WO2023240774A1 - 排水管道污泥有机无机组分在线分离碳源提取系统及方法 - Google Patents

排水管道污泥有机无机组分在线分离碳源提取系统及方法 Download PDF

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WO2023240774A1
WO2023240774A1 PCT/CN2022/110744 CN2022110744W WO2023240774A1 WO 2023240774 A1 WO2023240774 A1 WO 2023240774A1 CN 2022110744 W CN2022110744 W CN 2022110744W WO 2023240774 A1 WO2023240774 A1 WO 2023240774A1
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sludge
module
pipe
mud
separation
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PCT/CN2022/110744
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English (en)
French (fr)
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孙永利
郑兴灿
李鹏峰
杨敏
隋克俭
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中国市政工程华北设计研究总院有限公司
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Priority to US18/038,019 priority Critical patent/US11932564B2/en
Publication of WO2023240774A1 publication Critical patent/WO2023240774A1/zh

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    • 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
    • C02F11/127—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
    • 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
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • 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
    • C02F11/12—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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/105—Phosphorus compounds
    • 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
    • C02F2201/005—Valves
    • 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
    • C02F2303/02—Odour removal or prevention of malodour
    • 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
    • C02F2303/16—Regeneration of sorbents, filters
    • 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
    • C02F2303/24—Separation of coarse particles, e.g. by using sieves or screens
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the invention belongs to the technical field of drainage, and specifically relates to an online separation carbon source extraction system and method for organic and inorganic components of drainage pipeline sludge.
  • the current treatment and disposal of dredging sludge in urban drainage pipe networks mainly has the following problems: 1 Burning or using soil as landfill cover not only fails to realize the resource utilization of organic matter in the sludge, but also produces greenhouse gases such as CO 2 and CH 4 ; 2 Under the centralized treatment mode, the transportation of large amounts of dredged sludge in the drainage pipe network is heavy workload and high transportation costs. During the transportation process, the sludge leaks and leaks, causing non-point source pollution. It is difficult to select land for the construction of centralized sludge treatment stations, and it is difficult to find a way out for sludge disposal. .
  • the mesh grille is a fixed circular mesh plate arranged horizontally;
  • the mud distribution pipe is provided with a mud outlet, and the mud outlet is located above the mesh grille;
  • the rinsing device is mainly used for intermittent rinsing of large-size particles trapped on the surface of the mesh grille and cleaning after the system is finished.
  • the rinsing device is fixedly connected to the rotating scraper, and the inlet The end is connected to the water inlet system through a hose;
  • the rectifying sludge bucket is located below the mesh grille and is used to collect sludge passing through the mesh grille and adjust the sludge flow.
  • the collected sludge enters the sludge outlet through the first sludge outlet pipe.
  • the cyclone separation module ;
  • the cyclone separation module is used for separation of organic and inorganic components of dredging sludge and extraction of organic carbon sources under high-speed cyclone conditions, and includes a variable frequency stirring motor, an adjustable stirring blade, a mud inlet pipe, a dosing system, a separation bucket, and a 2. Sludge discharge pipe, discharge valve, inorganic component discharge pipe, drain pipe and drain valve;
  • the separation bucket is arranged at the bottom of the cyclone separation module and is used to collect the inorganic components separated from the sludge.
  • the lower end of the separation bucket is provided with a discharge valve and an inorganic component discharge pipe;
  • the evacuation pipe is arranged in the middle of the cyclone separation module and is used for emptying the sludge in the main part of the cyclone separation module after the system work is completed;
  • the screen slag pressing module is used for dewatering and pressing the screen slag screened by the mesh grid, and includes a driving motor, a pressing tank and a slag discharge tank.
  • the pressing tank is connected to the slag entering tank through a vertical channel.
  • the slag discharge chute is set obliquely upward and extends out of the side of the system outer box;
  • the deodorization module is used for physical adsorption treatment of odor emitted during the desilting sludge treatment process. It adopts unpowered deodorization and includes fillers and exhaust devices.
  • the bottom surface is provided with mesh air inlets; the fillers include granular activated carbon.
  • one end of the exhaust device is connected to the top center of the deodorizing module, and the other end extends out of the side of the system outer box.
  • the height of the rotating scraper is 4cm, the length is the same as the radius of the mesh grille, and it is made of a combination of hard material and elastic rubber material.
  • the elastic rubber material is disposed freely on the rotating scraper.
  • the length of the lower part of the end is 1/3 of the length of the rotating scraper, and the height is 1/2 of the height of the rotating scraper.
  • a rinse nozzle is provided at intervals of 10-20 cm on the rinse device.
  • the rinse nozzle is arranged obliquely downward at an angle of 45° to the vertical direction.
  • the rinse nozzle is located on the side of the rotating scraper. above; above
  • the length of the slag entering tank is 1/3 of the radius of the mesh grille, the width is 100-120mm, the height is 120-150mm, and the top is 2cm higher than the surface of the mesh grille to prevent sludge from entering.
  • the bottom of the outer box of the system is provided with pulleys to facilitate the flexible movement of the system at the site of online sludge separation in the drainage pipe network.
  • the mud inlet of the mud distribution pipe is connected to the pressure mud outlet pipe, and the pressure mud outlet pipe is connected to the suction pump provided by the sludge cleaning vehicle in the drainage pipe network.
  • the suction pump passes through the mud suction pipe. It is connected to the bottom of the blocked sewage inspection well at the end of the dredging section of the drainage pipe network.
  • the second sludge outlet pipe of the cyclone separation module is connected to the sewage inspection well in the surrounding drainage pipe network through a sludge discharge pipe.
  • the separation bucket of the cyclone separation module is made of plexiglass with a thickness of 10-12cm, which facilitates the actual volume of inorganic components mainly separated from fine sand and extra-fine sand during the dredging sludge treatment process.
  • the outer wall of the system main body and the system outer box are all made of stainless steel, and the diameter of the system main body is 60-80cm.
  • control module is arranged on the front of the system outer box, and is connected to the variable frequency drive motor of the pre-treatment module, the variable frequency mixing motor of the cyclone separation module, the discharge valve and the exhaust pipe through lines.
  • the evacuation valve is electrically connected to the drive motor of the screen slag pressing module, and the power supply of the control module is a public power distribution cabinet around the dredging pipe section of the drainage pipe network or a vehicle-mounted diesel generator at the dredging site.
  • embodiments of the present invention provide a method for online separation of organic and inorganic components of drainage pipe sludge and carbon source extraction, which uses the above-mentioned online separation of organic and inorganic components of drainage pipe sludge and carbon source extraction system for extraction, including the following steps :
  • a. Use the suction pump provided by the drainage pipe network sludge cleaning vehicle to pump the desilted sludge in the drainage pipe network through the suction pipe and pressure sludge outlet pipe to the mud distribution pipe of the pre-treatment module, and then rotate the scraper Under the continuous push of the mud pipe, the mud from the mud distribution pipe is spread on the surface of the mesh grille. Most of the sludge quickly passes through the circular mesh on the mesh grille and enters the cone below the mesh grille under the action of gravity. At the same time, the large-sized particles in the dredging sludge are trapped on the upper surface of the mesh grille.
  • the sludge processed by the pre-treatment module in step a passes through the first sludge outlet pipe and the chemicals added by the dosing system vertically enter the main part of the cyclone separation module through the sludge inlet pipe, and is driven by a variable frequency stirring motor.
  • the organic components that is, the organic carbon source wrapped and adsorbed on the surface of fine sand and other substances in the dredging sludge, are stripped into the liquid phase.
  • the low-density sludge mixture mainly composed of organic components, is in the middle and upper part of the cyclone separation module.
  • the inorganic inert components such as fine sand and some extra-fine sand in the dredged sludge are removed under the combined action of centrifugal force and gravity. Enter the bottom separation bucket; whether the dosing system is running is specifically determined based on the actual phosphate concentration in the dredging sludge and the demand for phosphorus resources;
  • the sludge processed by the cyclone separation module obtained in step b is discharged into the nearby sewage inspection well of the surrounding drainage pipe network through the second sludge outlet pipe and the sludge discharge pipe, and the outlet of the sludge discharge pipe is connected to the sewage inspection well.
  • the inorganic inert components separated in step b are combined with the actual volume and passed through the inorganic unit through the control of the emptying valve and the discharge valve.
  • the discharge pipes are intermittently discharged to special collection buckets, and uniformly transported to surrounding urban sewage treatment plants for further sand-water separation and sedimentation separation of phosphorus-containing chemical sludge;
  • the odorous gases such as hydrogen sulfide emitted during the treatment of steps a and b naturally enter the deodorization module set at the upper part of the system.
  • the treated odor is connected to the cylindrical deodorizer. Exhaust air from the upper center of the module.
  • the volatile matter ratio VSS/SS of the sludge processed by the cyclone separation module is not less than 0.5, and the carbon-nitrogen ratio COD/TN is not less than 15, and can be resourcefully utilized for high emissions at the end of the drainage pipe network.
  • a supplementary carbon source for standard urban sewage treatment plants; the VSS/SS of inorganic inert components such as fine sand separated by the cyclone separation module is less than 3%, and can be resourcefully utilized as engineering construction materials.
  • the circular fixed mesh grille of the present invention does not need to be driven by a motor to rotate during the pre-treatment process of sludge removal, and is always in a horizontal static state. It achieves continuous normal operation through the rotation of the rotating scraper instead of flushing with high-pressure water. Filtration, the effective filtration area accounts for more than 95%. Compared with traditional grilles, the effective filtration area (generally less than 25%) and filtration flux are significantly improved.
  • Figure 1 is a schematic structural diagram of a carbon source extraction system for online separation of organic and inorganic components of drainage pipe sludge according to an embodiment of the present invention.
  • Figure 4 is a schematic structural diagram of the deodorization module in the extraction system of Figure 1.
  • the rinsing device 4 is mainly used for intermittent rinsing of large-size particles trapped on the surface of the mesh grille 2 and cleaning after the system is finished.
  • the rinsing device 4 is fixedly connected to the rotating scraper 3, and the inlet end is connected through a hose. 10 is connected to the water inlet system 9, and the hose 10 is lined with steel wire;
  • the slag entry tank 8 is provided at the diagonal corner of the mud distribution pipe 7 and close to the edge of the mesh grille 2, so that the scraper 3 can be rotated to scrape in the large-size particles in the dredging sludge trapped by the mesh grille 2;
  • the cyclone separation module 18 is used for separation of organic and inorganic components of dredging sludge and extraction of organic carbon sources under high-speed cyclone conditions.
  • the height is 75-80cm and includes a variable frequency stirring motor 21, an adjustable stirring blade 22, a mud inlet pipe 20, Dosing system 19, separation bucket 23, second mud outlet pipe 26, discharge valve 24, inorganic component discharge pipe 25, drain pipe 27 and drain valve 28;
  • the deodorizing module 29 is a cylindrical structure with a height of 15-20cm.
  • the bottom surface is provided with a mesh air inlet. It adopts unpowered deodorization and is used for physical adsorption treatment of odor emitted during the desilting sludge treatment process.
  • It includes a filler 30 and an exhaust device 31, with a mesh air inlet hole provided on the bottom; the filler 30 includes granular activated carbon, one end of the exhaust device 31 is connected to the top center of the deodorizing module 29, and the other end extends out of the side of the system outer box 33.
  • the height of the rotating scraper 3 is 4cm, and the length is the same as the radius of the mesh grille 2. It is made of a combination of hard material 304 stainless steel and elastic rubber material.
  • the elastic rubber material is set at the lower part of the free end of the rotating scraper 3, and the length is The length of the scraper 3 is 1/3, the height is 1/2 of the height of the rotating scraper 3, and the remaining main part is made of hard material.
  • a rinse nozzle 5 is provided at intervals of 10-20 cm on the rinse device 4.
  • the rinse nozzle 5 is arranged obliquely downward at an angle of 45° to the vertical direction.
  • the rinse nozzle 5 is located above the rotating scraper 3;
  • the length of the slag entering tank 8 is 1/3 of the radius of the mesh grille 2, the width is 100-120mm, and the height is 120-150mm.
  • the top is 2cm higher than the surface of the mesh grille 2 to prevent sludge from entering.
  • the bottom of the system outer box 33 is provided with pulleys 34 to facilitate the flexible movement of the system at the drainage pipe network 40 dredging and sludge online separation site.
  • the second sludge outlet pipe 26 of the cyclone separation module 18 is connected to the sewage inspection well 42 in the surrounding drainage pipe network 40 through the sludge discharge pipe 41 .
  • the separation bucket 23 of the cyclone separation module 18 is made of plexiglass with a thickness of 10-12cm, which facilitates observation of the actual volume of the inorganic components separated mainly from fine sand and extra-fine sand during the dredging sludge treatment process;
  • the outer wall of the system main body and the system outer box 33 are made of stainless steel, and the diameter of the system main body is 60-80cm.
  • the control module 32 is arranged on the front of the system outer box 33 and is connected to the variable frequency drive motor 6 of the pretreatment module 1, the variable frequency mixing motor 21 of the cyclone separation module 18, the discharge valve 24 and the exhaust valve installed on the exhaust pipe 27 through lines.
  • the valve 28 is electrically connected to the drive motor 15 of the screen slag pressing module 14, and the power supply of the control module 32 is the public power distribution cabinet around the dredging pipe section of the drainage pipe network 40 or the vehicle-mounted diesel generator at the dredging site.
  • the deodorization module 29, the pre-treatment module 1 and the cyclone separation module 18 are spliced together to facilitate the maintenance and repair of the variable frequency drive motor 6, the variable frequency mixing motor 21 and the drive motor 15 and the adjustment of the installation height of the adjustable stirring paddle 22.
  • the large-size particles in the dredging sludge are trapped on the upper surface of the mesh grille 2, and pass through the mesh grille 2 at intervals of 5-10 minutes.
  • the high-pressure water column rinses the rinse nozzle 5 of the intermittent rinse device 4 for one operation, it passes through the square slag entering slot 8 with a width of 100-120mm and enters the pressing slot of the screen slag pressing module 14 through the vertical channel 17.
  • the screen slag discharged from the slag discharge chute 16 is collected in a special collection bucket and then transported to the surrounding garbage transfer station as domestic waste;
  • step a the sludge treated by the pre-treatment module 1 passes through the first sludge outlet pipe 13 and the chemicals added by the dosing system 19 vertically enter the main part of the cyclone separation module 18 through the sludge inlet pipe 20.
  • the organic components namely organic carbon
  • the source is stripped into the liquid phase, and the low-density sludge mixture dominated by organic components is in the middle and upper part of the cyclone separation module 18.
  • inorganic inert components such as fine sand and some extra-fine sand in the sludge are removed. It enters the bottom separation bucket 23 under the combined action of centrifugal force and gravity; whether the dosing system 19 is running is specifically determined based on the actual phosphate concentration in the dredging sludge (whether ⁇ 10 mg/L) and the phosphorus resource utilization needs;
  • the sludge processed by the cyclone separation module 18 obtained in step b is discharged into the nearby sewage inspection well 42 of the surrounding drainage pipe network 40 through the second sludge outlet pipe 26 and the sludge discharge pipe 41, and the outlet of the sludge discharge pipe 41 It is connected below the water level of the sewage inspection well 42 to avoid the ineffective loss of part of the carbon source extracted from the dredging sludge due to water drop and oxygenation; the inorganic inert components separated in step b are combined with the actual volume through the drain valve 28 and control the discharge valve 24 to intermittently discharge to a special collection bucket through the inorganic component discharge pipe 25, and uniformly transport it to surrounding urban sewage treatment plants for further sand-water separation and sedimentation separation of phosphorus-containing chemical sludge;
  • the malodorous gases such as hydrogen sulfide emitted during the treatment of steps a and b naturally enter the deodorization module 29 provided at the upper part of the system.
  • the treated odor is connected to the cylindrical deodorization module. 29 is discharged from the exhaust device 31 in the upper center.
  • the volatile matter ratio VSS/SS and the carbon-nitrogen ratio COD/TN of the sludge processed by the cyclone separation module 18 are not less than 0.5 and 15 respectively, and can be resourcefully utilized for high-discharge standard urban sewage treatment at the end of the drainage pipe network 40 A supplementary carbon source for the plant; the VSS/SS of inorganic inert components such as fine sand separated by the cyclone separation module 18 is less than 3%, and can be resourcefully utilized as engineering construction materials.
  • a method for online separation of organic and inorganic components in drainage pipe sludge and carbon source extraction is used for extraction, including the following steps:
  • the malodorous gases such as hydrogen sulfide emitted during the treatment process of steps a and b naturally enter the deodorization module 29 located at the upper part of the system.
  • the treated odor gas is connected to the cylindrical deodorizer
  • the exhaust device 31 in the upper center of the module 29 discharges.
  • the volatile matter ratio VSS/SS and the carbon-nitrogen ratio COD/TN of the sludge processed by the cyclone separation module 18 are 0.6 and 20 respectively, and can be resourcefully utilized in the high-discharge standard urban sewage treatment plant at the end of the drainage pipe network 40 Supplement carbon source; the volatile matter ratio VSS/SS of inorganic inert components such as fine sand separated by the cyclone separation module 18 is 2.5%, and can be resourcefully utilized as engineering construction materials.
  • the screen slag pressing module 14 After being rinsed by the high-pressure water column of the rinse nozzle 5 of the intermittent rinse device 4 that runs every 5 minutes, it enters the screen slag pressing module 14 through the vertical channel 17 through the square slag entry chute 8 with a width of 120 mm for dehydration and pressing. , the screen slag discharged from the slag discharge chute 16 is collected in a special collection bucket and then transported as domestic waste to the nearby garbage transfer station;
  • the inorganic inert components such as fine sand and some extra-fine sand in the dredged sludge are removed under the combined action of centrifugal force and gravity. Enter the separation bucket 23; whether the dosing system 19 is running is specifically determined based on the actual phosphate concentration in the dredging sludge (whether ⁇ 10 mg/L) and the phosphorus resource utilization needs;
  • the sludge processed by the cyclone separation module 18 obtained in step b is discharged into the nearby sewage inspection well 42 of the surrounding drainage pipe network 40 through the second sludge outlet pipe 26 and the sludge discharge pipe 41, and the outlet of the sludge discharge pipe 41 It is connected below the water level of the sewage inspection well 42 to avoid the ineffective loss of part of the carbon source extracted from the dredging sludge due to water drop and oxygenation; the separated inorganic inert components such as fine sand obtained in step b are combined with the actual volume through the discharge
  • the empty valve 28 and the discharge valve 24 are controlled to intermittently discharge the inorganic components to a special collection bucket through the inorganic component discharge pipe 25, and are uniformly transported to the surrounding urban sewage treatment plants for further sand-water separation and sedimentation separation of phosphorus-containing chemical sludge;
  • the circular mesh with an inner diameter of 2.5mm enters the conical rectifying mud bucket 11 at the bottom of the mesh grille 2, and at the same time, the large-size particles in the dredging sludge are trapped on the surface of the mesh grille 2 , after being rinsed by the high-pressure water column of the rinse nozzle 5 of the intermittent rinse device 4 that runs every 10 minutes, it passes through the square slag entry chute 8 with a width of 100 mm and enters the screen slag pressing module 14 through the vertical channel 17 for dehydration and pressing.
  • the screen slag discharged from the slag discharge chute 16 is collected in a special collection bucket and then transported to the nearby garbage transfer station as domestic waste;
  • the pre-treated sludge obtained in step a enters the cyclone separation module 18 vertically through the first sludge outlet pipe 13 and the chemical added by the dosing system 19 through the sludge inlet pipe 20.
  • the organic components that is, the organic carbon source, that are wrapped and adsorbed on the surface of fine sand and other substances in the dredging sludge are stripped into the liquid phase.
  • the low-density sludge mixture mainly composed of organic components is located in the middle and upper part of the cyclone separation module 18.
  • the inorganic inert components such as fine sand and some extra-fine sand in the dredged sludge are affected by the comprehensive action of centrifugal force and gravity. down into the separation bucket 23; whether the dosing system 19 is running is specifically determined based on the actual phosphate concentration in the dredging sludge (whether ⁇ 10 mg/L) and the phosphorus resource utilization needs;
  • the sludge processed by the cyclone separation module 18 obtained in step b is discharged into the nearby sewage inspection well 42 of the surrounding drainage pipe network 40 through the second sludge outlet pipe 26 and the sludge discharge pipe 41, and the outlet of the sludge discharge pipe 41 It is connected below the water level of the sewage inspection well 42 to avoid the ineffective loss of part of the carbon source extracted from the dredging sludge due to water drop and oxygenation; the separated inorganic inert components such as fine sand obtained in step b are combined with the actual volume through the discharge
  • the empty valve 28 and the discharge valve 24 are controlled to intermittently discharge the inorganic components to a special collection bucket through the inorganic component discharge pipe 25, and are uniformly transported to the surrounding urban sewage treatment plants for further sand-water separation and sedimentation separation of phosphorus-containing chemical sludge;
  • the treated odor gas is connected to the cylindrical
  • the exhaust device 31 at the upper center of the deodorizing module 29 discharges air.
  • the volatile matter ratio VSS/SS and the carbon-nitrogen ratio COD/TN of the sludge processed by the cyclone separation module 18 are 0.5 and 15 respectively, and can be resourcefully utilized in high-discharge standard urban sewage treatment plants at the end of the drainage pipe network 40 Supplement carbon source; the volatile matter ratio VSS/SS of inorganic inert components such as fine sand separated by the cyclone separation module 18 is 1.5%, and can be resourcefully utilized as engineering construction materials.

Abstract

本发明涉及一种排水管道污泥有机无机组分在线分离碳源提取系统及方法，所述提取系统包括系统外箱，所述系统外箱内设置有系统主体，所述系统主体从上至下依次包括拼接在一起的除臭模块、前处理模块及旋流分离模块，所述旋流分离模块的上部侧壁设置有栅渣压榨模块，所述前处理模块、旋流分离模块及栅渣压榨模块分别与控制模块电连接。通过采用排水管道污泥有机无机组分在线分离碳源提取系统对排水管网清淤污泥的在线就地快速处理，可解决现有城镇排水管网清淤污泥集中处理处置方法普遍存在的产生CO2、CH4等温室气体、大量清淤污泥运输工作量大、运输过程污泥跑冒滴漏产生面源污染、集中污泥处理站建设用地选取难等实际问题。

Description

排水管道污泥有机无机组分在线分离碳源提取系统及方法 技术领域
本发明属于排水技术领域，具体涉及一种排水管道污泥有机无机组分在线分离碳源提取系统及方法。
背景技术
与欧美等发达国家不同，我国城市污水收集管网普遍存在高水位、低流速等实际运行问题，导致污水中大量颗粒态有机物等沉积于管道，部分管段沉积污泥深度甚至达管径的50％，是当前我国城市生活污水集中收集率偏低的主要成因，据统计，2020年全国平均污水集中收集率仅64％，很多城市只有20％-30％。管网沉积污泥还会影响污水收集效能、厌氧产生大量CH 4等温室气体，并且在雨水冲刷下会成为城市水体的重要污染源。
现状城市排水管网清淤污泥的处理处置主要存在以下问题：①焚烧或作为填埋覆盖用土不但未实现污泥中有机质的资源化利用，还会产生CO 2、CH 4等温室气体；②集中处理模式下，排水管网大量清淤污泥运输工作量大、运输成本高，运输过程污泥跑冒滴漏产生面源污染，集中污泥处理站建设用地选取难，污泥处置出路难等。
因此，亟需提出一种排水管网清淤污泥有机无机组分在线分离碳源提取系统及方法，对创新城镇排水管网清淤污泥处理处置模式、实现城市污水集中收集率提升和排水系统碳减排、助力我国排水行业绿色低碳高质量发展具有重要现实意义。
发明内容
本发明的目的是克服现有技术存在的不足，提供一种排水管道污泥有机无机组分在线分离碳源提取系统及方法，通过采用排水管道污泥有机无机组分在线分离碳源提取系统对排水管网清淤污泥的在线就地快速处理，可解决现有城镇排水管网清淤污泥集中处理处置方法普遍存在的产生CO 2、CH 4等温室气体、大量清淤污泥运输工作量大、运输过程污泥跑冒滴漏产生面源污染、集中污泥处理站建设用地选取难等实际问题。
为实现以上技术目的，本发明实施例采用的技术方案是：
第一方面，本发明实施例提供了一种排水管道污泥有机无机组分在线分离碳源提取系统，包括系统外箱，所述系统外箱内设置有系统主体，所述系统主体从上至下依次包括拼接在一起的除臭模块、前处理模块及旋流分离模块，所述旋流分离模块的上部侧壁设置有栅渣压榨模块，所述前处理模块、旋流分离模块及栅渣压榨模块分别与控制模块电连接；
所述前处理模块用于筛除清淤污泥中的大粒径颗粒物，包括网板格栅、转动刮板、淋洗装置、变频驱动电机、配泥管、入渣槽、整流泥斗、排泥阀和第一出泥管；
所述网板格栅为水平设置的固定式圆形网板；
所述配泥管上设置有出泥口，所述出泥口位于所述网板格栅的上方；
所述转动刮板的底部与所述网板格栅的上表面相切，所述转动刮板由变频驱动电机驱动，用于所述配泥管出泥在所述网板格栅表面的分布；
所述淋洗装置主要用于所述网板格栅表面截留的大粒径颗粒物的间歇性淋洗和系统工作结束后的清洗，所述淋洗装置固定连接在所述转动刮板上，进口端通过软管与进水系统连接；
所述入渣槽设置于所述配泥管的对角并靠近所述网板格栅的边缘，便于所述转动刮板将所述网板格栅截留的清淤污泥中的大粒径颗粒物刮入；
所述整流泥斗位于所述网板格栅的下方，用于收集通过所述网板格栅的污泥并对污泥流量进行调节，收集的污泥经所述第一出泥管进入所述旋流分离模块；
所述旋流分离模块用于高速旋流状态下清淤污泥有机无机组分分离和有机碳源提取，包括变频搅拌电机、可调节搅拌桨、进泥管、加药系统、分离斗、第二出泥管、排放阀、无机组分排放管、排空管及排空阀；
所述变频搅拌电机驱动可调节搅拌桨转动，所述可调节搅拌桨设置在所述旋流分离模块的中上部；
所述进泥管竖直设置在所述第二出泥管的对侧，所述进泥管的进口端通过三通分别与所述加药系统及第一出泥管连接，出口端设置在所述旋流分离模块运行液位以下15-20cm；
所述分离斗设置在所述旋流分离模块的底部，用于收集污泥中分离出的无机组分，所述分离斗的下端设置有排放阀及无机组分排放管；
所述排空管设置于旋流分离模块的中部，用于系统工作结束后旋流分离模块主体部分污泥的排空；
所述栅渣压榨模块用于所述网板格栅筛除的栅渣的脱水压榨，包括驱动电机、压榨槽和出渣槽，所述压榨槽通过竖直通道与所述入渣槽连接，所述出渣槽斜向上设置，并伸出所述系统外箱侧面；
所述除臭模块用于清淤污泥处理过程中散发的臭气的物理吸附处理，采用无动力除臭，包括填料和排气装置，底面设置网状进气孔；所述填料包括颗粒活性炭，所述排气装置一端与除臭模块的顶部中心部位连接，另一端伸出所述系统外箱侧面。
进一步地，所述转动刮板的高度为4cm，长度与所述网板格栅的半径相同，由硬质材料和弹性胶皮材料组合制成，所述弹性胶皮材料设置在所述转动刮板自由端的下部，长度为所述转动刮板长度的1/3，高度为所述转动刮板高度的1/2。
进一步地，所述淋洗装置上每间隔10-20cm设置有一个淋洗喷头，所述淋洗喷头与竖直方向呈45°斜向下设置，所述淋洗喷头位于所述转动刮板的上方；
所述入渣槽的长度是所述网板格栅半径的1/3，宽度为100-120mm，高度为120-150mm，顶部比所述网板格栅表面高出2cm，防止污泥进入。
进一步地，所述系统外箱的底部设置有滑轮，便于系统在排水管网清淤污泥在线分离现场的灵活移动。
进一步地，所述配泥管的进泥口与压力出泥管连接，所述压力出泥管与排水管网污泥清通车自带的抽吸泵连接，所述抽吸泵通过吸泥管与排水管网清淤段末端封堵的污水检查井的底部连接。
进一步地，所述旋流分离模块的第二出泥管通过排泥管道与周边排水管网中的污水检查井连接。
进一步地，所述旋流分离模块的分离斗采用厚度为10-12cm的有机玻璃制成，便于清淤污泥处理过程中分离出的以细砂和特细砂为主的无机组分实际容积的观察；所述系统主体的外壁及系统外箱均采用不锈钢材料，系统主体的直径为60-80cm。
进一步地，所述控制模块设置于所述系统外箱正面，通过线路分别与所述前处理模块的变频驱动电机、所述旋流分离模块的变频搅拌电机、排放阀和设置于排空管上的排空阀及所述栅渣压榨模块的驱动电机电连接，所述控制模块的供电电源为排水管网清淤管段周边的公共配电柜或清淤现场车载柴油发电机。
第二方面，本发明实施例提供了一种排水管道污泥有机无机组分在线分离碳源提取方法，利用上述的排水管道污泥有机无机组分在线分离碳源提取系统进行提取，包括以下步骤：
a、利用排水管网污泥清通车自带的抽吸泵将排水管网中的清淤污泥经吸泥管和压力出泥管抽至前处理模块的配泥管中，在转动刮板的连续推动下，所述配泥管出泥在网板格栅的表面布泥，大部分污泥在重力作用下快速通过网板格栅上的圆形网孔进入网板格栅下方的圆锥形整流泥斗，同时清淤污泥中大粒径颗粒物被截留于网板格栅的上表面，经间歇运行的淋洗装置的淋洗喷头的高压水柱淋洗后，通过入渣槽经竖直通道进入栅渣压榨模块的压榨槽进行脱水压榨处理，出渣槽排出的栅渣采用专用收集桶收集后作为生活垃圾就近运至周边垃圾中转站；
b、步骤a中经前处理模块处理后的污泥经第一出泥管和加药系统投加的药剂一起经进泥管竖直进入旋流分离模块的主体部分，在由变频搅拌电机驱动的可调节搅拌桨的高速旋转作用下，经水力停留时间1-3min的旋流分离，清淤污泥中细砂等物质表面包裹和吸附的有机组分即有机碳源被剥离进入液相，以有机组分为主的密度小的污泥混合液处于旋流分离模块的中上部，同时清淤污泥中的细砂、部分特细砂等无机惰性组分在离心力和重力的综合作用下进入底部分离斗中；其中所述加药系统是否运行根据清淤污泥中实际磷酸盐浓度和磷资源化需求进行具体确定；
c、步骤b所得的经旋流分离模块处理后的污泥经第二出泥管和排泥管道就 近排入周边排水管网的污水检查井，且排泥管道的出口接至污水检查井的水位以下，避免跌水充氧导致从清淤污泥中提取的部分碳源被无效损耗；步骤b分离出的所述无机惰性组分结合实际容积通过排空阀和排放阀的控制经无机组分排放管间歇排放至专用收集桶，并统一运输至周边城镇污水处理厂进行进一步砂水分离和含磷化学污泥的沉淀分离；
d、步骤a和步骤b处理过程中散发的硫化氢等恶臭气体自然进入设置于系统上部的除臭模块，通过颗粒态活性炭填料的物理吸附处理，处理后的臭气由接至圆柱形除臭模块上部中心的排气装置排出。
进一步地，经所述旋流分离模块处理后的污泥的挥发分比例VSS/SS不低于0.5、碳氮比COD/TN不低于15，能够资源化利用于排水管网末端的高排放标准城镇污水处理厂的补充碳源；经所述旋流分离模块分离出的细砂等无机惰性组分的VSS/SS低于3％，能够资源化利用于工程建筑材料。
本发明实施例的技术方案具有以下有益效果：
1、本发明通过将排水管道污泥有机无机组分在线分离碳源提取系统直接嫁接于排水管网清通车污泥抽吸泵的出泥口，对排水管网清淤污泥进行在线就地快速处理，实现无机组分的分离和碳源的提取，可解决现有城镇排水管网清淤污泥集中处理处置方法普遍存在的污泥有机质资源化利用率低、产生CO 2、CH 4等温室气体、大量清淤污泥运输工作量大、运输过程污泥跑冒滴漏产生面源污染、集中污泥处理站建设用地选取难、污泥处置出路难等实际问题。
2、与现有排水管网清淤污泥集中处理处置方法相比，本发明具有工艺单元一体化集成、清淤污泥在线就地处理、污泥资源化利用率高、提升城市生活污水集中收集率、降低排水系统碳排放、节约城镇污水厂碳源投加成本等优点。
3、本发明的圆形固定式网板格栅在清淤污泥前处理过程中无需电机驱动而转动，一直处于水平静止状态，通过转动刮板的旋转而非利用高压水的冲洗实现连续正常过滤，有效过滤面积占比高达95％以上，与传统格栅相比，有效过滤面积(一般不足25％)和过滤通量显著提升。
4、本发明针对性、实用性和可操作性强，可为城镇排水管网清淤污泥的处理提供新模式，对助力我国排水行业绿色低碳高质量发展具有重要现实意义。
附图说明
图1是本发明实施例排水管道污泥有机无机组分在线分离碳源提取系统的结构示意图。
图2是图1提取系统中前处理模块的结构示意图。
图3是图1提取系统中旋流分离模块结构示意图。
图4是图1提取系统中除臭模块的结构示意图。
附图标记说明：1-前处理模块；2-网板格栅；3-转动刮板；4-淋洗装置；5-淋洗喷头；6-变频驱动电机；7-配泥管；8-入渣槽；9-进水系统；10-软管；11-整流泥斗；12-排泥阀；13-第一出泥管；14-栅渣压榨模块；15-驱动 电机；16-出渣槽；17-竖直通道；18-旋流分离模块；19-加药系统；20-进泥管；21-变频搅拌电机；22-可调节搅拌桨；23-分离斗；24-排放阀；25-无机组分排放管；26-第二出泥管；27-排空管；28-排空阀；29-除臭模块；30-填料；31-排气装置；32-控制模块；33-系统外箱；34-滑轮；35-排水管网污泥清通车；36-抽吸泵；37-压力出泥管；38-吸泥管；39-封堵的污水检查井；40-排水管网；41-排泥管道；42-污水检查井。
具体实施方式
如图1-4所示，一种排水管道污泥有机无机组分在线分离碳源提取系统，包括系统外箱33及其内设置的系统主体，系统主体呈圆柱形，从上至下依次包括拼接在一起的除臭模块29、前处理模块1及旋流分离模块18，其中旋流分离模块18的上部侧壁设置有栅渣压榨模块14，前处理模块1、旋流分离模块18及栅渣压榨模块14分别与控制模块32电连接；
前处理模块1用于筛除清淤污泥中的大粒径颗粒物，主体部分高度30-40cm，包括网板格栅2、转动刮板3、淋洗装置4、变频驱动电机6、配泥管7、入渣槽8、整流泥斗11、排泥阀12和第一出泥管13；
其中网板格栅2为水平设置的固定式圆形网板，其上均匀设置有孔径为2-3mm的圆形网孔；配泥管7上等距离设置有3-4个出泥口，出泥口位于网板格栅2的上方；转动刮板3的底部与网板格栅2的上表面相切，转动刮板3由变频驱动电机6驱动，用于配泥管7出泥在网板格栅2表面的分布；
淋洗装置4主要用于网板格栅2表面截留的大粒径颗粒物的间歇性淋洗和系统工作结束后的清洗，淋洗装置4固定连接在转动刮板3上，进口端通过软管10与进水系统9连接，所述软管10带有钢丝内衬；
入渣槽8设置于配泥管7的对角并靠近网板格栅2的边缘，便于转动刮板3将网板格栅2截留的清淤污泥中的大粒径颗粒物刮入；
整流泥斗11位于所述网板格栅2的下方，用于收集通过网板格栅2的污泥并对污泥流量进行调节，收集的污泥经第一出泥管13进入旋流分离模块18；
旋流分离模块18用于高速旋流状态下清淤污泥有机无机组分分离和有机碳源提取，高度为75-80cm，包括变频搅拌电机21、可调节搅拌桨22、进泥管20、加药系统19、分离斗23、第二出泥管26、排放阀24、无机组分排放管25、排空管27及排空阀28；
变频搅拌电机21驱动可调节搅拌桨22转动，转速结合污泥无机有机组分分离效果进行调节，可调节搅拌桨22设置在旋流分离模块18的中上部，可调节搅拌桨22的安装高度、搅拌转速和搅拌桨型式均根据无机组分分离效果进行调整；
进泥管20竖直设置在所述第二出泥管26的对侧，进泥管20的进口端通过三通分别与加药系统19及第一出泥管13连接，出口端设置在旋流分离模块运行液位以下15-20cm；加药系统19投加药剂主要为氢氧化钙溶液，主要用于磷酸盐浓度≥10mg/L下污泥中磷酸盐的强化去除和资源化；
分离斗23设置在旋流分离模块18的底部，用于收集污泥中分离出的无机组分，分离斗23的下端设置有排放阀24及无机组分排放管25；
排空管27设置于旋流分离模块18的中部，用于系统工作结束后旋流分离模块18主体部分污泥的排空；
栅渣压榨模块14用于网板格栅2筛除的栅渣的脱水压榨，包括驱动电机15、压榨槽和出渣槽16，压榨槽通过竖直通道17与入渣槽8连接，出渣槽16斜向上45°设置，并伸出所述系统外箱33侧面；
除臭模块29为圆柱形结构，高度为15-20cm，底面设置网状进气孔，采用无动力除臭，用于清淤污泥处理过程中散发的臭气的物理吸附处理，包括填料30和排气装置31，底面设置网状进气孔；填料30包括颗粒活性炭，排气装置31一端与除臭模块29的顶部中心部位连接，另一端伸出系统外箱33侧面。
转动刮板3的高度为4cm，长度与网板格栅2的半径相同，由硬质材料304不锈钢和弹性胶皮材料组合制成，弹性胶皮材料设置在转动刮板3自由端的下部，长度为转动刮板3长度的1/3，高度为转动刮板3高度的1/2，其余主体部分采用硬质材料制成。
淋洗装置4上每间隔10-20cm设置有一个淋洗喷头5，所述淋洗喷头5与竖直方向呈45°斜向下设置，淋洗喷头5位于转动刮板3的上方；
入渣槽8的长度是网板格栅2半径的1/3，宽度为100-120mm，高度为120-150mm，顶部比网板格栅2表面高出2cm，防止污泥进入。
系统外箱33的底部设置有滑轮34，便于系统在排水管网40清淤污泥在线分离现场的灵活移动。
配泥管7的进泥口与压力出泥管37连接，压力出泥管37与排水管网污泥清通车35自带的抽吸泵36连接，抽吸泵36通过吸泥管38与排水管网40清淤段末端封堵的污水检查井39的底部连接。
旋流分离模块18的第二出泥管26通过排泥管道41与周边排水管网40中的污水检查井42连接。
旋流分离模块18的分离斗23采用厚度为10-12cm的有机玻璃制成，便于清淤污泥处理过程中分离出的以细砂和特细砂为主的无机组分实际容积的观察；系统主体的外壁及系统外箱33均采用不锈钢材料，系统主体的直径为60-80cm。
控制模块32设置于系统外箱33正面，通过线路分别与前处理模块1的变频驱动电机6、旋流分离模块18的变频搅拌电机21、排放阀24和设置于排空管27上的排空阀28及栅渣压榨模块14的驱动电机15电连接，控制模块32的供电电源为排水管网40清淤管段周边的公共配电柜或清淤现场车载柴油发电机。
除臭模块29、前处理模块1及旋流分离模块18拼接，便于变频驱动电机6、变频搅拌电机21、驱动电机15的检修保养和可调节搅拌桨22安装高度的调整。
一种排水管道污泥有机无机组分在线分离碳源提取方法，利用上述排水管道污泥有机无机组分在线分离碳源提取系统进行提取，包括以下步骤：
a、利用排水管网污泥清通车35自带的抽吸泵36将排水管网40中的清淤污泥经吸泥管38和压力出泥管37抽至前处理模块1的配泥管7中，在转动刮板3的连续推动下，所述配泥管7出泥在网板格栅2的表面布泥，大部分污泥在重力作用下快速通过网板格栅2上内径2-3mm的圆形网孔进入网板格栅2下方的圆锥形整流泥斗11，同时清淤污泥中大粒径颗粒物被截留于网板格栅2的上表面，经每间隔5-10min运行1次的间歇运行的淋洗装置4的淋洗喷头5的高压水柱淋洗后，通过宽度为100-120mm的方形入渣槽8经竖直通道17进入栅渣压榨模块14的压榨槽进行脱水压榨处理，出渣槽16排出的栅渣采用专用收集桶收集后作为生活垃圾就近运至周边垃圾中转站；
b、步骤a中经前处理模块1处理后的污泥经第一出泥管13和加药系统19投加的药剂一起经进泥管20竖直进入旋流分离模块18的主体部分，在由变频搅拌电机21驱动的可调节搅拌桨22的高速旋转作用下，经水力停留时间1-3min的旋流分离，清淤污泥中细砂等物质表面包裹和吸附的有机组分即有机碳源被剥离进入液相，以有机组分为主的密度小的污泥混合液处于旋流分离模块18的中上部，同时清淤污泥中的细砂、部分特细砂等无机惰性组分在离心力和重力的综合作用下进入底部分离斗23中；其中所述加药系统19是否运行根据清淤污泥中实际磷酸盐浓度(是否≥10mg/L)和磷资源化需求进行具体确定；
优选地，所述加药系统19投加药剂主要为氢氧化钙溶液，主要用于磷酸盐浓度≥10mg/L时污泥中磷酸盐的强化去除和资源化利用；当磷酸盐浓度≥10mg/L时，加药系统运行，当磷酸盐浓度<10mg/L时，加药系统不运行；
c、步骤b所得的经旋流分离模块18处理后的污泥经第二出泥管26和排泥管道41就近排入周边排水管网40的污水检查井42，且排泥管道41的出口接至污水检查井42的水位以下，避免跌水充氧导致从清淤污泥中提取的部分碳源被无效损耗；步骤b分离出的所述无机惰性组分结合实际容积通过排空阀28和排放阀24的控制经无机组分排放管25间歇排放至专用收集桶，并统一运输至周边城镇污水处理厂进行进一步砂水分离和含磷化学污泥的沉淀分离；
d、步骤a和步骤b处理过程中散发的硫化氢等恶臭气体自然进入设置于系统上部的除臭模块29，通过填料30的物理吸附处理，处理后的臭气由接至圆柱形除臭模块29上部中心的排气装置31排出。
经旋流分离模块18处理后的污泥的挥发分比例VSS/SS和碳氮比COD/TN分别不低于0.5和15，能够资源化利用于排水管网40末端的高排放标准城镇污水处理厂的补充碳源；经旋流分离模块18分离出的细砂等无机惰性组分的VSS/SS低于3％，能够资源化利用于工程建筑材料。
在本发明的描述中，需要理解的是，方位词如“上、下”“左、右”等所指示的方位或位置关系通常是基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，在未作相反说明的情况下，这些方位词并不指示和暗 示所指的装置或元件必须具有特定的方位或者以特定的方位构造和操作，因此不能理解为对本发明保护范围的限制。
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合附图及实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅用以解释本发明，并不用于限定本发明。
实施例1
一种排水管道污泥有机无机组分在线分离碳源提取方法，利用上述排水管道污泥有机无机组分在线分离碳源提取系统进行提取，包括以下步骤：
a、利用排水管网污泥清通车35自带的抽吸泵36将排水管网中的清淤污泥经吸泥管38和压力出泥管37抽至前处理模块1的配泥管7中，在高度为4cm的转动刮板3的连续推动下，配泥管7出泥在网板格栅2的表面布泥，大部分污泥在重力作用下快速通过水平设置的圆形网板格栅2的内径3mm的圆形网孔进入网板格栅2下方的圆锥形整流泥斗11，同时清淤污泥中大粒径颗粒物被截留于网板格栅2的表面，经每间隔10min运行一次的间歇运行淋洗装置4的淋洗喷头5的高压水柱淋洗后，通过宽度为100mm的方形入渣槽8经竖直通道17进入栅渣压榨模块14进行脱水压榨处理，出渣槽16排出的栅渣采用专用收集桶收集后作为生活垃圾就近运至周边垃圾中转站；
b、经前处理模块1处理后的污泥经第一出泥管13和加药系统19投加的药剂一起经进泥管20竖直进入旋流分离模块18，在由变频搅拌电机21驱动的可调节搅拌桨22的高速旋转作用下，经水力停留时间1min的旋流分离，清淤污泥中细砂等物质表面包裹和吸附的有机组分即有机碳源被剥离进入液相，以有机组分为主的密度小的污泥混合液处于旋流分离模块18的中上部，同时清淤污泥中的细砂、部分特细砂等无机惰性组分在离心力和重力的综合作用下进入分离斗23中；其中加药系统19是否运行根据清淤污泥中实际磷酸盐浓度(是否≥10mg/L)和磷资源化需求进行具体确定；
c、步骤b所得的经旋流分离模块18处理后的污泥经第二出泥管26和排泥管道41就近排入周边排水管网40的污水检查井42，且排泥管道41的出口接至污水检查井42的水位以下，避免跌水充氧导致从清淤污泥中提取的部分碳源被无效损耗；步骤b所得的分离出的细砂等无机惰性组分结合实际容积通过排空阀28和排放阀24的控制经无机组分排放管25间歇排放至专用收集桶，并统一运输至周边城镇污水处理厂进行进一步砂水分离和含磷化学污泥的沉淀分离；
d、步骤a和步骤b处理过程中散发的硫化氢等恶臭气体自然进入位于系统上部的除臭模块29，通过颗粒活性炭填料30的物理吸附处理，处理后的臭气由接至圆柱形除臭模块29上部中心的排气装置31排出。
经旋流分离模块18处理后的污泥的挥发分比例VSS/SS和碳氮比COD/TN分别为0.6和20，能够资源化利用于排水管网40末端的高排放标准城镇污水处理厂的补充碳源；经旋流分离模块18分离出的细砂等无机惰性组分的挥发分 比例VSS/SS为2.5％，能够资源化利用于工程建筑材料。
实施例2
一种排水管道污泥有机无机组分在线分离碳源提取方法，包括以下步骤：
a、利用排水管网污泥清通车35自带的抽吸泵36将排水管网40中的清淤污泥经吸泥管38和压力出泥管37抽至前处理模块1的配泥管7，在高度4cm的转动刮板3的连续推动下，配泥管7出泥在固定式圆形网板格栅2的表面布泥，大部分污泥在重力作用下快速通过水平设置的圆形网板格栅2的内径2mm的圆形网孔进入网板格栅2下部的圆锥形整流泥斗11，同时清淤污泥中大粒径颗粒物被截留于网板格栅2的表面，经每间隔5min运行一次的间歇运行淋洗装置4的淋洗喷头5的高压水柱淋洗后，通过宽度为120mm的方形入渣槽8经竖直通道17进入栅渣压榨模块14进行脱水压榨处理，出渣槽16排出的栅渣采用专用收集桶收集后作为生活垃圾就近运至周边垃圾中转站；
b、经前处理模块1处理后的污泥经第一出泥管13和加药系统19投加的药剂一起经进泥管20竖直进入旋流分离模块18，在由变频搅拌电机21驱动的可调节搅拌桨22的高速旋转作用下，经水力停留时间3min的旋流分离，清淤污泥中细砂等物质表面包裹和吸附的有机组分即有机碳源被剥离进入液相，以有机组分为主的密度小的污泥混合液处于旋流分离模块18的中上部，同时清淤污泥中的细砂、部分特细砂等无机惰性组分在离心力和重力的综合作用下进入分离斗23中；其中加药系统19是否运行根据清淤污泥中实际磷酸盐浓度(是否≥10mg/L)和磷资源化需求进行具体确定；
c、步骤b所得的经旋流分离模块18处理后的污泥经第二出泥管26和排泥管道41就近排入周边排水管网40的污水检查井42，且排泥管道41的出口接至污水检查井42的水位以下，避免跌水充氧导致从清淤污泥中提取的部分碳源被无效损耗；步骤b所得的分离出的细砂等无机惰性组分结合实际容积通过排空阀28和排放阀24的控制经无机组分排放管25间歇排放至专用收集桶，并统一运输至周边城镇污水处理厂进行进一步砂水分离和含磷化学污泥的沉淀分离；
d、步骤a和步骤b处理过程中散发的硫化氢等恶臭气体自然进入设置于系统上部的除臭模块29，通过颗粒态活性炭填料30的物理吸附处理，处理后的臭气由接至圆柱形除臭模块29上部中心的排气装置31排出。
经旋流分离模块18处理后的污泥的挥发分比例VSS/SS和碳氮比COD/TN分别为0.55和17.5，能够资源化利用于排水管网40末端的高排放标准城镇污水处理厂的补充碳源；经旋流分离模块18分离出的细砂等无机惰性组分的挥发分比例VSS/SS为2％，能够资源化利用于工程建筑材料。
实施例3
一种排水管道污泥有机无机组分在线分离碳源提取方法，包括以下步骤：
a、利用排水管网污泥清通车35自带的抽吸泵36将排水管网40中的清淤污泥经吸泥管38和压力出泥管37抽至前处理模块1的配泥管7，在高度4cm 的转动刮板3的连续推动下，配泥管7出泥在固定式圆形网板格栅2的表面布泥，大部分污泥在重力作用下快速通过水平设置的圆形网板格栅2的内径2.5mm的圆形网孔进入网板格栅2下部的圆锥形整流泥斗11，同时清淤污泥中大粒径颗粒物被截留于网板格栅2的表面，经每间隔10min运行一次的间歇运行淋洗装置4的淋洗喷头5的高压水柱淋洗后，通过宽度为100mm的方形入渣槽8经竖直通道17进入栅渣压榨模块14进行脱水压榨处理，出渣槽16排出的栅渣采用专用收集桶收集后作为生活垃圾就近运至周边垃圾中转站；
b、步骤a所得的经前处理后的污泥经第一出泥管13和加药系统19投加的药剂一起经进泥管20竖直进入旋流分离模块18，在由变频搅拌电机21驱动的可调节搅拌桨22的高速旋转作用下，经水力停留时间2min的旋流分离，清淤污泥中细砂等物质表面包裹和吸附的有机组分即有机碳源被剥离进入液相，以有机组分为主的密度小的污泥混合液处于旋流分离模块18的中上部，同时清淤污泥中的细砂、部分特细砂等无机惰性组分在离心力和重力的综合作用下进入分离斗23中；其中加药系统19是否运行根据清淤污泥中实际磷酸盐浓度(是否≥10mg/L)和磷资源化需求进行具体确定；
c、步骤b所得的经旋流分离模块18处理后的污泥经第二出泥管26和排泥管道41就近排入周边排水管网40的污水检查井42，且排泥管道41的出口接至污水检查井42的水位以下，避免跌水充氧导致从清淤污泥中提取的部分碳源被无效损耗；步骤b所得的分离出的细砂等无机惰性组分结合实际容积通过排空阀28和排放阀24的控制经无机组分排放管25间歇排放至专用收集桶，并统一运输至周边城镇污水处理厂进行进一步砂水分离和含磷化学污泥的沉淀分离；
d、步骤a和步骤b处理过程中散发的硫化氢等恶臭气体自然进入设置于系统上部的除臭模块29，通过颗粒态活性炭填料30的物理吸附处理，处理后的臭气由接至圆柱形除臭模块29上部中心的排气装置31排出。
经旋流分离模块18处理后的污泥的挥发分比例VSS/SS和碳氮比COD/TN分别为0.5和15，能够资源化利用于排水管网40末端的高排放标准城镇污水处理厂的补充碳源；经旋流分离模块18分离出的细砂等无机惰性组分的挥发分比例VSS/SS为1.5％，能够资源化利用于工程建筑材料。
最后所应说明的是，以上具体实施方式仅用以说明本发明的技术方案而非限制，尽管参照实例对本发明进行了详细说明，本领域的普通技术人员应当理解，可以对本发明的技术方案进行修改或者等同替换，而不脱离本发明技术方案的精神和范围，其均应涵盖在本发明的权利要求范围当中。

Claims (10)

  1. 一种排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，包括系统外箱(33)，所述系统外箱(33)内设置有系统主体，所述系统主体从上至下依次包括拼接在一起的除臭模块(29)、前处理模块(1)及旋流分离模块(18)，所述旋流分离模块(18)的上部侧壁设置有栅渣压榨模块(14)，所述前处理模块(1)、旋流分离模块(18)及栅渣压榨模块(14)分别与控制模块(32)电连接；
    所述前处理模块(1)用于筛除清淤污泥中的大粒径颗粒物，包括网板格栅(2)、转动刮板(3)、淋洗装置(4)、变频驱动电机(6)、配泥管(7)、入渣槽(8)、整流泥斗(11)、排泥阀(12)和第一出泥管(13)；
    所述网板格栅(2)为水平设置的固定式圆形网板；
    所述配泥管(7)上设置有出泥口，所述出泥口位于所述网板格栅(2)的上方；
    所述转动刮板(3)的底部与所述网板格栅(2)的上表面相切，所述转动刮板(3)由变频驱动电机(6)驱动，用于所述配泥管(7)出泥在所述网板格栅(2)表面的分布；
    所述淋洗装置(4)主要用于所述网板格栅(2)表面截留的大粒径颗粒物的间歇性淋洗和系统工作结束后的清洗，所述淋洗装置(4)固定连接在所述转动刮板(3)上，进口端通过软管(10)与进水系统(9)连接；
    所述入渣槽(8)设置于所述配泥管(7)的对角并靠近所述网板格栅(2)的边缘，便于所述转动刮板(3)将所述网板格栅(2)截留的清淤污泥中的大粒径颗粒物刮入；
    所述整流泥斗(11)位于所述网板格栅(2)的下方，用于收集通过所述网板格栅(2)的污泥并对污泥流量进行调节，收集的污泥经所述第一出泥管(13)进入所述旋流分离模块(18)；
    所述旋流分离模块(18)用于高速旋流状态下清淤污泥有机无机组分分离和有机碳源提取，包括变频搅拌电机(21)、可调节搅拌桨(22)、进泥管(20)、加药系统(19)、分离斗(23)、第二出泥管(26)、排放阀(24)、无机组分排放管(25)、排空管(27)及排空阀(28)；
    所述变频搅拌电机(21)驱动可调节搅拌桨(22)转动，所述可调节搅拌桨(22)设置在所述旋流分离模块(18)的中上部；
    所述进泥管(20)竖直设置在所述第二出泥管(26)的对侧，所述进泥管(20)的进口端通过三通分别与所述加药系统(19)及第一出泥管(13)连接，出口端设置在所述旋流分离模块(18)运行液位以下15-20cm；
    所述分离斗(23)设置在所述旋流分离模块(18)的底部，用于收集污泥中分离出的无机组分，所述分离斗(23)的下端设置有排放阀(24)及无机组分排放管(25)；
    所述排空管(27)设置于旋流分离模块(18)的中部，用于系统工作结束后旋流分离模块(18)主体部分污泥的排空；
    所述栅渣压榨模块(14)用于所述网板格栅(2)筛除的栅渣的脱水压榨，包括驱动电机(15)、压榨槽和出渣槽(16)，所述压榨槽通过竖直通道(17)与所述入渣槽(8)连接，所述出渣槽(16)斜向上设置，并伸出所述系统外箱(33)侧面；
    所述除臭模块(29)用于清淤污泥处理过程中散发的臭气的物理吸附处理，采用无动力除臭，包括填料(30)和排气装置(31)，底面设置网状进气孔；所述填料(30)包括颗粒活性炭，所述排气装置(31)一端与除臭模块(29)的顶部中心部位连接，另一端伸出所述系统外箱(33)侧面。
  2. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述转动刮板(3)的高度为4cm，长度与所述网板格栅(2)的半径相同，由硬质材料和弹性胶皮材料组合制成，所述弹性胶皮材料设置在所述转动刮板(3)自由端的下部，长度为所述转动刮板(3)长度的1/3，高度为所述转动刮板(3)高度的1/2。
  3. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述淋洗装置(4)上每间隔10-20cm设置有一个淋洗喷头(5)，所述淋洗喷头(5)与竖直方向呈45°斜向下设置，所述淋洗喷头(5)位于所述转动刮板(3)的上方；
    所述入渣槽(8)的长度是所述网板格栅(2)半径的1/3，宽度为100-120mm，高度为120-150mm，顶部比所述网板格栅(2)表面高出2cm，防止污泥进入。
  4. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述系统外箱(33)的底部设置有滑轮(34)，便于系统在排水管网(40)清淤污泥在线分离现场的灵活移动。
  5. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述配泥管(7)的进泥口与压力出泥管(37)连接，所述压力出泥管(37)与排水管网污泥清通车(35)自带的抽吸泵(36)连接，所述抽吸泵(36)通过吸泥管(38)与排水管网(40)清淤段末端封堵的污水检查井(39)的底部连接。
  6. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述旋流分离模块(18)的第二出泥管(26)通过排泥管道(41)与周边排水管网(40)中的污水检查井(42)连接。
  7. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述旋流分离模块(18)的分离斗(23)采用厚度为10-12cm的有机玻璃制成，便于清淤污泥处理过程中分离出的以细砂和特细砂为主的无机组分实际容积的观察；所述系统主体的外壁及系统外箱(33)均采用不锈钢材料，系统主体的直径为60-80cm。
  8. 根据权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统，其特征在于，所述控制模块(32)设置于所述系统外箱(33)正面，通过线路分别与所述前处理模块(1)的变频驱动电机(6)、所述旋流分离模块(18)的变频搅拌电机(21)、排放阀(24)和设置于排空管(27)上的排空阀(28)及所述栅渣压榨模块(14)的驱动电机(15)电连接，所述控制模块(32)的供电电源为排水管网(40)清淤管段周边的公共配电柜或清淤现场车载柴油发电机。
  9. 一种排水管道污泥有机无机组分在线分离碳源提取方法，其特征在于，利用权利要求1所述的排水管道污泥有机无机组分在线分离碳源提取系统进行提取，包括以下步骤：
    a、利用排水管网污泥清通车(35)自带的抽吸泵(36)将排水管网(40)中的清淤污泥经吸泥管(38)和压力出泥管(37)抽至前处理模块(1)的配泥管(7)中，在转动刮板(3)的连续推动下，所述配泥管(7)出泥在网板格栅(2)的表面布泥，大部分污泥在重力作用下快速通过网板格栅(2)上的圆形网孔进入网板格栅(2)下方的圆锥形整流泥斗(11)，同时清淤污泥中大粒径颗粒物被截留于网板格栅(2)的上表面，经间歇运行的淋洗装置(4)的淋洗喷头(5)的高压水柱淋洗后，通过入渣槽(8)经竖直通道(17)进入栅渣压榨模块(14)的压榨槽进行脱水压榨处理，出渣槽(16)排出的栅渣采用专用收集桶收集后作为生活垃圾就近运至周边垃圾中转站；
    b、步骤a中经前处理模块(1)处理后的污泥经第一出泥管(13)和加药系统(19)投加的药剂一起经进泥管(20)竖直进入旋流分离模块(18)的主体部分，在由变频搅拌电机(21)驱动的可调节搅拌桨(22)的高速旋转作用下，经水力停留时间1-3min的旋流分离，清淤污泥中有机碳源被剥离进入液相，以有机组分为主的密度小的污泥混合液处于旋流分离模块(18)的中上部，同时清淤污泥中的无机惰性组分在离心力和重力的综合作用下进入底部分离斗(23)中；其中所述加药系统(19)是否运行根据清淤污泥中实际磷酸盐浓度和磷资源化需求进行具体确定；
    c、步骤b所得的经旋流分离模块(18)处理后的污泥经第二出泥管(26)和排泥管道(41)就近排入周边排水管网(40)的污水检查井(42)，且排泥管道(41)的出口接至污水检查井(42)的水位以下；步骤b分离出的所述无机惰性组分结合实际容积通过排空阀(28)和排放阀(24)的控制经无机组分排放管(25)间歇排放至专用收集桶，并统一运输至周边城镇污水处理厂进行进一步砂水分离和含磷化学污泥的沉淀分离；
    d、步骤a和步骤b处理过程中散发的恶臭气体自然进入设置于系统上部的除臭模块(29)，通过填料(30)的物理吸附处理，处理后的臭气由接至圆柱形除臭模块(29)上部中心的排气装置(31)排出。
  10. 根据权利要求9所述的排水管道污泥有机无机组分在线分离碳源提取方法，其特征在于，经所述旋流分离模块(18)处理后的污泥的挥发分比例 VSS/SS不低于0.5、碳氮比COD/TN不低于15，能够资源化利用于排水管网(40)末端的高排放标准城镇污水处理厂的补充碳源；经所述旋流分离模块(18)分离出的无机惰性组分的VSS/SS低于3％，能够资源化利用于工程建筑材料。
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CN215516967U (zh) * 2021-08-25 2022-01-14 印维良 一种用于工业废水深度处理装置
CN114751616A (zh) * 2022-06-16 2022-07-15 中国市政工程华北设计研究总院有限公司 排水管道污泥有机无机组分在线分离碳源提取系统及方法

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