WO2012132799A1 - 水熱反応利用の汚泥メタン発酵処理方法及びシステム - Google Patents

水熱反応利用の汚泥メタン発酵処理方法及びシステム Download PDF

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Publication number
WO2012132799A1
WO2012132799A1 PCT/JP2012/055770 JP2012055770W WO2012132799A1 WO 2012132799 A1 WO2012132799 A1 WO 2012132799A1 JP 2012055770 W JP2012055770 W JP 2012055770W WO 2012132799 A1 WO2012132799 A1 WO 2012132799A1
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Prior art keywords
sludge
circulation path
circulation
methane fermentation
moisture content
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PCT/JP2012/055770
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English (en)
French (fr)
Japanese (ja)
Inventor
多田羅　昌浩
茂 菊池
信之 篠原
Original Assignee
鹿島建設株式会社
三菱長崎機工株式会社
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Application filed by 鹿島建設株式会社, 三菱長崎機工株式会社 filed Critical 鹿島建設株式会社
Priority to CN201280023941.6A priority Critical patent/CN103547537B/zh
Priority to KR1020127020844A priority patent/KR101228196B1/ko
Publication of WO2012132799A1 publication Critical patent/WO2012132799A1/ja

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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
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/001—Upstream control, i.e. monitoring for predictive control
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/05—Conductivity or salinity
    • C02F2209/055—Hardness
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a sludge methane fermentation treatment method and system utilizing a hydrothermal reaction, and more particularly to a method and system for methane fermentation treatment after sludge discharged from a sewage treatment plant or a wastewater treatment plant is reduced in molecular weight by a hydrothermal reaction. .
  • sludge In wastewater treatment plants such as sewage treatment plants, chemical factories, and food factories, the activated sludge method that microbially decomposes organic matter in sewage and wastewater is widely used, and a large amount containing solid matter such as undegraded organic matter and grown microorganisms.
  • Raw sludge and surplus sludge (hereinafter, both are collectively referred to as sludge).
  • Sludge must be disposed of as industrial waste, and many sludges have been disposed of in landfills after dehydration or incineration, but recently they have been reduced in volume and volume by avoiding incineration from the viewpoint of preventing global warming.
  • methane fermentation treatment technology that can reduce the volume and volume of sludge and at the same time recover methane gas as an energy resource is underway.
  • methane fermentation treatment technology it is possible to decompose sludge into methane gas using conventional methane fermentation treatment technology, the sludge contains a large amount of difficult-to-decompose solids derived from microorganisms, so the decomposition efficiency is low and it is decomposed into methane gas. It takes a very long time (for example, 15 to 30 days or more of digestion days), and there is a problem that the scale of equipment becomes large.
  • methane fermentation treatment is performed after sludge is depolymerized by pretreatment such as alkali treatment, ozone treatment, and ultrasonic treatment (for example, Patent Document 1). reference).
  • pretreatment such as alkali treatment, ozone treatment, and ultrasonic treatment
  • these pretreatments have not yet reached an economic balance from the viewpoint of energy consumption.
  • hydrothermal reaction hydrolysis reaction with high-temperature and high-pressure water
  • Hydrothermal reaction is hydrolysis using high-temperature and high-pressure water (hereinafter sometimes referred to as hot water) having an ionic product nearly 300 times lower than the critical point of water (374 ° C., 22 MPa) but having a temperature and pressure lower than 300 times. While it is a reaction and can hydrolyze sludge containing solids to a low molecule that can be easily fermented to methane in a short time by hydrolyzing action of hot water, it has weaker decomposition power than supercritical water reaction, Since it can be taken out before being decomposed into inorganic substances, it is said to be suitable for pretreatment of sludge (see Patent Documents 2 and 3).
  • hot water high-temperature and high-pressure water
  • Patent Document 2 the sludge slurry stored in the supply tank 6 is supplied to the hydrothermal reaction device 10a by a supply device (high pressure pump or the like) 7 through a heater 11a having a predetermined temperature.
  • a method for producing methane gas is disclosed in which, after molecularization, the aqueous phase separated from the low molecular weight treated product is introduced into the methane fermentation tank 20 by a metering pump 19a and subjected to methane fermentation.
  • the low molecular weight processed product after the hydrothermal reaction is temporarily stored in the raw material tank 19 and separated into three layers of an oil phase, an aqueous phase and a solid phase by a centrifuge (not shown), and the separated aqueous phase is separated into methane. Introduce into the fermenter 20. Methane gas generated in the methane fermentation tank 20 is collected in the gas tank 23 through a pipe.
  • a continuous hydrothermal reaction apparatus 10a for continuously reducing the molecular weight of sludge slurry
  • a batch type hydrothermal reaction apparatus can also be used.
  • Patent Document 3 discloses a sludge pretreatment method using a pulverization tank 8a, a supply tank 6, and a circulating hydrothermal reactor 10 as shown in FIG.
  • the sludge stored in the pulverization tank 8a in the illustrated example is pulverized into a slurry while circulating through a pulverization pump 8b and a three-way valve 8c (switched to the pulverization tank 8a side), and then the three-way valve 8c (supply tank). 6 is switched to the supply tank 6, and further supplied to the suction side of the circulation pump 14 of the hydrothermal reactor 10 via the supply device (Mono pump, etc.) 7 and the inlet 9. .
  • the supply device Monitoringo pump, etc.
  • the circulation type hydrothermal reaction apparatus 10 in the illustrated example includes a hydrothermal reactor 11 including a heat exchanger, a gas-liquid separator 12 and a circulation pump 14, and the supplied sludge slurry is converted into the hydrothermal reactor 11.
  • the molecular weight is reduced while circulating in the circulation path connecting the gas-liquid separator 12 and the circulation pump 14.
  • the sludge slurry continuously fed from the feed passage 9 to the hydrothermal reactor 10 is heated by the circulation pump 14 while ascending the inside of the thin tube group (heat exchanger) in the hydrothermal reactor 11.
  • the reaction temperature of the hydrothermal reaction hereinafter sometimes referred to as hot water temperature
  • the molecular weight is reduced, and the resultant is sent to the gas-liquid separator 12 via the upper communication pipe 11a.
  • the pressure difference between the hydrothermal reactor 11 and the gas-liquid separator 12 is eliminated by the pressure equalizing tube 11b, and the liquid level of the gas-liquid separator 12 is maintained constant by the control device 15.
  • a part of the decomposition aqueous solution (sludge with reduced molecular weight) in the gas-liquid separator 12 is self-pressured and overflows the liquid level control valve 15a. It is output to the outside of the reaction apparatus 10 through the passage 15b, and the remaining decomposition aqueous solution is returned again into the hydrothermal reactor 11 by the circulation pump 14 and circulated.
  • the internal volume of the circulation path coincide with the product (xy) of the sludge slurry feed amount x and the decomposition aqueous solution circulation time y, the sludge slurry circulation time y in the hydrothermal reactor 10 is kept constant.
  • the decomposition aqueous solution output to the outside can have a uniform concentration.
  • reference numeral 16 denotes a thermometer of the gas-liquid separator 12
  • reference numeral 17 denotes a pressure gauge with a pressure relief valve 17a
  • reference numeral 18 denotes a safety valve.
  • JP 2000-288594 A International Publication No. 2004/037731 Pamphlet JP 2008-296192 A JP 2000-167523 A
  • the continuous (or batch) hydrothermal reactor 10a shown in FIG. 5 is capable of reducing the molecular weight of a sludge slurry having a relatively low concentration, but sludge containing a high concentration of solids.
  • the pretreatment using the hydrothermal reactor 10a of FIG. 5 requires that the sludge be heated at a low concentration containing a large amount of water, and therefore requires relatively large heating energy for the low molecular weight treatment. Issues remain.
  • the circulating hydrothermal reaction apparatus 10 as shown in FIG. 6 can also perform a low molecular weight treatment on a high-concentration sludge slurry containing solids (for example, a sludge slurry having a solid content of 30 to 70% by weight). is there. That is, in the hydrothermal reactor 10 of FIG.
  • the circulation type hydrothermal reactor 10 must be periodically stopped to clean the scales fixed in the circulation path, while ensuring as long an operation duration as possible and avoiding an undesired blockage. In order to maintain the operation stably, it is required to suppress the growth of the scale in the circulation path to prevent the separation and dropping during the operation.
  • an object of the present invention is to provide a method and system capable of methane fermentation treatment of sludge energy-efficiently and stably over a long period of time using a circulating hydrothermal reaction.
  • the sludge Sa is adjusted to a predetermined moisture content, and then the adjusted sludge Sa is hydrothermally treated.
  • Low molecular weight sludge Sc that is sent to the circulation paths 14a and 14b connecting the reactor 11 and the gas-liquid separator 12 and circulated for a predetermined time at a predetermined temperature and pressure to lower the molecular weight and is output from the circulation paths 14a and 14b.
  • the sludge that continuously detects the scale adhering state in the circulation paths 14a and 14b and sends it to the circulation paths 14a and 14b according to the fluctuation of the adhering condition.
  • the water content of Sa is adjusted.
  • the sludge methane fermentation treatment system utilizing hydrothermal reaction includes a moisture content adjusting device 4 for adjusting the sludge S to a predetermined moisture content, a moisture content.
  • a circulating hydrothermal reactor that sends the adjusted sludge Sa to the circulation paths 14a and 14b connecting the hydrothermal reactor 11 and the gas-liquid separator 12 and circulates them at a predetermined temperature and pressure for a predetermined time to reduce the molecular weight. 10.
  • the adjustment device 4 adjusts the moisture content of the sludge Sa according to the fluctuation of the fixing state detected by the detection device 30.
  • the detection device 30 is a flow meter 31 and a flow control valve 32 that control the circulation flow rate of the sludge Sa in the circulation paths 14a and 14b to a predetermined flow rate.
  • the scale sticking situation in the circulation paths 14a and 14b is detected from the opening degree.
  • the detection device 30 is a thermometer 35 for measuring the surface temperature of the circulation paths 14a and 14b, and the scale sticking state in the circulation paths 14a and 14b is determined from the surface temperature of the circulation path 14b. May be detected.
  • a cleaning device 40 for performing water displacement cleaning or chemical cleaning for the inside of the circulation paths 14a and 14b of the hydrothermal reaction device 10 as shown in the figure, instead of or in addition to the adjustment of the moisture content of the sludge Sa described above. Then, the cleaning device 40 is driven according to the change in the fixed state.
  • the sludge S to be treated is adjusted to a predetermined moisture content by the moisture content adjusting device 4 before the sludge S is retained in the fermentation tank 20 and subjected to the methane fermentation treatment.
  • the sludge Sa is fed into the circulation paths 14a and 14b connecting the hydrothermal reactor 11 and the gas-liquid separator 12 and circulated for a predetermined time at a predetermined temperature and pressure to reduce the molecular weight. Since the scale sticking situation in the circulation paths 14a and 14b is continuously detected and the moisture content of the sludge Sa is adjusted by the adjusting device 4 according to the fluctuation of the sticking situation, the following effects are produced.
  • the scale fixing state in the hydrothermal reaction apparatus 10 may vary depending on the viscosity and other types of sludge S, but various adjustments can be made by adjusting the moisture content of the sludge S according to fluctuations in the scale fixing state. The sludge S can be reduced in energy efficiency efficiently.
  • FIG. 2 shows an embodiment in which the methane fermentation treatment system of the present invention is applied to volume reduction / reduction of sewage sludge S generated at the sewage treatment plant 1, for example.
  • the system of the illustrated example includes a moisture content adjusting device 4 that adjusts the moisture content of the sludge S, a circulating hydrothermal reaction device 10, and a methane fermentation tank 20.
  • Raw sludge and excess sludge S (for example, water content of about 97%) generated in the sewage treatment plant 1 are temporarily stored in the mixed sludge tank 2 and adjusted to a predetermined water content suitable for the hydrothermal reactor 10 by the water content adjusting device 4.
  • the sludge Sa after moisture content adjustment (hereinafter sometimes referred to as concentration-adjusted sludge Sa) is supplied to the reactor 10 via the supply tank 6.
  • concentration-adjusted sludge Sa concentration-adjusted sludge Sa
  • the water content adjusting device 4 includes the condensing agent adding device 5 to condense as much as possible the solid content having a small particle size in the sludge S and send it to the hydrothermal reaction device 10 so that the solid content is filtrated. In addition, it is prevented from being directly introduced into the methane fermentation tank 20.
  • the moisture content adjusting device 4 in the illustrated example is a concentration device such as a vacuum dehydrator, a centrifugal separator, or a filter press (overpressure dehydrator) that normally dehydrates and concentrates the sludge S having a high moisture content. Accordingly, a water supply device for adding water to the sludge S having a low water content and diluting it may be used, and both a concentration device and a water supply device may be included.
  • the concentration-adjusted sludge Sa whose water content has been adjusted by the adjusting device 4 is temporarily stored in the supply tank 6 and then continuously fed into a hydrothermal reaction device 10 described later by a supply device 7 such as a Mono pump.
  • the supply device 7 may be provided with a pulverizer 8 or a stirring device 6a (see FIG. 6), and the solid content in the concentration-adjusted sludge Sa may be appropriately pulverized or stirred before being supplied to the reactor 10. Further, as described above with reference to FIG. 6, the concentration-adjusted sludge Sa from the adjusting device 4 including the pulverization tank 8a and the pulverization pump 8b is pulverized by the pulverization tank 8a and the pulverization pump 8b and stored in the supply tank 6. Also good. By reducing the particle diameter D p of the solids by crushing the density adjustment sludge Sa, to reduce the terminal settling velocity u of the solids described below, resulting solids settling and fixed inside the reactor 10 Can be difficult.
  • FIG. 1 is an explanatory diagram of a methane fermentation treatment system in which the circulation type hydrothermal reaction device 10 of FIG. 2 is enlarged and displayed.
  • the reactor 10 in the illustrated example has a hydrothermal reactor 11 and a gas-liquid separator 12 that heat the concentration-adjusted sludge Sa to a predetermined temperature (hot water temperature of hydrothermal reaction) under a predetermined pressure.
  • the circulation pump 14 and the circulation paths 14a and 14b connecting them, and the concentration adjustment sent from the delivery path 9 to the circulation path 14a on the inlet side (suction side) of the circulation pump 14 by the delivery amount x The sludge Sa is reduced in molecular weight by circulating for a predetermined time y between the hydrothermal reactor 11 and the gas-liquid separator 12.
  • the illustrated hydrothermal reactor 10 connects the hydrothermal reactor 11 to an energy conversion device 25 (for example, a boiler), and converts methane gas G recovered in a methane fermentation tank 20 described later in the energy conversion device 25 into a heating medium (for example, steam, heat transfer oil, etc.) is converted into heating energy of H, supplied to the hydrothermal reactor 11, and the concentration-adjusted sludge Sa in the circulation paths 14a, 14b is 160 to 200 ° C. by heat exchange with the heating medium H. It is heated to a hot water temperature (for example, about 180 ° C.). Further, a pressure gauge 17 with a pressure valve 17a (see FIG.
  • the circulation rate v of the concentration-adjusted sludge Sa in the circulation paths 14a, 14b is the end of the solid content in the sludge. It sets so that it may become larger than the sedimentation speed u (v> u).
  • the terminal sedimentation velocity u of the solid content is obtained by using the gravitational acceleration g, the density ⁇ f of hot water and the viscosity ⁇ f , and the particle diameter D p and the density ⁇ p of the solid content suspended therein. It can be calculated by equation (1) based on the Stokes equation.
  • the formula (1) indicates that the terminal sedimentation velocity u increases as the solid content density ⁇ p increases or the particle diameter D p increases.
  • the terminal settling velocity u is at least 0
  • the range is from .004 to a maximum of 2.32 (m / sec). Therefore, for example, in the hydrothermal reactor 10 set to about 180 ° C., if the circulation speed v is set to 2.32 ⁇ 1.3 ⁇ 3 (m / sec) or more based on the above-described experimental findings of the present inventors. In addition, it is possible to suppress the sedimentation and sticking of the solid content in the circulation paths 14a and 14b.
  • a flow meter 31 and a flow control valve 32 are provided in the circulation path 14 b on the discharge side (delivery side) of the circulation pump 14, and the flow rate connected to the flow meter 31 and the flow control valve 32.
  • the control device 33 controls the circulation speed v of the concentration-adjusted sludge Sa in the circulation paths 14a and 14b to 1.3 times or more of the final sedimentation speed u of the solids, or at least 3 (m / sec) or more. is doing.
  • the circulation speed v in the circulation path 14b is measured by the flow meter 31, and the opening degree of the flow control valve 32 (for example, the cross-sectional area of the circulation path 14b by the throttle valve) is controlled so that the speed v becomes the set speed. ing.
  • the moisture content adjusting device 4 In order to further improve the energy efficiency in the circulating hydrothermal reactor 10, it is desirable to adjust the moisture content of the concentration-adjusted sludge Sa by the moisture content adjusting device 4. For example, in the reactor 10, it is possible to reduce the molecular weight of the sludge Sa whose moisture content has been adjusted within the range of 85 to 95%. However, the lower the moisture content of the concentration-adjusted sludge Sa, the higher the heating in the reactor 10 is. Energy can be kept small. However, as described above, even in the circulation type reactor 10, it is inevitable that the scale gradually settles and adheres to the inner surfaces of the circulation paths 14a and 14b. However, since the viscosity (and frictional force) increases as the moisture content of the concentration-adjusted sludge Sa decreases, the scale is more likely to adhere to the inner surfaces of the circulation paths 14a and 14b.
  • the hydrothermal reaction device 10 in the illustrated example continuously detects the scale adhesion state of the inner surfaces of the circulation paths 14a and 14b, and adjusts the moisture content of the concentration adjustment sludge Sa by the moisture content adjusting device 4 according to the scale adhesion state.
  • the thickness (or growth rate) of the scales on the inner surfaces of the circulation paths 14a and 14b is controlled by switching.
  • a measurement window is provided in the circulation paths 14a and 14b, and the measurement windows are appropriately opened and closed and visually confirmed.
  • an appropriate detection device 30 is preferably provided on the circulation paths 14a and 14b. For example, as shown in FIG.
  • a flow meter 31 and a flow control valve 32 provided in the circulation path 14b are used as the detection device 30, and the pressure loss in the circulation paths 14a and 14b is determined from the opening of the flow control valve 32. An increase is obtained, and the scale thickness (or growth rate) can be detected by calculation without stopping and opening the reactor 10 from the increase.
  • FIG. 1B shows another embodiment of the present invention in which a thermometer 35 for measuring the surface temperature (iron skin temperature) of the circulation paths 14a and 14b is used as a scale fixing state detection device 30.
  • a thermometer 35 for measuring the surface temperature (iron skin temperature) of the circulation paths 14a and 14b is used as a scale fixing state detection device 30.
  • the internal temperature of the circulation paths 14a and 14b for example, 180 ° C.
  • the temperature is lowered by the heat transfer coefficient h and the thermal conductivity of the pipe, and the surface temperature of the circulation paths 14a and 14b becomes (internal temperature ⁇ ) ° C.
  • the scale is fixed to the inner surfaces of the circulation paths 14a and 14b as shown in FIG.
  • the internal temperature (for example, 180 ° C.) is the heat transfer coefficient h of the boundary film inside the pipe and the heat conduction of the scale.
  • the temperature is lowered by the degree ⁇ ′ and the thermal conductivity ⁇ of the pipe, and the surface temperature becomes (internal temperature ⁇ ) ° C. That is, the surface temperature of the circulation paths 14a and 14b is lower than the internal temperature, and the temperature drop is necessarily increased by the fixing of the scale ( ⁇ > ⁇ ).
  • the film heat transfer coefficient h inside the pipe, the scale, and the thermal conductivity ⁇ ′ and ⁇ of the pipe can be obtained by calculation and analysis from the operating conditions of the reactor 10 and the properties of the concentration-adjusted sludge Sa. If the analysis value is used, the scale thickness (or growth rate) can be detected by calculating from the temperature drop ⁇ between the surface temperature (iron temperature) and the internal temperature without stopping and opening the reactor 10.
  • the reactor 10 is detected by detecting the scale fixing state from both the opening degree of the flow control valve 32 shown in FIG. 1 (A) and the surface temperature of the circulation paths 14a and 14b shown in FIG. 1 (B). It detects the fluctuation of the scale fixing situation inside quickly and accurately.
  • the illustrated hydrothermal reaction apparatus 10 is provided with a control device 38 that controls the moisture content adjusting device 4 by inputting a signal of a scale fixing state (for example, a scale thickness or a growth rate) detected by the fixing state detecting device 30. Yes.
  • the adjustment device 4 For example, after the initial moisture content of the concentration-adjusted sludge Sa is set to about 90 to 92% by the adjustment device 4, the operation of the hydrothermal reactor 10 is started, and the scale thickness (or growth rate) is below a predetermined allowable value. When the initial moisture content is maintained and the scale thickness (or growth rate) exceeds a predetermined allowable value, the moisture content of the concentration-adjusted sludge Sa by the moisture content adjusting device 4 is switched to about 93 to 95% via the control device 38. .
  • the control device 38 is not essential for the present invention, and for example, the moisture content adjusting device 4 can be manually switched based on the detection result of the detection device 30.
  • the concentration-adjusted sludge Sa is circulated at a flow rate of 3 (m / sec) or more for about 30 to 90 minutes while heating to 160 to 200 ° C. under a pressure of 1 MPa
  • the decomposition aqueous solution (low molecular weight-adjusted sludge) Sb output from the liquid level control valve 15a (see FIG. 6) of the gas-liquid separator 12 to the outside of the reactor 10 through the overflow path 15b is subjected to methane fermentation treatment.
  • a suitable low molecular organic substance having high degradability can be obtained.
  • the sludge Sb that has been reduced in molecular weight by the hydrothermal reactor 10 passes through the raw material tank 19 and the filtrate of the moisture content adjusting device 4 together with the methane fermentation tank 20 (see FIG. 2). ).
  • the methane fermentation tank 20 of FIG. 2 has a microorganism fixed bed 21 that holds the methane fermentation microorganism group at a high concentration, and retains the introduced low-molecular sludge Sb for a required time to contact the methane fermentation microorganism group. Decomposes to methane gas G.
  • the fermenter 20 can be filled with glass fiber or carbon fiber microbial carriers to form a fixed bed 21 (see Patent Document 4).
  • the methane fermentation tank 20 can be provided with a heat retention device (not shown) for maintaining the low molecular weight sludge Sb at the activation temperature of the methane fermentation microorganism group, and the low molecular weight sludge in the fermentation tank 20 by the heat retention device.
  • Sb is maintained at a fermentation temperature suitable for a methane fermentation microorganism, for example, at a medium temperature (about 37 ° C.) or a high temperature (about 55 ° C.) (see Patent Document 4).
  • the methane fermenter 20 used in the present invention is not limited to the illustrated example, and a floating bed system may be used instead of the fixed bed.
  • the methane gas G generated in the methane fermentation tank 20 is taken out via a gas line, desulfurized by a desulfurizer as necessary, and then stored in a gas tank 23.
  • the methane gas G stored in the gas tank 23 is converted into heating energy of a heating medium (for example, steam, heat transfer oil, etc.) H by the energy conversion device 25 (for example, a boiler) and used for heating the hydrothermal reaction device 10. be able to.
  • a heating medium for example, steam, heat transfer oil, etc.
  • the digested sludge remaining in the methane fermentation tank 20 after the recovery of the methane gas G is sent to the dehydrator 28 via the return tank 27, the filtrate is returned to the sewage treatment plant 1 as the return water D, and the remaining dehydrated sludge Sd is converted into the conventional dewatered sludge Sd.
  • the sewage sludge S discharged from the sewage treatment plant 1 according to the embodiment of FIG. 1 is subjected to methane fermentation treatment by the system of the present invention, so that the dewatered sludge Sd is 1/3 to 1/5 of the sewage sludge S by the dehydrator 28.
  • the volume can be reduced.
  • the present invention adjusts the moisture content of the sludge S according to the fluctuation of the scale fixing situation in the hydrothermal reaction apparatus 10, it is possible to suppress the required energy of the hydrothermal reaction as small as possible while preventing the growth of the scale, Sludge can be stably reduced in molecular weight for a long time with high energy efficiency. Further, by increasing the energy efficiency of the hydrothermal reactor 10, the required energy of the hydrothermal reactor 10 can be covered by the energy of methane gas recovered from the methane fermentation tank 20, and the volume of sludge S can be reduced and reduced by itself. It can be expected to be a system.
  • the scale fixing state in the hydrothermal reaction apparatus 10 may change depending on the viscosity and other types of sludge S, but various sludges S can be classified by adjusting the moisture content of the sludge S according to the scale fixing state. Regardless, the molecular weight can be reduced with high energy efficiency.
  • a cleaning device 40 that performs water displacement cleaning or chemical cleaning of the inside of the circulation paths 14a and 14b of the hydrothermal reaction device 10, and the above-described fixing state detection device 30 detects the scale fixing state. Accordingly, the cleaning device 40 can be driven.
  • the washing device 40 is driven according to the detection of the scale sticking state by the detection device 30. Thus, it is possible to determine whether or not the cleaning is necessary without stopping / opening the reaction apparatus 10 and to clean the reaction apparatus 10 at an optimal time.
  • the cleaning device 40 in the illustrated example is connected to an inlet path 9 of the hydrothermal reactor 10 via a switching valve 41 and to an overflow path 15b of the hydrothermal reactor 10 via a switching valve 42. And an extraction path.
  • the switching valve 41 is switched while the operation of the hydrothermal reactor 10 is continued, and the washing water W is continuously injected into the inlet path 9 for a predetermined time.
  • the inside of the circulation paths 14a and 14b is replaced with water.
  • the operation of the hydrothermal reactor 10 is stopped and the switching valves 41 and 42 are switched to connect the inlet path 9 and the overflow path 15b with the cleaning apparatus 40, respectively.
  • medical agent W is inject
  • the normal scale fixed to the circulation paths 14a and 14b is almost peeled off by performing water replacement inside the apparatus (continuous injection of the washing water W) for about 2 hours.
  • step S105 in the flowchart of FIG. 4
  • the switching valves 41 and 42 are returned to reconnect the inlet passage 9 and the overflow passage 15b with the supply tank 6 and the raw material tank 19 to adjust the concentration of the initial moisture content (about 90 to 92%).
  • the hydrothermal reaction of the sludge Sa can be resumed.
  • Even when the scales are relatively firmly laminated in the circulation paths 14a and 14b, for example, hydrogen peroxide-based chemical cleaning (circulation of the chemical W) can be performed almost for two hours (step). (See S106).
  • FIG. 4 shows an example of a flowchart of control of the moisture content adjusting device 4 and the cleaning device 40 by the control device 38.
  • the moisture content adjusting device 4 is set to the initial moisture content (about 90 to 92%), and then the operation of the hydrothermal reaction device 10 is started (see step S101). Based on the detected value (scale thickness or growth rate), an abnormal tendency (necessity of cleaning) in the circulation paths 14a and 14b is determined (see step S102).
  • the scale thickness (or growth rate) when the scale thickness (or growth rate) is below a predetermined allowable value, it is determined that there is no abnormality and normal operation of the initial moisture content is continued. Whether or not the moisture content adjusting device 4 or the cleaning device 40 needs to be driven is determined according to the detected value of the thickness or the growth rate (see step S103).
  • Step S103 in the flowchart of FIG. 4 classifies the abnormal level into three stages based on the detection value (scale thickness or growth rate) of the sticking state detection device 30. For example, when the detected value exceeds the predetermined allowable value but is less than the predetermined limit value (level 1), the water content adjusting device 4 is controlled by the control device 38 so that the water content of the concentration-adjusted sludge Sa is about 93 to 95%. The operation of the hydrothermal reactor 10 is continued while switching to (step S104). Further, when the detected value is not less than the predetermined limit value but less than the predetermined abnormal value (level 2), the switching valve 41, 42 is switched while the operation of the hydrothermal reactor 10 is continued, and the cleaning water W is injected.
  • the detection value scale thickness or growth rate
  • Step S105 The inside of the circulation paths 14a and 14b of the reaction apparatus 10 is washed by water replacement.
  • a scale thickness (or growth rate) equal to or greater than a predetermined abnormal value is detected (level 3)
  • the operation of the hydrothermal reactor 10 is stopped and the inside of the circulation paths 14a and 14b is chemically cleaned by the cleaning device 40 ( Step S106).
  • the hydrothermal reactor 10 can be recovered by water replacement for about 2 hours in the circulation paths 14a and 14b. After the water replacement, the initial moisture content is normal immediately by returning the switching valves 41 and 42. Since the operation can be returned to the operation (step S101), it is not necessary to stop the operation of the hydrothermal reactor 10. Accordingly, while appropriately adjusting the moisture content of the sludge Sa (step S104) by the moisture content adjusting device 4, the water replacement cleaning (step S105) of the circulation paths 14a and 14b is performed about once every 10 days to January.
  • the hydrothermal reactor 10 can be stably operated (continuous operation) for a long time, and the chemical cleaning (step S106) of the circulation paths 14a and 14b is performed once every six months to once a year or on the assumption. It is sufficient if it is performed when abnormal scale sticking occurs.

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PCT/JP2012/055770 2011-03-27 2012-03-07 水熱反応利用の汚泥メタン発酵処理方法及びシステム WO2012132799A1 (ja)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2746231A1 (en) * 2012-12-19 2014-06-25 CS Carbon Solutions Method and apparatus for the treatment of process water from a hydrothermal organic material conversion process
WO2017102814A1 (de) * 2015-12-15 2017-06-22 Terranova Energy Gmbh Verfahren zur faulung und hydrothermalen karbonisierung von klärschlamm
JP2018143903A (ja) * 2017-03-01 2018-09-20 鹿島建設株式会社 メタン発酵バイオリアクタ及びその洗浄方法

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105331376B (zh) * 2015-11-27 2017-10-10 华中农业大学 基于微波水热碳化的新鲜生物质高值化处理装置及方法
JP6927510B2 (ja) * 2016-07-08 2021-09-01 学校法人金井学園 加熱撹拌装置
WO2019026780A1 (ja) * 2017-07-31 2019-02-07 学校法人長崎総合科学大学 バイオフィルター装置及びこれを用いた下水汚泥残渣脱水ろ液処理システム
JP6925032B2 (ja) * 2017-07-31 2021-08-25 学校法人長崎総合科学大学 バイオフィルター装置及びこれを用いた下水汚泥残渣脱水ろ液処理システム
JP7144027B2 (ja) * 2018-05-25 2022-09-29 学校法人長崎総合科学大学 液肥の製造方法
CN112716293B (zh) * 2021-01-27 2022-12-06 上海朴道水汇环保科技股份有限公司 一种检测饮水机加热热胆水垢的方法及系统

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000140620A (ja) * 1998-11-06 2000-05-23 Hitachi Ltd 超臨界流体を用いた反応装置
JP2002224690A (ja) * 2001-02-01 2002-08-13 Shinko Pantec Co Ltd 有機性被処理液の酸化処理装置及びそのスケール除去方法
JP2008002875A (ja) * 2006-06-21 2008-01-10 Ihi Corp 水熱処理装置の閉塞検知方法
JP2008296192A (ja) * 2007-06-04 2008-12-11 Osaka Prefecture Univ 循環型連続式亜臨界水反応処理装置
JP2011507673A (ja) * 2007-09-03 2011-03-10 ピーエムシー コリア カンパニー リミテッド スラッジ処理装置及び方法

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007063027A1 (de) 2007-12-28 2009-07-09 Neue Magnetodyn Gmbh Kontaktvorrichtung für die Osteosynthese

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000140620A (ja) * 1998-11-06 2000-05-23 Hitachi Ltd 超臨界流体を用いた反応装置
JP2002224690A (ja) * 2001-02-01 2002-08-13 Shinko Pantec Co Ltd 有機性被処理液の酸化処理装置及びそのスケール除去方法
JP2008002875A (ja) * 2006-06-21 2008-01-10 Ihi Corp 水熱処理装置の閉塞検知方法
JP2008296192A (ja) * 2007-06-04 2008-12-11 Osaka Prefecture Univ 循環型連続式亜臨界水反応処理装置
JP2011507673A (ja) * 2007-09-03 2011-03-10 ピーエムシー コリア カンパニー リミテッド スラッジ処理装置及び方法

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2746231A1 (en) * 2012-12-19 2014-06-25 CS Carbon Solutions Method and apparatus for the treatment of process water from a hydrothermal organic material conversion process
WO2017102814A1 (de) * 2015-12-15 2017-06-22 Terranova Energy Gmbh Verfahren zur faulung und hydrothermalen karbonisierung von klärschlamm
JP2018143903A (ja) * 2017-03-01 2018-09-20 鹿島建設株式会社 メタン発酵バイオリアクタ及びその洗浄方法

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