WO2013103124A1 - Procédé et dispositif de traitement biologique pour eaux usées organiques - Google Patents

Procédé et dispositif de traitement biologique pour eaux usées organiques Download PDF

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Publication number
WO2013103124A1
WO2013103124A1 PCT/JP2012/083883 JP2012083883W WO2013103124A1 WO 2013103124 A1 WO2013103124 A1 WO 2013103124A1 JP 2012083883 W JP2012083883 W JP 2012083883W WO 2013103124 A1 WO2013103124 A1 WO 2013103124A1
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biological treatment
treatment tank
last
tank
stage
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PCT/JP2012/083883
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English (en)
Japanese (ja)
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繁樹 藤島
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栗田工業株式会社
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Priority to CN201280066071.0A priority Critical patent/CN104039715B/zh
Priority to JP2013552420A priority patent/JP5874741B2/ja
Publication of WO2013103124A1 publication Critical patent/WO2013103124A1/fr

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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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/08—Aerobic processes using moving contact bodies
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2806—Anaerobic processes using solid supports for microorganisms
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • 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
    • C02F2101/20—Heavy metals or heavy metal compounds
    • C02F2101/22—Chromium or chromium compounds, e.g. chromates
    • 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
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • 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
    • C02F2209/22—O2
    • 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
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the present invention relates to a biological treatment method and apparatus for organic wastewater that can be used for treatment of organic wastewater in a wide concentration range such as domestic wastewater, sewage, food factory, pulp factory, semiconductor production wastewater, and liquid crystal production wastewater.
  • the present invention relates to a biological treatment method and apparatus for organic wastewater that can improve treatment efficiency and reduce the amount of excess sludge generation without deteriorating the quality of treated water.
  • the activated sludge method used when biologically treating organic wastewater is widely used for sewage treatment, industrial wastewater treatment, and the like because of its advantages such as good treated water quality and easy maintenance.
  • the BOD volumetric load in the activated sludge method is generally about 0.5 to 0.8 kg / m 3 / d, a large site area is required.
  • 20 to 40% of the decomposed BOD is converted into microbial cells, that is, sludge, a large amount of excess sludge is generated.
  • the activated sludge method includes a membrane activated sludge method that uses a membrane separator for solid-liquid separation of sludge and treated water, and a sedimentation basin type activated sludge method that uses a sedimentation basin.
  • a fluidized bed method with a carrier added For high load treatment of organic waste water, a fluidized bed method with a carrier added is known. When this method is used, it is possible to operate with a BOD volume load of 3 kg / m 3 / d or more. However, in this method, the amount of generated sludge is about 30 to 50% of the decomposed BOD, which is higher than that of the normal activated sludge method.
  • Patent Document 1 organic wastewater is first treated with bacteria in a first treatment tank, and organic matter contained in the wastewater is oxidatively decomposed and converted into non-aggregating bacterial cells, and then in a second treatment tank. It is described that excess sludge can be reduced by predatory removal of the sticking protozoa. Patent Document 1 describes that according to this method, a high-load operation is possible and the processing efficiency of the activated sludge method is improved.
  • Patent Document 2 describes a countermeasure against deterioration in processing performance due to fluctuations in the quality of raw water, which is a problem in the processing method of Patent Document 1.
  • the method includes “adding a microbial preparation or seed sludge to the first treatment tank when the quality of the first treated water deteriorates”.
  • Patent Document 3 discloses that flocs that are preyed by sonication or mechanical stirring when protozoa or metazoans prey on bacteria, yeast, actinomycetes, algae, fungi, or wastewater treatment primary sediment sludge or surplus sludge. A method to make the flock size smaller than the animal's mouth is proposed.
  • Patent Document 4 There is a method described in Patent Document 4 as a biological treatment method of organic wastewater by a multi-stage treatment of fluidized bed and activated sludge process.
  • the activated sludge process at the latter stage is operated at a low load of BOD sludge load 0.1 kg-BOD / kg-MLSS / d, so that the sludge can be self-oxidized and the amount of sludge extraction can be reduced.
  • the above-mentioned multistage activated sludge method using the predatory action of micro animals is actually used for organic wastewater treatment, and depending on the target wastewater, it is possible to improve the treatment efficiency and reduce the amount of generated sludge.
  • this sludge reduction effect is often not stable.
  • the present invention solves the above-mentioned conventional problems, and in the biological treatment of organic wastewater to which the multistage activated sludge method is applied, the amount of generated sludge is greatly reduced and the treatment efficiency is improved by high-load operation and is stable. It is an object of the present invention to provide a biological treatment method and apparatus for organic wastewater for improving the quality of treated water.
  • the organic wastewater biological treatment method of the present invention is the organic wastewater biological treatment method in which organic wastewater having a COD Cr volumetric load of 1 kg / m 3 / d or more is biologically treated in a biological treatment tank provided in multiple stages.
  • the first biological treatment water in which the dispersal bacteria are increased is generated by the decomposition of the organic matter by the dispersal bacteria, and the swing bed carrier is installed in the last-stage biological treatment tank.
  • a biofilm is attached, and the last-stage biological treatment water of the last-stage biological treatment tank is settled and separated by an upward flow of LV1 to 20 m / h in or outside the last-stage biological treatment tank, and any of the sludge It is returned to the biological treatment tank.
  • the organic wastewater biological treatment apparatus of the present invention is an organic wastewater biological treatment apparatus for biologically treating organic wastewater having a COD Cr volumetric load of 1 kg / m 3 / d or more in multiple stages.
  • the first biologically treated water in which the dispersal bacteria increased is generated by the decomposition of the organic matter by the dispersal bacteria
  • the swing bed carrier is installed in the last biological treatment tank, and the biofilm is attached to the swing bed carrier.
  • a biological treatment apparatus for organic wastewater that generates stage biologically treated water, wherein the last stage biologically treated water provided inside or outside the last stage biologically treated tank is LV1 to 20 m / h in an upward flow It is characterized by comprising sedimentation separation means for sedimentation and return means for returning sedimentation sludge to any biological treatment tank.
  • the sedimentation separation is performed in a non-aggregating manner.
  • the “non-aggregation method” refers to an operation method in which the flocculant is not added continuously or intermittently from the biological treatment tank to the sedimentation separation means during normal operation. Temporary addition of flocculant at the start-up of equipment with little sludge or sludge disassembly trouble does not fall under "addition of flocculant during normal operation”. Even if a flocculant is temporarily added at times, it is included in the “non-aggregation method”. In addition, a case where a small amount of an aggregating agent that does not substantially perform the aggregating treatment is added to the non-aggregating method.
  • the addition amount of a small amount of the flocculant that does not substantially perform the flocculant treatment varies depending on the type of flocculant to be used, but in terms of constant addition, the inorganic flocculant is 100 mg / L or less, high The molecular flocculant is 1 mg / L or less.
  • the present invention does not exclude any coagulation treatment of the supernatant water obtained by sedimentation separation.
  • a partition is provided on the drain outlet side of the last-stage biological treatment tank to form an ascending flow path.
  • the liquid in the tank is circulated upwardly at LV1-20m / h to settle and separate the sludge.
  • the settled sludge is returned to the last biological treatment tank, and the supernatant water that has risen through the ascending channel is discharged out of the tank. To do.
  • a sheet-like foamed plastic is suitable.
  • an oscillating bed carrier is provided as a scaffold for fixed filtration predatory microanimals that prey on dispersal bacteria.
  • a rocking bed carrier produces sludge with good sedimentation, so that it has a higher LV (1 to 20 m / h) than the LV of 0.5 m / h or less that is generally employed in sedimentation separation after biological treatment.
  • the sedimentation is separated in h).
  • This sedimentation separation can also be a non-aggregation method. According to the non-aggregation type sedimentation separation, sludge with poor sedimentation can be discharged out of the tank, and sludge with good sedimentation can be selectively retained in the tank.
  • the oscillating bed carrier but also sludge with good sedimentation can be used as a scaffold for minute animals to maintain a high microorganism concentration.
  • a partition is provided on the outlet side of the last biological treatment tank, and the water in the tank is passed in an upward flow of LV1 to 20 m / h, and only the sludge with good sedimentation property that does not float is left in the tank. It is preferable to do so.
  • a sedimentation separation means a sedimentation tank may be provided after the last biological treatment tank.
  • FIG. 1 to 4 are system diagrams showing an embodiment of a biological treatment method and apparatus for organic wastewater according to the present invention.
  • 1 is a first biological treatment tank
  • 2 is a second biological treatment tank
  • 11 and 21 are air diffusers
  • 12 is a fluidized bed carrier
  • 16 is a screen for carrier separation
  • 22 is a rocking bed carrier.
  • reference numeral 23 denotes a partition plate provided in the second biological treatment tank 2
  • reference numeral 24 denotes an ascending channel. In the ascending channel 24, sludge is settled and separated.
  • members having the same function are denoted by the same reference numerals.
  • raw water (organic wastewater) is introduced into the first biological treatment tank 1 at a BOD volumetric load of 1 kg / m 3 / d or more, for example, 1 to 20 kg / m 3 / d, and aerated by an air diffuser 11.
  • 70% or more, desirably 80% or more, more desirably 85% or more of the organic component (soluble BOD) is oxidatively decomposed by dispersible bacteria (non-aggregating bacteria).
  • the pH of the first biological treatment tank 1 is preferably 6 to 8.5. However, when the raw water such as food manufacturing wastewater contains a lot of oil, or when the raw water such as semiconductor manufacturing wastewater or liquid crystal manufacturing wastewater contains a lot of organic solvent or cleaning agent, the pH is 8 It can be ⁇ 9.
  • the water flow to the 1st biological treatment tank 1 shall be a transient type.
  • the BOD volumetric load of the first biological treatment tank 1 is 1 kg / m 3 / d or more, for example 1 to 20 kg / m 3 / d
  • HRT raw water residence time
  • HRT raw water residence time
  • the first biological treatment tank 1 is composed of two or more tanks, or a fluidized bed carrier is added.
  • high load processing with a BOD volumetric load of 5 kg / m 3 / d or more is also possible.
  • the shape of the fluidized bed carrier is arbitrary such as a spherical shape, a pellet shape, a hollow cylindrical shape, a thread shape, and a plate shape, and the size (diameter) is about 0.1 to 10 mm.
  • the material of the carrier is arbitrary such as a natural material, an inorganic material, or a polymer material, and a gel material may be used.
  • the filling rate of the carrier added to the first biological treatment tank 1 is excessively high, dispersal bacteria are not generated, and bacteria adhere to the carrier or filamentous bacteria grow. Therefore, by setting the filling rate of the carrier to be added to the first biological treatment tank 1 to 10% or less, desirably 5% or less, for example 0.5 to 5%, dispersible bacteria that are not affected by concentration fluctuation and are easy to prey. Can be generated.
  • the filling rate of the carrier represents the ratio of the volume of the carrier to the volume of the liquid in the first biological treatment tank 1.
  • the dissolved oxygen (DO) concentration in the first biological treatment tank 1 may be 1 mg / L or less, preferably 0.5 mg / L or less to suppress the growth of filamentous bacteria.
  • Treated water from the first biological treatment tank 1 (first biological treated water) is passed through the second biological treatment tank 2 at the subsequent stage, aerated, and oxidative decomposition of remaining organic components, self-degradation of dispersible bacteria. And reduce excess sludge by predation of micro-animals.
  • filtration predation type microanimals such as stag beetles and stag beetles are suitable.
  • a partition plate 23 is provided so as to surround the outlet portion, and is divided into an ascending flow path 24 and a biological treatment chamber. .
  • the upper end of the partition plate 23 protrudes from the water surface of the second biological treatment tank 2.
  • the lower end of the partition plate 23 is located 2 m or more from the water surface of the second biological treatment tank 2, particularly 3 to 4 m below.
  • the partition plate 23 faces a part of the side wall of the second biological treatment tank 2, and a rising channel 24 is formed between the side wall and the partition plate 23.
  • the lower part of the ascending channel 24 communicates with the biological treatment chamber in the second biological treatment tank 2.
  • the supernatant water flows out of the tank 2 through the outlet part of the tank 2.
  • the air diffuser 21 is installed away from the ascending channel 24, and the air diffuser 21 does not exist below the ascending channel 24. This is to prevent bubbles from the diffuser tube 21 from directly flowing into the ascending flow path 24.
  • the LV of the upward flow in the upward flow path 24 is 1 to 20 m / h, preferably 3 to 15 m / h.
  • a surplus sludge take-out pipe 25 is provided in the biological treatment chamber of the second biological treatment tank 2.
  • the sludge settled in the ascending flow path 24 returns to the second biological treatment tank 2.
  • the supernatant water from which the sludge is separated by ascending the ascending channel 24 flows out of the tank 2 from the outlet.
  • the supernatant water that flows out may contain sludge with poor sedimentation.
  • the dissolved oxygen (DO) concentration in the second biological treatment tank 2 is preferably about 1 to 4 mg / L.
  • the second biological treatment tank 2 it is necessary to use an operation condition and a treatment apparatus that allow the microanimal and the bacteria to remain in the system in order to use the action of the microanimal having a slower growth rate than the bacteria and the autolysis of the bacteria. . Therefore, the second biological treatment tank 2 is provided with a rocking bed carrier 22, and sludge is adhered to the surface to form a biological film. By installing this rocking bed carrier, the amount of micro-animal retained in the tank increases.
  • the swing bed carrier 22 is preferably disposed above the air diffuser 21.
  • the swing bed carrier preferably has an apparent surface area that is large enough for a micro animal to lay eggs and grow easily. Moreover, the rocking bed carrier is preferably one that has flexibility, does not inhibit water flow, and easily peels off the biofilm.
  • a soft sheet that satisfies the following conditions is preferable. 1) As for the sheet size, it is preferable that the length of the tank in the depth direction is 100 to 400 cm, the depth of the tank in the horizontal direction is 5 to 200 cm, and the thickness is 0.5 to 5 cm. 2) It is preferable to have at least two surfaces having an apparent surface area of 500 cm 2 or more. 3)
  • the material is preferably a foamed synthetic resin (foamed plastic), particularly a flexible polyurethane foam.
  • the pore diameter is preferably 0.05 to 10 mm in order to allow sludge to adhere easily and to be easily removed.
  • the number of foam cells is preferably 5 to 125 cells / 25 mm.
  • carrier a thing with uniform distribution of a foam cell is preferable. If there are too many foamed cells in the porous carrier or if the cell diameter is too large, the mechanical strength of the porous carrier will be reduced. Therefore, as described above, the number of cells / 25 mm (cells existing in a 25 mm length range) Number) is preferably about 125/25 mm. Conversely, if the number of foamed cells is too small or the cell diameter is too small, the function as a porous carrier cannot be obtained sufficiently.
  • the lower limit of / 25 mm is preferably about 5/25 mm.
  • a photo of the porous carrier taken with a scanning electron microscope was used to measure the number of foamed cells intersecting the straight line 25 mm in the length direction at a plurality of locations. The average value of the results can be calculated and obtained.
  • the oscillating bed carrier When a porous sheet-like oscillating bed carrier such as a thin plate-like or strip-like lightweight polyurethane foam is installed in the second biological treatment tank 2, the oscillating bed carrier has sufficient elasticity, Even if it is thin, it has sufficient mechanical strength and is not damaged by bending in the water flow in the tank. Moreover, by bending, it mixes uniformly, without inhibiting the water flow in a tank, and a sludge containing liquid comes to flow uniformly also into the porous structure of a support
  • a preferred installation form of the swing bed carrier is as follows.
  • the [apparent surface area of the rocking bed carrier] / [volume of the biological treatment tank] is 1 to 50 [m ⁇ 1 ].
  • the apparent surface area is the surface area of the outer surface that does not take into account the surface area inside the porous body.
  • the total surface area of six surfaces (length ⁇ width ⁇ 2 + length ⁇ thickness ⁇ 2 + thickness ⁇ width ⁇ 2)
  • the filling rate of the rocking bed carrier is 0.1 to 20% of the total volume of the biological treatment tank after the biological treatment tank with micro animals (including the biological treatment tank in the return line). . (Increased carrier amount with increasing load)
  • a strip-shaped sheet is installed in the tank as the rocking bed carrier so that the longitudinal direction of the rocking bed carrier is the depth direction of the tank (vertically downward).
  • the direction in the short direction of the swing bed carrier is not particularly limited, and for example, it can be installed in the tank so as to be substantially perpendicular to the direction of water flow from the inflow side to the outflow side.
  • the capacity of the second biological treatment tank is larger than the size of the carrier, prepare a plurality of pieces with fasteners attached to the upper and lower surfaces of the carrier, and use them in the depth direction of the second biological treatment tank and / Or a predetermined number in parallel in the width direction, fixing a fastener with a carrier attached to a frame material made of SUS or the like to form a unit, and further, this carrier unit in the second biological treatment tank as needed Provide multiple sheets in the direction of water flow.
  • the second biological treatment tank 2 may be further filled with a fluidized bed carrier in addition to the rocking bed carrier.
  • a fluidized bed carrier the aforementioned one used for the first biological treatment tank is suitable.
  • the filling rate of the carrier is excessively high, mixing in the tank, sludge decay, etc. may occur.
  • the filling rate is preferably about 0.5 to 30%, particularly about 1 to 10%.
  • the pH of the second biological treatment tank 2 may be 7.0 or less.
  • the second biological treatment tank 2 not only the filtration predation type micro-animal that prey on the dispersed cells but also the aggregate predation type micro-animal that can prey on the floc sludge grows. Since the latter prey on flocs while swimming, if prioritized, sludge is eaten and becomes sludge in which fine floc pieces are scattered (sludge with poor sedimentation). In addition, this floc piece causes clogging of the membrane particularly in the membrane activated sludge method in which membrane separation is performed in the latter stage. Therefore, in order to thin out aggregate predation type micro-animals, it is desirable to control SRT (sludge retention time) to be constant within a range of 60 days or less, preferably 45 days or less. However, if the SRT is less than 15 days, it is unnecessarily frequent and the number of not only the aggregate predation type micro-animals but also the filter predation type micro-animals is reduced too much.
  • SRT sludge retention time
  • the first biological treatment tank 1 it is necessary to decompose most of the organic matter, that is, 70% or more of the wastewater BOD, desirably 80% or more, and convert it into microbial cells.
  • the organic substances When the organic substances are completely decomposed, flocs are not formed in the second biological treatment tank 2, and there is not enough nutrients for the growth of micro-animals. Only sludge with poor compaction (sludge with poor sedimentation) is excellent. It becomes an occupied biological treatment tank. Therefore, as shown in FIG.
  • the MLSS at this time includes MLSS for the carrier adhering.
  • the separated water that has been separated by settling with an upward flow of LV 1 to 20 m / h may be subjected to membrane separation, coagulation sedimentation, or pressurized flotation as solid-liquid separation.
  • membrane separation coagulation sedimentation
  • pressurized flotation as solid-liquid separation.
  • the amount of coagulant added can be reduced.
  • FIG. 3 the supernatant water after sedimentation from the second biological treatment tank 2 is coagulated in the coagulation tank 4, and then precipitated in the solid-liquid separation tank (sedimentation tank) 5 to be separated into treated water and sedimented sludge. To do.
  • the flocculant it is preferable to use an inorganic flocculant or an inorganic flocculant and an organic polymer flocculant.
  • the inorganic flocculant is not particularly limited, and any inorganic flocculant that has been conventionally used for wastewater coagulation sedimentation treatment can be used.
  • ferrous sulfate, ferric sulfate, ferrous chloride, ferric chloride, ferric sulfate and other iron-based flocculants, aluminum sulfate, aluminum chloride, polyaluminum chloride and other aluminum-based A flocculant etc. are mentioned.
  • These inorganic flocculants may be used alone or in combination of two or more.
  • the amount of the inorganic flocculant added varies depending on the type of inorganic flocculant and the properties of the raw water, and cannot be generally stated, but is usually about 50 to 500 mg / L.
  • the flocculation treatment in which the inorganic flocculant is added it is preferable to adjust to pH conditions suitable for the inorganic flocculant.
  • an alkali such as sodium hydroxide or an acid such as sulfuric acid or hydrochloric acid can be used for pH adjustment.
  • the coagulation reaction tank is preferably stirred at about 70 to 200 rpm.
  • organic polymer flocculant used to coarsen the flocs formed by the flocculant treatment with the inorganic flocculant there is no particular limitation on the organic polymer flocculant used to coarsen the flocs formed by the flocculant treatment with the inorganic flocculant, and any organic polymer flocculant usually used in wastewater flocculation can be used. is there.
  • poly (meth) acrylic acid, a copolymer of (meth) acrylic acid and (meth) acrylamide, and alkali metal salts thereof may be used as long as they are anionic. If it is nonionic, poly (meth) acrylamide etc. are mentioned.
  • a homopolymer composed of a cationic monomer such as dimethylaminoethyl (meth) acrylate or a quaternary ammonium salt thereof, dimethylaminopropyl (meth) acrylamide or a quaternary ammonium salt thereof, or a copolymer with these cationic monomers.
  • a cationic monomer such as dimethylaminoethyl (meth) acrylate or a quaternary ammonium salt thereof, dimethylaminopropyl (meth) acrylamide or a quaternary ammonium salt thereof, or a copolymer with these cationic monomers.
  • examples thereof include a copolymer with a polymerizable nonionic monomer.
  • These organic polymer flocculants may be used alone or in combination of two or more.
  • the amount of the organic polymer flocculant added is appropriately determined according to the type of organic polymer flocculant and the properties of the raw water, but is usually about 0.5 to 5 mg / L.
  • sludge is settled and separated by the ascending flow path 24 in the second biological treatment tank 2, but the sludge mixed water in the second biological treatment tank 2 is taken out as shown in FIG. Introduced into the separation tank 3 and separated into solid and liquid, separated into treated water and settled sludge, a part of the settled sludge (tank sludge) is returned to the second biological treatment tank 2 and the remainder as extra sludge You may make it take out. Sludge mixed water is introduced into the lower part of the solid-liquid separation tank 3 and is raised at LV 1 to 20 m / h for solid-liquid separation. The supernatant water is taken out from the upper part of the tank 3. The settled sludge is taken out from the bottom of the tank 3. In FIG. 4, neither the partition plate 23 nor the trough is provided in the outflow part of the second biological treatment tank 2.
  • the biological treatment tank may be provided in three or more stages by providing a third biological treatment tank after the first biological treatment tank 1 and the second biological treatment tank 2.
  • each tank may be provided independently, or each tank may be formed by partitioning one tank with a partition plate.
  • the final stage biological treatment tank is provided with the rocking bed carrier 22, and the final stage biological treatment water is supplied to LV1 to 20 m / h in or outside the final stage biological treatment tank.
  • Example 1 (flow: FIG. 1)]
  • COD Cr 1250 mg / L organic wastewater (food manufacturing wastewater) using a first biological treatment tank 1 (no sludge return) having a capacity of 88 L and a second biological treatment tank 2 having a capacity of 150 L )
  • the second biological treatment tank 2 is provided with an ascending flow path 24 partitioned by a partition plate 23.
  • the liquid in the tank was circulated through the ascending flow path 24 at an LV of 5 m / h, and the sludge was settled and separated.
  • the settled sludge returns to the second biological treatment tank 2 and the supernatant water flows out of the second biological treatment tank 2.
  • Excess sludge in the second biological treatment tank 2 was taken out from the take-out pipe 25.
  • the DO in the first biological treatment tank 1 was 0.5 mg / L, and the second biological treatment tank 2 was operated so that the DO was 2 to 3 mg / L.
  • a fluidized bed carrier 12 having a filling rate of 5% and 5 mm square is added to the first biological treatment tank 1, and a plate-like polyurethane foam (length 100 cm, width 30 cm, thickness 1 cm) is added to the second biological treatment tank 2.
  • One swing bed carrier 22 was installed.
  • the COD Cr volumetric load for the first biological treatment tank is 8.6 kg-COD Cr / m 3 / d, HRT 3.5 h, the total COD Cr volumetric load 2 kg-COD Cr / m 3 / d, HRT 9.5 h Drove.
  • Example 2 (flow: FIG. 3)
  • 50 mg / L of PAC as an aggregating agent and 1 mg / L of an anionic polymer aggregating agent (Cliff Rock PA331 manufactured by Kurita Kogyo Co., Ltd.) are added to the second biologically treated water from the second biological treatment tank 2.
  • the coagulation tank 4 and the precipitation tank 5 were subjected to coagulation sedimentation treatment.
  • the second biological treatment tank 2 is not provided with the partition plate 23 and the ascending flow path 24. Otherwise, the operation was performed under the same conditions as in Example 1.
  • Example 3 (flow: FIG. 1)
  • the process is performed under the same conditions as in Example 1 except that the position of the partition plate 23 is adjusted so that the LV of the ascending channel 24 becomes 1 m / h and the horizontal sectional area of the ascending channel 24 is increased five times. went.
  • Example 4 (flow: FIG. 1)] The process is performed under the same conditions as in Example 1 except that the position of the partition plate 23 is adjusted so that the LV of the ascending channel 24 becomes 15 m / h and the horizontal sectional area of the ascending channel 24 is reduced to 1/3. Went.
  • Example 5 (flow: FIG. 1)] The process is performed under the same conditions as in Example 1 except that the position of the partition plate 23 is adjusted so that the LV of the ascending channel 24 is 20 m / h and the horizontal sectional area of the ascending channel 24 is reduced to 1 ⁇ 4. Went.
  • Example 6 (flow: FIG. 4)
  • the second biological treatment tank 2 is not provided with the partition plate 23 and the ascending flow path 24. Instead, a part of the settled sludge in the solid-liquid separation tank 3 was returned to the second biological treatment tank 2. The sedimentation sludge was not returned to the first biological treatment tank 1.
  • the other processes were performed under the same conditions as in Example 1.
  • Example 1 (flow: FIG. 1)] The process is performed under the same conditions as in Example 1 except that the position of the partition plate 23 is adjusted so that the LV of the ascending channel 24 becomes 0.5 m / h and the horizontal sectional area of the ascending channel 24 is increased 10 times. Went.
  • the horizontal cross-sectional area of the ascending flow path 24 surrounded by the partition plate 23 occupies about 40% of the entire horizontal cross-sectional area of the second biological treatment tank 2.
  • the biological treatment did not proceed sufficiently.
  • SS in the treated water is 90 mg / L
  • Example 2 (flow: FIG. 1)] The processing is performed under the same conditions as in Example 1 except that the position of the partition plate 23 is adjusted so that the LV of the ascending channel 24 is 25 m / h and the horizontal sectional area of the ascending channel 24 is reduced to 1/5. Went.
  • the SS of the treated water was 300 mg / L
  • the sludge was not extracted from the tank
  • the sludge conversion rate was 0.24 kg-SS / kg-COD Cr .

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  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biological Treatment Of Waste Water (AREA)
  • Activated Sludge Processes (AREA)
  • Physical Water Treatments (AREA)

Abstract

La présente invention a pour but de réduire significativement le volume de boue généré ainsi que d'augmenter l'efficacité de traitement par fonctionnement en charge élevée et obtenir de l'eau traitée d'une qualité stable. L'invention concerne un procédé et un dispositif de traitement biologique pour des eaux usées organiques. Dans un premier réservoir de traitement biologique (1), une première eau traitée biologiquement est produite, laquelle possède des bactéries dispersées accrues par suite de la décomposition de matière organique par des bactéries dispersées, et dans un second réservoir de traitement biologique (2), une seconde eau traitée biologiquement est produite par traitement de film biologique à l'aide d'un lit à balancement (22). La seconde eau traitée biologiquement est amenée à passer à travers le trajet d'écoulement ascendant (24) à l'intérieur du second réservoir de traitement biologique (2) à une vitesse linéaire LV de 1 à 20 m/h, et la boue est par là précipitée et séparée et la boue précipitée est renvoyée à la chambre de traitement biologique à l'intérieur du second réservoir de traitement biologique (2).
PCT/JP2012/083883 2012-01-06 2012-12-27 Procédé et dispositif de traitement biologique pour eaux usées organiques WO2013103124A1 (fr)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015151571A1 (fr) * 2014-03-31 2015-10-08 栗田工業株式会社 Procédé et appareil pour le traitement biologique d'eaux usées organiques
CN106061906A (zh) * 2014-07-01 2016-10-26 栗田工业株式会社 有机性排水的生物处理方法和生物处理装置
JP2019048254A (ja) * 2017-09-08 2019-03-28 オルガノ株式会社 有機性排水の処理方法及び処理装置

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106795021B (zh) * 2014-10-10 2022-03-15 奥加诺株式会社 废水处理方法及废水处理装置
JP2022122572A (ja) * 2021-02-10 2022-08-23 オルガノ株式会社 水処理方法及び水処理装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006057249A1 (fr) * 2004-11-24 2006-06-01 Hitachi Zosen Corporation Appareil de dessalement de l’eau de mer utilisant un procede d’osmose inverse a membrane
JP2008238026A (ja) * 2007-03-27 2008-10-09 Matsushita Electric Ind Co Ltd 排水処理装置
JP2011224544A (ja) * 2010-03-31 2011-11-10 Kurita Water Ind Ltd 有機性排水の生物処理方法および装置

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4474930B2 (ja) * 2004-02-02 2010-06-09 栗田工業株式会社 有機性排水の生物処理方法
CN101175700B (zh) * 2005-04-12 2011-04-27 栗田工业株式会社 有机废水的生物处理方法和生物处理装置
CN101279809B (zh) * 2008-05-30 2011-01-19 北京碧水源科技股份有限公司 生物填料摇动床
CN102209689A (zh) * 2008-11-11 2011-10-05 株式会社神钢环境舒立净 水处理装置及水处理方法
JP2011092811A (ja) * 2009-10-27 2011-05-12 Asahi Kasei Engineering Kk 排水処理装置及び排水処理方法
WO2011122217A1 (fr) * 2010-03-31 2011-10-06 栗田工業株式会社 Procédé et dispositif de traitement biologique de l'eau polluée par des produits organiques

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006057249A1 (fr) * 2004-11-24 2006-06-01 Hitachi Zosen Corporation Appareil de dessalement de l’eau de mer utilisant un procede d’osmose inverse a membrane
JP2008238026A (ja) * 2007-03-27 2008-10-09 Matsushita Electric Ind Co Ltd 排水処理装置
JP2011224544A (ja) * 2010-03-31 2011-11-10 Kurita Water Ind Ltd 有機性排水の生物処理方法および装置

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015151571A1 (fr) * 2014-03-31 2015-10-08 栗田工業株式会社 Procédé et appareil pour le traitement biologique d'eaux usées organiques
CN106132881A (zh) * 2014-03-31 2016-11-16 栗田工业株式会社 有机性排水的生物处理方法和装置
CN106132881B (zh) * 2014-03-31 2018-04-17 栗田工业株式会社 有机性排水的生物处理方法和装置
CN106061906A (zh) * 2014-07-01 2016-10-26 栗田工业株式会社 有机性排水的生物处理方法和生物处理装置
JP2019048254A (ja) * 2017-09-08 2019-03-28 オルガノ株式会社 有機性排水の処理方法及び処理装置

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CN104039715A (zh) 2014-09-10
MY167611A (en) 2018-09-20

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