圾、污泥等含湿度高、粘滞性强难以流动的物料流动与加热与干燥的问题，具有系统简单、换热系数高、物料干燥程度高、设备能耗小等优点，为垃圾、污泥进一步资源化利用创造有利条件。
A steam fluidized heating sludge drying system, comprising a bubbling bed sludge dryer, a cyclone purifier and a steam regenerator connected in sequence, the bubbling bed sludge dryer is from the inlet to the outlet direction It is divided into at least two upper-connected spaces, and an air distribution chamber is arranged below each space. The slag discharge pipe of the cyclone purifier is inserted under the bed material layer of the first space. The steam regenerator includes the main work chamber, drainage tank and auxiliary water tank. The drainage tank and auxiliary water tank are located on both sides of the main working chamber. The main working chamber is spaced from top to bottom with a plurality of heat exchange surfaces. The main working chamber communicates with each cloth through pipes. Air chamber connection. The utility model effectively solves the problems of flow, heating and drying of materials with high humidity and strong viscosity such as garbage and sludge, which are difficult to flow. and other advantages, creating favorable conditions for further resource utilization of garbage and sludge.
Description
Technical Field
The utility model relates to a sludge treatment system, in particular to a sludge drying system heated by steam fluidization.
Background
In recent years, with the increase of the national demand for waste treatment, reduction, detoxification and recycling of solid waste having a high water content, such as municipal sludge and industrial sludge, are important directions and policies for sludge treatment. Sludge drying and calcining are the main ways of sludge reduction and harmlessness. The thermal power plant has unique advantages in the aspects of sludge drying and calcining, can effectively recover heat generated by sludge combustion while providing heating media with various qualities for sludge drying, and really achieves sludge reduction, harmless and resource treatment. Because the water content of the sludge is as high as 60-80%, the sludge generally needs to be dried in order to reduce the influence of the sludge on a boiler. At present, a mature sludge drier in the market can only dry sludge until the water content is 30-40%, and if the water content of the sludge is further reduced, the drying equipment and the drying energy consumption are greatly increased.
The sludge is difficult to flow and has viscosity, which brings great difficulty to the manufacture of heating and drying equipment, and more importantly, the sludgeAmmonia gas and H are released in the mud heating and drying process2S, combustible volatile gas and other harmful and dangerous gases, thereby limiting the heating mode of the sludge and the selection of the heating medium. The sludge drying technology which is applied in more market at present mainly comprises a flue gas thin layer drying technology, the technology utilizes low-temperature flue gas to heat sludge, and flue gas waste heat is utilized, but the technology has the problems of huge equipment, difficult flue gas purification treatment and the like. The other sludge drying technology which is more applied is a disc or paddle type sludge drying technology, the sludge is heated by utilizing a heat transfer mode of steam passing through partition walls, and due to the characteristics of the sludge, the technology has the defects of small heat exchange coefficient, low effective utilization rate of a heat exchange surface, low material drying degree, large equipment, high energy consumption, small capacity of single equipment and the like.
SUMMERY OF THE UTILITY MODEL
The technical problem to be solved by the utility model is to overcome the above-mentioned defects existing in the prior art and provide a
The utility model provides a technical scheme that its technical problem adopted is: the utility model provides a sludge drying system of steam fluidization heating, includes tympanic bulla bed sludge drying ware, whirlwind formula clarifier and the steam regenerator who connects gradually, tympanic bulla bed sludge drying ware separates into the space of two at least upper portions intercommunications from entry to export orientation, and the below in every space all is equipped with the wind distribution chamber, and the sediment pipe of whirlwind formula clarifier inserts the bed material layer below in first space, the steam regenerator includes main studio, drain box and expansion tank, and drain box, expansion tank are located the both sides of main studio, the main studio in from last to a plurality of heat exchange surfaces of interval arrangement down, the main studio passes through the pipeline and is connected with each wind distribution chamber.
Further, the heat exchange surface includes snakelike heat exchanger tube bank and sprays heat exchanger tube bank, whirlwind clarifier is connected with snakelike heat exchanger tube bank, snakelike heat exchanger tube bank with spray heat exchanger tube bank through the pipe connection that is located the main work room outside, it is connected with the drain box to spray heat exchanger tube bank, the upper portion air space of drain box and the upper portion air space of auxiliary water tank pass through residual gas heat exchanger tube bank and be connected, the lower part water space of drain box and the lower part water space of auxiliary water tank pass through the condensate water heat exchanger tube bank and be connected, the auxiliary water tank passes through the pipeline and is connected with the spraying layer that is located the main work room, the spraying layer is located and sprays the heat exchanger tube bank top.
The spraying layer is provided with a distribution pipe network and an atomizing nozzle, and the atomizing nozzle adopts a mechanical atomizing mode.
Further, an inlet header is arranged at an inlet of the snakelike heat exchange tube bundle, and an outlet header is arranged at an outlet of the snakelike heat exchange tube bundle; and a steam distribution box is arranged at the inlet of the spraying heat exchange tube bundle, and a steam collection box is arranged at the outlet of the spraying heat exchange tube bundle.
Furthermore, a booster fan is arranged on a pipeline connecting the cyclone purifier and the main working chamber.
Furthermore, a steam reheater is arranged on a main pipeline connecting the main working chamber and the air distribution chamber.
Furthermore, the upper end of the bubbling bed sludge drier is provided with a steam outlet, and the lower end of the bubbling bed sludge drier is provided with a dry sludge outlet.
Furthermore, the lower end of the auxiliary water tank is provided with a first sewage outlet, the upper end of the auxiliary water tank is provided with a gas outlet, and the lower end of the main working chamber is provided with a second sewage outlet.
Further, the spraying heat exchange tube bundle, the residual gas heat exchange tube bundle and the condensed water heat exchange tube bundle are all straight-through tube bundles.
The utility model discloses the effectual material that has solved rubbish, mud etc. and contain humidity height, viscosity are strong to be difficult to the flow flows and the problem of heating and drying, has advantages such as the system is simple, heat transfer coefficient is high, material drying degree is high, equipment energy consumption is little, creates the advantage for rubbish, the further resource utilization of mud.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
As shown in fig. 1, the present embodiment includes a bubbling bed sludge drier 1, a cyclone purifier 2, a booster fan 3, a steam regenerator 4, etc. connected in sequence.
The upper part of the bubbling bed sludge dryer 1 is a cuboid bubbling bed 101, 3 middle low walls 102 are arranged in the bubbling bed along the length direction, and the heights of the low walls are gradually decreased. The rectangular bubbling bed is divided into 4 upper communicated spaces by the low wall, air distribution chambers 104 are arranged below the first space to the fourth space, steam inlets 107 are arranged on the air distribution chambers 104, and wet sludge inlets 105 are arranged above the first space. An ash deposition hopper 103 is arranged below the fourth space, a dry sludge outlet 106 is arranged below the ash deposition hopper 103, and a steam outlet 108 is arranged above the ash deposition hopper 103. Preferably, a spare connector 109 is arranged at the top of the dryer and used for adding heat carrier materials such as high-temperature dust (such as high-temperature slag or ash discharged from a fluidized bed boiler).
The cyclone purifier 2 preferentially adopts a rotary spray drying purification tower to purify steam, lime slurry is sprayed into the cyclone purifier 2 to remove smoke dust and acid gas entering the steam, particles separated by the purifier are discharged into the bubbling bed 101 through a slag discharge pipe, and the slag discharge pipe of the cyclone purifier 2 penetrates through a top plate of a first space of the bubbling bed 101 to be inserted into the lower part of a bed material layer of the space.
The steam regenerator 4 is composed of a main working chamber 401, a drain tank 408 and an auxiliary water tank 411, which are all rectangular cavities, and the drain tank 408 and the auxiliary water tank 411 are tightly attached to two sides of the main working chamber 401 and are flush with the lower bottom surface of the main working chamber.
The main working chamber 401 is internally provided with heat exchange surfaces such as a serpentine heat exchange tube bundle 403, a spray layer 412, a spray heat exchange tube bundle 406, a residual gas heat exchange tube bundle 410, a condensed water heat exchange tube bundle 409 and the like from top to bottom in sequence. The serpentine heat exchange tube bundle 403 is connected with the cyclone purifier 2, an inlet header 402 is arranged at the inlet of the serpentine heat exchange tube bundle 403, and an outlet header 404 is arranged at the outlet of the serpentine heat exchange tube bundle 403; the spray heat exchange tube bundle 406 is a straight-through tube bundle, the spray heat exchange tube bundle 406 penetrates through the main working chamber 401, a steam distribution box 405 is arranged at the inlet of the spray heat exchange tube bundle 406, a steam collection box 407 is arranged at the outlet of the spray heat exchange tube bundle 406, the serpentine heat exchange tube bundle 403 is connected with the spray heat exchange tube bundle 406 through a pipeline positioned outside the main working chamber 401, and the spray heat exchange tube bundle 406 is connected with the steam trap 408 through a pipeline positioned outside the main working chamber 401. The upper air space of the steam trap 408 is connected to the upper air space of the expansion tank 411 by a residual air heat exchange tube bundle 410, and the lower water space of the steam trap 408 is connected to the lower water space of the expansion tank 411 by a condensed water heat exchange tube bundle 409. Residue gas heat exchange tube bundle 410 and condensate heat exchange tube bundle 409 traverse main working chamber 401.
The booster fan 3 is located on a pipeline connecting the cyclone purifier 2 and the main working chamber 401.
The auxiliary water tank 411 is connected to an inlet of the regeneration pump 5 through a pipeline, an outlet of the regeneration pump 5 is connected to the spray layer 412 through a pipeline, and generally, the spray layer 412 is provided with a distribution pipe network and an atomizing nozzle which adopts a mechanical atomizing mode.
The upper part of the main working chamber 401 is provided with a regeneration steam outlet 413 which is connected to the inlet of the steam reheater 6 through a pipeline, and the outlets of the steam reheater 6 are respectively connected to the steam inlet 107 of the air distribution chamber 104 through pipelines.
The bottom of the main working chamber 401 is provided with a second sewage draining port 414, the bottom of the auxiliary water tank 411 is provided with a first sewage draining port 415, and the upper part of the auxiliary water tank 411 is provided with a noncondensable air draining port 416.
When the bubbling bed sludge drier works, bed materials are filled in the bubbling bed sludge drier 1, and the bed materials can be coal ash, sand or dry sludge and other fine particles. Fresh steam with the pressure of about 10kPa and the temperature of 200-300 ℃ enters the bubbling bed 101 from the air distribution chamber 104, blows bed materials into a dispersed state, continuously turns over the middle low wall, moves from the left end to the right end, namely moves from the wet sludge inlet 105 to the dry sludge outlet 106, finally, larger particles fall into the ash deposition hopper 103 and are discharged out of the bubbling bed sludge drier 1, finer sludge ash enters the cyclone purifier 2 along with the steam, 90-95% of dust particles are captured and enter the bubbling bed 101 again, and the circulation of the fine ash particles is completed; and controlling the circulation multiplying power of the fine ash to be about 3-5 times by controlling the fluidization speed of the steam. Wet sludge with the water content of 60-80% is crushed into sludge particles with the particle size of about 3-5 mm, the sludge particles enter the sludge drier from a wet sludge inlet 105 of the bubbling bed sludge drier 1, are wrapped by fine ash particles in the bubbling bed 101 in an internal rotation mode, are dispersed in bed materials and move along with the bed materials, the wet sludge particles continuously absorb heat of hot bed materials and steam in the moving process, moisture is evaporated and dried, and finally the sludge particles are discharged out of the drier.
The steam transfers heat to wet sludge and dries the wet sludge, and then the wet sludge is discharged from a steam outlet of the bubbling bed sludge drier 1, the temperature of the steam is reduced and maintained at about 150 ℃, and the discharged steam carries sludge ash particles and H separated out in the sludge drying process2S, methane and other gases form spent steam. The exhausted steam enters the cyclone purifier 2 to remove dust and acid gas in the sewage, and then the exhausted steam passes through the booster fan 3, so that the pressure of the exhausted steam is increased by about 80-100 kPa, and the condensation point of the sewage steam under the corresponding pressure is increased to about 120 ℃. Then the exhausted steam enters the steam regenerator 4, the steam in the steam regenerator 4 passes through the heat exchange surfaces of the serpentine heat exchange tube bundle 403, the spray heat exchange tube bundle 406, the residual gas heat exchange tube bundle 410, the condensed water heat exchange tube bundle 409 and the like in sequence, the steam is condensed into water with the temperature of about 120 ℃, and non-condensable gas is separated out and discharged out of the system. In the serpentine heat exchange tube bundle 403, the exhausted steam transfers heat to the new steam generated by the steam regenerator 4, the temperature is reduced to be close to the saturation temperature, but the exhausted steam is still dry steam, after passing through the spray heat exchange tube bundle 406, the steam is converted into wet steam with higher humidity, and the wet steam enters the steam trap 408, and the condensed water and the gas are primarily separated.
The gas space and the water space of steam trap 408 and auxiliary water tank 411 are respectively communicated through residual gas heat exchange tube bundle 410 and condensate heat exchange tube bundle 409, and both the tube bundles are immersed in the lower water tank in main working chamber 401, when residual gas enters auxiliary water tank 411 from steam trap 408 through residual gas heat exchange tube bundle 410, steam in the gas is further condensed to heat water in main working chamber 401, condensate in steam trap 408 enters auxiliary water tank 411 through condensate heat exchange tube bundle 409, when passing through condensate heat exchange tube bundle 409, when the temperature of the condensate is reduced, the condensate in main working chamber 401 is heated to evaporate. The non-condensable gas is finally discharged from the gas discharge port 416 above the subtank 411.
The water in the auxiliary water tank 411 is pressurized and atomized by the regeneration pump 5 and then sprayed to the upper part of the spraying heat exchange tube bundle 406 in the main working chamber 401. The pressure in the main working chamber 401 is maintained to be about 10kPa, the saturation temperature of water under the corresponding pressure is about 105 ℃, the pressure of atomized and sprayed water drops is rapidly reduced and evaporated, the dropped water drops absorb heat on the surface of the spraying heat exchange tube bundle 406 to be further evaporated to generate new steam, and the unevaporated water drops finally fall into a water pool below to absorb the heat of the heat exchange tube bundle in the water pool to be evaporated.
The temperature of new steam generated in the main working chamber 401 is about 120-130 ℃ after being heated by the serpentine heat exchange tube bundle 403, the new steam has a certain superheat degree, is discharged from the steam regenerator 4 to become new steam, absorbs external heat through the steam reheater 4, the temperature rises to about 250 ℃, and the new steam enters the bubbling bed sludge drier 1 again to realize steam circulation.
The exhausted steam is converted into new steam in the regenerator and a small amount of dust brought into the steam regenerator 4 along with the exhausted steam is deposited below each water tank along with the condensed water and is discharged through a drain outlet in the circulating process. The main heat loss of the system comprises the heat loss of the blowdown of the steam regenerator, the physical heat loss brought by the discharge of the dry sludge of the drier and the heat brought by the non-condensable gas, and the temperature levels of the blowdown, ash discharge and exhaust of the system are lower. The heat absorbed by the conventional sludge drier in sludge drying is discharged out of the system in the form of sewage vapor, and the heat is difficult to recover while a large amount of cooling water is consumed. Compared with the conventional sludge drying technology, the sludge drying device has small energy loss, and the required energy is supplemented from the steam reheater.
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. In particular, simple changes, such as simply changing the bubbling bed pattern or changing the arrangement of the heat exchange surfaces in the steam regenerator, are also within the scope of the present claims.
What is not described in detail in the specification is prior art that is well known to those skilled in the art.
Claims (9)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120926884.9U CN214881080U (en) | 2021-04-30 | 2021-04-30 | A steam fluidized heating sludge drying system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120926884.9U CN214881080U (en) | 2021-04-30 | 2021-04-30 | A steam fluidized heating sludge drying system |
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| Publication Number | Publication Date |
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| CN214881080U true CN214881080U (en) | 2021-11-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120926884.9U Withdrawn - After Issue CN214881080U (en) | 2021-04-30 | 2021-04-30 | A steam fluidized heating sludge drying system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113045178A (en) * | 2021-04-30 | 2021-06-29 | 中国能源建设集团湖南省电力设计院有限公司 | Sludge drying system heated by steam fluidization |
-
2021
- 2021-04-30 CN CN202120926884.9U patent/CN214881080U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113045178A (en) * | 2021-04-30 | 2021-06-29 | 中国能源建设集团湖南省电力设计院有限公司 | Sludge drying system heated by steam fluidization |
| CN113045178B (en) * | 2021-04-30 | 2025-01-24 | 中国能源建设集团湖南省电力设计院有限公司 | A sludge drying system using steam fluidization heating |
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| GR01 | Patent grant | ||
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| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20211126 Effective date of abandoning: 20250124 |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20211126 Effective date of abandoning: 20250124 |