WO2011035460A1 - 一种污水污泥浓缩脱水好氧风干一体化的方法 - Google Patents

一种污水污泥浓缩脱水好氧风干一体化的方法 Download PDF

Info

Publication number
WO2011035460A1
WO2011035460A1 PCT/CN2009/001280 CN2009001280W WO2011035460A1 WO 2011035460 A1 WO2011035460 A1 WO 2011035460A1 CN 2009001280 W CN2009001280 W CN 2009001280W WO 2011035460 A1 WO2011035460 A1 WO 2011035460A1
Authority
WO
WIPO (PCT)
Prior art keywords
sludge
sewage
aerobic
drying
particles
Prior art date
Application number
PCT/CN2009/001280
Other languages
English (en)
French (fr)
Inventor
钟环声
吴学伟
吴嘉聪
孙志明
杨海英
Original Assignee
广州普得环保设备有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 广州普得环保设备有限公司 filed Critical 广州普得环保设备有限公司
Priority to US13/498,495 priority Critical patent/US8808419B2/en
Priority to KR1020127010541A priority patent/KR101467204B1/ko
Priority to JP2012530071A priority patent/JP5526344B2/ja
Priority to EP09849648.2A priority patent/EP2484641A4/en
Publication of WO2011035460A1 publication Critical patent/WO2011035460A1/zh

Links

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
    • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
    • C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
    • 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
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
    • A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
    • A61L2/02—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor using physical phenomena
    • A61L2/08—Radiation
    • A61L2/10—Ultraviolet radiation
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
    • A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
    • A61L2/16—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor using chemical substances
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • 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
    • 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
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • 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
    • 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
    • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
    • C02F11/143—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • 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
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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 field of sewage sludge treatment methods, and specifically relates to a method for integrating concentrated dewatering and aerobic air drying to treat excess sludge.
  • the sewage sludge treatment method commonly used in China first injects excess sludge with a water content of 99% or more into a gravity concentration tank, and after 12 to 24 hours, the supernatant liquid is discharged, and the excess sludge can be concentrated to a water content of about 97%;
  • the concentrated sludge is chemically tempered by cationic polyacrylamide, and the tempered sludge is injected into a centrifugal dewatering machine, a belt dewatering machine or a plate and frame filter press, and the sludge can be dehydrated to a moisture content of 80 after discharging the filtrate.
  • the dehydrated sludge is first pre-dispersed into granules or noodles, and then dried in a drying device for drying.
  • the dried sludge has a moisture content of about 40 ⁇ 30% ; the dried sludge can be directly Landfill disposal can also be carried out by incineration. It can also be used for resource utilization such as cement, brick making, garden fertilizer production, and low calorific value fuel.
  • the currently used sludge treatment methods have the following problems: (1) The sludge concentration efficiency is low, and the gravity concentration time is as long as 12 hours or more, resulting in a large volume of the sludge concentration tank, and the sludge is prone to spoilage and odor during the concentration process; (2) The sludge dewatering efficiency is low, the sludge moisture content is high after dewatering, the sludge volume is huge, and the water in the sludge to be evaporated in the subsequent heat treatment process is more, which leads to extremely high investment and operation cost of the heat treatment equipment; 3) Dewatered sludge with a water content of 80 to 75% is a semi-solid with high viscosity, which is difficult to disperse during the drying process, and heat transfer of sludge in the viscose phase of the sludge (water content: 60 to 40%) The mass transfer efficiency is low, the sludge drying energy consumption is high, and the sludge particles are prone to the "s
  • the object of the present invention is to solve the above problems and provide a sludge concentrated dehydration aerobic air-drying system with high sewage concentration and dewatering efficiency, low drying energy consumption, less tail gas pollution, low equipment investment and running cost, and high safety performance.
  • the method is suitable for treating the excess sludge generated in the sewage treatment plant.
  • the technical scheme of the invention is realized as follows: a sewage sludge concentration dehydration aerobic wind thousand integration
  • the method includes the following steps:
  • Organic agent quenching and tempering adding an organic tempering agent to the excess sludge having a water content of 98% to 99.8%, and stirring for 10 to 180 seconds to improve the sedimentation performance of the excess sludge;
  • Inorganic agent quenching and tempering First, add Fe 3+ soluble compound to the remaining sludge after concentration, stir for 10 to 180 seconds to carry out mixing reaction, and then add lime particles to the sludge.
  • crushing and dispersing crushing and dispersing the sludge cake into sludge particles to increase the specific surface area of the sludge during drying and improving the drying efficiency;
  • Aerobic air drying input dry air below 90 °C between the static, moving or turning sludge particles, so that the sludge produces aerobic exothermic reaction. Under the combined action of external heat and internal heat, sludge particles The water in the water is evaporated to make the sludge moisture content below 38%.
  • the sludge particles are physically or chemically sterilized; the physical or chemical sterilization treatment may be increased according to the requirements of sludge resource utilization, and the physical sterilization treatment may be ultraviolet sterilization, chemical
  • the sterilization treatment may be ozone sterilization, high chlorine or high oxygen substance sterilization; the sterilization method may also be other sterilization methods.
  • the tail gas generated by aerobic air drying is discharged after being washed with water.
  • the washing water may be neutral pure water washing, alkaline washing to remove the spoiled acid gas generated by aerobic fermentation, pickling to remove possible ammonia gas, and the source of the washing water may be preferentially discharged from the cold exchanger. Condensed water, the insufficient part can be added to the water source.
  • the dried sludge particles are further pulverized to the requirements for resource utilization.
  • the further pulverizing of the sludge particles is to use a screw machine to squeeze the materials against each other and rub
  • the crushing machine may be a single spiral or two or more spiral groups.
  • the excess sludge in the step (1) is produced in a sewage treatment plant during the production process, which is 98% to 99.8%; the organic tempering agent added may be a cationic polypropylene having a molecular weight of 800 to 1500.
  • Amide when added, the concentration is 0.05 ⁇ 0.5% polyacrylamide solution, and the polyacrylamide powder is added. The amount is 0.05 ⁇ 0.5% of the dry weight of the sludge; the polyacrylamide has the function of electrostatic neutralization and adsorption bridging, which is beneficial to improve the sedimentation performance of the sludge, achieve the effect of rapid concentration and increase concentration efficiency.
  • the preferred concentration of dry powder for polyacrylamide is 0.15%.
  • the gravity in the step (2) is concentrated to the natural precipitation of the sludge, and the gravity concentration time is 30 to 150 minutes; the gravity concentration can simultaneously remove the interstitial water and the surface adsorbed water in the sludge, and the gravity concentrated sludge
  • the water content is 86 to 95%.
  • the Fe 3+ soluble compound is preferably a ferric chloride solution, the concentration of the ferric chloride solution is greater than or equal to 35%, and the dosage of the ferric chloride solution is 0.3 to the dry weight of the sludge.
  • the ferric chloride solution is preferably added in an amount of 5%; the effective calcium oxide content in the lime particles is not less than 60%, and the dosage of the lime particles is 3 to 150% of the dry mass of the sludge ;
  • the ferric chloride solution and the lime particles have the functions of electrostatic neutralization, net-sweeping, providing skeleton, improving sludge compressibility and hydrophobicity, releasing part of cell water, etc., and are beneficial to improving sludge dewatering efficiency and obtaining moisture content. Lower dewatered sludge.
  • the lime particles should have a particle size greater than or equal to 60 mesh.
  • the pressure of the sludge pressurized conveying in the step (4) is 0.5 to 2.5 MPa, and the plate and frame filter press
  • the dewatering can simultaneously remove the capillary-bound water and part of the cell water in the sludge, and the dewatered sludge cake has a water content of 41 to 69%.
  • the sludge filter cake crushing in the step (5) may be implemented in a sludge cake crushing device, and the sludge cake crushing device comprises a spindle, a cage, a spindle motor and a casing, and the spindle motor passes The connector is connected with the main shaft.
  • the main shaft is provided with a plurality of crushing blades, and the outer side of the main shaft is covered with a cage body; the outer side of the cage body is provided with a casing, and the cage body is porous; the sludge filter cake is porous in the sludge filter cake breaking device In the shape of the cage, the sludge filter cake is broken and collided with each other, and the sludge particles smaller than the size of the cage hole are discharged outside the cage, thereby realizing the crushing and dispersing of the sludge filter cake.
  • the size of the cage hole is 3mn! ⁇ 30mm, when the particles are naturally stacked, the bulk density is small, which is favorable for gas in and out.
  • the flipping of the sludge filter cake in the cage may be that the cage is stationary by the inner spindle of the cage and the blades disposed on the main shaft, or may be driven 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 smaller the tumbling speed; The lower the moisture content of the cake, the higher the turning speed. Strive to reduce the shear force on the capillary channel formed inside the sludge filter cake, so that the sludge particles remain relatively loose, the specific surface area is larger, in order to facilitate the subsequent aerobic air drying process. 2 The greater the turning speed, the larger the discharge amount of the sludge crushing and dispersing device; the smaller the turning speed, the smaller the discharge amount of the sludge filter cake crushing and dispersing device.
  • the preferred sludge cake crushing and dispersing speed is the linear outermost point linear velocity between 5 mra/s and 100 mm/s. Power range of spindle motor: 0 ⁇ 20KW.
  • the dry air in the step (6) is generated by the refrigerant being absorbed by the compressor in the cold exchanger and releasing heat in the heat exchanger; the ambient air is drawn by the fan, first in the The cold exchanger is cooled to condensate, and the condensation temperature is controlled between 0 ° C and L 5 ° C, and then the temperature is raised to between 0 ° C and 90 ° C in the heat exchanger to form unsaturated drying. air.
  • the beneficial effects of the invention are as follows: (1) by adjusting the residual sludge organically, the sedimentation performance of the excess sludge is improved, the sludge concentration efficiency is improved, the concentration time is shortened, and the volume of the concentration tank is reduced; (2) The concentrated sludge is subjected to inorganic quenching and tempering to improve the compressibility and hydrophobicity of the sludge, and release part of the cell water in the sludge.
  • the dewatering efficiency of the sludge can be improved by the pressure filtration dehydration of the high pressure plate frame.
  • 1 is a process flow diagram of a method for integrating sewage dewatering, aerobic and air drying in sewage sludge according to the present invention.
  • 2 is a schematic structural view of a sludge filter cake aerobic air drying device of the present invention;
  • Figure 3 is a schematic cross-sectional view showing the A-A cross section of the sludge filter cake aerobic air drying device of the present invention
  • Figure 4 is a schematic cross-sectional view showing the B-B cross section of the sludge filter cake aerobic air drying device of the present invention
  • Fig. 5 is a partially enlarged view showing a portion C of the sludge cake of the present invention.
  • a method for integrating sewage sludge dewatering and aerobic air drying comprises the following steps:
  • Organic agent quenching and tempering adding an organic tempering agent to the excess sludge having a water content of 98% to 99.8%, and stirring for 10 to 180 seconds to improve the sedimentation performance of the excess sludge; 8% ⁇ The sludge produced by the sewage treatment plant in the production process, which is 98% ⁇ 99. 8%.
  • the organic tempering agent added may be a cationic polyacrylamide (PAM) having a molecular weight of 800 to 1500, and a polyacrylamide solution having a concentration of 0.05 to 0.5% is added during the addition, and the dry powder dosage of the polyacrylamide is sludge.
  • the dry basis mass is 0.05 ⁇ 0.5%.
  • the preferred concentration of the acrylamide solution is 0.1 to 0.2%, and the preferred concentration of the dry powder of the polyacrylamide is 0.15%.
  • Polyacrylamide has the function of electrostatic neutralization and adsorption bridging, which is beneficial to improve the sedimentation performance of sludge, achieve the effect of rapid concentration and increase concentration efficiency.
  • the solution containing the Fe 3+ soluble compound is preferably a ferric chloride solution, the concentration of the ferric chloride solution is greater than or equal to 35%, and the dosage of the ferric chloride solution is 0.3 to 10% of the mass of the sludge dry basis.
  • the ferric chloride solution is preferably added in an amount of 5%.
  • the effective calcium oxide content in the lime particles is not less than 60%, and the dosage of the lime particles is 3 to 150% of the dry weight of the sludge; the ferric chloride solution and the lime particles have electrostatic neutralization, net trapping, and providing The skeleton, improving the compressibility and hydrophobicity of the sludge, releasing part of the cell water, etc., are beneficial to improving the dewatering efficiency of the sludge and obtaining dewatered sludge having a low water content.
  • the lime particles should have a particle size greater than or equal to 60 mesh.
  • the sludge cake crushing can be realized in a sludge cake crushing device, the sludge cake crushing device, comprising a spindle, a cage, a spindle motor and a casing, and the spindle motor is connected to the spindle through a connector, on the spindle There are several crushing blades, and the outer side of the main shaft is covered with a cage.
  • the outer side of the cage is provided with an outer casing, and the cage is porous; the sludge filter cake is turned in a porous cage of the sludge cake crushing device, causing the sludge filter cake to collide and rub against each other and be broken. Sludge particles smaller than the size of the cage pores are discharged outside the cage, thereby achieving crushing and dispersing of the sludge filter cake.
  • the speed of the sludge filter cake in the cage is the linear speed of the outermost point of the cage body between 5mm / S ⁇ 100mm / s, the power range of the spindle motor: 0 ⁇ 20KW.
  • the size of the cage hole is 3mn! ⁇ 30mm, when the particles are naturally stacked, the bulk density is small, which is conducive to gas in and out.
  • the flipping of the sludge filter cake in the cage can be a cage that is stationary by the cage spindle and is placed in the main Driven by the blades of the shaft, it can also be driven 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 smaller the tumbling speed; The lower the moisture content of the cake, the higher the turning speed. Strive to reduce the damage of shearing force on the existing capillary channel 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. 2 The greater the turning speed, the larger the discharge amount of the sludge crushing and dispersing device; the smaller the turning speed, the smaller the discharge amount of the sludge filter cake crushing and dispersing device.
  • Aerobic air drying input dry air to the static, moving or turning sludge particles, so that the sludge produces an aerobic exothermic reaction. Under the combined action of external heat and internal heat, the water in the sludge particles is evaporated. come out.
  • 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 normal temperature air is drawn by the fan, and is first cooled in the cold exchanger to The condensed water is precipitated, the condensation temperature is controlled between 0 ⁇ 1515 ⁇ , and then the temperature in the heat exchanger is raised to 0° (: ⁇ 90°C to form unsaturated dry air.
  • the sludge particle translation speed 0 ⁇
  • the sludge particles are physically or chemically sterilized; the physical or chemical sterilization treatment may be increased according to the requirements of sludge resource utilization, and the physical sterilization treatment may be ultraviolet sterilization, chemical sterilization.
  • the treatment may be ozone sterilization, high chlorine or high oxygen substance sterilization; the sterilization method may also be other sterilization methods.
  • the tail gas generated by aerobic air drying is discharged after being washed with water.
  • the step water washing may be a neutral pure water washing, caustic washing to remove the spoiled acid gas generated by aerobic fermentation, and pickling to remove the ammonia gas which may be generated.
  • the source of the washing water can preferentially use the condensed water discharged from the cold exchanger, and the insufficient portion can be added with the water source. Place
  • the dried sludge particles are further pulverized to the requirements for resource utilization.
  • the resource utilization may be fertilizer production, brick making, fuel utilization, fillers, and the like.
  • the further pulverizing of the sludge particles is performed by using a screw machine to squeeze the materials against each other and rubbing; the screw machine may be a single spiral or two or more spiral groups. Screw conveyor speed range: 0 ⁇ 10 kg / sec, power range: 0 ⁇ ; 10KW.
  • the steps (5) and (6) are carried out by a sludge filter cake aerobic air drying device.
  • the cake crushing and dispersing mechanism 2 the sludge aerobic air drying mechanism, the discharging crushing mechanism, the drying wind generating mechanism, the exhaust gas collecting 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.
  • 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 an outer casing, and the cage is porous; the sludge filter cake is turned in a porous cage of the sludge cake crushing device, causing the sludge filter cake to collide with each other and be broken, less than The sludge particles of the size of the cage holes are discharged outside the cage, thereby achieving the crushing and dispersing of the sludge filter cake.
  • the sludge aerobic drying mechanism includes a conveyor belt 12, a transmission mechanism 15, a sludge thickness regulator 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, thereby improving the drying efficiency, and the thickness of the preferred sludge particles is controlled at lOirai! ⁇ 500mm.
  • 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 a steel mesh,
  • Filter cloth, plastic net, etc. can be made of materials that can be 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 process of sludge falling down, the sludge is irradiated with ultraviolet light 19 to sterilize'. Ultraviolet lamps 19 are placed on the corresponding wall at 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 conveyor comprising at least one spiral comminution conveying rod.
  • a preferred pulverizing conveying rod 16 is provided in the preferred 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 device 5 by the condensate pump 10.
  • the dry air is introduced into the dry air outlet 11 in the conveyor belt 12 through the air duct 18 to dry the sludge particles on the conveyor belt 12.
  • the dry air outlet 11 can blow up and down.
  • An exhaust gas collection and washing mechanism is arranged on the upper part of the sludge aerobic drying mechanism, including an induced draft fan 3 and The exhaust gas washing device 5; the sludge filter crushing and dispersing mechanism 2 is connected to the air inlet of the draft fan 3 through the air passage, and the outlet of the draft fan 3 is connected to the exhaust gas washing device 5 through the air passage.
  • the dry tail gas is transported to the exhaust gas washing device 5 by the sludge filter crushing and dispersing mechanism 2.
  • 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 1 mm. / S ⁇ 10mm / S adjustable between.
  • the sludge on the stencil conveyor belt passes through the sludge thickness regulator 13, which can control the sludge thickness to lOmn! ⁇ 500mm between.
  • 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 stencils of the respective conveyor belts 12, and the sludge particles on the upper and lower steel slabs provide a dry and good oxygen source.
  • Each conveyor belt 12 has a plurality of dry air inlets 11 thereon.
  • the dry air and the moisture in the sludge particles undergo heat and mass transfer, so that the sludge particles are dehydrated and dried.
  • the dry exhaust gas is collected by the induced draft fan 3 through the sludge filter crusher and dispersing device 2, and is blown into the exhaust 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 excess sludge with a moisture content of 99.8% is sent to the organic quenching and agitating tank, and the concentration of 0.1% of the cation 12 million molecular weight polyacrylamide solution and the dosage of the polyacrylamide dry powder are added to the sludge. 2%, the organically tempered sludge is transported to a gravity concentration tank. After centrifuging for 120 minutes, the separated supernatant was discharged, and the concentrated sludge had a water content of 95%, and the concentrated sludge was sent to a dehydration step.
  • the concentrated sludge is transported to the inorganic quenching and stirring tank, and a ferric chloride solution having a concentration of 38% is firstly added to the sludge and stirred for 10 seconds, and the dosage of the ferric chloride is sludge dried. 2.3% of the base mass; then add lime particles to the sludge and stir for 60 seconds, wherein the effective calcium oxide content is 70%, and the calcium oxide dosage is 12% of the sludge dry basis mass;
  • the quenched and tempered sludge is sent to the plate and frame filter through the screw pump In the machine, the injection pressure of the screw pump is IMPa; after the filtrate is discharged, the moisture content of the filter cake is 61%.
  • the sludge filter cake is broken into sludge particles and then dropped onto a conveyor belt to be dispersed into a sludge particle layer.
  • the sludge cake crushing can be achieved by a corresponding sludge cake crushing device.
  • the dry air having a temperature of 85 Torr is input to the sludge particle layer on the slow moving conveyor belt; 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. Dry air is transported through the air duct to the dry air inlet between the upper and lower stencils of the conveyor belts of each layer. When passing through the bottom layer and surface sludge particles, it provides oxygen for the aerobic reaction of the sludge and absorbs the sludge particles.
  • the moisture makes the sludge particles dehydrated and dried.
  • the conveyor belt is arranged above the layer, and the first layer conveyor belt is provided with a mud particle layer thickness adjuster.
  • the thickness of the sludge particles on the conveyor belt was adjusted to 200 mm; the linear speed of the conveyor belt movement was 2 mm/s.
  • the total residence time of the sludge particles in the conveyor belt is 20h.
  • the source of the washing water preferentially uses the condensed water discharged from the cold exchanger, and the insufficient water source is added.
  • the sludge particles on the bottommost conveyor belt are transported to the end, they are further broken by falling into a screw machine disposed at the lowermost conveyor belt, and the moisture content of the finished sludge particles is 36%.
  • the excess sludge with a water content of 99.5% is sent to the organic quenching and agitating tank, and a concentration of 0.1% of the cation 15 million molecular weight polyacrylamide solution is added to the sludge, and the dosage of the polyacrylamide is
  • the sludge dry basis mass is 0.15%, and the organically tempered sludge is transported to a gravity concentration tank. After concentration by gravity for 2 hours, the separated supernatant was discharged, and the concentrated sludge had a water content of 93%, and the concentrated sludge was sent to a dehydration step.
  • the concentrated sludge is sent to the inorganic quenching and stirring tank, and a ferric chloride solution having a concentration of 38% is firstly added to the sludge and stirred for 2 minutes.
  • the dosage of ferric chloride is sludge dry. 5.5% of the base mass; then add lime particles to the sludge and stir for 12 minutes, wherein the calcium oxide content is 72%, and the calcium oxide dosage is 12% of the sludge dry basis mass;
  • the sludge after the quality is transported to the plate and frame filter press by the screw pump.
  • the injection pressure of the screw pump is IMPa; after the filtrate is discharged, the moisture content of the filter cake is 58%.
  • the sludge filter cake is broken into sludge particles and then dropped onto a conveyor belt to be dispersed into a sludge particle layer.
  • the sludge cake crushing can be achieved by a corresponding sludge cake crushing device.
  • the dry air of the temperature of 60 ° C is input into the sludge granule layer on the slow moving conveyor belt; 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. . Dry air is transported through the air duct to the dry air inlet between the upper and lower stencils of the conveyor belts of each layer.
  • the conveyor belt When passing through the bottom layer and surface sludge particles, it provides oxygen for the aerobic reaction of the sludge and absorbs the sludge particles. The moisture makes the sludge particles dehydrated and dried.
  • the conveyor belt is arranged above the layer, and the first layer conveyor belt is provided with a mud particle layer thickness adjuster. 5 ⁇ / ⁇ The line speed of the conveyor belt is adjusted to 2. 5mm / s. The total residence time of the sludge particles in the conveyor belt was 18 h. When the sludge particles on the upper conveyor belt are transported to the end, they are automatically turned down to the lower conveyor belt and moved in the opposite direction. Physical or chemical sterilization of the sludge granule layer on the conveyor belt.
  • the exhaust gas carrying the sludge moisture is extracted by the negative pressure outside the sludge particle layer, and is discharged after washing with water.
  • the source of the washing water preferentially uses the condensed water discharged from the cold exchanger, and the insufficient water source is added.
  • the excess sludge of the moisture content of 99.3% is sent to the organic quenching and agitating tank, and the concentration of 0.1% of the cation of 12 million molecular weight polyacrylamide solution is added to the sludge, and the dosage of the polyacrylamide is 1% of the dry mass of the sludge is transported to the gravity concentration tank. After gravity concentration for 1 hour, the separated supernatant was discharged, and the concentrated sludge had a water content of 93%, and the concentrated sludge was sent to a dehydration step.
  • the concentrated sludge is transported to the inorganic quenching and boring tank, and a ferric chloride solution having a concentration of 38% is firstly added to the sludge and stirred for 1 minute, and the dosage of the ferric chloride is sludge. 5% ⁇ The 5% of the dry mass of the sludge is added to the sludge and the mixture is stirred for 15 minutes, wherein the effective calcium oxide content is 75%, the dosage of calcium oxide is 15.5% of the dry weight of the sludge. Then, the quenched and tempered sludge is sent to the plate and frame filter press through a screw pump, and the injection pressure of the screw pump is IMPa; after the filtrate is discharged, the moisture content of the filter cake is 53%.
  • the sludge filter cake is broken into sludge particles and then dropped onto a conveyor belt to be dispersed into a sludge particle layer.
  • the sludge cake crushing can be achieved by a corresponding sludge cake crushing device.
  • the dry air of the temperature of 48 ° C is input into the sludge particle layer on the slow moving conveyor belt; the dry air is formed by condensing and separating the air at room temperature in the cold exchanger and heating the temperature in the heat exchanger. . Dry air is transported through the air duct to the dry air inlet between the upper and lower stencils of the conveyor belts of each layer. When passing through the bottom layer and surface sludge particles, it provides oxygen for the aerobic reaction of the sludge and absorbs the sludge particles.
  • the moisture makes the sludge particles dehydrated and dried.
  • the conveyor belt is arranged above the layer, and the first layer conveyor belt is provided with a mud particle layer thickness adjuster. 5 ⁇ / ⁇ The thickness of the conveyor belt is adjusted to a thickness of 1. 5mm / S.
  • the total residence time of the sludge particles in the conveyor belt was 25 h.
  • the source of the washing water preferentially uses the condensed water discharged from the cold exchanger, and the insufficient water source is added.
  • the sludge particles on the bottommost conveyor belt are transported to the end, they fall to the bottom layer. Further broken in the screw machine with the lower part, the moisture content of the finished sludge particles was 33%.
  • the excess sludge having a water content of 99% is sent to the organic quenching and agitating tank, and a concentration of 0.1% of the cation 10 million molecular weight polyacrylamide solution is added to the sludge, and the dosage of the polyacrylamide is sludge. 0. 08% of the dry basis mass, and then the organically tempered sludge is transported to a gravity concentration tank. Concentration by gravity 1. After 5 hours, the separated supernatant was discharged, and the concentrated sludge had a water content of 90%, and the concentrated sludge was sent to a dewatering process.
  • the concentrated sludge is sent to the inorganic quenching and boring tank, and a concentration of 38.8% of ferric chloride solution is added to the sludge and stirred for 30 seconds.
  • the dosage of ferric chloride is
  • the granules of the dry mass of the sludge is 8.4.
  • the granules are added to the sludge and the mixture is stirred for 10 minutes.
  • the calcium oxide content is 70%. %;
  • the tempered sludge is then sent to the plate and frame filter press through a screw pump, and the injection pressure of the screw pump is IMPa; after the filtrate is discharged, the moisture content of the filter cake is 51%.
  • the sludge filter cake is broken into sludge particles and then dropped onto a conveyor belt to be dispersed into a sludge particle layer.
  • the sludge cake crushing can be achieved by a corresponding sludge cake crushing device.
  • the dry air of the temperature of 25 ° C is input into the sludge particle layer on the slow moving conveyor belt; the dry air is formed by condensing and separating the air at room temperature in the cold exchanger and heating the temperature in the heat exchanger. . Dry air is transported through the air duct to the dry air inlet between the upper and lower stencils of the conveyor belts of each layer. When passing through the bottom layer and surface sludge particles, it provides oxygen for the aerobic reaction of the sludge and absorbs the sludge particles.
  • the moisture makes the sludge particles dehydrated and dried.
  • the conveyor belt is arranged above the layer, and the first layer conveyor belt is provided with a mud particle layer thickness adjuster.
  • the thickness of the conveyor belt is adjusted to 200 mm; the linear velocity of the conveyor belt is 0. 2 mm / s.
  • the total residence time of the sludge particles in the conveyor belt was 45 h.
  • the source of the washing water can preferentially use the condensed water discharged from the cold exchanger, and the insufficient water source is added.
  • the sludge particles on the lowermost conveyor belt are transported to the end, they are further crushed by falling into a screw machine disposed at the lowermost portion of the lowermost conveyor belt, and the moisture content of the finished sludge particles is 31%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Environmental & Geological Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Mechanical Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Veterinary Medicine (AREA)
  • Epidemiology (AREA)
  • General Health & Medical Sciences (AREA)
  • Animal Behavior & Ethology (AREA)
  • Public Health (AREA)
  • Inorganic Chemistry (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Toxicology (AREA)
  • Molecular Biology (AREA)
  • Treatment Of Sludge (AREA)
  • Apparatus For Disinfection Or Sterilisation (AREA)
  • Treating Waste Gases (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Description

一种污水污泥浓缩脱水好氧风干一体化的方法 技术领域
本发明属于污水污泥处理方法的领域， 具体为处理剩余污泥的一种浓缩脱 水好氧风干一体化的方法。
背景技术
目前， 城镇污水处理厂多采用活性污泥法来处理污水。 在处理过程中， 污 水中的有机物质、 病毒细菌、 金属污染物等会转移至活性污泥中， 含水率 99% 以上、 有机质含量较高的剩余污泥成为污水处理厂中的主要废弃物。 污水污泥 的处理处置也成为污水处理厂的一大难题， 制约着城镇的建设发展。
当前国内常用的污水污泥处理方法， 先将含水率 99%以上的剩余污泥注入 重力浓縮池， 12〜24小时后排出上清液， 剩余污泥可浓缩至含水率约 97% ; 再 采用阳离子聚丙烯酰胺对浓缩后的污泥进行化学调质， 调质后的污泥注入离心 脱水机、 带式脱水机或板框压滤机中， 排出滤液后污泥可脱水至含水率 80〜75 % ; 脱水后的污泥先被预分散成为颗粒状或面条状， 再进入干燥装置中进行热 干燥， 干燥后的污泥含水率约为 40〜30% ; 干燥后的污泥可直接填埋处置， 也 可进行焚烧， 也可制水泥、 制砖、 生产园林肥料、 生产低热值燃料等进 行资源化利用。 当前常用的污泥处理方法存在以下问题： （1 )污泥浓缩效率低， 重力浓缩时间长达 12小时以上， 导致污泥浓縮池容积大， 而且污泥在浓缩过程 中容易腐败发臭； （2)污泥脱水效率低， 脱水后污泥含水率较高， 污泥量庞大， 后续热处理过程中需要蒸发的污泥中的水分较多， 导致热处理的设备投资和运 行成本极高； （3 )含水率 80〜75%的脱水污泥是粘性较大的半固体， 在干燥过 程中难以分散， 而且在污泥的粘胶相阶段 （含水率 60〜40% ) 中污泥的传热传 质效率较低， 污泥干燥能耗高， 污泥颗粒容易出现外干内湿的 "糖心现象"。 发明内容
本发明的目的在于解决上述存在的问题， 提供一种污水污泥浓缩脱水效率 高、 干燥能耗低、 尾气污染少、 设备投资与运行成本低、 安全性能高的污泥浓 缩脱水好氧风干一体化的方法， 适用于处理污水处理厂中产生的剩余污泥。
本发明的技术方案是这样实现的： 一种污水污泥浓缩脱水好氧风千一体化 的方法， 包括以下步骤：
( 1 )有机药剂调质： 向含水率为 98%〜99. 8%的剩余污泥中投加有机调质 剂， 并充分搅拌 10~180秒， 以改善剩余污泥的沉降性能；
(2)将经有机药剂调质后的剩余污泥进行重力浓缩， 将所分离出来的上清 液， 引入污水处理设施进行后续处理；
(3)无机药剂调质： 先向浓縮后的剩余污泥中投加含 Fe3+可溶性化合物， 搅拌 10〜180秒进行混合反应， 再向污泥中投加石灰颗粒
并搅拌 30〜300秒， 以改善污泥的可压缩性和疏水性， 并释放出污泥中的部分 细胞水；
(4)机械脱水 ： 将无机药剂调质后的剩余污泥加压输送至板框压滤脱水 机中， 排出滤液， 得到脱水后的污泥滤饼， 所排出的排出滤液引入污水处理设 施进行后续处理。
(5)破碎分散： 将污泥滤饼破碎分散成污泥颗粒， 以增大干燥时污泥的比 表面积， 提高干燥效率；
(6)好氧风干： 向静止、移动或翻动着的污泥颗粒间输入 90°C以下的干燥 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， 污泥颗粒中的 水分被蒸发出来， 使污泥含水率在 38%以下。
所述的（6)步骤中， 对污泥颗粒进行物理或化学杀菌处理； 所述的物理或 化学杀菌处理可艮据污泥资源化利用的要求而增加， 物理杀菌处理可以是紫外 线杀菌， 化学杀菌处理可以是臭氧杀菌、 高氯或者高氧物质杀菌； 杀菌的方式 还可以是其它杀菌方式。
所述的（6)步骤中， 好氧风干产生的尾气经水洗后排放。 所述水洗水可以 是中性的纯水洗、 碱洗以去除由于好氧发酵产生的腐败酸性气体， 酸洗以去 除可能产生的氨气， 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。
所述的（6)步骤后，对干燥后的污泥颗粒进一步粉碎至资源化利用的要求。 所述对污泥颗粒进一步粉碎是利用螺旋机令物料相互挤压、 磨擦
进行破碎； 所述的螺旋机可以是单独一条螺旋， 也可以是两条以上的螺旋组制 成。
所述（1 ) 步骤中的剩余污泥为污水处理厂在生产过程中产生的， 其为 98 %〜99. 8%； 投加的有机调质剂可以是分子量为 800〜1500的阳离子聚丙烯酰 胺， 投加时配置成浓度为 0.05〜0.5%聚丙烯酰胺溶液， 聚丙烯酰胺的千粉投加 量为污泥干基质量的 0.05〜0.5%； 聚丙烯酰胺具有静电中和吸附架桥功能，有利 于提高污泥的沉降性能， 达到快速浓縮、 提高浓缩效率的效果。 聚丙烯酰胺的 干粉投加的优选浓度为 0.15 %。
所述（2)步骤中的重力浓缩为污泥自然沉淀， 重力浓縮的时间为 30〜150 分钟； 重力浓縮可同时去除污泥中的间隙水和表面吸附水， 重力浓缩后的污泥 含水率为 86〜95 %。
所述（3 )步骤中含 Fe3+可溶性化合物优选三氯化铁溶液， 三氯化铁溶液的 浓度大于等于 35 %，三氯化铁溶液的投加量为污泥干基质量的 0.3〜10%；三氯 化铁溶液优选投加量为 5 % ; 所述石灰颗粒中有效氧化钙含量不低于 60%， 石 灰颗粒的投加量为污泥干基质量的 3〜150%; 三氯化铁溶液和石灰颗粒具有静 电中和、 网捕卷扫、 提供骨架、 改善污泥可压縮性和疏水性、 释放部分细胞水 等作用， 有利于提高污泥的脱水效率， 获得含水率较低的脱水污泥。 所述的石 灰颗粒的颗粒度应大于等于 60目。
所述（4)步骤中污泥加压输送的压力为 0.5〜2.5MPa， 板框压滤
脱水可同时去除污泥中的毛细结合水和部分的细胞水， 脱水后的污泥滤饼含水 率为 41〜69%。
所述（5)步骤中的污泥滤饼破碎可以是在污泥滤饼破碎装置中实现的， 所 述的污泥滤饼破碎装置， 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， 笼体为多孔状； 污泥滤饼在污泥滤饼破碎装置的多孔状的 笼体内翻动， 使污泥滤饼间产生相互碰撞和磨擦而被破碎， 小于笼体孔的大小 的污泥颗粒被排出笼体外， 从而实现了污泥滤饼的破碎分散。
所述的笼体孔的大小在 3mn！〜 30mm，此颗粒自然堆放时，堆密度较小，有利 于气体进出。 污泥滤饼在笼体内的翻动可以是笼体静止由笼内主轴和设置在主 轴的叶片带动的， 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， 翻动速度越小； 污泥滤饼 的含水率越低， 翻动速度越大。 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翻动速度越大， 污泥破碎分散装置的出料量越大； 翻动速 度越小， 污泥滤饼破碎分散装置的出料量越小。 优选的污泥滤饼破碎分散翻动 速度为径向最外点的线速度在 5mra/s〜100mm/s之间。主轴电机的功率范围： 0〜 20KW。
所述步骤（6)步骤中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〜： L5°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。
本发明的有益效果是： （1 )通过对剩余污泥进行有机调质， 提高了剩余污 泥的沉降性能， 以提高污泥浓缩效率， 缩短浓缩时间， 减少浓缩池容积； （2) 通过对浓縮后的污泥进行无机调质， 改善污泥的可压缩性和疏水性， 并释放出 污泥中的部分细胞水， 在高压板框压滤脱水的作用下可提高污泥的脱水效率， 获得含水率较低的污泥滤饼， 相应地减少了脱水污泥量， 减轻了后续热处理的 负担； （3)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； （4)破碎后的污泥颗粒在 好氧放热的作用下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； （5)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； （6 )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； （7) 出料粉碎机构附带破碎功能， 出料污泥颗粒松散， 便于后续的资源化利用。
附图说明
图 1为本发明一种污水污泥浓缩脱水好氧风干一体化的方法的工艺流程图。 图 2是本发明的污泥滤饼好氧风干装置的结构示意图；
图 3是本发明的污泥滤饼好氧风干装置的 A- A截面结构示意图；
图 4是本发明的污泥滤饼好氧风干装置的 B-B截面结构示意图；
图 5是本发明的污泥滤饼好氧风干装置的 C部局部放大图。
具体实施方式
以下结合附图和具体实施例对本发明进行详细的说明。
一种污水污泥浓縮脱水好氧风干一体化的方法， 如图 1所示， 包括以下步 骤：
( 1 ))有机药剂调质： 向含水率为 98%〜99. 8%的剩余污泥中投加有机调 质剂， 并充分搅拌 10~180秒， 以改善剩余污泥的沉降性能； 剩余污泥为污水处 理厂在生产过程中产生的， 其为 98%〜99. 8%。 投加的有机调质剂可以是分子 量为 800〜1500的阳离子聚丙烯酰胺 (PAM), 投加时配置成浓度为 0.05〜0.5 %聚丙烯酰胺溶液， 聚丙烯酰胺的干粉投加量为污泥干基质量的 0.05〜0.5%。聚 丙烯酰胺溶液优选的浓度为 0.1〜0.2%， 聚丙烯酰胺的干粉投加的优选浓度为 0.15 %。 聚丙烯酰胺具有静电中和吸附架桥功能， 有利于提高污泥.的沉降性能， 达到快速浓缩、 提高浓缩效率的效果。
(2)将经有机药剂调质后的剩余污泥进行重力浓缩， 将所分离出来的上清 液， 引入污水处理设施进行后续处理， 后续处理的过程为普通污水处理的过程。 重力浓缩为污泥自然沉淀， 重力浓缩的时间为 30〜150分钟； 童力浓缩可同时 去除污泥中的间隙水和表面吸附水， 重力浓缩后的污泥含水率为 86〜95 %。
(3)无机药剂调质： 先向浓缩后的剩余污泥中投加含 Fe3+可溶性化合物溶 液， 搅拌 10〜180秒进行混合反应， 再向污泥中投加石灰颗粒并搅拌 30〜300 秒， 以改善污泥的可压缩性和疏水性， 并释放出污泥中的部分细胞水。 含 Fe3+ 可溶性化合物溶液优选三氯化铁溶液， 三氯化铁溶液的浓度大于等于 35 %， 三 氯化铁溶液的投加量为污泥干基质量的 0.3〜10%。三氯化铁溶液优选投加量为 5 %。石灰颗粒中有效氧化钙含量不低于 60%，石灰颗粒的投加量为污泥干基质 量的 3〜150%； 三氯化铁溶液和石灰颗粒具有静电中和、 网捕卷扫、提供骨架、 改善污泥可压缩性和疏水性、 释放部分细胞水等作用， 有利于提高污泥的脱水 效率，获得含水率较低的脱水污泥。所述的石灰颗粒的颗粒度应大于等于 60目。
(4)机械脱水 ： 将无机药剂调质后的剩余污泥加压输送至板框压滤脱水 机中， 排出滤液， 得到脱水后的污泥滤饼， 所排出的排出滤液引入污水处理设 施进行后续处理。 污泥加压输送的压力为 0.5~2.5MPa， 板框压滤脱水可同时去 除污泥中的毛细结合水和部分的细胞水， 脱水后的污泥滤饼含水率为 41~69%。
( 5)破碎分散： 将污泥滤饼破碎分散成污泥颗粒， 以增大干燥时污泥的比 表面积， 提高干燥效率。
污泥滤饼破碎可以是在污泥滤饼破碎装置中实现的， 所述的污泥滤饼破碎 装置， 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， 笼体为多孔状； 污泥滤饼在污泥滤饼破碎装置的 多孔状的笼体内翻动， 使污泥滤饼间产生相互碰撞和磨擦而被破碎， 小于笼体 孔的大小的污泥颗粒被排出笼体外， 从而实现了污泥滤饼的破碎分散。 污泥滤 饼在笼体内翻动速度为笼体径向最外点的线速度在 5mm/S〜100mm/s之间，主轴 电机的功率范围： 0〜20KW。
所述的笼体孔的大小在 3mn！〜 30mm， 此颗粒自然堆放时， 堆密度较小， 有利 于气体进出。 污泥滤饼在笼体内的翻动可以是笼体静止由笼内主轴和设置在主 轴的叶片带动的， 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， 翻动速度越小； 污泥滤饼 的含水率越低， 翻动速度越大。 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翻动速度越大， 污泥破碎分散装置的出料量越大； 翻动速 度越小， 污泥滤饼破碎分散装置的出料量越小。
(6)好氧风干： 向静止、 移动或翻动着的污泥颗粒间输入干燥空气， 让污 泥产生好氧放热反应， 在外热与内热的共同作用下， 污泥颗粒中的水分被蒸发 出来。 所述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 0Ό〜15Ό之间，然后在热交换器中温度 被提高到 0° (：〜 90°C之间，形成不饱和干燥空气。所述的污泥颗粒平移速度： 0〜
0. 2米/秒， 或翻动角速度： 0〜1转 /秒， 功率范围： 0〜； L0KW。 干燥空气的流量 范围： 0〜20000m3/h， 功率范围： 0〜50KW。
所述的（6)步骤中， 对污泥颗粒进行物理或化学杀菌处理； 所述的物理或 化学杀菌处理可根据污泥资源化利用的要求而增加， 物理杀菌处理可以是紫外 线杀菌， 化学杀菌处理可以是臭氧杀菌、 高氯或者高氧物质杀菌； 杀菌的方式 还可以是其它杀菌方式。
所述的（6)步骤中， 好氧风干产生的尾气经水洗后排放。 所述步水洗可以 是中性的纯水洗， 碱洗以去除由于好氧发酵产生的腐败酸性气体， 酸洗以去 除可能产生的氨气。 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。 所
所述的（6)步骤后，对干燥后的污泥颗粒进一步粉碎至资源化利用的要求。 所述的资源化利用可以是制肥、 制砖、 燃料利用、 填充料等。 所述对污泥颗粒 进一步粉碎是利用螺旋机令物料相互挤压、 磨擦进行破碎； 所述的螺旋机可以 是单独一条螺旋， 也可以是两条以上的螺旋组制成。 螺旋机输送速度范围： 0〜 10公斤 /秒， 功率范围： 0〜； 10KW。
所述的 （5)步骤和 （6)步骤是通过污泥滤饼好氧风干装置来实现。
污泥滤饼好氧风干装置， 如图 2、 图 3和图 4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 M,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： 其包括主轴、 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， 笼体为多孔状； 污泥滤饼在污泥滤饼破碎 装置的多孔状的笼体内翻动， 使污泥滤饼间产生相互碰撞和磨擦而被破碎， 小 于笼体孔的大小的污泥颗粒被排出笼体外， 从而实现了污泥滤饼的破碎分散。
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 lOirai！〜 500mm。 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 lmm/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 1
将含水率 99. 8%的剩余污泥输送至有机调质搅拌槽中，向污泥中投加浓度为 0. 1%的阳离子 1200万分子量聚丙烯酰胺溶液， 聚丙烯酰胺干粉的投加量为污泥 干基质量的 0. 2%， 将有机调质后的污泥输送至重力浓缩池中。 重力浓缩 120分 钟后排出所分离出来的上清液，浓缩后的污泥含水率为 95%，将浓缩污泥输送至 脱水工序中。
将浓缩后的污泥输送至无机调质搅拌槽中，先向污泥中投加浓度为 38%的三 氯化铁溶液并充分搅拌 10秒，三氯化铁的投加量为污泥干基质量的 2. 3%;再向 污泥中投加石灰颗粒并充分搅拌 60秒， 其中有效氧化钙含量为 70%， 氧化钙的 投加量为污泥干基质量的 12%;然后将调质后的污泥通过螺杆泵输送至板框压滤 机中， 螺杆泵的注入压力为 IMPa; 排出滤液后， 滤饼含水率为 61%。
将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。 向缓慢运动输送带上的污 泥颗粒层内正压输入温度为 85 Ό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为 200mm; 输送带运动的线速度为 2mm/s。污泥 颗粒在输送带中的全程停留时间为 20h。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， 对输送带上的污泥颗粒层进行 物理或者化学杀菌。 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， 水洗水的来源优先使用从冷交换器中排出的冷凝水， 不足部分外加水 源。 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， 成品污泥颗粒的含水率为 36%。
实施例 2
将含水率 99. 5%的剩余污泥输送至有机调质搅拌槽中，向污泥中投加浓度为 0. 1%的阳离子 1500万分子量聚丙烯酰胺溶液，聚丙烯酰胺的投加量为污泥干基 质量的 0. 15%,再将有机调质后的污泥输送至重力浓缩池中。重力浓缩 2小时后 排出所分离出来的上清液，浓缩后的污泥含水率为 93%，将浓缩污泥输送至脱水 工序中。
将浓缩后的污泥输送至无机调质搅拌槽中，先向污泥中投加浓度为 38%的三 氯化铁溶液并充分搅拌 2分钟， 三氯化铁的投加量为污泥干基质量的 5. 5%; 再 向污泥中投加石灰颗粒并充分搅拌 12分钟， 其中氧化钙含量为 72%， 氧化钙的 投加量为污泥干基质量的 12%;然后将调质后的污泥通过螺杆泵输送至板框压滤 机中， 螺杆泵的注入压力为 IMPa; 排出滤液后， 滤饼含水率为 58%。 将污泥滤 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。 向缓慢运动输送带上的污泥颗粒层内正 压输入温度为 60°C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 带上的厚度调节为 200mm; 输送带运动的线速度为 2. 5mm/s。污泥颗粒在输送带 中的全程停留时间为 18h。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。 对输送带上的污泥颗粒层进行物理或者化学 杀菌。 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， 水洗 水的来源优先使用从冷交换器中排出的冷凝水， 不足部分外加水源。 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， 成品污泥颗粒的含水率为 34%。
实施例 3
将含水率 99. 3%的剩余污泥输送至有机调质搅拌槽中，向污泥中投加浓度为 0. 1%的阳离子 1200万分子量聚丙烯酰胺溶液， 聚丙烯酰胺的投加量为污泥干基 质量的 0. 1%， 再将有机调质后的污泥输送至重力浓縮池中。 重力浓缩 1小时后 排出所分离出来的上清液，浓缩后的污泥含水率为 93%，将浓缩污泥输送至脱水 工序中。
将浓缩后的污泥输送至无机调质搅泮槽中，先向污泥中投加浓度为 38%的三 氯化铁溶液并充分搅拌 1分钟， 三氯化铁的投加量为污泥干基质量的 4. 5%; 再 向污泥中投加石灰颗粒并充分搅拌 15分钟， 其中有效氧化钙含量为 75%， 氧化 钙的投加量为污泥干基质量的 15. 5%;然后将调质后的污泥通过螺杆泵输送至板 框压滤机中， 螺杆泵的注入压力为 IMPa; 排出滤液后， 滤饼含水率为 53%。
将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。 向缓慢运动输送带上的污 泥颗粒层内正压输入温度为 48 °C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为 200mm; 输送带运动的线速度为 1. 5mm/S。污 泥颗粒在输送带中的全程停留时间为 25h。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， 对输送带上的污泥颗粒层进 行物理或者化学杀菌。 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， 水洗水的来源优先使用从冷交换器中排出的冷凝水， 不足部分外加 水源。 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， 成品污泥颗粒的含水率为 33%。
实施例 4
将含水率 99%的剩余污泥输送至有机调质搅拌槽中， 向污泥中投加浓度为 0. 1%的阳离子 1000万分子量聚丙烯酰胺溶液，聚丙烯酰胺的投加量为污泥干基 质量的 0. 08%,再将有机调质后的污泥输送至重力浓缩池中。重力浓缩 1. 5小时 后排出所分离出来的上清液，浓缩后的污泥含水率为 90%，将浓缩污泥输送至脱 水工序中。
将浓缩后的污泥输送至无机调质搅泮槽中， 先向污泥中投加浓度为 38. 8% 的三氯化铁溶液并充分搅拌 30秒， 三氯化铁的投加量为污泥干基质量的 6. 5%； 再向污泥中投加石灰颗粒并充分搅拌 10分钟， 其中氧化钙含量为 70%， 氧化钙 的投加量为污泥干基质量的 8. 4%; 然后将调质后的污泥通过螺杆泵输送至板框 压滤机中， 螺杆泵的注入压力为 IMPa; 排出滤液后， 滤饼含水率为 51%。
将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。 向缓慢运动输送带上的污 泥颗粒层内正压输入温度为 25°C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为 200mm; 输送带运动的线速度为 0. 2mm/s。污 泥颗粒在输送带中的全程停留时间为 45h。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， 对输送带上的污泥颗粒层进 行物理或者化学杀菌。 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， 水洗水的来源可优先使用从冷交换器中排出的冷凝水， 不足部分外 加水源。 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， 成品污泥颗粒的含水率为 31%。

Claims

权 利 要 求 书
1、一种污水污泥浓缩脱水好氧风干一体化的方法，其特征在于， 包括以下步骤：
(1 )有机药剂调质： 向含水率为 98%〜99. 8%的剩余污泥中投 加有机调质剂， 并充分搅拌 10~180秒；
(2)将经有机药剂调质后的剩余污泥进行重力浓缩， 将所分离 出来的上清液引入污水处理设施进行后续处理；
(3 ) 无机药剂调质： 先向浓缩后的剩余污泥中投加含 Fe3+可溶 性化合物溶液，搅拌 10〜180秒进行混合反应，再向污泥中投加石灰 颗粒， 搅拌 30〜300秒；
(4)机械脱水 ：将无机药剂调剂后的剩余污泥加压输送至板框 压滤脱水机中， 排出滤液， 得到脱水后的污泥滤饼；
(5)破碎分散： 将污泥滤饼破碎分散成污泥颗粒；
(6)好氧风干： 向静止、 移动或翻动着的污泥颗粒间输入干燥 空气， 让污泥产生好氧放热反应。
2、 如权利要求 1所述的一种污水污泥浓縮脱水好氧风干一体化 的方法， 其特征在于， 所述的 （6) 步骤中， 对污泥颗粒进行物理或 化学杀菌处理；所述的物理杀菌处理是紫外线杀菌，化学杀菌处理是 臭氧杀菌、 高氯或者高氧物质杀菌。
3、 如权利要求 1所述的一种污水污泥浓縮脱水好氧风干一体化 的方法， 其特征在于， 所述的 （6)步骤中， 好氧风干产生的尾气经 水洗后排放。
4、 如权利要求 1所述的一种污水污泥浓缩脱水好氧风干一体化 的方法， 其特征在于， 所述的 （6)步骤后， 对干燥后的污泥颗粒进 一步粉碎至资源化利用的要求。
5、 如权利要求 4所述的一种污水污泥浓縮脱水好氧风干一体化 的方法，其特征在于，所述对污泥颗粒进一步粉碎是利用螺旋机令物 料相互挤压、磨擦进行破碎；所述的螺旋机是单独一条螺旋或两条以 上的螺旋组制成。
6、 如权利要求 1所述的一种污水污泥浓縮脱水好氧风干一体化 的方法， 其特征在于， 所述（1 )步骤中投加的有机调质剂是阳离子 聚丙烯酰胺， 投加时配置成浓度为 0.05〜0.5 %聚丙烯酰胺溶液， 聚 丙烯酰胺的干粉投加量为污泥干基质量的 0.05~0.5%。
7、如权利要求 1所述的一种污水污泥浓缩脱水好氧风干一体化 的方法， 其特征在于， 所述（2)步骤中的重力浓缩为污泥自然沉淀， 重力浓缩的时间为 30〜150分钟， 重力浓缩后的污泥含水率为 86〜 95 %。
8、如权利要求 1所述的一种污水污泥浓缩脱水好氧风干一体化 的方法， 其特征在于， 所述（3)步骤中含 Fe3+可溶性化合物溶液为 三氯化铁溶液， 三氯化铁溶液的浓度大于等于 35 %， 三氯化铁溶液 的投加量为污泥干基质量的 0.3〜10%； 所述石灰颗粒中有效氧化钙 含量不低于 60% , 石灰颗粒的投加量为污泥干基质量的 3〜150%。
9、如权利要求 8所述的一种污水污泥浓缩脱水好氧风干一体化 的方法， 其特征在于， 所述的石灰颗粒的颗粒度大于等于 60目。
10、如权利要求 1所述的一种污水污泥浓缩脱水好氧风干一体化 的方法， 其特征在于， 所述 （4 ) 步骤中污泥加压输送的压力为 0.5~2.5MPa, 脱水后的污泥滤饼含水率为 41~69%。
11、 如权利要求 1所述的一种污水污泥浓縮脱水好氧风干一体 化的方法， 其特征在于， 所述（5) 步骤中的污泥滤饼破碎是在污泥 滤饼破碎装置中实现的，所述的污泥滤饼破碎装置，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， 笼体 为多孔状；污泥滤饼在污泥滤饼破碎装置的多孔状的笼体内翻动，使 污泥滤饼间产生相互碰撞和磨擦而被破碎，小于笼体孔的大小的污泥 颗粒被排出笼体外实现了污泥滤饼的破碎分散。
12、 如权利要求 11所述的一种污水污泥浓缩脱水好氧风干一 体化的方法， 其特征在于， 所述的笼体孔的大小在 3mir！〜 30皿。
13、 如权利要求 1所述的一种污水污泥浓缩脱水好氧风干一体 化的方法， 其特征在于， 所述步骤 （6) 步骤中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。
14、如权利要求 3所述的一种污水污泥浓缩脱水好氧风干一体化 的方法， 其特征在于， 所述的水洗是中性的纯水洗、碱洗或酸洗， 水 洗的水使用从冷交换器中排出的冷凝水， 不足部分为外加水源。
PCT/CN2009/001280 2009-09-28 2009-11-18 一种污水污泥浓缩脱水好氧风干一体化的方法 WO2011035460A1 (zh)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US13/498,495 US8808419B2 (en) 2009-09-28 2009-11-18 Method of integration of concentration-dehydration and aerobic air-drying of sewage sludge
KR1020127010541A KR101467204B1 (ko) 2009-09-28 2009-11-18 하수 슬러지의 농축-탈수 및 호기적 공기-건조의 통합 방법
JP2012530071A JP5526344B2 (ja) 2009-09-28 2009-11-18 下水汚泥の濃縮‐脱水および好気的空気乾燥を統合する方法
EP09849648.2A EP2484641A4 (en) 2009-09-28 2009-11-18 PROCESS FOR INTEGRATION OF DEHYDRATION-CONCENTRATION AND AEROBIC DRYING OF PURIFYING STREAM SLUDGE

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN200910192762.5 2009-09-28
CN2009101927625A CN101691273B (zh) 2009-09-28 2009-09-28 一种污水污泥浓缩脱水好氧风干一体化的方法

Publications (1)

Publication Number Publication Date
WO2011035460A1 true WO2011035460A1 (zh) 2011-03-31

Family

ID=42080012

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2009/001280 WO2011035460A1 (zh) 2009-09-28 2009-11-18 一种污水污泥浓缩脱水好氧风干一体化的方法

Country Status (6)

Country Link
US (1) US8808419B2 (zh)
EP (1) EP2484641A4 (zh)
JP (1) JP5526344B2 (zh)
KR (1) KR101467204B1 (zh)
CN (1) CN101691273B (zh)
WO (1) WO2011035460A1 (zh)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9902770B2 (en) 2013-03-15 2018-02-27 Janssen Biotech, Inc. Interferon alpha and omega antibody antagonists
CN110564455A (zh) * 2019-09-18 2019-12-13 华陆工程科技有限责任公司 一种煤制气装置细渣干燥方法
CN112759226A (zh) * 2020-12-31 2021-05-07 江苏亿洲再生资源科技有限公司 一种污泥处理装置
TWI733908B (zh) * 2016-11-23 2021-07-21 大陸商廣州新致晟環保科技機械設備有限公司 乾化污泥的組合裝置和其乾燥方法

Families Citing this family (43)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101691273B (zh) * 2009-09-28 2012-07-04 广州普得环保设备有限公司 一种污水污泥浓缩脱水好氧风干一体化的方法
CN101671106B (zh) * 2009-09-28 2012-11-07 广州普得环保设备有限公司 一种污泥滤饼好氧风干的方法及装置
CN102249514A (zh) * 2010-05-17 2011-11-23 唐菊香 出厂污泥低能干化处理方法
CN101863611A (zh) * 2010-06-13 2010-10-20 东南大学 一种污泥深度脱水的方法
CN102452784A (zh) * 2010-11-03 2012-05-16 四川四通欧美环境工程有限公司 城市污泥资源化利用干化装置
CN102001812B (zh) * 2010-11-22 2012-06-06 杭州苏堤环保实业有限公司 污泥深度脱水工艺
CN102092918B (zh) * 2011-01-14 2012-09-26 中环保水务投资有限公司 一种城市生活脱水污泥生物干化处理方法
CN102173557B (zh) * 2011-03-10 2013-04-24 北京科技大学 一种低热值剩余污泥处置方法
CN102173558B (zh) * 2011-03-10 2013-04-03 北京科技大学 一种脱硫石灰处置剩余污泥的工艺方法
CN102229464B (zh) * 2011-06-02 2013-03-27 杭州中威净水材料有限公司 一种污泥高度脱水干化的方法
CN102303944B (zh) * 2011-08-22 2014-08-27 广州新致晟环保科技机械设备有限公司 脱水污泥再处理方法
CN103253846B (zh) * 2012-02-16 2014-04-23 浙江绿色时代环保科技有限公司 污泥高效脱水系统
CN102617013A (zh) * 2012-04-24 2012-08-01 浙江海拓环境技术有限公司 一种污泥浓缩、脱水处理方法
CN104418480A (zh) * 2013-08-22 2015-03-18 谷尚昆 污泥干燥一体化集成设备
KR101579103B1 (ko) 2013-09-02 2015-12-23 한국과학기술연구원 특정미생물을 이용한 하수슬러지처리장치
CN103588373A (zh) * 2013-11-15 2014-02-19 杭州智水水务科技有限公司 一种剩余污泥产酸并脱水的方法
TWI511807B (zh) * 2014-07-15 2015-12-11 Kyokado Co Ltd The use of multi-point injection of the original location of the purification method
CN105819652A (zh) * 2015-01-07 2016-08-03 广州新致晟环保科技机械设备有限公司 污泥干化系统和方法
CN105819653B (zh) * 2015-01-07 2023-12-29 广州正晟科技有限公司 污泥干化的控制系统
KR102403512B1 (ko) 2015-04-30 2022-05-31 삼성전자주식회사 공기 조화기의 실외기, 이에 적용되는 컨트롤 장치
LU92738B1 (fr) * 2015-06-11 2016-12-12 Biocarbon Ind Sarl Procede et installation de preparation de biomasse
KR101590408B1 (ko) * 2015-07-31 2016-02-01 주식회사 우리종합기술 소규모 하·폐수 처리 시스템
KR101590139B1 (ko) * 2015-07-31 2016-01-29 주식회사 우리종합기술 Puv 처리조와 슬러지 건조시스템을 갖춘 하ㆍ폐수처리시스템
CN106517719A (zh) * 2015-09-14 2017-03-22 黄浩 污泥(或粪便、淤泥)快速脱水除臭的智能化干化处理系统
CN105384320B (zh) * 2015-11-25 2018-08-17 中南大学 一种提高亚硝化反应器污泥沉降性能的方法
CN105688468B (zh) * 2016-02-02 2018-02-06 耿春茂 一种烘干隔膜板框压滤系统
ITUA20163510A1 (it) * 2016-05-17 2017-11-17 M C E S R L Man Consulting Engineering Procedimento per il trattamento del fango di depurazione con riciclo della materia di scarto
CN106116074B (zh) * 2016-08-04 2019-07-09 北京同创碧源水务科技发展有限公司 利用重力浓缩及光解让污泥深度脱水的方法
CN106360260A (zh) * 2016-09-05 2017-02-01 福州昌盛食品有限公司 一种面皮熟化过程的紫外线消毒方法及设备
JP6869126B2 (ja) * 2017-06-30 2021-05-12 月島機械株式会社 汚泥の処理方法および処理装置
US10682585B2 (en) * 2017-07-12 2020-06-16 James William Masten, JR. High-efficiency sludge dehydrator using an adaptive mechanical vapor re-compression process
CN108445829B (zh) * 2018-03-12 2020-07-10 广州晟启能源设备有限公司 污泥除湿干化控制系统及污泥除湿干化机
CN108751591B (zh) * 2018-06-20 2021-03-30 浙江鑫广环保科技有限公司 一种印染废水处理方法及系统
CN108821541A (zh) * 2018-09-06 2018-11-16 四川安赛吉节能环保科技有限公司 一种污泥恒温干化系统
CN109704530A (zh) * 2019-03-05 2019-05-03 龚典局 一种铝氧化污泥综合利用方法
CN109928598B (zh) * 2019-03-28 2020-12-18 北京科技大学 基于空气介质循环的污泥深度干化方法及系统
CN110204363B (zh) * 2019-07-01 2021-07-27 徐勇利 一种环境友好型污泥氧化处理余热处理装置及其使用方法
CN110590117A (zh) * 2019-08-12 2019-12-20 安徽国祯环卫科技有限公司 一种杀菌脱水多功能污泥处理新方法
CN110451758A (zh) * 2019-08-22 2019-11-15 天津壹新环保工程有限公司 河道底泥资源化利用方法及系统
CN111167846B (zh) * 2020-01-19 2021-08-24 北京建工环境修复股份有限公司 一种土壤淋洗修复减量系统及其施工方法
CN111792793A (zh) * 2020-07-24 2020-10-20 淮安港淮建设发展有限公司 一种城市污水污泥综合处理系统及工艺
CN113776303A (zh) * 2021-10-12 2021-12-10 中国十七冶集团有限公司 一种给排水工程用脱水机及其脱水方法
CN117342776B (zh) * 2023-12-04 2024-03-19 中煤科工集团杭州研究院有限公司 一种污泥复合调理及深度脱水方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH06134500A (ja) * 1992-10-21 1994-05-17 Nippon Steel Corp 汚泥類の処理方法
CN2463048Y (zh) * 2000-12-28 2001-12-05 天地科技股份有限公司唐山分公司 用于压滤机滤饼定量破碎与干燥的碎干机
JP2004160329A (ja) * 2002-11-12 2004-06-10 Terunaito:Kk 汚泥処理方法
CN1669956A (zh) * 2004-03-18 2005-09-21 昆明柯利欣环保科技有限公司 一种高效污水处理方法
CN1986788A (zh) * 2006-12-12 2007-06-27 广州铬德工程有限公司 污泥脱水的化学调理剂及其脱水方法
CN101007695A (zh) * 2007-01-19 2007-08-01 广州普得环保设备有限公司 一种污泥发酵脱水干燥方法
CN101234841A (zh) * 2008-01-02 2008-08-06 广州普得环保设备有限公司 一种污泥浓缩脱水的方法

Family Cites Families (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5110463A (ja) * 1974-07-17 1976-01-27 Minoru Hosoya Chikufunkansosochi
JPS5662590A (en) * 1979-10-25 1981-05-28 Hitachi Kiden Kogyo Ltd Processing method for waste liquid generated in aerobic fermentation processing stage
JPS5939597Y2 (ja) * 1980-09-02 1984-11-05 東和空調株式会社 汚泥物質の乾燥装置
JPS58183998A (ja) * 1982-04-21 1983-10-27 Towa Kucho Kk 汚泥乾燥方法
JPS5982996A (ja) 1982-11-04 1984-05-14 Ebara Infilco Co Ltd 含水物の乾燥方法
JPS59183896A (ja) * 1983-03-31 1984-10-19 Kurita Water Ind Ltd 汚泥脱水方法
JPS61181600A (ja) 1984-04-25 1986-08-14 Sanyo Chem Ind Ltd 汚泥脱水用助剤および方法
JPS6314916Y2 (zh) * 1985-07-10 1988-04-26
JPS6213544A (ja) 1986-06-05 1987-01-22 Minoru Hiromasa プリント基板廃材から銅成分を回収すると共にポリ塩化アルミニウムを製造する方法
JPH0621723B2 (ja) * 1986-08-18 1994-03-23 株式会社前川製作所 空気の除湿乾燥用のヒ−トポンプ装置
JPH03275200A (ja) * 1990-03-26 1991-12-05 Kurita Water Ind Ltd 有機性汚泥の濃縮脱水方法
DE4116146A1 (de) 1990-10-18 1992-04-23 Klein Alb Gmbh Co Kg Verfahren zum entwaessern von suspensionen od. dgl. schlammartigen gemischen
US5279637A (en) 1990-10-23 1994-01-18 Pcl Environmental Inc. Sludge treatment system
JP3083880B2 (ja) * 1991-07-15 2000-09-04 イーグル工業株式会社 半導体圧力センサ用ハーメチックシール構造およびその製造方法
JP3222278B2 (ja) * 1993-07-23 2001-10-22 ハイモ株式会社 汚泥脱水法
JP3401881B2 (ja) * 1993-12-21 2003-04-28 栗田工業株式会社 消化汚泥の洗浄濃縮方法および洗浄濃縮剤
JP2887439B2 (ja) * 1994-02-10 1999-04-26 川崎重工業株式会社 ガス脱臭を伴う有機性余剰汚泥の乾燥方法及び装置
JPH0731999U (ja) 1994-07-28 1995-06-16 鹿島建設株式会社 セグメント連結用の通しボルト
JPH1130476A (ja) * 1997-07-10 1999-02-02 Jsr Corp 乾燥方法、及び乾燥装置
US6409788B1 (en) * 1998-01-23 2002-06-25 Crystal Peak Farms Methods for producing fertilizers and feed supplements from agricultural and industrial wastes
JP2001018000A (ja) * 1999-07-08 2001-01-23 Kankyo Gijutsu Kaihatsu Kk スラッジの処理方法および処理装置
JP3659473B2 (ja) 1999-09-07 2005-06-15 Ｊｆｅプラント＆サービス株式会社 汚泥の乾燥方法
JP2001276785A (ja) * 2000-04-04 2001-10-09 Grobal Clean:Kk 生ごみ乾燥装置及び生ごみ処理方法
JP2001314832A (ja) * 2000-05-08 2001-11-13 Kozo Aoyama 生ゴミ連続乾燥機
JP2002177983A (ja) 2000-12-13 2002-06-25 Sumitomo Heavy Ind Ltd 廃水処理装置
DE20110292U1 (de) * 2001-06-21 2002-10-24 Kühn Umweltprodukte GmbH, 29683 Fallingbostel Vorrichtung zum Eindicken oder Entwässern von Schlämmen, Sedimenten aus Gewässern o.dgl., insbesondere von Überschußschlämmen in Kläranlagen
JP2003154399A (ja) * 2001-11-22 2003-05-27 Mitsuishi Seisakusho:Kk 余剰汚泥処理システム
JP3771887B2 (ja) 2002-09-17 2006-04-26 新日本製鐵株式会社 活性汚泥の利用方法
JP3706097B2 (ja) 2002-10-18 2005-10-12 実 富田 有機廃棄物発酵処理システム
JP3957652B2 (ja) * 2003-03-26 2007-08-15 株式会社クボタ 産業用除湿乾燥機
JP2004329023A (ja) * 2003-04-30 2004-11-25 Taisei Corp 水稲育苗培土
JP4194421B2 (ja) * 2003-05-28 2008-12-10 株式会社西原環境テクノロジー コンポスト装置
JP2005103397A (ja) 2003-09-29 2005-04-21 Toyota Motor Corp 排水汚泥の乾燥装置
JP2007130545A (ja) 2005-11-09 2007-05-31 Kansai Electric Power Co Inc:The 排水処理方法及び排水処理装置
JP5457620B2 (ja) 2006-09-27 2014-04-02 日環特殊株式会社 汚泥減容炭化装置とその方法と有機性排水処理システム
CN201263998Y (zh) * 2008-08-22 2009-07-01 同济大学 污泥破碎混合机
CN201288115Y (zh) * 2008-09-22 2009-08-12 武汉路德科技有限责任公司 多能源干化污泥设备
CN101691273B (zh) * 2009-09-28 2012-07-04 广州普得环保设备有限公司 一种污水污泥浓缩脱水好氧风干一体化的方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH06134500A (ja) * 1992-10-21 1994-05-17 Nippon Steel Corp 汚泥類の処理方法
CN2463048Y (zh) * 2000-12-28 2001-12-05 天地科技股份有限公司唐山分公司 用于压滤机滤饼定量破碎与干燥的碎干机
JP2004160329A (ja) * 2002-11-12 2004-06-10 Terunaito:Kk 汚泥処理方法
CN1669956A (zh) * 2004-03-18 2005-09-21 昆明柯利欣环保科技有限公司 一种高效污水处理方法
CN1986788A (zh) * 2006-12-12 2007-06-27 广州铬德工程有限公司 污泥脱水的化学调理剂及其脱水方法
CN101007695A (zh) * 2007-01-19 2007-08-01 广州普得环保设备有限公司 一种污泥发酵脱水干燥方法
CN101234841A (zh) * 2008-01-02 2008-08-06 广州普得环保设备有限公司 一种污泥浓缩脱水的方法

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9902770B2 (en) 2013-03-15 2018-02-27 Janssen Biotech, Inc. Interferon alpha and omega antibody antagonists
US10155809B2 (en) 2013-03-15 2018-12-18 Janssen Biotech, Inc. Interferon alpha and omega antibody antagonists
TWI733908B (zh) * 2016-11-23 2021-07-21 大陸商廣州新致晟環保科技機械設備有限公司 乾化污泥的組合裝置和其乾燥方法
CN110564455A (zh) * 2019-09-18 2019-12-13 华陆工程科技有限责任公司 一种煤制气装置细渣干燥方法
CN112759226A (zh) * 2020-12-31 2021-05-07 江苏亿洲再生资源科技有限公司 一种污泥处理装置

Also Published As

Publication number Publication date
KR101467204B1 (ko) 2014-12-01
EP2484641A4 (en) 2014-01-22
EP2484641A1 (en) 2012-08-08
CN101691273A (zh) 2010-04-07
CN101691273B (zh) 2012-07-04
US20120247165A1 (en) 2012-10-04
KR20120095883A (ko) 2012-08-29
JP2013505816A (ja) 2013-02-21
JP5526344B2 (ja) 2014-06-18
US8808419B2 (en) 2014-08-19

Similar Documents

Publication Publication Date Title
WO2011035460A1 (zh) 一种污水污泥浓缩脱水好氧风干一体化的方法
JP5705858B2 (ja) 汚泥濾過ケーキを好気的に空気乾燥する方法および装置
CN102276130B (zh) 污泥资源化处理装置及其对污泥进行处理的方法
CN100450947C (zh) 一种污泥干化工艺
CN206783511U (zh) 一种污泥深度脱水、干化、碳化处理处置系统
CN107867790A (zh) 一种污泥自供热脱水干燥方法及系统
CN110092557A (zh) 一种污泥资源化利用处理系统及方法
CN201842753U (zh) 城市污泥资源化利用干化装置
CN206783512U (zh) 一种污泥复合调质深度脱水、干化、碳化处理处置系统
CN108503003A (zh) 基于微波-极性介质物质的污水污泥快速干化处理工艺
CN109912139B (zh) 一种处理剩余活性污泥的方法
CN105000778B (zh) 一种污泥减量处理系统
CN116002945A (zh) 一种污泥无热干化方法
CN217368429U (zh) 一种高含盐木质粉末活性炭高效再生系统
CN213407831U (zh) 一种用于处理海绵生产废水的处理系统
CN110183083B (zh) 皮革污泥干化减量方法和装置
CN114471499A (zh) 一种高含盐木质粉末活性炭高效再生系统及方法
CN110204168A (zh) 制革污泥资源化处理方法和装置
CN218465669U (zh) 一种污泥干化装置
CN213856256U (zh) 一种分布式餐厨垃圾生化处理系统
CN211734162U (zh) 基于重介质辅助污泥薄膜干燥系统
CN212269845U (zh) 污泥干化减量处理系统
CN218811268U (zh) 一种污泥分离及高值化利用的装置
CN213793412U (zh) 一种分布式餐厨垃圾生化处理系统
CN212532713U (zh) 连续式污泥干化装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09849648

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 2012530071

Country of ref document: JP

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 20127010541

Country of ref document: KR

Kind code of ref document: A

REEP Request for entry into the european phase

Ref document number: 2009849648

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2009849648

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 13498495

Country of ref document: US