WO2011035459A1 - 一种污泥滤饼好氧风干的方法及装置 - Google Patents

一种污泥滤饼好氧风干的方法及装置 Download PDF

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Publication number
WO2011035459A1
WO2011035459A1 PCT/CN2009/001279 CN2009001279W WO2011035459A1 WO 2011035459 A1 WO2011035459 A1 WO 2011035459A1 CN 2009001279 W CN2009001279 W CN 2009001279W WO 2011035459 A1 WO2011035459 A1 WO 2011035459A1
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WO
WIPO (PCT)
Prior art keywords
sludge
filter cake
drying
conveyor belt
air
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2009/001279
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English (en)
French (fr)
Inventor
钟环声
吴学伟
吴嘉聪
孙志明
杨海英
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GUANGZHOU PUDE ENVIRONMENTAL PROTECTION EQUIPMENT Ltd
Original Assignee
GUANGZHOU PUDE ENVIRONMENTAL PROTECTION EQUIPMENT Ltd
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Application filed by GUANGZHOU PUDE ENVIRONMENTAL PROTECTION EQUIPMENT Ltd filed Critical GUANGZHOU PUDE ENVIRONMENTAL PROTECTION EQUIPMENT Ltd
Priority to KR1020127010410A priority Critical patent/KR101479958B1/ko
Priority to EP20090849647 priority patent/EP2484640A4/en
Priority to US13/498,505 priority patent/US20120246965A1/en
Priority to JP2012530070A priority patent/JP5705858B2/ja
Publication of WO2011035459A1 publication Critical patent/WO2011035459A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/02—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by belts carrying the materials; with movement performed by belts propelling the materials over stationary surfaces
    • F26B17/08—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by belts carrying the materials; with movement performed by belts propelling the materials over stationary surfaces the belts being arranged in a sinuous or zig-zag path
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/30—Treatment of water, waste water, or sewage by irradiation
    • C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B1/00—Preliminary treatment of solid materials or objects to facilitate drying, e.g. mixing or backmixing the materials to be dried with predominantly dry solids
    • F26B1/005—Preliminary treatment of solid materials or objects to facilitate drying, e.g. mixing or backmixing the materials to be dried with predominantly dry solids by means of disintegrating, e.g. crushing, shredding, milling the materials to be dried
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/04—Disinfection
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/26—Reducing the size of particles, liquid droplets or bubbles, e.g. by crushing, grinding, spraying, creation of microbubbles or nanobubbles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying goods
    • F26B2200/18—Sludges, e.g. sewage, waste, industrial processes, cooling towers
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/20—Sludge processing

Definitions

  • the invention belongs to the technical field of sludge treatment, and specifically relates to a method and a device for aerobic air drying of a sludge filter cake which utilizes the combination of external energy and sludge thermal energy in the sludge drying process.
  • a large amount of sludge is generated during the sewage treatment process. In order to realize the resource utilization of the sludge, it is generally further dried after mechanical dewatering into a sludge filter cake.
  • the commonly used sludge filter cake drying method mainly adopts hot air drying, and the temperature of the sludge itself is directly or indirectly increased by the medium and high temperature hot air, so that the moisture in the sludge is quickly evaporated.
  • this treatment method there are five problems in this treatment method: one is high energy consumption for sludge drying; the other is difficult to treat sludge drying tail gas; the third is equipment investment; the fourth is poor equipment operation stability; the fifth is the possibility of dust explosion. .
  • the object of the present invention is to provide a sludge filter cake low-temperature air-drying method with low drying energy consumption, low tail gas pollution, low equipment investment, stable operation and high safety in view of the above-mentioned deficiencies of sludge filter cake treatment.
  • a sludge filter cake low temperature air drying method which comprises the following steps:
  • the sludge filter cake crushing and dispersing is realized as follows:
  • the sludge filter cake having a water content of 50% to 70% is turned in a porous or gap-like cage to cause collision and grinding between the sludge filter cakes.
  • the sludge is broken and broken, and the sludge whose outer diameter is smaller than the diameter of the cage or the gap is discharged out of the cage, thereby realizing the crushing and dispersing of the sludge filter cake.
  • the cage aperture or clearance distance is set at 3mn! Between ⁇ 30mm, in addition to the natural range of particles in the diameter range, the bulk density is small, which is conducive to gas in and out.
  • the flipping of the sludge filter cake in the cage may be driven by the spindle in the cage or by the rotation of the cage itself.
  • the tumbling speed of the sludge filter cake in the cage can be adjusted according to the water content of the sludge filter cake and the demand of the production according to the following rules: 1 the higher the water content of the sludge filter cake, the lower the tumbling speed; the sludge filter cake The lower the moisture content, the higher the turning speed.
  • the principle is to reduce the damage of the capillary channel formed by the shear force inside the sludge filter cake, so that the sludge particles remain relatively loose and the specific surface area is larger, so as to facilitate the subsequent aerobic air drying process.
  • the optimized sludge filter cake crushing and dispersing speed is the radial outermost point linear velocity between 5mm / s ⁇ 100mm / s.
  • the dry air is generated as follows: The refrigerant absorbs heat in the cold exchanger under the action of the compressor, and releases heat in the heat exchanger; the ambient air is drawn by the fan, and is first cooled in the cold exchanger. When the condensed water is precipitated, the condensation temperature is controlled between 0 ° C and 15 ° C, and then the temperature is raised to between 0 ° C and 90 ° C in the heat exchanger, and the air is increased in unsaturation under the double action. , become dry air.
  • the aerobic exothermic reaction of the sludge refers to a process in which the aerobic bacteria in the sludge decompose the organic matter in the sludge into carbon dioxide and water under the oxygen storage condition and release heat.
  • the aerobic heat release amount of the sludge may be between 0 and 20 KJ.kg- 1 , h- 1 .
  • the aerobic exothermic drying process of the sludge is a sterilization method for the pathogen itself in the sludge.
  • the physical or chemical sterilization treatment of the sludge particles may be increased according to the requirements of sludge resource utilization, and may be ultraviolet sterilization, ozone sterilization, high chlorine, high oxygen sterilization or other sterilization methods.
  • the exhaust gas is washed, and the source of water can be preferentially applied to the condensed water discharged from the cold exchanger, and the insufficient portion can be added with a water source.
  • the function of squeezing and rubbing the materials with each other by the screw machine causes the dried sludge particles to be further pulverized during the conveying process, and the screw machine may be a single spiral or two or more spirals. group.
  • the utility model relates to a sludge filter cake low-temperature air drying device, which comprises a sludge filter cake pre-crushing mechanism, a sludge air drying mechanism and a dry air generating mechanism, wherein the sludge filter cake pre-crushing mechanism is arranged at an upper part of the sludge air drying mechanism, the upper part thereof a feed port is provided;
  • the sludge wind mechanism comprises a conveyor belt and a transmission mechanism, Both ends of the conveyor belt are connected with the transmission mechanism, the conveyor belt is layered, and a discharge pulverizing mechanism is arranged below the bottommost conveyor belt, and a discharge port is provided at the end of the discharge pulverizing mechanism;
  • the drying air generating mechanism is connected to the air outlet provided in the sludge drying mechanism through the air passage.
  • the conveyor belt may be provided with 4 layers or more.
  • a sludge thickness adjuster is provided at the beginning of the first conveyor belt.
  • An ultraviolet lamp is disposed on the wall corresponding to the end of the conveyor belt.
  • the invention has the following advantages: First, the sludge filter cake is crushed and dispersed before drying, the granular sludge has a large specific surface area, and the heat and mass transfer efficiency is high when drying. The drying energy consumption is lower; Second, the broken sludge particles under the action of aerobic exotherm not only further reduce the drying energy consumption, accelerate the drying rate, but also play the role of deodorizing the sludge; During the drying process, the mud particles are moderate in motion, no dust is generated, and the production is stable and safe.
  • the low-temperature drying of the sludge does not cause the organic matter to be thermally cracked by the sludge, so that the dry tail gas can be discharged to the environmental standard after being washed with water;
  • the discharge crushing mechanism has a crushing function, and the discharged sludge particles are loose, which is convenient for resource utilization.
  • Fig. 1 is a flow chart showing the aerobic drying process of the sludge cake of the present invention.
  • FIG. 2 is a schematic structural view of a sludge filter cake aerobic air drying device of the present invention
  • FIG. 3 is a schematic cross-sectional view of the A-A section of the sludge filter cake aerobic air drying device of the present invention
  • FIG. 4 is a schematic cross-sectional view of the BB section of the sludge filter cake aerobic air drying device of the present invention
  • a sludge filter cake low temperature air drying method as shown in FIG. 1, includes the following steps:
  • the sludge filter cake is crushed and dispersed into a sludge particle layer to increase the specific surface area of the sludge.
  • the sludge filter cake crushing and dispersing is realized as follows: The sludge filter cake having a water content of 50% to 70% is turned in a porous or gap-like cage, causing collision and friction between the sludge filter cakes. And being When the crushed, the sludge whose outer diameter is smaller than the pore diameter or the gap distance of the cage is discharged outside the cage, thereby realizing the crushing and dispersing of the sludge filter cake.
  • the cage aperture or clearance distance is set at 3mn!
  • the bulk density is small, which is conducive to gas in and out.
  • the flipping of the sludge filter cake in the cage may be driven by the spindle in the cage or by the rotation of the cage itself.
  • the tumbling speed of the sludge filter cake in the cage can be adjusted according to the following conditions: according to the moisture content of the sludge cake and the demand of the production: 1 The higher the moisture content of the sludge cake, the lower the tumbling speed; The lower the moisture content of the cake, the higher the turning speed.
  • the principle is to reduce the damage of the capillary channel formed by the shear force inside the sludge filter cake, so that the sludge particles remain relatively loose and the specific surface area is larger, so as to facilitate the subsequent aerobic air drying process.
  • the higher the turning speed the larger the discharge amount of the sludge crushing and dispersing device; the lower the turning speed, the smaller the discharging amount of the sludge filter cake crushing and dispersing device.
  • the optimized sludge cake crushing and dispersing the turning speed is the radial outermost point of the line speed between 5mm / s ⁇ 100 legs / s.
  • the aerobic exothermic reaction of the sludge refers to a process in which the aerobic bacteria in the sludge decompose the organic matter in the sludge into carbon dioxide and water under the oxygen storage condition and release heat.
  • the aerobic calorific value of the sludge may range from 0 to 20 KJ.kg_h- 1 .
  • the dry air is generated as follows: The refrigerant absorbs heat in the cold exchanger under the action of the compressor, and releases heat in the heat exchanger; the ambient air is drawn by the fan, and is first cooled in the cold exchanger. When the condensed water is precipitated, the condensation temperature is controlled between 0 ° C and 15 ° C, and then the temperature is raised to between 0 ° C and 90 ° C in the heat exchanger, and the air is increased in unsaturation under the double action. , become dry air.
  • a throttle is disposed between the cold exchanger and the heat exchanger, and the restrictor may be a throttle. The condensed water produced by the cold exchanger is pumped into the water washing device.
  • the tail gas carrying the sludge moisture is extracted by the negative pressure outside the sludge particle layer, and is discharged after being washed with water.
  • the source of the washing water can preferentially use the condensed water discharged from the cold exchanger, and the insufficient portion can be supplied with a water source.
  • the requirements for further pulverization of the dried sludge particles to resource utilization is a function of squeezing and rubbing the materials with each other by using a screw machine, so that the dried sludge particles are further pulverized during the conveying process, and the screw machine may be a single spiral or more than two spirals. group.
  • the resource utilization may be fertilizer production, brick making, fuel utilization, fillers, etc.
  • a sludge filter cake aerobic air drying method comprising the following steps:
  • the sludge filter cake having a water content of 70 to 50% is broken into sludge particles and then dropped onto a conveyor belt to be dispersed into a sludge particle layer.
  • the sludge filter cake can be broken by a corresponding sludge cake crushing device.
  • the dry air is formed by condensing and separating the room temperature air in the cold exchanger and heating the temperature in the heat exchanger.
  • the temperature of the dry air can be between 0 and 90 ° C.
  • the dry air is transported through the air duct to the dry air inlet between the upper and lower steel meshes of the conveyor belts of each layer, and is dirty when passing through the bottom layer and surface sludge particles.
  • the aerobic reaction of the mud provides oxygen, while absorbing the moisture in the sludge particles, so that the sludge particles are dehydrated and dried.
  • the conveyor belt is layered above, and the first layer conveyor belt is provided with a mud particle layer thickness regulator.
  • moving conveyor line speed was set at between 1 mm / S ⁇ 10mm / S residence time of the sludge particles in the whole conveyor belt is 5h ⁇ 50h.
  • the sludge particle layer is irradiated and sterilized by ultraviolet light during the falling process;
  • the tail gas carrying the sludge moisture is extracted by the negative pressure outside the sludge particle layer, and is discharged after being washed with water.
  • the source of the washing water can preferentially use the condensed water discharged from the cold exchanger, and the insufficient portion can be supplied with a water source.
  • a sludge filter cake aerobic air drying device as shown in Fig. 2, Fig. 3, Fig. 4 and Fig. 5, comprises a sludge filter cake crushing and dispersing mechanism 2, a sludge aerobic air drying mechanism, a discharging crushing mechanism, and a drying wind Occurrence mechanism, exhaust gas collection and washing mechanism.
  • the sludge filter cake crushing and dispersing mechanism 2 is disposed at the upper portion of the sludge aerobic air drying mechanism.
  • the sludge cake crushing mechanism 2 is provided with a sludge filter feed port 1 in the upper part thereof, and the sludge filter cake is crushed into sludge particles in the sludge filter cake crushing and dispersing mechanism 2, and then falls to the sludge air drying mechanism through the discharge port.
  • the first layer of conveyor belt 12 is inside. Below the discharge opening of the sludge filter cake breaking and dispersing mechanism 2, the first layer conveyor belt 12 The starting end portion is provided with a fender 14 so that all the sludge particles coming out of the discharge port fall onto the first layer conveyor belt 12.
  • the structure of the sludge filter crushing and dispersing mechanism 2 may be: a spindle, a cage, a spindle motor and a casing, wherein the spindle motor is connected to the main shaft through a connector, and the spindle is provided with a plurality of crushing blades, and the outer side of the main shaft is covered with a cage; The outer side of the cage is provided with a casing, and the cage is porous or balanced.
  • the main shaft is disposed on the bearing housing, and the bearing housing is disposed on the main body bracket.
  • the middle portion of the outer casing is provided with a feeding port, and the cage body is fixed on the main body bracket by the connecting bracket.
  • the aperture or pore width on the cage is 3mn!
  • the outer casing may be a conical shell capable of functioning as an aggregate.
  • the installation angle of the crushing blade at the end of the spindle is a reverse propulsion mode, so that the sludge filter cake is pushed back into the crushing cage, and the sludge filter cake can be completely broken and discharged from the hole or gap in the cage.
  • a cleaning cage device is mounted on the crushing blade to keep the holes or pores in the cage unobstructed.
  • the line speed of the outermost point of the crushing blade is between 5 mm/s and 100 mm/s.
  • the sludge aerobic drying mechanism includes a conveyor belt 12, a transmission mechanism 15, a sludge thickness adjuster 13 and an ultraviolet lamp 19. Both ends of the conveyor belt 12 are connected to the transmission mechanism 15, and the transmission mechanism 15 drives the conveyor belt 12 through the shaft wheel and the speed regulating motor.
  • the mesh belt 20 of the conveyor belt 12 is disposed on the chain, and the chain is connected by connecting the long pins.
  • a sludge thickness adjuster 13 is disposed on the upper portion of the first conveyor belt 12 to control the thickness of the sludge particles in the conveyor belt 12 to improve drying efficiency, and the preferred sludge particle thickness is controlled in the range of 10 ⁇ 500.
  • the conveyor belt 12 is layered from top to bottom, and may be four or more layers, and the conveyor belt 12 of the lower layer is opposite to the conveying direction of the conveyor belt 12 of the upper layer.
  • the conveyor belt 12 can be made of a steel mesh, a filter cloth, a plastic mesh, and the like which can be both ventilated and ventilated.
  • the lower conveyor belt 12 is longer than the upper conveyor belt 12 so that when the sludge is conveyed to the end of the conveyor belt 12, the sludge of the upper conveyor belt 12 automatically falls in the opposite direction of the lower layer.
  • the stencil conveyor belt 12 is on. In the sludge falling process, the sludge is irradiated and sterilized by the ultraviolet lamp 19.
  • the ultraviolet light 19 is placed on the wall corresponding to the end of each conveyor belt.
  • a discharge pulverizing mechanism 16 is disposed at the bottom of the sludge air drying mechanism, and a discharge port 17 is disposed at an end of the discharge pulverizing mechanism 16, and the dry sludge on the lowermost conveyor belt 12 is reversed and falls on the discharge pulverizing mechanism 16 Upper, crushed while conveying, and finally discharged from the discharge port 17.
  • the discharge pulverizing mechanism 16 may be a counter-screw screw conveyor including at least one spiral pulverizing conveying rod.
  • a preferred pulverizing and conveying mechanism is provided in the discharge pulverizing mechanism 16.
  • the dry air generating mechanism is disposed at an upper portion of the sludge aerobic drying mechanism. Dry air generating mechanisms include cold exchangers, compressors, fans, and heat exchangers.
  • the fan 7 is disposed between the cold exchanger 8 and the heat exchanger 6.
  • the cold exchanger 8 is connected to the air inlet 9, and the condensed water condensed in the cold exchanger 8 is separated and collected by the condensate separator, and then sent to the exhaust water washing by the condensate pump 10.
  • the dry air is introduced into the dry air outlet 11 in the conveyor belt 12 through the air passage 18 to dry the sludge particles on the conveyor belt 12.
  • the dry air outlet 11 can blast downward and upward.
  • An exhaust gas collecting and washing mechanism is arranged on the upper part of the sludge aerobic air drying mechanism, including an induced draft fan 3 and an exhaust gas washing device 5; and the sludge filter crushing and dispersing mechanism 2 is connected to the air inlet of the induced draft fan 3 through the air duct, the induced draft fan The outlet of 3 is connected to the exhaust gas washing device 5 through the air duct.
  • the dry tail gas is transported to the exhaust gas washing device 5 by the sludge filter crushing and dispersing mechanism.
  • the exhausted water is discharged from the exhaust pipe at the upper portion of the exhaust gas washing device 5, and the washed sewage is discharged from the overflow port 4 in the middle of the exhaust gas washing device 5.
  • the sludge filter cake having a water content of 70% to 50% enters the sludge filter cake crushing and dispersing device 2 from the feed port 1, and the crushed sludge particles fall onto the steel mesh conveyor belt 12, and the linear speed of the conveyor belt is lram. Adjustable between /s ⁇ 10mm/s.
  • the sludge on the stencil conveyor belt passes through the sludge thickness regulator 13, which can control the sludge thickness at lOmn! ⁇ 500mm between.
  • the sludge When the sludge is transported to the end of the conveyor belt 12, the sludge is automatically turned down on the stencil conveyor belt moving in the opposite direction of the next layer, and the sludge is simultaneously irradiated and sterilized by the ultraviolet lamp 19 during the tumbling process, so that it reciprocates.
  • the sludge falls on the discharge pulverizing mechanism 16 placed at the lower portion of the apparatus, is broken while being conveyed, and is finally discharged from the discharge port 17 at the end of the discharge pulverizing mechanism 16.
  • the residence time of the sludge in the device can be adjusted from 5h to 50h, and the moisture content of the discharge can be adjusted between 50% and 5%.
  • Normal temperature air enters the cold exchanger 8 of the dry air generating mechanism from the air inlet 9, and the moisture in the air is condensed and precipitated, and then blown into the heat exchanger 6 through the blower 7 to be heated and heated to form unsaturated dry air, which is dry air.
  • the temperature can be adjusted from 0 to 90 °C.
  • the condensed water is discharged from the condensate separator in the cold exchanger 8, and then sent to the exhaust water washing device 5 through the condensate pump 10 to be used as the washed raw water.
  • the dry air is transported through the air duct 18 to the dry air outlets 11 between the upper and lower steel meshes of the respective conveyor belts 12, and the sludge particles on the upper and lower steel nets are provided with a dry and good oxygen source.
  • the dry air and the moisture in the sludge particles are heat and mass transfer, so that the sludge particles are dehydrated and dried.
  • the dry tail gas is collected by the induced draft fan 3 through the sludge filter cake crushing and dispersing device 2, and is blown into the tail gas washing device 5, and is discharged by bubbling with the exhaust gas, and the sewage is discharged from the overflow port 4 into the sewage pipe after washing.
  • the sludge filter cake having a water content of 70% enters the sludge filter cake crushing and dispersing device 2 from the feed port, and the crushed sludge particles fall onto the conveyor belt 12 of the sludge aerobic air drying mechanism, and the linear velocity of the conveyor belt 12 is 1. 5mm/s, the sludge thickness on the conveyor belt 12 is about 50111111.
  • the sludge is transported to the end of the conveyor belt 12, the sludge is automatically turned down on the conveyor belt 12 moving in the opposite direction of the next layer, and the sludge is simultaneously irradiated and sterilized by the ultraviolet lamp 19 during the turning process, so that it reciprocates.
  • Dry air temperature is 62 °C, respectively, is transported through the air duct to the dry air inlet 11 between the upper and lower steel meshes of the stencil conveyor belts, and the sludge particles on the upper and lower mesh belts provide dry wind.
  • the dried sludge falls on the discharge pulverizing mechanism 16 placed at the lower portion of the apparatus, is broken while being conveyed, and is finally discharged from the discharge port 17 at the end of the discharge pulverizing mechanism 16, and the discharge moisture content is 38%.
  • the residence time of the sludge in the sludge filter cake aerobic air drying device was 35h.
  • the dried sludge was packed and placed in the warehouse for 3 days, and the water content decreased to 35.
  • the sludge filter cake having a water content of 62% enters the sludge filter cake crushing and dispersing device 2 from the feed port 1, and the crushed sludge particles fall onto the conveyor belt 12 of the sludge aerobic air drying mechanism, and the linear velocity of the conveyor belt 12 At 3 mm/s, the sludge on the conveyor belt 12 has a thickness of about 80 paintings.
  • the sludge is transported to the end of the conveyor belt 12, the sludge is automatically turned down on the conveyor belt 12 which moves in the opposite direction in the next layer, and is simultaneously irradiated and sterilized by the ultraviolet lamp 19 during the turning of the sludge, so that it reciprocates.
  • the dry air temperature is 55 °C, and is separately transported through the air duct to the dry air outlet 11 between the upper and lower mesh belts of each conveyor belt 12, and the sludge particles on the upper and lower mesh belts provide dry air.
  • the dried sludge falls on the discharge pulverizing mechanism 16 placed at the lower part of the sludge aerobic drying mechanism, is crushed while being conveyed, and finally discharged from the discharge port 17 at the end of the discharge pulverizing mechanism 16, and the discharged water is discharged.
  • the rate is 33%.
  • the residence time of the sludge in the sludge filter cake in the aerobic air drying device was 28h.
  • the sludge filter cake having a water content of 54% enters the sludge filter cake crushing and dispersing mechanism 2 from the feed port 1, and the crushed sludge particles fall onto the conveyor belt 12 of the sludge aerobic air drying mechanism, and the linear velocity of the conveyor belt 12 At 5 mm/s, the sludge on the conveyor belt 12 has a thickness of about 110 mm.
  • the sludge is transported to the end of the conveyor belt 12, the sludge is automatically turned down on the conveyor belt 12 moving in the opposite direction of the next layer, and the sludge is simultaneously irradiated and sterilized by the ultraviolet lamp 19 during the tumbling process, so that it reciprocates.
  • the dry air temperature is 52 ° C, and is transported through the air duct 18 to the dry air inlet 11 between the upper and lower mesh belts of each conveyor belt 12 to provide dry air to the sludge particles on the upper and lower belts.
  • the dried sludge falls on the discharge pulverizing mechanism 16 placed at the lower part of the sludge aerobic drying mechanism, is crushed while being conveyed, and finally discharged from the discharge port at the end of the discharge pulverizing mechanism 16, and the water content of the discharge is 31%.
  • the residence time of the sludge in the sludge filter cake aerobic air drying device was 22h.

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Description

一种污泥滤饼好氧风干的方法及装置 技术领域
本发明属于污泥处理技术领域， 具体为使用在污泥干化过程中利用外 加能量和污泥自身热能相结合进行干燥的一种污泥滤饼好氧风干的方法及 装置。
背景技术
污水处理过程中会产生大量的污泥， 为了实现污泥的资源化利用， 一 般要在机械脱水成为污泥滤饼后， 作进一步的干燥处理。
目前， 常用的污泥滤饼干燥方法主要是采用热风烘干， 以中高温热风 直接或间接使污泥本身温度提高， 令污泥内的水分快速蒸发。 但这样的处 理方法存在如下五个问题： 一是污泥干燥能耗高； 二是污泥干燥尾气处理 难； 三是设备投资大； 四是设备运行稳定性差； 五是存在粉尘爆炸的可能 性。
发明内容
本发明目的是针对以上所述污泥滤饼处理存在的不足， 提供一种干燥 耗能低、 尾气污染低、 设备投资少、 运行稳定以及安全性高的污泥滤饼低 温风干方法。
本发明的技术方案是这样实现的： 一种污泥滤饼低温风干方法， 其包 括以下步骤：
( 1 ) 将污泥滤饼破碎分散成污泥颗粒层， 以增大污泥的比表面积；
(2) 向缓慢运动或翻动着的污泥颗粒层内正压送入一定温度的干燥空 气， 让污泥产生好氧放热反应， 在外热与内热的共同作用下， 水分从污泥 颗粒中蒸发出来， 并向干燥空气作传质运动；
( 3 ) 对缓慢运动或翻动着的污泥颗粒进行物理或化学杀菌处理；
(4)在污泥颗粒层外负压抽出携带了污泥水分的尾气，经水洗后排放;
(5)利用螺旋机令物料相互挤压和磨擦的功能使干燥后的污泥颗粒在 输送的过程中被进一步粉碎， 达至制肥、 制砖、 燃料利用、 填充料利用的 资源化要求。
所述的污泥滤饼破碎分散是这样实现的： 含水率在 50%〜70%间的污 泥滤饼在多孔状或间隙状的笼体内翻动， 使污泥滤饼间产生相互碰撞和磨 擦而被破碎， 颗粒外径小于笼体孔径或间隙距离的污泥被排出笼体外， 从 而实现了污泥滤饼的破碎分散。 笼体孔径或间隙距离设定在 3mn！〜 30mm之 间， 此外径范围的颗粒自然堆放时， 堆密度较小， 有利于气体的进出。 污 泥滤饼在笼体内的翻动可以是由笼内主轴带动的， 也可以是由笼体本身的 转动来带动的。 污泥滤饼在笼体内的翻动速度可以根据污泥滤饼含水率的 高低和产量的需要按如下规律来而调整： ①污泥滤饼的含水 越高， 翻动 速度越低； 污泥滤饼的含水率越低， 翻动速度越高。 原则是力求减小剪切 力对污泥滤饼内部本已形成的毛细通道的破坏， 使污泥颗粒保持相对松散 状态， 比表面积更大， 以利后续好氧风干工序的进行。 ②翻动速度越高， 污泥破碎分散装置的出料量越大； 翻动速度越低， 污泥滤饼破碎分散装置 的出料量越小。 优化的污泥滤饼破碎分散翻动速度为径向最外点的线速度 在 5mm/ s〜 100mm/s之间。
所述的干燥空气是这样产生的： 制冷剂在压缩机的作用下， 在冷交换 器中吸收热量， 在热交换器中放出热量； 常温空气由风机抽入， 首先在冷 交换器中被降温至冷凝水析出， 冷凝温度控制在 0°C〜15°C之间，然后在热 交换器中温度被提高到 0°C〜90°C之间，空气在这双重作用下不饱和度被提 高， 成为干燥空气。
所述的污泥好氧放热反应， 是指污泥中的好气细菌在存氧条件下把污 泥中的有机物分解为二氧化碳和水并放出热量的过程。 在本发明的污泥滤 饼破碎分散和干燥空气的作用下， 视污泥有机物含量的高低， 污泥好氧放 热量的范围可在 0〜20KJ. kg—1, h— 1之间。
污泥的好氧放热干燥过程， 对污泥中的病原体本身就是一种杀菌手段。 所述的对污泥颗粒进行物理或化学杀菌处理可根据污泥资源化利用的要求 而增加， 可以是紫外线杀菌， 可以是臭氧杀菌， 也可以是高氯、 高氧物质 杀菌或其它杀菌方式。
所述的尾气水洗， 水的来源可以优先适用从冷交换器中排出的冷凝水, 不足部分可以外加水源。
所述的利用螺旋机令物料相互挤压、 磨擦的功能使干燥后的污泥颗粒 在输送的过程中被进一步粉碎， 螺旋机可以是单独一条螺旋， 也可以是两 条或者两条以上的螺旋组。
一种污泥滤饼低温风干装置， 包括污泥滤饼预破碎机构、 污泥风干机 构和干燥风发生机构， 所述的污泥滤饼预破碎机构设置于污泥风干机构的 上部， 其上部设有进料口； 所述的污泥风千机构包括输送带和传动机构， 输送带的两端与传动机构连接， 输送带分层设置， 在最底层输送带的下方 设置有出料粉碎机构， 出料粉碎机构的末端设有出料口； 所述的干燥风发 生机构设置在污泥风干机构的上部， 干燥风发生机构通过风道与设置在污 泥风干机构内的出风口连接。
所述的输送带可以设置有 4层或者 4层以上。
在第一层输送带始端的设置有污泥厚度调节器。
在输送带的末端所对应的挂壁上设置有紫外线灯。
与现有技术相比， 本发明具有如下优点： 一是在干燥前先对污泥滤饼 进行破碎分散， 颗粒状的污泥具有较大的比表面积， 干燥时传热传质效率 较高， 干燥能耗较低； 二是破碎后的污泥颗粒在好氧放热的作用下， 不但 进一步降低了干燥能耗， 加快了干燥速率， 还起到了使污泥除臭的作用； 三是污泥颗粒在干燥的过程中， 运动状态缓和， 没有粉尘产生， 生产稳定、 安全； 四是污泥的低温干燥没有使污泥发生有机物热裂解反应， 使得干燥 尾气经过水洗后能达环保标准排放； 五是出料粉碎机构附带破碎功能， 出 料污泥颗粒松散， 便于资源化利用。
附图说明
图 1是本发明污泥滤饼好氧风干工艺流程图。
图 2是本发明污泥滤饼好氧风干装置结构示意图；
图 3是本发明污泥滤饼好氧风干装置的 A- A截面结构示意图； 图 4是本发明污泥滤饼好氧风干装置的 B-B截面结构示意图； 图 5是本发明污泥滤饼好氧风干装置的 C部局部放大图。
其中， 1为进料口； 2为污泥滤饼破碎分散机构； 3为引风机； 4为溢 流口； 5为尾气水洗装置； 6为热交换器； 7为风机； 8为冷交换器； 9为空 气进口； 10为冷凝水泵； 11为干燥风进口； 12为输送带； 13为污泥厚度 调节器； 14为挡泥板； 15为传动机构； 16为出料粉碎机构； 17为出料口； 18为干燥风通道； 19为紫外线灯； 20为网带； 21为连接长销。
具体实施方式
以下结合附图和具体实施例对本发明一种污泥滤饼好氧风干的方法及 装置进行详细的说明。
一种污泥滤饼低温风干方法， 如图 1所示， 其包括以下步骤：
( 1 )将污泥滤饼破碎分散成污泥颗粒层， 以增大污泥的比表面积。 所 述的污泥滤饼破碎分散是这样实现的： 含水率在 50%〜70%间的污泥滤饼 在多孔状或间隙状的笼体内翻动， 使污泥滤饼间产生相互碰撞和磨擦而被 破碎， 颗粒外径小于笼体孔径或间隙距离的污泥被排出笼体外， 从而实现 了污泥滤饼的破碎分散。 笼体孔径或间隙距离设定在 3mn！〜 30mm之间， 此 外径范围的颗粒自然堆放时， 堆密度较小， 有利于气体的进出。 污泥滤饼 在笼体内的翻动可以是由笼内主轴带动的， 也可以是由笼体本身的转动来 带动的。 污泥滤饼在笼体内的翻动速度可以根据污泥滤饼含水率的高低和 产量的需要按如下规律来而调整： ①污泥滤饼的含水率越高， 翻动速度越 低； 污泥滤饼的含水率越低， 翻动速度越高。 原则是力求减小剪切力对污 泥滤饼内部本已形成的毛细通道的破坏， 使污泥颗粒保持相对松散状态， 比表面积更大， 以利后续好氧风干工序的进行。 ②翻动速度越高， 污泥破 碎分散装置的出料量越大； 翻动速度越低， 污泥滤饼破碎分散装置的出料 量越小。 优化的污泥滤饼破碎分散翻动速度为径向最外点的线速度在 5mm/ s〜 100腿 / s之间。
( 2 )向缓慢运动或翻动着的污泥颗粒层内正压送入一定温度的干燥空 气， 让污泥产生好氧放热反应， 在外热与内热的共同作用下， 水分从污泥 颗粒中蒸发出来， 并向干燥空气作传质运动。 所述的污泥好氧放热反应， 是指污泥中的好气细菌在存氧条件下把污泥中的有机物分解为二氧化碳和 水并放出热量的过程。 在本发明的污泥滤饼破碎分散和干燥空气的作用下， - 视污泥有机物含量的高低， 污泥好氧放热量的范围可在 0〜20KJ. kg_ h— 1 之间。 所述的干燥空气是这样产生的： 制冷剂在压缩机的作用下， 在冷交 换器中吸收热量， 在热交换器中放出热量； 常温空气由风机抽入， 首先在 冷交换器中被降温至冷凝水析出， 冷凝温度控制在 0°C〜15°C之间，然后在 热交换器中温度被提高到 0°C〜90°C之间，空气在这双重作用下不饱和度被 提高， 成为干燥空气。 在冷交换器与热交换器之间设置有节流器， 节流器 可以是节流阀。 冷交换器产生的冷凝水被抽至水洗装置中。
(3)对缓慢运动或翻动着的污泥颗粒进行物理或化学杀菌处理。 虽然 污泥的好氧放热干燥过程， 对污泥中的病原体本身就是一种杀菌手段。 但 对污泥颗粒进行物理或化学杀菌处理可根据污泥资源化利用的要求而增 加， 可以是紫外线杀菌， 可以是臭氧杀菌， 也可以是高氯、 高氧物质杀菌 或其它杀菌方式。
(4)在污泥颗粒层外负压抽出携带了污泥水分的尾气，经水洗后排放。 所述的水洗水的来源可以优先使用从冷交换器中排出的冷凝水， 不足部分 可以外加水源。
(5 ) 对干燥后的污泥颗粒进一步粉碎至资源化利用的要求。 所述的进一步粉碎是利用螺旋机令物料相互挤压、 磨擦的功能使干燥 后的污泥颗粒在输送的过程中被进一步粉碎， 螺旋机可以是单独一条螺旋， 也可以是两条以上的螺旋组。 所述的资源化利用可以是制肥、 制砖、 燃料 利用、 填充料等
实施例 1
一种污泥滤饼好氧风干方法， 其包括以下步骤：
( 1 )将含水率为 70〜50%的污泥滤饼破碎成污泥颗粒后下落至输送带上 分散成污泥颗粒层， 污泥滤饼破碎可以通过相应的污泥滤饼破碎装置来实 现。
( 2 ) 向缓慢运动输送带上的污泥颗粒层内正压输入一定温度的干燥空 气； 所述干燥空气是常温空气在冷交换器内进行水分冷凝分离、 在热交换 器内升温后而成；干燥空气的温度可 ( 0〜90°C之间。干燥空气通过风道输 送至各层输送带的上下钢网之间的干燥空气进口中， 在穿越底层和表层污 泥颗粒时， 为污泥的好氧反应提供氧气， 同时吸收了污泥颗粒中的水分， 使污泥颗粒得到脱水干燥。 输送带分层以上设置， 首层输送带上设泥颗粒 层厚度调节器。 污泥颗粒在输送带上的厚度调节在 lOmn！〜 500mm之间； 输 送带运动的线速度为设定在 1 mm/S〜10mm/S之间。 污泥颗粒在输送带中的 全程停留时间为 5h〜50h。上层输送带上的污泥颗粒被输送至末端时自动翻 落至下层输送带上， 作反方向运动。
( 3 ) 对输送带上的污泥颗粒层进行物理或者化学杀菌。 优选的可以是 在污泥颗粒层在翻落的过程中被紫外线灯照射杀菌；
(4)在污泥颗粒层外负压抽出携带了污泥水分的尾气，经水洗后排放。 所述的水洗水的来源可以优先使用从冷交换器中排出的冷凝水， 不足部分 可以外加水源。
( 5 ) 最底层输送带上的污泥颗粒被输送到末端时， 下落至设置在最底 层输送带下部的螺旋机中进一步破碎。
一种污泥滤饼好氧风干装置， 如图 2、 图 3、 图 4和图 5所示， 包括污 泥滤饼破碎分散机构 2、污泥好氧风干机构、 出料粉碎机构、干燥风发生机 构、 尾气收集及水洗机构。
污泥滤饼破碎分散机构 2设置在污泥好氧风干机构的上部。 污泥滤饼 破碎机构 2上部设置有污泥滤饼进料口 1，污泥滤饼在污泥滤饼破碎分散机 构 2 内被破碎成为污泥颗粒后通过出料口下落至污泥风干机构内的首层输 送带 12上。 在污泥滤饼破碎分散机构 2的出料口下方， 首层输送带 12的 起始端部设置有挡泥板 14， 使出料口出来的污泥颗粒全部落入首层输送带 12上。 污泥滤饼破碎分散机构 2的结构可以是： 包括主轴、 笼体、 主轴电 机和外壳， 主轴电机通过连接器与主轴连接， 主轴上设置有若干破碎刀片， 主轴的外侧包覆有笼体； 笼体的外侧设置有外壳， 所述的笼体为多孔状或 平衡间隙状。 所述的主轴设置在轴承座上， 轴承座设置在主体支架上， 外 壳的中部位置设置有进料口， 笼体通过连接支架固定在主体支架上。 所述 的笼体上的孔径或孔隙宽度在 3mn！〜 30mm之间，且开孔率或孔隙率在 50 %〜 99%之间。 所述的外壳可以为能起集料作用的锥形壳体。 所述的主轴末端 的破碎刀片安装角度为反向推进方式， 使使污泥滤饼被反推至破碎笼体内， 保障污泥滤饼能被全部破碎并从笼体上的孔或间隙排出。 所述的破碎刀片 上安装有清扫笼体装置， 使笼体上的孔或孔隙保持畅通。 所述的破碎刀片 最外点的线速度为 5mm/s〜100mm/s之间。
污泥好氧风干机构包括输送带 12、 传动机构 15、 污泥厚度调节器 13 和紫外线灯 19。输送带 12的两端与传动机构 15连接，传动机构 15通过轴 轮和调速电机驱动输送带 12运转。 输送带 12的网带 20设置在链条上， 链 条通过连接长销连接。 在首层输送带 12的上部设置有污泥厚度调节器 13， 以控制污泥颗粒在输送带 12的厚度， 提高干燥效率， 优选的污泥颗粒的厚 度控制在 10匪〜 500腕。 输送带 12自上而下分层设置， 可以为四层或者四 层以上， 下层的输送带 12与上层的输送带 12的输送的运转方向相反。 输 送带 12可以是以钢网、 滤布、 塑料网等既能承物又能通风的物料制成。 在 一侧端部， 下层的输送带 12比上层的输送带 12长， 以使污泥被输送至输 送带 12的末端时， 上层的输送带 12的污泥自动翻落在下层反方向运动的 钢网输送带 12上。 在污泥翻落过程中， 污泥被紫外线灯 19照射杀菌。 紫 外线灯 19设置在每层输送带末端所对应的挂壁上。在污泥风干机构的底部 设置有出料粉碎机构 16, 出料粉碎机构 16的末端设置有出料口 17, 最底 层输送带 12上的干燥污泥反转掉下来落在出料粉碎机构 16上， 边输送边 破碎， 最后从出料口 17中排出。 出料粉碎机构 16可以为对滚螺旋输送机， 其包括最少一条螺旋粉碎输送杆。优选的出料粉碎机构 16内设置有 2条螺 旋粉碎输送杆。
干燥空气发生机构设置在污泥好氧风干机构的上部。 干燥空气发生机 构包括冷交换器、 压缩机、 风机和热交换器。 风机 7设置在冷交换器 8与 热交换器 6之间。 冷交换器 8与空气入口 9连接， 在冷交换器 8中凝结的 冷凝水通过冷凝水分离器分离并收集， 然后被冷凝水泵 10输送至尾气水洗 装置 5内。 干燥空气通过风道 18导入至输送带 12内的干燥空气出口 11， 对输送带 12上的污泥颗粒进行干燥。干燥风出口 11可以向下和向上鼓风。
在污泥好氧风干机构的上部设置有尾气收集及水洗机构，包括引风机 3 和尾气水洗装置 5;在污泥滤饼破碎分散机构 2通过风道与引风机 3的进风 口连接， 引风机 3的出口通过风道和尾气水洗装置 5连接。 干燥尾气借道 污泥滤饼破碎分散机构 2被输送至排尾气水洗装置 5中。 水洗后的尾气在 尾气水洗装置 5上部的排风管排出， 水洗后的污水从尾气水洗装置 5中部 的溢流口 4排出。
含水率在 70%〜50%的污泥滤饼从进料口 1进入污泥滤饼破碎分散装 置 2， 破碎后的污泥颗粒下落至钢网输送带 12 上， 输送带的线速度为 lram/s〜10mm/s之间可调。 钢网输送带上的污泥经过污泥厚度调节器 13， 可将污泥厚度控制在 lOmn！〜 500mm之间。 当污泥被输送至输送带 12的末端 时， 污泥自动翻落在下一层反方向运动的钢网输送带上， 污泥翻动过程中 同时被紫外线灯 19进行照射杀菌， 如此往复。 污泥下落在置于装置下部的 出料粉碎机构 16上， 边输送边破碎， 最后从出料粉碎机构 16末端的出料 口 17中被排出。 通过调节输送带速， 污泥在装置内的停留时间从 5h〜50h 可调， 出料含水率在 50%〜5%之间可调。
常温空气从空气入口 9进入干燥空气发生机构的冷交换器 8，空气中的 水分被冷凝析出后， 经风机 7鼓入热交换器 6进行加热提温， 形成不饱和 的干燥空气， 干燥空气的温度可以 0至 90°C可调。 冷凝水从冷交换器 8中 的冷凝水分离器排出， 然后经过冷凝水泵 10输送至尾气水洗装置 5中， 作 为水洗原水利用。 干燥空气通过风道 18分别输送至各输送带 12上下钢网 之间的干燥风出口 11中，向上下层钢网上的污泥颗粒提供干燥和好氧气源。 每条输送带 12上有若干个干燥空气进口 11。干燥空气与污泥颗粒中水分进 行传热传质， 使污泥颗粒得到了脱水干燥。 干燥尾气由引风机 3通过污泥 滤饼破碎分散装置 2收集， 鼓入尾气水洗装置 5中， 以鼓泡方式进行尾气 水洗后排放， 水洗后污水从溢流口 4排进污水管道。
实施例 2
含水率 70%的污泥滤饼从进料口进入污泥滤饼破碎分散装置 2， 破碎 后的污泥颗粒下落至污泥好氧风干机构的输送带 12上， 输送带 12的线速 度为 1. 5mm/s， 输送带 12上的污泥厚度约为50111111。 当污泥被输送至输送带 12的末端时，污泥自动翻落在下一层反方向运动的输送带 12上，污泥翻动 过程中同时被紫外线灯 19进行照射杀菌， 如此往复。 干燥空气温度为 62 °C，通过风道分别输送至各钢网输送带上下钢网之间的干燥空气进口 11中， 向上下层网带上的污泥颗粒提供干燥风。 干燥后的污泥下落在置于装置下 部的出料粉碎机构 16上， 边输送边破碎， 最后从出料粉碎机构 16的末端 的出料口 17中被排出， 出料含水率在 38%。污泥在污泥滤饼好氧风干装置 内的停留时间 35h。 干燥污泥打包后于仓库内放置 3天， 含水率下降为 35 实施例 3
含水率 62 %的污泥滤饼从进料口 1进入污泥滤饼破碎分散装置 2， 破 碎后的污泥颗粒下落至污泥好氧风干机构的输送带 12上， 输送带 12的线 速度为 3mm/s， 输送带 12上的污泥厚度约为 80画。 当污泥被输送至输送带 12的末端时，污泥自动翻落在下一层反方向运动的输送带 12上，污泥翻动 过程中同时被紫外线灯 19进行照射杀菌， 如此往复。 干燥空气温度为 55 °C， 通过风道分别输送至各输送带 12上下网带之间的干燥风出口 11中， 向上下层网带上的污泥颗粒提供干燥空气。 干燥后的污泥下落在置于污泥 好氧风干机构下部的出料粉碎机构 16上， 边输送边破碎， 最后从出料粉碎 机构 16的末端的出料口 17中被排出， 出料含水率 33%。 污泥在污泥滤饼 好氧风干装置内的停留时间 28h。
实施例 4
含水率 54%的污泥滤饼从进料口 1进入污泥滤饼破碎分散机构 2， 破 碎后的污泥颗粒下落至污泥好氧风干机构的输送带 12上， 输送带 12的线 速度为 5mm/s， 输送带 12上的污泥厚度约为 110mm。 当污泥被输送至输送 带 12的末端时， 污泥自动翻落在下一层反方向运动的输送带 12上， 污泥 翻动过程中同时被紫外线灯 19进行照射杀菌， 如此往复。干燥空气温度为 52°C， 通过风道 18分别输送至各输送带 12上下网带之间的干燥空气进口 11 中， 向上下层网带上的污泥颗粒提供干燥空气。 干燥后的污泥下落在置 于污泥好氧风干机构下部的出料粉碎机构 16上， 边输送边破碎， 最后从出 料粉碎机构 16的末端的出料口中被排出， 出料含水率在 31 %。污泥在污泥 滤饼好氧风干装置内的停留时间 22h。

Claims

权 利 要 求 书
1、 一种污泥滤饼好氧风干方法， 其特征在于， 包括以下步骤-
( 1 ) 将污泥滤饼破碎分散成污泥颗粒层；
(2 ) 向缓慢运动或翻动着的污泥颗粒层内正压送入干燥空气， 让污泥 产生好氧放热反应， 在外热与内热的共同作用下， 水分从污泥颗粒中蒸发出 来， 并向干燥空气作传质运动；
(3 ) 对缓慢运动或翻动着的污泥颗粒进行物理或化学杀菌处理；
(4) 在污泥颗粒层外负压抽出携带了污泥水分的尾气， 水洗后排放；
(5) 对干燥后的污泥颗粒进一步粉碎至资源化利用的要求。
,
2、 如权利要求 1所述的一种污泥滤饼好氧风干方法， 其特征在于， 所 述的污泥滤饼破碎分散是这样实现的: 含水率在 50%〜70%间的污泥滤饼 在多孔状或间隙状的笼体内翻动， 使污泥滤饼间产生相互碰撞和磨擦而被 破碎， 颗粒外径小于笼体孔径或间隙距离的污泥被破碎排出笼体外； 笼体 孔径或间隙距离设定在 3mn！〜 30mm之间。
3、 如权利要求 2所述的一种污泥滤饼好氧风干方法， 其特征在于， 所 述的笼体翻动的径向最外点的线速度在 5mm/s〜100mm/S之间。
4、 如权利要求 1所述的一种污泥滤饼好氧风干方法， 其特征在于， 所 述的干燥空气是这样产生的： 制冷剂在压缩机的作用下， 在冷交换器中吸 收热量， 在热交换器中放出热量； 常温空气由风机抽入， 首先在冷交换器 中被降温至冷凝水析出，冷凝温度控制在 0°C〜15°C之间，然后在热交换器 中温度被提高到 0°C〜90°C之间， 形成不饱和干燥空气。
5、 如权利要求 1所述的一种污泥滤饼好氧风干方法， 其特征在于： 所 述的 （3 ) 步骤中， 对污泥颗粒进行物理杀菌处理为紫外线杀菌， 化学杀菌 是臭氧杀菌、 高氯或者高氧物质杀菌。
6、 如权利要求 1所述的一种污泥滤饼好氧风干方法， 其特征在于： 所 述的 （4) 步骤中的水洗水来源是从冷交换器中排出的冷凝水。
7、 如权利要求 1所述的一种污泥滤饼好氧风干方法， 其特征在于: 所 述的 （5 ) 步骤中 进一步粉碎是利用螺旋机令物料相互挤压、 磨擦的功能 使干燥后的污泥颗粒在输送的过程中被进一步粉碎， 螺旋机是单独一条螺 旋， 或者是两条以上的螺旋组。
8、 一种污泥滤饼低温风干装置， 其特征在于： 包括污泥滤饼预破碎机 构、 污泥风干机构和干燥风发生机构， 所述的污泥滤饼预破碎 ft构设置于 污泥风干机构的上部， 其上部设有进料口； 所述的污泥风干机构包括输送 带和传动机构， 输送带的两端与传动机构连接， 输送带分层设置， 在最底 层输送带的下方设置有出料粉碎机构， 出料粉碎机构的末端设有出料口； 所述的干燥风发生机构设置在污泥风干机构的上部， 干燥风发生机构通过 风道与设置在污泥风干机构内的出风口连接。
9、 如权利要求 8所述的一种污泥滤饼好氧风干装置， 其特征在于： 所 述的输送带可以设置有 4层或者 4层以上； 在输送带的末端所对应的挂壁 上设置有紫外线灯。 '
10、 如权利要求 8所述的一种污泥滤饼好氧风干装置， 其特征在于： 在第一层输送带始端的设置有污泥厚度调节器。
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