WO2015149520A1 - 一种基于热水解技术的污泥脱水***及工艺 - Google Patents

一种基于热水解技术的污泥脱水***及工艺 Download PDF

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Publication number
WO2015149520A1
WO2015149520A1 PCT/CN2014/090726 CN2014090726W WO2015149520A1 WO 2015149520 A1 WO2015149520 A1 WO 2015149520A1 CN 2014090726 W CN2014090726 W CN 2014090726W WO 2015149520 A1 WO2015149520 A1 WO 2015149520A1
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Prior art keywords
sludge
hydrothermal
reactor
unit
flash
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PCT/CN2014/090726
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English (en)
French (fr)
Inventor
王树众
钱黎黎
唐兴颖
孙盼盼
Original Assignee
西安交通大学
西安市万丰能源环保科技有限公司
王树众
钱黎黎
唐兴颖
孙盼盼
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Application filed by 西安交通大学, 西安市万丰能源环保科技有限公司, 王树众, 钱黎黎, 唐兴颖, 孙盼盼 filed Critical 西安交通大学
Priority to US14/917,013 priority Critical patent/US9926216B2/en
Publication of WO2015149520A1 publication Critical patent/WO2015149520A1/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
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/025—Thermal hydrolysis
    • 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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • 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
    • C02F2301/00—General aspects of water treatment
    • C02F2301/02—Fluid flow conditions
    • C02F2301/026—Spiral, helicoidal, radial
    • 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
    • C02F2303/06—Sludge reduction, e.g. by lysis
    • 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
    • C02F2303/10—Energy recovery
    • 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
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • 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
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • the invention relates to the technical field of sludge treatment, in particular to an urban sludge dewatering system and a process.
  • Municipal sludge is a by-product of urban sewage treatment and is a general term for a small amount of sediment, particulate matter and floating matter produced by conventional methods for treating urban sewage. It mainly has the following characteristics:
  • composting, landfilling and incineration are common methods for sludge disposal, and these methods all have certain requirements on the moisture content of the sludge.
  • the sludge filling water content needs to be less than 60%, and the sludge composting needs to be added with a leavening agent to adjust the water content to about 50%.
  • the sludge incineration needs to reduce the moisture content of the sludge to about 30%. Therefore, a wet sludge having a moisture content of about 80% requires further dehydration treatment.
  • the further dewatering of the sludge can be carried out by a thermal drying method, which can reduce the moisture content of the sludge to less than 50%, the volume reduction effect is good, and the product is stable.
  • the method has high technical requirements, complicated management, large energy consumption, and high processing cost.
  • the thermal drying method of sludge it takes 887025kcal of heat per ton of water to be evaporated, and 107m 3 of natural gas with a combined heat value of 8300kcal.
  • the sludge hydrothermal treatment technology is a technology that heats the sludge, hydrolyzes the viscous organic matter in the sludge under a certain temperature and pressure, destroys the colloidal structure of the sludge, and improves the dehydration performance and anaerobic digestion performance, which is also called thermal conditioning.
  • the hydrothermal treatment technology divides the hydrothermal treatment into two types, thermal hydrolysis and wet oxidation, according to whether or not an oxidizing agent is added during the treatment. Thermal hydrolysis does not pass through the oxidant, while wet oxidation requires the introduction of an oxidant into the reactor.
  • the sludge thermal hydrolysis technology can further reduce the water content of the sludge more efficiently and economically.
  • the technology is based on the principle of cell wall breaking, which can realize the dehydration and drying of sludge with low energy consumption and high efficiency.
  • the conventional thermal hydrolysis dehydration process system is prone to clogging, and the reduction effect is not obvious.
  • the object of the present invention is to provide a sludge dewatering system and a process based on thermal hydrolysis technology, which can effectively reduce the moisture content of sludge after dewatering, thereby achieving the requirement of reduction, and the system is not easy Blocked.
  • a sludge dewatering system based on thermal hydrolysis technology comprising a homogenization slurry unit, a hydrothermal unit, a flash reactor, a waste heat recovery unit and a dewatering machine;
  • the homogenization slurry unit comprises a sludge storage tank, a sludge homogenizer and a first single screw pump; the lower part of the sludge storage tank is connected to the sludge inlet end of the sludge homogenizer; the sludge at the upper part of the sludge homogenizer The outlet end is connected to the inlet end of the hydrothermal unit through the first single screw pump;
  • the outlet end of the hydrothermal unit is connected to the inlet end of the upper part of the flash reactor, and the outlet end of the flash sludge at the lower part of the flash reactor is connected to the inlet of the waste heat recovery unit;
  • the outlet of the waste heat recovery unit is connected to the dehydrator;
  • the dewatering filtrate output pipe of the dehydrator is connected to the inlet end of the first low-pressure variable frequency pump, and the outlet end of the first low-pressure variable-frequency pump is connected to the inlet end of the ejecting fluid of the ejector;
  • the flash reactor is Flash steam
  • the outlet is connected to the inlet end of the ejector fluid, the outlet of the ejector is connected to the inlet end of the ejector mixture at the lower part of the sludge homogenizer, and the waste steam outlet end at the upper part of the sludge homogenizer is connected to the sludge dilution of the dehydrator Liquid output pipe.
  • a further improvement of the present invention is that the outlet end of the flash reactor of the flash sludge is connected to the inlet end of the second single screw pump, and the outlet end of the second single screw pump is connected to the inlet side of the shell side of the heat exchanger; the boiler feed water pipe and cooling
  • the cooling water outlet of the tower is connected to the inlet end of the second low-voltage variable frequency pump, and the outlet end of the second low-voltage variable frequency pump is connected to the tube side inlet end of the heat exchanger; the outlet end of the heat exchanger tube side is divided into two, respectively connected to the heating furnace
  • the inlet end and the inlet end of the cooling tower; the outlet end of the heat exchanger shell side is connected to the dehydrator.
  • a further improvement of the invention resides in that the sludge storage tank is disposed above the sludge homogenizer; the sludge homogenizer is disposed above the first single screw pump.
  • hydrothermal unit is a batch hydrothermal unit or a continuous hydrothermal unit
  • the intermittent hydrothermal unit comprises a hydrothermal steam heater, a first batch hydrothermal reactor and a second batch hydrothermal reactor; the outlet of the first single screw pump is connected to the lower sludge inlet end of the hydrothermal steam heater The hot water vapor outlet end of the heating furnace is connected to the water heat steam inlet end of the lower part of the water heat steam heater, and the upper outlet end of the water heat steam heater is connected with the first batch type hydrothermal reactor and the second intermittent hydrothermal reaction in parallel.
  • the first batch type hydrothermal reactor and the second batch type hydrothermal reactor are connected in parallel; the first batch type hydrothermal reactor and the second batch type hydrothermal reactor have electric cut-offs at the inlet end and the outlet end a valve; an outlet end of the first batch hydrothermal reactor and the second batch hydrothermal reactor are connected to an inlet end of the upper portion of the flash reactor;
  • the continuous hydrothermal unit comprises a continuous hydrothermal reactor, and the continuous hydrothermal reactor is a radial hydrothermal reactor or a tower hydrothermal reactor;
  • the radial flow hydrothermal reactor is a container having a height to diameter ratio of less than 1; including an inner cylinder, a draft tube, an outer cylinder, an inner cylinder agitator and a cylinder wall, and the inner cylinder agitator is disposed inside the inner cylinder, and the diversion tube is arranged Outside the inner cylinder, the outer cylinder is disposed at the inner circumference of the cylinder wall; the outlet of the first single screw pump and the hot water vapor outlet of the heating furnace are connected to the lower inlet pipe of the inner cylinder, and the outlet connection of the lower part of the annular space between the outer cylinder and the cylinder wall is flashed The inlet end of the upper portion of the steaming reactor;
  • the tower hydrothermal reactor is a vessel with a lower aspect ratio of greater than 2; the bottom of the tower hydrothermal reactor is equipped with an axial force agitator, and the upper part is a stirrer without axial force; the first single screw
  • the outlet of the pump and the hot steam outlet of the furnace are connected to the lower inlet of the tower hydrothermal reactor; the upper outlet of the tower hydrothermal reactor is connected to the inlet end of the upper portion of the flash reactor.
  • a sludge dewatering process based on thermal hydrolysis technology comprising the following steps:
  • the auger is quantitatively input to the sludge inlet end of the lower part of the sludge homogenizer, and the sludge treated by the sludge homogenizer is input to the first single screw pump through the sludge outlet end of the upper part of the sludge homogenizer, and passes through the first single
  • the sludge treated by the screw pump enters the hydrothermal unit; part of the dewatered filtrate from the dehydrator acts as a diluent through the first low-pressure variable-frequency pump into the ejector to ignite the flash steam, and after the ejector, the mixed fluid enters the sludge homogenizer
  • the sludge input from the sludge storage tank is homogenized and slurryed, and the sludge homogenizer is provided with a stirrer; the waste steam generated by the sludge homogenizer is sent to the sludge dilution liquid pipe from the dehydrator for absorption;
  • the waste heat recovery unit comprises a heating furnace, a cooling tower, a second low-pressure variable frequency pump, a second single-screw pump and a heat exchanger; the circulating cooling water from the boiler feed water and the cooling tower first enters the second low-pressure variable-frequency pump to be boosted, and then The flash sludge pressurized by the second single screw pump exchanges heat in the heat exchanger; the outlet fluid of the heat exchanger is divided into two, one is used as circulating cooling water, and the other is used as boiler inlet water; the heat exchanger outlet The fluid that is circulating cooling water enters the cooling tower for cooling, and the heat after cooling However, the sludge enters the dehydrator for dehydration, and the fluid at the outlet of the heat exchanger as the boiler water enters the heating furnace to generate water and heat steam to provide heat to the hydrothermal unit;
  • a further improvement of the present invention is that the mechanical dewatered sludge in step 1) has a water content of 80% and a viscosity of 50,000 mPa ⁇ s to 150,000 mPa ⁇ s; and the moisture content of the sludge from the first single screw pump is 84% to 85. %, the temperature is 90 ° C ⁇ 100 ° C, the viscosity is less than 8000 mPa ⁇ s;
  • the water content of the sludge from the hydrothermal unit is 86% to 88%, the temperature is 170 ° C to 180 ° C, and the viscosity is less than 100 mPa ⁇ s.
  • a further improvement of the present invention is that the diluent enters the ejector nozzle under the action of a low pressure variable frequency pump to illuminate the surrounding flash steam, and the two fluids are thoroughly mixed during the ejector.
  • a further improvement of the present invention is that the hydrothermal unit is a batch type hydrothermal unit; the intermittent hydrothermal unit comprises a sludge water heat steam heater, a first batch type hydrothermal reactor and a second intermittent water heat unit.
  • the reactor; the sludge from the first single screw pump enters the hydrothermal steam heater from the lower part for rapid stirring and heating, and is heated to the thermal hydrolysis and then exits from the upper part into the first batch type hydrothermal reactor to make the sludge first.
  • the reaction in the batch hydrothermal reactor at the same time, the sludge in the second batch hydrothermal reactor is discharged into the flash reactor through the pressure difference, after the first batch hydrothermal reactor reaches the reaction time, the first A batch of hydrothermal reactor begins to drain mud, while a second batch of hydrothermal reactor begins to enter the mud and react, thus circulating.
  • a further improvement of the present invention is that the hydrothermal unit is a radial hydrothermal reactor or a tower hydrothermal reactor;
  • the radial flow hydrothermal reactor comprises an inner cylinder, a draft tube, an outer cylinder, an inner cylinder agitator and a cylinder wall, and the homogenized slurry sludge and the hot water steam from the heating furnace enter into the lower inlet pipe of the inner cylinder, and then Under the action of the inner cylinder agitator, the reaction parameters are reached, the viscosity is reduced, and the overflow enters the guide tube.
  • the outlet from the lower part of the draft tube enters the large space of the outer tube, radiates outward flow, and finally the sludge after the hydrothermal reaction
  • the annular space entering between the outer cylinder and the cylinder wall is collected and flows out through the outlet of the lower portion;
  • the tower hydrothermal reactor is fed in and out, the bottom of the tower hydrothermal reactor adopts a strong agitator with axial force, and the upper part of the tower hydrothermal reactor adopts an agitator without axial force; homogenized slurry
  • the hot steam from the sludge and the heating furnace enters from the lower part of the tower hydrothermal reactor, and is circulated and stirred under the action of a strong agitator with axial force to reach the reaction parameters, and then continuously enters the lower part of the tower hydrothermal reactor.
  • the promotion of the homogenized slurry sludge in the space, the sludge reaching the reaction parameters enters the upper part of the tower hydrothermal reactor, and finally the sludge flows out at the upper outlet of the tower hydrothermal reactor.
  • a further improvement of the present invention is that the heat exchanger is a sleeve heat exchanger, a plate heat exchanger, a spiral plate heat exchanger or a heat pipe heat exchanger;
  • the dewatering machine is a plate and frame filter press, belt type Filter press, centrifuge, box filter press or diaphragm filter press.
  • the present invention has the following beneficial effects:
  • the invention homogenizes the sludge before entering the first single screw pump, and the viscosity is significantly reduced to facilitate transportation.
  • the sludge storage tank, the sludge homogenizer and the first single screw pump are gradually lowered in height arrangement, so the homogenized slurry unit is reliable in transportation and is not easy to be blocked.
  • the sludge storage tank in the homogenization slurry unit adopts the method of first chopping and then auger transport to ensure that the sludge that is quantitatively entered into the sludge homogenization is small particles, and the homogenization efficiency is improved.
  • the dilution liquid in the homogenization slurry unit adopts the filtrate after sludge dewatering, on the one hand, the treatment amount of the dewatering filtrate can be reduced, the system water can be saved, and the heat of the dewatering filtrate can be recovered on the other hand.
  • the dilution liquid and the flash steam in the homogenization slurry unit are mixed in the ejector. Due to the ejector action, the mixing efficiency is high, and the flash steam pressure can be solved, and the sludge homogenizer cannot be directly entered. problem.
  • the ejector mixture is then fed into the sludge homogenizer and the sludge is homogenized.
  • the waste steam generated in the homogenization slurry process is then introduced into the diluent pipe for absorption, which can avoid the odor caused by entering the atmosphere, and can further preheat the dilution liquid to some extent.
  • the hydrothermal unit of the present invention has various forms and can be operated intermittently or continuously.
  • the hydrothermal steam heater can be heated up and down to ensure sufficient time for the sludge to reach the optimum reaction parameters.
  • a radial hydrothermal reactor or a tower hydrothermal reactor can be used, both of which combine heating and reaction, wherein the radial hydrothermal reactor follows the flow radius Increase, sludge flow rate Reduced, so the reaction time can be effectively guaranteed; and the tower hydrothermal reactor has a large aspect ratio, running in and out, and the upper part uses an agitator with only axial force, so that the upper sludge can only rely on the lower sludge The thrust flows to the outlet, so the reaction time can be effectively guaranteed.
  • the waste heat recovery unit of the present invention recovers part of the heat of the flash sludge by using the boiler feed water, thereby saving the fuel amount of the heating furnace.
  • the viscosity of the fluid on both sides of the heat exchanger is low, so the heat exchanger is not easily blocked.
  • FIG. 1 is a flow chart of a sludge dehydration process based on thermal hydrolysis technology of the present invention
  • Figure 2 is a schematic view of a batch type hydrothermal unit of the present invention
  • Figure 3 is a schematic view of a radial flow hydrothermal reactor of the present invention.
  • Figure 4 is a schematic view of a tower hydrothermal reactor of the present invention.
  • a sludge dewatering system based on thermal hydrolysis technology of the present invention comprises a homogenization slurry unit, a hydrothermal unit, a flash reactor, a waste heat recovery unit and a dehydrator.
  • Homogenization slurry unit connection method mechanical dewatered sludge is stored in the sludge storage tank 1 while the strong shear agitator in the sludge storage tank 1 chopped the sludge, and the chopped small granular sludge
  • the sludge agitator 1 is disposed above the sludge inlet end of the sludge homogenizer 2 by the lower auger of the sludge storage tank 1, and the sludge storage tank 1 is disposed above the sludge homogenizer 2 for better transportation.
  • a part of the dehydrated filtrate from the dehydrator 6 enters the inlet end of the first low-pressure variable frequency pump 111 as a diluent, and the outlet end of the first low-pressure variable-frequency pump 111 is connected to the inlet end of the ejector 9 while the flash output of the flash reactor 4 is output.
  • the steam is also introduced into the ejector 9, and together with the ejector of the diluent, enters the inlet end of the ejector mixture at the lower portion of the sludge homogenizer 2, and the sludge outlet end at the upper portion of the sludge homogenizer 2 enters the first single screw pump After boosting 101, the water heat unit 3 is entered.
  • the sludge homogenizer 2 is disposed above the first single screw pump 101, and the waste steam outlet end of the upper portion of the sludge homogenizer 2 is connected to the dehydrator 6 Come out of the sludge dilution pipe.
  • the flash reactor connection mode the sludge from the homogenization slurry unit enters the inlet end of the hydrothermal unit 3, and the outlet end of the hydrothermal unit 3 is connected to the inlet end of the upper portion of the flash reactor 4, and the lower portion of the flash reactor 4 The flash sludge outlet end is connected to the waste heat recovery unit.
  • the flash vapor outlet end of the upper portion of the flash reactor 4 is connected to the inlet end of the ejector 9.
  • the waste heat recovery unit is connected in such a manner that the flash sludge from the flash reactor 4 enters the inlet end of the second single screw pump 102, and the outlet end of the second single screw pump 102 is connected to the shell side inlet end of the heat exchanger 5.
  • the boiler feed water and the cooling water from the cooling tower 7 enter the inlet end of the second low-pressure variable frequency pump 112, and the outlet end of the second low-pressure variable-frequency pump 112 is connected to the tube-side inlet end of the heat exchanger 5 and exchanges heat with the flash sludge.
  • the heat exchanger 5 tube side outlet end boiler feed water enters the inlet end of the heating furnace 8, the heat exchanger 5 tube side outlet end circulating cooling water enters the cooling tower 7 for cooling, and the heat exchanger 5 shell side outlet end sludge enters the dewatering machine 6 ,
  • the dewatered cake after dewatering is transported out, and a part of the dehydrated filtrate enters the inlet end of the first low-pressure variable frequency pump 111, and the remaining dehydrated filtrate is returned to the sewage treatment plant for treatment.
  • the hydrothermal unit 3 can be operated intermittently or continuously.
  • the intermittent water heat unit 13 the basic flow connection method is as follows:
  • the homogenized slurry sludge enters the lower sludge inlet end of the hydrothermal steam heater 12, and the hot steam at the outlet end of the heating furnace 8 enters the water-heat steam inlet end of the hydrothermal steam heater 12, and the upper outlet of the hydrothermal steam heater 12
  • the first batch hydrothermal reactor 131 and the second batch hydrothermal reactor 132 are connected at the end, wherein the first batch hydrothermal reactor 131 and the second batch hydrothermal reactor 132 are connected in parallel.
  • the hydrothermal unit 3 can be operated intermittently or continuously.
  • the continuous hydrothermal unit comprises a continuous hydrothermal reactor, which may be a radial hydrothermal reactor 14 or a tower hydrothermal reactor 15. Referring to Figure 3, the basic flow connection of the radial hydrothermal reactor 14 is as follows:
  • the radial flow hydrothermal reactor 14 is a vessel having a height to diameter ratio of less than 1, and is divided into an inner cylinder 141, a draft tube 142, an outer cylinder 143, an inner cylinder agitator 144 and a cylinder wall 145, and homogenized slurry sludge and
  • the hot water vapor from the heating furnace 8 enters the inlet pipe at the lower portion of the inner cylinder 141, and then reaches the reaction parameters under the action of the inner cylinder agitator 144, the viscosity is remarkably lowered, and the overflow enters the draft tube 142 from the lower portion of the draft tube 142.
  • the outlet enters the large space of the outer cylinder 143, and radiates outwardly to ensure the reaction time.
  • the sludge after the hydrothermal reaction enters the annular space between the outer cylinder and the cylinder wall, and then flows out through the lower outlet.
  • the tower hydrothermal reactor 15 is a vessel having a height to diameter ratio of more than 2, and is driven in and out.
  • the lower portion of the tower hydrothermal reactor 15 is a strong agitator 151 having an axial force, and the upper portion of the tower hydrothermal reactor 15 is used.
  • Agitator 152 without axial force. All The slurry slurry and the hot steam coming out of the heating furnace 8 enter from the lower part of the tower hydrothermal reactor 15, and are circulated and stirred under the action of a strong agitator 151 having an axial force to reach the reaction parameters, and then continuously enter the tower.
  • the adsorption of the homogenized slurry sludge in the lower space of the hydrothermal reactor 15 reaches the upper part of the tower hydrothermal reactor 15 with the reaction parameters, because the upper part of the tower hydrothermal reactor 15 is non-axial.
  • the force of the agitator 152 ensures the reaction time, and finally the sludge flows out at the upper outlet of the tower hydrothermal reactor 15.
  • a sludge dewatering process based on thermal hydrolysis technology shown in Figure 1 comprises the following steps:
  • a mechanically dewatered sludge having a moisture content of about 80% and a viscosity of 50,000 mPa ⁇ s to 100,000 mPa ⁇ s is stored in the sludge storage tank 1 while a strong shear agitator in the sludge storage tank 1 is applied to the sludge.
  • the chopped small-grained sludge is quantitatively input to the sludge inlet end of the lower part of the sludge homogenizer 2 through the auger at the lower part of the sludge storage tank 1, and the particle size reduction can improve the subsequent homogenization. effect.
  • the sludge storage tank 1 is disposed above the sludge homogenizer 2, and the sludge homogenizer 2 is disposed above the first single screw pump 101 for better transport of the sludge and is not easily blocked.
  • the partially dehydrated filtrate from the dehydrator 6 is used as a diluent to enter the ejector 9 to ignite the flash steam through the first low-pressure variable frequency pump 111, and the mixing efficiency of the ejector is high, and the flash steam pressure can be solved, and the direct entry cannot be directly entered.
  • the mixed fluid enters the sludge homogenizer 2 and the sludge input from the sludge storage tank 1 is homogenized and slurryed, and the sludge homogenizer 2 is provided with a stirrer, and the mixing efficiency is high.
  • the homogenized slurry has a water content of 84%-85%, a temperature of 90°C ⁇ 100°C, and a viscosity reduced from about 100,000 mPa ⁇ s to about 8000 mPa ⁇ s.
  • the sludge presents a homogeneous slurry fluid.
  • the state facilitates the transportation of the first single screw pump 101, and at the same time, the heat of the flash steam is recovered in the homogenization slurry unit, thereby saving the amount of the water heat steam, thereby saving the fuel amount of the gas furnace 8.
  • the waste steam generated in the homogenization pulping process is then taken into the sludge diluent pipe from the dehydrator 6 for absorption, so that the waste steam can be prevented from entering the atmosphere to cause odor, and the diluent can be further preheated to some extent.
  • the homogenized slurry sludge enters the hydrothermal unit 3, and the hydrothermal unit 3 can be operated intermittently or continuously.
  • the hot water in the waste heat recovery unit enters the hydrothermal unit 3 to heat the sludge, and during the heating process, the micro in the sludge.
  • the bioflocs are dissolved, the microbial cells are broken, and the organic matter in the sludge is hydrolyzed to reduce the viscosity of the sludge and reduce the binding ability of the viscous material to water.
  • the sludge when the sludge is heated to a certain temperature, the organic cells in the sludge are broken, the macromolecular organic matter in the cells is released and hydrolyzed, and the water combined with various macromolecules is also released, resulting in water being easier to Separation of sludge particles.
  • the water content of the sludge from the hydrothermal unit is 86% to 88%, the temperature is 170 ° C to 180 ° C, and the viscosity is less than 100 mPa ⁇ s.
  • the waste heat recovery unit includes a heating furnace 8, a cooling tower 7, a second low pressure variable frequency pump 112, a second single screw pump 102, and a heat exchanger 6.
  • the circulating cooling water from the boiler feed water and the cooling tower 7 is first introduced into the second low-pressure variable frequency pump 112 to be boosted, and then exchanged with the flash sludge pressurized by the second single-screw pump 102 in the heat exchanger 5, and the flashing is performed.
  • the mud viscosity is low and the heat exchanger 5 is not easily clogged.
  • the outlet of the heat exchanger 5 circulates the cooling water into the cooling tower 7 for cooling, and the cooled sludge after the heat exchange enters the dehydrator 6 for dehydration, and the heat exchanger 5 exits the boiler feed water into the heating furnace 8 to generate water and hot steam as the hydrothermal unit.
  • the waste heat recovery unit recovers the heat of the partially flashed sludge by using the boiler feed water, thereby saving the fuel amount of the heating furnace 8.
  • the temperature of the flash sludge is reduced after passing through the waste heat recovery unit, and the water and sludge particles are separated to facilitate the subsequent dehydration step.
  • the intermittent hydrothermal unit 13 includes a sludge hydrothermal steam heater 12, a first batch hydrothermal reactor 131, and a second batch hydrothermal reactor 132, and the sludge from the homogenization slurry unit enters the water heat from the lower portion.
  • the steam heater 12 performs rapid agitation and heating. Since the hydrothermal steam heater 12 is moved in and out, the residence time can be ensured, so that the sludge can be ensured from the upper part after heating to the optimum parameters of thermal hydrolysis.
  • the outlet enters the first batch hydrothermal reactor 131 or the second batch hydrothermal reactor 132 to generate a hydrothermal reaction, and the hydrothermal reactor intermittently operates and the electric shut-off valve can control the sludge in the hydrothermal reactor. Input and output, so the reaction time can be accurately controlled.
  • the radial flow hydrothermal reactor 14 is a vessel having a height to diameter ratio of less than 1, and is divided into an inner cylinder 141, a draft tube 142, an outer cylinder 143, an inner cylinder agitator 144 and a cylinder wall 145, and homogenized slurry sludge and
  • the hot water steam from the heating furnace 8 enters into the lower inlet pipe of the inner cylinder 141, and then reaches the reaction parameters under the action of the inner cylinder agitator 144, and the viscosity is reduced to less than 100 mPa ⁇ s, and the fluidity is very good, and the water can be smoothly overflowed.
  • the flow enters the guide tube 142, and the lower portion of the guide tube 142 is provided with an outlet, and the sludge reaching the reaction parameter can enter the large space of the outer tube 143 from the guide tube 142 due to the high diameter of the radial flow hydrothermal reactor 14.
  • the ratio is very small, so the sludge is radiant outward flow.
  • the flow radius increases, the flow rate decreases, so that the reaction time can be ensured in the limited space of the reactor.
  • the sludge after the hydrothermal reaction enters the outside.
  • the annular space between the barrel and the wall of the barrel is collected and flows out through the outlet of the lower portion.
  • the tower hydrothermal reactor 15 is a vessel having a height to diameter ratio of more than 2 and is fed in and out.
  • the bottom of the tower hydrothermal reactor 15 adopts a strong agitator 151 with axial force, so that the incoming homogenized slurry sludge and the hydrothermal steam can be circulated and stirred under the action of the strong agitator 151 to quickly reach the reaction parameters,
  • the gradual entry into the homogenized slurry sludge in the lower space of the tower hydrothermal reactor 15 causes the sludge having the reaction parameters to enter the upper portion of the tower hydrothermal reactor 15; since the upper portion of the tower hydrothermal reactor 15 is used
  • the agitator 152 has no axial force, so that the upper sludge can only flow to the outlet by the thrust of the lower sludge, so the reaction time can be effectively ensured, and the final sludge flows out at the upper outlet of the tower hydrothermal reactor 15.

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Abstract

一种基于热水解技术的污泥脱水***，包括均质浆化单元、水热单元（3）、闪蒸反应器（4）、余热回收单元和脱水机（6）。还公开了一种基于热水解技术的污泥脱水工艺，机械脱水污泥在污泥储罐（1）中得到切碎后被输入到污泥均质器（2）进行处理，经过第一单螺杆泵（101）处理后进入水热单元（3）；脱水机（6）出来的部分脱水滤液作为稀释液通过第一低压变频泵（111）进入引射器（9）中引射闪蒸蒸汽，引射后混合流体进入污泥均质器（2）中和污泥储罐（1）输入的污泥进行均质浆化，污泥均质器（2）中设有搅拌器；污泥均质器（2）产生的废蒸汽通入脱水机（6）出来的污泥稀释液管道中进行吸收；余热回收单元中的水热蒸汽进入水热单元（3）对污泥进行加热；水热单元（3）出来的水热污泥进入闪蒸反应器（4）发生闪蒸，产生闪蒸蒸汽和闪蒸污泥，其中闪蒸蒸汽进入引射器（9）中，闪蒸污泥进入余热回收单元中。该***可有效降低脱水后污泥的含水率，且不易堵塞。

Description

一种基于热水解技术的污泥脱水***及工艺 技术领域
本发明涉及污泥处理技术领域，特别涉及一种城市污泥脱水***及工艺。
背景技术
城市污泥是城镇污水处理过程中的副产物，是对采用常规方法处理城市污水所产生的少量沉淀物、颗粒物和漂浮物等物质的统称。其主要具有以下几个特点：
(1)产量大，无害化率低：污泥年产量为2800万吨(含水率80％，2011年)，3/4未有效处理。
(2)含水率高，水分难以脱除：传统污泥机械脱水方式仅能将污泥含水率降低到80％左右。
(3)有害性和有用性：城市污泥存在多种有机污染物和重金属，直接排放对环境有害，但是其热值高(7500～15000kJ/kg干污泥)，可以资源化利用。
目前，堆肥、填埋和焚烧是污泥处置常用的方法，这些方法都对污泥的含水率有一定要求。例如污泥填埋含水率需要低于60％，污泥堆肥需要添加膨松剂调整至含水率50％左右，污泥焚烧需要将污泥的含水率降低到30％左右。因此，含水率80％左右的湿污泥需要进一步的脱水处理。
污泥进一步的脱水可以采用热干化方法，该方法可以将污泥的含水率降低到50％以下，减容效果好，产品稳定。但是该方法技术要求高，管理较复杂，耗费大量能源，处理成本较高。污泥热干化法中蒸发每吨水需要消耗887025kcal的热量，合热值为8300kcal的天然气107m3。如湿污泥的水分按80％，干化到10％，则每吨干污泥大约需消耗428m3的天然 气及300kW·h的电力，则每吨干污泥的干化成本达到1144.9元(不计人员工资，设备折旧等)。这就存在建的起，用不起问题。因此，急需一种经济的方法代替传统热干化法。
污泥水热处理技术是将污泥加热，在一定温度和压力下使污泥中的粘性有机物水解，破坏污泥的胶体结构，改善脱水性能和厌氧消化性能的技术，也称热调质。水热处理技术按照处理过程中是否加入氧化剂，把水热处理分成热水解和湿式氧化两种。热水解没有通入氧化剂，而湿式氧化需要向反应器内通入氧化剂。
污泥热水解技术可以进一步高效经济地降低污泥的含水率，该技术是基于细胞破壁原理，可以低能耗、高效率地实现污泥的脱水干化。但是，传统热水解脱水工艺***容易堵塞，且减量化效果不明显。
发明内容
本发明的目的在于提供一种基于热水解技术的污泥脱水***及工艺，该污泥脱水***/工艺可以有效降低脱水后污泥的含水率，从而达到减量化的要求，且***不易堵塞。
为了实现上述目的，本发明采用如下技术方案：
一种基于热水解技术的污泥脱水***，包括均质浆化单元、水热单元、闪蒸反应器、余热回收单元和脱水机；
均质浆化单元包括污泥储罐、污泥均质器和第一单螺杆泵；污泥储罐下部连接污泥均质器下部的污泥入口端；污泥均质器上部的污泥出口端通过第一单螺杆泵连接水热单元的入口端；
水热单元的出口端连接闪蒸反应器上部的入口端，闪蒸反应器下部的闪蒸污泥出口端连接余热回收单元的入口；
余热回收单元的出口连接脱水机；脱水机的脱水滤液输出管道连接第一低压变频泵的入口端，第一低压变频泵的出口端连接引射器的引射流体入口端；闪蒸反应器的闪蒸蒸汽 出口连接引射器的被引射流体入口端，引射器的出口连接污泥均质器下部的引射混合物入口端，污泥均质器上部的废蒸汽出口端连接脱水机的污泥稀释液输出管道。本发明进一步的改进在于：闪蒸反应器闪蒸污泥出口端连接第二单螺杆泵的入口端，第二单螺杆泵的出口端连接换热器的壳侧入口端；锅炉给水管道和冷却塔的冷却水出口连接第二低压变频泵的入口端，第二低压变频泵的出口端连接换热器的管侧入口端；换热器管侧出口端一分为二，分别连接加热炉的入口端和冷却塔的入口端；换热器壳侧出口端连接脱水机。
本发明进一步的改进在于：污泥储罐设置在污泥均质器的上方；污泥均质器设置在第一单螺杆泵的上方。
本发明进一步的改进在于：水热单元为间歇式水热单元或连续式水热单元；
所述间歇式水热单元包括水热蒸汽加热器、第一间歇式水热反应器和第二间歇式水热反应器；第一单螺杆泵的出口连接水热蒸汽加热器下部污泥入口端，加热炉的水热蒸汽出口端连接水热蒸汽加热器下部的水热蒸汽入口端，水热蒸汽加热器上部出口端连接并联的第一间歇式水热反应器和第二间歇式水热反应器，其中第一间歇式水热反应器和第二间歇式水热反应器并联；第一间歇式水热反应器和第二间歇式水热反应器的入口端和出口端均设有电动截止阀；第一间歇式水热反应器和第二间歇式水热反应器的出口端均连接闪蒸反应器上部的入口端；
所述连续式水热单元包括连续式水热反应器，连续式水热反应器为辐流式水热反应器或塔式水热反应器；
辐流式水热反应器是一个高径比小于1的容器；包括内筒、导流筒、外筒、内筒搅拌器和筒壁，内筒搅拌器设置于内筒内部，导流筒设置于内筒外部，外筒设置于筒壁内周；第一单螺杆泵的出口和加热炉的水热蒸汽出口连接内筒下部入口管，外筒和筒壁之间环形空间下部的出口连接闪蒸反应器上部的入口端；
塔式水热反应器是一个下进上出高径比大于2的容器；塔式水热反应器下部采用有轴向力的搅拌器，上部采用无轴向力的搅拌器；第一单螺杆泵的出口和加热炉的水热蒸汽出口连接塔式水热反应器下部入口；塔式水热反应器上部出口连接闪蒸反应器上部的入口端。
一种基于热水解技术的污泥脱水工艺，包括以下步骤：
1)机械脱水污泥在污泥储罐中储存的同时，污泥储罐中的强剪切力搅拌器对污泥进行切碎，切碎后的小颗粒污泥通过污泥储罐下部的绞龙定量输入到污泥均质器下部的污泥入口端，经过污泥均质器处理的污泥通过污泥均质器上部的污泥出口端输入第一单螺杆泵，经过第一单螺杆泵处理的污泥进入水热单元；脱水机出来的部分脱水滤液作为稀释液通过第一低压变频泵进入引射器中引射闪蒸蒸汽，引射后混合流体进入污泥均质器中和污泥储罐输入的污泥进行均质浆化，污泥均质器中设有搅拌器；污泥均质器产生的废蒸汽通入脱水机出来的污泥稀释液管道中进行吸收；
2)余热回收单元中的水热蒸汽进入水热单元对污泥进行加热，在加热过程中，污泥中的微生物絮体解散，微生物细胞破裂，污泥中的有机物水解进而降低了污泥的黏度，降低了黏性物质对水的束缚能力；
3)水热单元出来的水热污泥从闪蒸反应器的上部进入，通过闪蒸反应器内部的扩容和入口管出的节流降压，水热污泥发生闪蒸，闪蒸后吸热，水热污泥温度降低，最后产生闪蒸蒸汽和闪蒸污泥，其中闪蒸蒸汽进入引射器中，闪蒸污泥进入余热回收单元中；
4)余热回收单元包括加热炉、冷却塔、第二低压变频泵、第二单螺杆泵和换热器；锅炉给水和冷却塔出来的循环冷却水首先进入第二低压变频泵升压，然后和经第二单螺杆泵升压的闪蒸污泥在换热器中换热；换热器出口流体分为两股，一股作为循环冷却水，另一股作为锅炉进水；换热器出口作为循环冷却水的那股流体进入冷却塔中冷却，换热后的冷 却污泥进入脱水机进行脱水，换热器出口作为锅炉进水的那股流体进入加热炉中加热产生水热蒸汽为水热单元提供热量；
5)脱水后的脱水泥饼外运，脱水滤液一部分用来进入均质浆化单元的引射器中，剩余脱水滤液返回污水处理厂处理。
本发明进一步的改进在于：步骤1)中机械脱水污泥的含水率为80％，粘度为50,000mPa·s到150,000mPa·s；第一单螺杆泵出来的污泥含水率为84％～85％，温度为90℃～100℃，粘度小于8000mPa·s；
水热单元出来的污泥含水率为86％～88％，温度为170℃～180℃，粘度小于100mPa·s。
本发明进一步的改进在于：稀释液在低压变频泵的作用下进入所述引射器喷嘴，引射周围的闪蒸蒸汽，两股流体在引射的过程中进行充分混合。
本发明进一步的改进在于：所述水热单元为间歇式水热单元；所述间歇式水热单元包括污泥水热蒸汽加热器、第一间歇式水热反应器和第二间歇式水热反应器；第一单螺杆泵出来的污泥从下部进入水热蒸汽加热器进行快速搅拌和加热，加热到热水解后从上部出来进入第一间歇式水热反应器使污泥在第一间歇式水热反应器中反应，同时，将第二间歇式水热反应器中的污泥通过压差向闪蒸反应器中排出，待第一间歇式水热反应器达到反应时间后，第一间歇式水热反应器开始排泥，而第二间歇式水热反应器开始进泥和反应，如此循环。
本发明进一步的改进在于：所述水热单元为辐流式水热反应器或塔式水热反应器；
辐流式水热反应器包括内筒、导流筒、外筒、内筒搅拌器和筒壁，均质浆化污泥和加热炉出来的水热蒸汽在内筒下部入口管进入，然后在内筒搅拌器的作用下达到反应参数，粘度降低，溢流进入导流筒，从导流筒下部的出口进入外筒大空间内，辐射式的向外流动，最后水热反应后的污泥进入外筒和筒壁之间的环形空间汇集后经下部的出口流出；
所述塔式水热反应器下进上出，塔式水热反应器下部采用有轴向力的强力搅拌器，塔式水热反应器上部采用无轴向力的搅拌器；均质浆化污泥和加热炉出来的水热蒸汽从塔式水热反应器下部进入，在有轴向力的强力搅拌器的作用下循环搅拌达到反应参数后，随着不断进入塔式水热反应器下部空间的均质浆化污泥的推动作用，达到反应参数的污泥进入塔式水热反应器上部，最终污泥在塔式水热反应器上部出口流出。
本发明进一步的改进在于：所述换热器为套管式换热器、板式换热器、螺旋板式换热器或热管式换热器；所述脱水机为板框压滤机、带式压滤机、离心机、箱式压滤机或者隔膜压滤机。
相对于现有技术，本发明具有以下有益效果：
1、本发明在污泥进入第一单螺杆泵之前先对其进行了均质，粘度显著降低，方便输运。污泥储罐、污泥均质器和第一单螺杆泵高度布置上逐渐降低，因此均质浆化单元输运可靠，不易堵塞。均质浆化单元中污泥储罐采用先切碎后绞龙输运的方式保证定量进入污泥均质的污泥都为小颗粒，提高均质效率。均质浆化单元中稀释液采用污泥脱水后滤液，一方面可以减少脱水滤液的处理量，节约***用水，另一方面可以回收脱水滤液的热量。均质浆化单元中稀释液和闪蒸蒸汽是在引射器中混合的，由于引射作用，混合效率较高，且能解决闪蒸蒸汽压力较低，不能直接进入污泥均质器的问题。引射混合物再一起进入污泥均质器中和污泥进行均质浆化。均质浆化过程中产生的废蒸汽再通入稀释液管道中进行吸收，可以避免进入大气造成异味，同时能在一定程度上进一步预热稀释液。
2、本发明的水热单元有多种形式，可以间歇式运行，也可以连续式运行。对于间歇式水热单元，水热蒸汽加热器下进上出可以保证加热时间，使得污泥有足够时间达到最佳反应参数。对于连续式水热单元，可以采用辐流式水热反应器或者塔式水热反应器，这两种反应器都集加热和反应为一体，其中辐流式水热反应器随着流动半径的增大，污泥流速 降低，因此反应时间可以有效保证；而塔式水热反应器具有大的高径比，下进上出，且上部采用仅有轴向力的搅拌器，这样上部污泥仅能靠下部污泥的推力流向出口，因此反应时间可以有效保证。
3、本发明的余热回收单元采用锅炉给水回收了闪蒸污泥的部分热量，从而可以节约加热炉的燃料量。余热回收单元中，换热器两侧流体的粘度都较低，因此换热器不易堵塞。
附图说明
图1为本发明的基于热水解技术的污泥脱水工艺流程图；
图2为本发明的间歇式水热单元示意图；
图3为本发明的辐流式水热反应器示意图；
图4为本发明的塔式水热反应器示意图。
图中：1、污泥储罐，2、污泥均质器，3、水热单元，4、闪蒸反应器，5、换热器，6、脱水机，7、冷却塔，8、加热炉，9、引射器，101、第一单螺杆泵，102、第二单螺杆泵，111、第一低压变频泵，112、第二低压变频泵，12、水热蒸汽加热器，13、间歇式水热单元，131、第一间歇式水热反应器，132、第二间歇式水热反应器，14、辐流式水热反应器，141、辐流式水热反应器内筒，142、辐流式水热反应器导流筒，143、辐流式水热反应器外筒，144、内筒搅拌器；145、辐流式水热反应器筒壁；15、塔式水热反应器，151、塔式水热反应器下部有轴向力强力搅拌器，152、塔式水热反应器上部无轴向力搅拌器。
图1中的图例和仪表代码含义见表1
表1
Figure PCTCN2014090726-appb-000001
Figure PCTCN2014090726-appb-000002
具体实施方式
参照图1所示，本发明的一种基于热水解技术的污泥脱水***，包括均质浆化单元、水热单元、闪蒸反应器、余热回收单元和脱水机。
均质浆化单元连接方式：机械脱水污泥在污泥储罐1中储存的同时污泥储罐1中的强剪切力搅拌器对污泥进行切碎，切碎后的小颗粒污泥通过污泥储罐1下部绞龙定量输送到污泥均质器2下部的污泥入口端，为了更好的输运，污泥储罐1设置在污泥均质器2的上方。脱水机6出来的部分脱水滤液作为稀释液进入第一低压变频泵111的入口端，第一低压变频泵111的出口端连接引射器9的入口端，同时，闪蒸反应器4输出的闪蒸蒸汽也进入引射器9，在稀释液的引射下一起进入污泥均质器2下部的引射混合物入口端，污泥均质器2上部的污泥出口端进入第一单螺杆泵101升压后进入水热单元3，为了更好的输运，污泥均质器2设置在第一单螺杆泵101的上方，污泥均质器2上部的废蒸汽出口端连接脱水机6出来的污泥稀释液管道。
闪蒸反应器连接方式：均质浆化单元出来的污泥进入水热单元3的入口端，水热单元3的出口端连接闪蒸反应器4上部的入口端，闪蒸反应器4下部的闪蒸污泥出口端连接余热回收单元。闪蒸反应器4上部的闪蒸蒸汽出口端连接连接引射器9的入口端。
余热回收单元连接方式：闪蒸反应器4出来的闪蒸污泥进入第二单螺杆泵102的入口端，第二单螺杆泵102的出口端连接换热器5的壳侧入口端。锅炉给水和冷却塔7出来的冷却水进入第二低压变频泵112的入口端，第二低压变频泵112的出口端连接换热器5的管侧入口端和闪蒸污泥换热。换热器5管侧出口端锅炉给水进入加热炉8的入口端，换热器5管侧出口端循环冷却水进入冷却塔7中冷却，换热器5壳侧出口端污泥进入脱水机6， 脱水后的脱水泥饼外运，一部分脱水滤液进入第一低压变频泵111的入口端，剩余脱水滤液返回污水处理厂处理。
水热单元3可以间歇式运行或者连续式运行。参照图2所示，间歇式水热单元13，基本流程连接方式如下：
均质浆化污泥进入水热蒸汽加热器12下部污泥入口端，加热炉8出口端的水热蒸汽进入水热蒸汽加热器12下部的水热蒸汽入口端，水热蒸汽加热器12上部出口端连接第一间歇式水热反应器131和第二间歇式水热反应器132，其中第一间歇式水热反应器131和第二间歇式水热反应器132并联。水热蒸汽加热器12和第一间歇式水热反应器131之间，水热蒸汽加热器12和第二间歇式水热反应器132之间，第一间歇式水热反应器131出口端，第二间歇式水热反应器132出口端均设有电动截止阀。
水热单元3可以间歇式运行或者连续式运行。连续式水热单元包括连续式水热反应器，连续式水热反应器可以是辐流式水热反应器14也可以是塔式水热反应器15。参照图3所示，辐流式水热反应器14基本流程连接方式如下：
辐流式水热反应器14是一个高径比小于1的容器，分为内筒141、导流筒142、外筒143、内筒搅拌器144和筒壁145，均质浆化污泥和加热炉8出来的水热蒸汽在内筒141下部入口管进入，然后在内筒搅拌器144的作用下达到反应参数，粘度显著降低，溢流进入导流筒142，从导流筒142下部的出口进入外筒143的大空间内，辐射式的向外流动以保证反应时间，最后水热反应后的污泥进入外筒和筒壁之间的环形空间汇集后经下部的出口流出。
参考图4所示，塔式水热反应器15基本流程连接方式如下：
塔式水热反应器15是一个高径比大于2的容器，下进上出，塔式水热反应器15下部采用有轴向力的强力搅拌器151，塔式水热反应器15上部采用无轴向力的搅拌器152。均 质浆化污泥和加热炉8出来的水热蒸汽从塔式水热反应器15下部进入，在有轴向力的强力搅拌器151的作用下循环搅拌达到反应参数后，随着不断进入塔式水热反应器15下部空间的均质浆化污泥的推动作用，达到反应参数的污泥进入塔式水热反应器15上部，由于塔式水热反应器15上部采用的是无轴向力的搅拌器152，所以能够保证反应时间，最终污泥在塔式水热反应器15上部出口流出。
图1所示的一种基于热水解技术的污泥脱水工艺，包括以下步骤：
1)含水率80％左右，粘度为50,000mPa·s到100,000mPa·s的机械脱水污泥在污泥储罐1中储存的同时污泥储罐1中的强剪切力搅拌器对污泥进行切碎，切碎后的小颗粒污泥通过污泥储罐1下部的绞龙定量输入到污泥均质器2下部的污泥入口端，颗粒粒径的减小可以提高后续的均质效果。污泥储罐1设置在污泥均质器2的上方，污泥均质器2设置在第一单螺杆泵101的上方是为了污泥更好的输运，不易堵塞。脱水机6出来的部分脱水滤液作为稀释液通过第一低压变频泵111进入引射器9中引射闪蒸蒸汽，引射的混合效率高，且能解决闪蒸蒸汽压力较低，不能直接进入污泥均质器2的问题。引射后混合流体再进入污泥均质器2中和污泥储罐1输入的污泥进行均质浆化，污泥均质器2中设有搅拌器，混合效率高。均质浆化后污泥的含水率为84％～85％，温度为90℃～100℃，粘度由初始的约100,000mPa·s降低到了8000mPa·s左右，污泥呈现均相浆状流体的状态，方便第一单螺杆泵101的输运，同时在均质浆化单元回收了闪蒸蒸汽的热量，节约了水热蒸汽的量，从而节约了燃气炉8的燃料量。均质浆化过程中产生的废蒸汽再通入脱水机6出来的污泥稀释液管道中进行吸收，可以废蒸汽避免进入大气造成异味，同时能在一定程度上进一步预热稀释液。
2)均质浆化污泥进入水热单元3中，水热单元3可以间歇式运行也可以连续式运行。余热回收单元中的水热蒸汽进入水热单元3对污泥进行加热，在加热过程中，污泥中的微 生物絮体解散，微生物细胞破裂，污泥中的有机物水解进而降低了污泥的黏度，降低了黏性物质对水的束缚能力。此外，当污泥被加热至一定温度时，污泥中的有机物细胞破裂，胞内的大分子有机物释放并水解，胞内与各类大分子相结合的水也被释放，导致水更容易与污泥颗粒分离。水热单元出来的污泥含水率为86％～88％，温度为170℃～180℃，粘度小于100mPa·s。
3)水热单元3出来的水热污泥从闪蒸反应器4的上部进入，通过闪蒸反应器4内部的扩容和入口管出的节流降压，水热污泥发生闪蒸，闪蒸后吸热，水热污泥温度降低，最后经过产生闪蒸蒸汽和闪蒸污泥，其中闪蒸蒸汽进入均质浆化单元的引射器9中，闪蒸污泥进入余热回收单元中。
4)余热回收单元包括加热炉8、冷却塔7、第二低压变频泵112、第二单螺杆泵102和换热器6。锅炉给水和冷却塔7出来的循环冷却水首先进入第二低压变频泵112升压，然后和经第二单螺杆泵102升压的闪蒸污泥在换热器5中换热，闪蒸污泥粘度较低，换热器5不易堵塞。换热器5出口循环冷却水进入冷却塔7中冷却，换热后的冷却污泥进入脱水机6进行脱水，换热器5出口锅炉给水进入加热炉8中加热产生水热蒸汽为水热单元提供热量。余热回收单元采用锅炉给水回收了部分闪蒸污泥的热量，从而可以节约加热炉8的燃料量。同时，闪蒸污泥经过余热回收单元后温度降低，水和污泥颗粒分离，方便后续脱水步骤的进行。
5)脱水后的脱水泥饼外运，脱水滤液一部分用来进入均质浆化单元的引射器9中，剩余脱水滤液返回污水处理厂处理。由于污泥经过水热反应后细胞破壁，胞内水分释放，有机物水解，胶体结构破坏，粘性降低，所以经过最后脱水后含水率可以显著降低，对于离心脱水含水率可以达到50％左右，对于压滤脱水含水率可以达到30％左右。
图2所示的间歇式水热单元13的工作原理如下：
间歇式水热单元13包括污泥水热蒸汽加热器12、第一间歇式水热反应器131和第二间歇式水热反应器132，均质浆化单元出来的污泥从下部进入水热蒸汽加热器12中进行快速搅拌和加热，由于水热蒸汽加热器12是下进上出的，所以能保证停留时间，这样就能保证污泥在加热到热水解最佳参数后才从上部出口进入第一间歇式水热反应器131或者第二间歇式水热反应器132中发生水热反应，由于水热反应器间歇式交替运行且电动截止阀可以控制水热反应器中污泥的输入和输出，因此反应时间可以准确控制。
图3所示的辐流式水热反应器14的工作原理如下：
辐流式水热反应器14是一个高径比小于1的容器，分为内筒141、导流筒142、外筒143、内筒搅拌器144和筒壁145，均质浆化污泥和加热炉8出来的水热蒸汽在内筒141下部入口管中进入，然后在内筒搅拌器144的作用下达到反应参数，粘度降低到100mPa·s以下，流动性非常好，就能平稳地溢流进入导流筒142，导流筒142下部设有出口，达到反应参数的污泥就能从导流筒142进入外筒143的大空间内，由于辐流式水热反应器14的高径比很小，所以污泥是辐射式的向外流动，随着流动半径的增大，流速降低，这样就能在反应器的有限空间内保证反应时间，最后水热反应后的污泥进入外筒和筒壁之间的环形空间汇集后经下部的出口流出。
图4所示的塔式水热反应器15的工作原理如下：
塔式水热反应器15是一个高径比大于2的容器，下进上出。塔式水热反应器15下部采用有轴向力的强力搅拌器151，可以使进来的均质浆化污泥以及水热蒸汽在强力搅拌器151的作用下循环搅拌快速达到反应参数，随着不断进入塔式水热反应器15下部空间的均质浆化污泥的推动作用，达到反应参数的污泥进入塔式水热反应器15的上部；由于塔式水热反应器15的上部采用无轴向力的搅拌器152，这样上部污泥仅能靠下部污泥的推力流向出口，因此反应时间可以有效保证，最终污泥在塔式水热反应器15的上部出口流出。

Claims (10)

  1. 一种基于热水解技术的污泥脱水***，其特征在于，包括均质浆化单元、水热单元、闪蒸反应器、余热回收单元和脱水机；
    均质浆化单元包括污泥储罐(1)、污泥均质器(2)和第一单螺杆泵(101)；污泥储罐(1)下部连接污泥均质器(2)下部的污泥入口端；污泥均质器(2)上部的污泥出口端通过第一单螺杆泵(101)连接水热单元(3)的入口端；
    水热单元(3)的出口端连接闪蒸反应器(4)上部的入口端，闪蒸反应器(4)下部的闪蒸污泥出口端连接余热回收单元的入口；
    余热回收单元的出口连接脱水机(6)；脱水机(6)的脱水滤液输出管道连接第一低压变频泵(111)的入口端，第一低压变频泵(111)的出口端连接引射器(9)的引射流体入口端；闪蒸反应器(4)的闪蒸蒸汽出口连接引射器(9)的被引射流体入口端，引射器(9)的出口连接污泥均质器(2)下部的引射混合物入口端，污泥均质器(2)上部的废蒸汽出口端连接脱水机(6)的污泥稀释液输出管道。
  2. 根据权利要求1所述的一种基于热水解技术的污泥脱水***，其特征在于，闪蒸反应器(4)闪蒸污泥出口端连接第二单螺杆泵(102)的入口端，第二单螺杆泵(102)的出口端连接换热器(5)的壳侧入口端；锅炉给水管道和冷却塔(7)的冷却水出口连接第二低压变频泵(112)的入口端，第二低压变频泵(112)的出口端连接换热器(5)的管侧入口端；换热器(5)管侧出口端一分为二，分别连接加热炉(8)的入口端和冷却塔(7)的入口端；换热器(5)壳侧出口端连接脱水机(6)。
  3. 根据权利要求1所述的一种基于热水解技术的污泥脱水***，其特征在于，污泥储罐(1)设置在污泥均质器(2)的上方；污泥均质器(2)设置在第一单螺杆泵(101)的上方。
  4. 根据权利要求1所述的一种基于热水解技术的污泥脱水***，其特征在于，水热 单元(3)为间歇式水热单元(13)或连续式水热单元；
    所述间歇式水热单元(13)包括水热蒸汽加热器(12)、第一间歇式水热反应器(131)和第二间歇式水热反应器(132)；第一单螺杆泵(101)的出口连接水热蒸汽加热器(12)下部污泥入口端，加热炉(8)的水热蒸汽出口端连接水热蒸汽加热器(12)下部的水热蒸汽入口端，水热蒸汽加热器(12)上部出口端连接并联的第一间歇式水热反应器(131)和第二间歇式水热反应器(132)，其中第一间歇式水热反应器(131)和第二间歇式水热反应器(132)并联；第一间歇式水热反应器(131)和第二间歇式水热反应器(132)的入口端和出口端均设有电动截止阀；第一间歇式水热反应器(131)和第二间歇式水热反应器(132)的出口端均连接闪蒸反应器(4)上部的入口端；
    所述连续式水热单元包括连续式水热反应器，连续式水热反应器为辐流式水热反应器(14)或塔式水热反应器(15)；
    辐流式水热反应器(14)是一个高径比小于1的容器；包括内筒(141)、导流筒(142)、外筒(143)、内筒搅拌器(144)和筒壁(145)，内筒搅拌器(144)设置于内筒(141)内部，导流筒(142)设置于内筒(141)外部，外筒(143)设置于筒壁(145)的内周；第一单螺杆泵(101)的出口和加热炉(8)的水热蒸汽出口连接内筒(141)下部入口管，外筒(143)和筒壁(145)之间环形空间下部的出口连接闪蒸反应器(4)上部的入口端；
    塔式水热反应器(15)是一个下进上出高径比大于2的容器；塔式水热反应器(15)下部采用有轴向力的搅拌器(151)，上部采用无轴向力的搅拌器(152)；第一单螺杆泵(101)的出口和加热炉(8)的水热蒸汽出口连接塔式水热反应器(15)下部入口；塔式水热反应器(15)上部出口连接闪蒸反应器(4)上部的入口端。
  5. 一种基于热水解技术的污泥脱水工艺，其特征在于，包括以下步骤：
    1)机械脱水污泥在污泥储罐(1)中储存的同时，污泥储罐(1)中的强剪切力搅拌 器对污泥进行切碎，切碎后的小颗粒污泥通过污泥储罐(1)下部的绞龙定量输入到污泥均质器(2)下部的污泥入口端，经过污泥均质器(2)处理的污泥通过污泥均质器(2)上部的污泥出口端输入第一单螺杆泵(101)，经过第一单螺杆泵(101)处理的污泥进入水热单元(3)；脱水机(6)出来的部分脱水滤液作为稀释液通过第一低压变频泵(111)进入引射器(9)中引射闪蒸蒸汽，引射后混合流体进入污泥均质器(2)中和污泥储罐(1)输入的污泥进行均质浆化，污泥均质器(2)中设有搅拌器；污泥均质器(2)产生的废蒸汽通入脱水机(6)出来的污泥稀释液管道中进行吸收；
    2)余热回收单元中的水热蒸汽进入水热单元(3)对污泥进行加热，在加热过程中，污泥中的微生物絮体解散，微生物细胞破裂，污泥中的有机物水解进而降低了污泥的黏度，降低了黏性物质对水的束缚能力；
    3)水热单元(3)出来的水热污泥从闪蒸反应器(4)的上部进入，通过闪蒸反应器(4)内部的扩容和入口管出的节流降压，水热污泥发生闪蒸，闪蒸后吸热，水热污泥温度降低，最后产生闪蒸蒸汽和闪蒸污泥，其中闪蒸蒸汽进入引射器(9)中，闪蒸污泥进入余热回收单元中；
    4)余热回收单元包括加热炉(8)、冷却塔(7)、第二低压变频泵(112)、第二单螺杆泵(102)和换热器(5)；锅炉给水和冷却塔(7)出来的循环冷却水首先进入第二低压变频泵(112)升压，然后和经第二单螺杆泵(102)升压的闪蒸污泥在换热器(5)中换热；换热器(5)出口流体分为两股，一股作为循环冷却水，另一股作为锅炉进水；换热器(5)出口作为循环冷却水的那股流体进入冷却塔(7)中冷却，换热后的冷却污泥进入脱水机(6)进行脱水，换热器(5)出口作为锅炉进水的那股流体进入加热炉(8)中加热产生水热蒸汽为水热单元提供热量；
    5)脱水后的脱水泥饼外运，脱水滤液一部分用来进入均质浆化单元的引射器(9)中， 剩余脱水滤液返回污水处理厂处理。
  6. 根据权力要求5所述的工艺，其特征在于，步骤1)中机械脱水污泥的含水率为80％，粘度为50,000mPa·s到150,000mPa·s；第一单螺杆泵(101)出来的污泥含水率为84％～85％，温度为90℃～100℃，粘度小于8000mPa·s；
    水热单元(3)出来的污泥含水率为86％～88％，温度为170℃～180℃，粘度小于100mPa·s。
  7. 根据权力要求5所述的工艺，其特征在于，稀释液在低压变频泵的作用下进入所述引射器喷嘴，引射周围的闪蒸蒸汽，两股流体在引射的过程中进行充分混合。
  8. 根据权力要求5所述的工艺，其特征在于，所述水热单元(3)为间歇式水热单元；所述间歇式水热单元包括污泥水热蒸汽加热器、第一间歇式水热反应器和第二间歇式水热反应器；第一单螺杆泵(101)出来的污泥从下部进入水热蒸汽加热器进行快速搅拌和加热，加热到热水解后从上部出来进入第一间歇式水热反应器使污泥在第一间歇式水热反应器中反应，同时，将第二间歇式水热反应器中的污泥通过压差向闪蒸反应器中排出，待第一间歇式水热反应器达到反应时间后，第一间歇式水热反应器开始排泥，而第二间歇式水热反应器开始进泥和反应，如此循环。
  9. 根据权力要求5所述的工艺，其特征在于，所述水热单元(3)为辐流式水热反应器或塔式水热反应器；
    辐流式水热反应器包括内筒、导流筒、外筒、内筒搅拌器和筒壁，均质浆化污泥和加热炉出来的水热蒸汽在内筒下部入口管进入，然后在内筒搅拌器的作用下达到反应参数，粘度降低，溢流进入导流筒，从导流筒下部的出口进入外筒大空间内，辐射式的向外流动，最后水热反应后的污泥进入外筒和筒壁之间的环形空间汇集后经下部的出口流出；
    所述塔式水热反应器下进上出，塔式水热反应器下部采用有轴向力的强力搅拌器，塔 式水热反应器上部采用无轴向力的搅拌器；均质浆化污泥和加热炉出来的水热蒸汽从塔式水热反应器下部进入，在有轴向力的强力搅拌器的作用下循环搅拌达到反应参数后，随着不断进入塔式水热反应器下部空间的均质浆化污泥的推动作用，达到反应参数的污泥进入塔式水热反应器上部，最终污泥在塔式水热反应器上部出口流出。
  10. 根据权力要求5所述的工艺，其特征在于，所述换热器为套管式换热器、板式换热器、螺旋板式换热器或热管式换热器；所述脱水机为板框压滤机、带式压滤机、离心机、箱式压滤机或者隔膜压滤机。
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