WO2012017834A1 - 嫌気性消化方法 - Google Patents
嫌気性消化方法 Download PDFInfo
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- WO2012017834A1 WO2012017834A1 PCT/JP2011/066611 JP2011066611W WO2012017834A1 WO 2012017834 A1 WO2012017834 A1 WO 2012017834A1 JP 2011066611 W JP2011066611 W JP 2011066611W WO 2012017834 A1 WO2012017834 A1 WO 2012017834A1
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- sludge
- fixed bed
- carrier
- anaerobic digestion
- digestion method
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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
- C02F3/28—Anaerobic digestion processes
- C02F3/2806—Anaerobic processes using solid supports for microorganisms
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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
- C02F3/10—Packings; Fillings; Grids
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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
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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
- C02F3/28—Anaerobic digestion 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
- C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
- C02F2209/105—Particle number, particle size or particle characterisation
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- 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 contains sewage sludge, sludge generated from industrial waste treatment facilities, sludge containing organic matter of livestock waste such as chicken manure, and a large amount (5000 mg / L or more) of suspended solids (SS).
- the present invention relates to an anaerobic digestion method in which organic wastewater is anaerobically digested by a fixed bed.
- anaerobic digestion method a method of reducing the volume by anaerobic digestion by introducing sewage sludge into a digestion tank is known. This method is provided with gas stirring or mechanical stirring means inside the digestion tank, and is put into the sewage sludge or the like without any special pretreatment, and is subjected to anaerobic digestion by thoroughly mixing with the stirring means. It is.
- sludge is conditioned to at least fluid high-concentration slurry containing organic matter-containing solids, and the conditioned sludge is used as a fluid medium, with a true specific gravity of 2.0 or more and
- a method of digesting in an anaerobic digester having a fluidized bed formed by flowing a carrier having an average particle size of 2.0 to 5.0 mm ⁇ is disclosed (for example, see Patent Document 1). This method prevents clogging in the digestion tank and outflow of the carrier to the outside of the tank, improves the contact efficiency between the methane bacteria fixed on the carrier and sludge, and enhances the sludge digestion reaction. It is an object.
- anaerobic digestion method in addition to the method disclosed in Patent Document 1, a method is disclosed in which the ratio of the flow stop time to the flow time is set to 30 or less, and the fluidized bed is operated intermittently. (For example, refer to Patent Document 2).
- This method aims to reduce the energy required for flow while maintaining the significant shortening of the digestion days, which is an advantage of the fluidized bed method.
- anaerobic digestion method in an anaerobic fluidized bed bioreactor using a bioadhesive carrier, by performing primary treatment within 10 days of digestion, the methane bacteria group is added to the suspended sludge in the anaerobic fluidized bed.
- a method is disclosed in which a secondary treatment is carried out using a floating sludge-type anaerobic bioreactor using this methanogen group (see, for example, Patent Document 3). The purpose of this method is to provide a low-cost process that can reduce the number of days of digestion, obtain high reaction efficiency.
- the carrier is flowed in order to improve the contact efficiency between the supplied sludge and the bioadhesive carrier, the necessary pump capacity is increased and the processing cost is increased. Further, when the carrier flows, the carriers come into contact with each other, and the methane bacteria grown on the surface of the carrier are peeled off, the concentration of the retained methane bacteria is lowered, and the digestion reaction is hindered. Furthermore, since the carriers are in contact with each other, the carriers themselves are worn. In order to reduce the wear of the carrier due to flow, the carrier is required to have strength, so that the carrier that can be used is limited, and a carrier having a large porosity cannot be used. As a result, processing efficiency decreases.
- the present invention has been made in view of the above circumstances, and sludge and biofouling can be achieved by uniformly dispersing sludge without clogging the fixed layer composed of the biofouling carrier constituting the lower layer of the fixed bed. It is an object of the present invention to provide an anaerobic digestion method that improves the contact efficiency with methane bacteria held on a carrier, improves the sludge digestion reaction rate, and prevents wear of the bioadhesive carrier.
- the anaerobic digestion method treats sediment sludge obtained by precipitating sewage or waste liquid, sludge composed of livestock waste sludge, or organic waste water containing 5000 mg / L or more of suspended solids.
- the target is a method of biological treatment using a fixed bed using a bioadhesive carrier made of a spherical porous body.
- a part of the processing target supplied to the fixed bed is extracted from the upper layer of the fixed bed, and the extracted processing target is supplied to the fixed layer made of a bioadhesive carrier that constitutes the lower layer of the fixed bed,
- a bioadhesive carrier composed of a spherical porous body having an average particle size of 4.0 mm or more
- the treatment target is uniformly dispersed without causing the bioadhesive carrier to flow or clogging the fixed layer.
- the object to be treated is circulated in the fixed bed.
- the filling rate of the bioadhesive carrier with respect to the total volume of the fixed bed is preferably 30 to 70%.
- the biological adhesion carrier preferably has a true specific gravity of 1.5 to 4.0 g / cm 3 .
- the bioadhesive carrier preferably has an average particle size of 4.0 mm to 15.0 mm.
- the bioadhesive carrier preferably has a porosity of 40 to 70%.
- the speed at which the treatment target is circulated in the fixed bed is preferably 0.1 m / hr to 10 m / hr.
- the treatment target is biologically treated.
- the digestion gas or nitrogen gas generated in the fixed bed is supplied to the treatment target supply pipe of the fixed bed or the lower part of the fixed bed, and the bioadhesive carrier is stirred by the digestion gas or the nitrogen gas. Good.
- the supply speed of the digestion gas or the nitrogen gas supplied to the processing target supply pipe or the lower part of the fixed layer is 5 to 40 m / hr.
- a part of the processing target is extracted from the upper layer of the fixed bed, and the extracted processing target is supplied to the fixed layer composed of the bioadhesive carrier that constitutes the lower layer of the fixed bed. Circulate the subject.
- the treatment target can be made uniform without causing the bioadhesive carrier to flow and without blocking the fixed layer. Can be dispersed. As a result, the contact efficiency between the treatment target and the methane bacteria held on the bioadhesive carrier is improved, and the solid matter contained in the treatment target is further refined when passing through the fixed layer.
- Digestion reaction rate is improved.
- the bioadhesive carrier does not flow, the growth of methane bacteria on the bioadhesive carrier is promoted, and the bioadhesive carrier constituting the fixed layer is retained at a high concentration. Therefore, methane bacteria are held at a high concentration in the fixed bed in the fixed bed, the digestion reaction rate in the fixed bed is increased, and the operation can be highly efficient.
- part of the methane bacteria grown on the bioadhesive carrier and held at a high concentration is peeled off and supplied to the object to be treated. Therefore, if a complete mixing tank is provided after the fixed bed, complete mixing Methane fermentation is maintained in the tank, and biological treatment proceeds.
- the bioadhesive carrier does not flow due to the flow to be treated, it is possible to prevent the bioadhesive carriers from rubbing against each other and wearing out.
- FIG. 1 is a schematic configuration diagram of an anaerobic digester used in an anaerobic digestion method according to an embodiment of the present invention.
- the anaerobic digester 10 of the present embodiment is generally configured from a fixed bed 20 and a complete mixing tank 30 connected thereto.
- the fixed bed 20 accommodates sludge (treatment target) and performs a digestion treatment, a biological adhesion carrier 22, a sludge supply pipe 23 (treatment target supply pipe), a sludge outflow pipe 24, and a sludge circulation pipe. 25, a circulation pump 26, a stirrer 27, and a gas supply pipe 29.
- the complete mixing tank 30 is generally composed of a processing tank 31 that stores sludge discharged from the fixed bed 20 and performs a digestion process, a sludge discharge pipe 32, and a stirrer 33.
- a large number of spherical biofouling carriers 22 are filled in the lower part of the treatment tank 21.
- the fixed layer 28 made of the bioadhesive carrier 22 constitutes the lower layer of the fixed bed 20.
- the bioadhesive carrier 22 holds methane bacteria that produce methane from organic substances under anaerobic conditions.
- the sludge supply pipe 23 supplies (introduces) sludge to the inside from the outside of the treatment tank 21.
- a nozzle 23 a provided at the tip of the sludge supply pipe 23 is disposed in the fixed layer 28.
- the sludge outflow pipe 24 causes sludge to flow out from the upper layer of the fixed bed 20 to the outside (specifically, the complete mixing tank 30).
- the sludge outflow pipe 24 is provided from the upper part of the treatment tank 21 to the treatment tank 31 of the complete mixing tank 30.
- the sludge circulation pipe 25 is provided for extracting a part of the sludge from the upper layer of the fixed bed 20 and supplying the extracted sludge to the fixed layer 28 uniformly.
- the sludge circulation pipe 25 is provided from the upper part of the processing tank 21 to the sludge supply pipe 23 as a base end, and is connected to the sludge supply pipe 23 outside the processing tank 21.
- tube 25 of the processing tank 21 is located in the perpendicular direction lower side rather than the connection location with the sludge outflow pipe
- the sludge circulation pipe 25 is connected to the sludge supply pipe 23, but the tip of the sludge circulation pipe 25 may be directly disposed in the fixed layer 28.
- a circulation pump 26 is provided for extracting a part of the sludge from the upper layer of the fixed bed 20 and supplying the extracted sludge to the fixed layer 28.
- the stirrer 27 stirs the sludge in the upper layer of the fixed bed 20.
- the stirrer 27 is provided in the upper part of the processing tank 21.
- the stirring blade 27 a of the stirrer 27 is disposed in the upper part (upper layer of the fixed bed 20) in the processing tank 21.
- the gas supply pipe 29 is branched into two on the way.
- One of the two branched gas supply pipes 29 is connected to the sludge supply pipe 23.
- a nozzle 29a is provided at the other end of the gas supply pipe 29 branched into two.
- the nozzle 29 a is disposed in the lower part in the fixed layer 28.
- the gas supply pipe 29 is separated from the digested gas generated in the fixed bed 20 or the fixed bed 20 below the sludge supply pipe 23 (specifically, the nozzle 23 a) or the fixed bed 28 constituting the lower layer of the fixed bed 20. Supply nitrogen gas from the body gas supply.
- the sludge discharge pipe 32 discharges the digested sludge from the upper layer of the complete mixing tank 30 to the outside.
- the sludge discharge pipe 32 is provided in the upper part of the processing tank 31.
- the stirrer 33 stirs the sludge in the treatment tank 31 uniformly.
- the stirrer 33 is provided in the upper part of the processing tank 31.
- the stirring blade 33 a of the stirrer 33 is disposed in the central portion in the processing tank 31.
- the sludge 41 to be treated is supplied from the outside of the fixed bed 20 into the treatment tank 21 through the sludge supply pipe 23.
- the sludge 41 consists of sedimentation sludge obtained by precipitating sewage or waste liquid, or livestock waste sludge.
- the sludge 41 supplied into the treatment tank 21 via the sludge supply pipe 23 is uniformly supplied to the fixed layer 28 from the nozzle 23 a provided at the tip of the sludge supply pipe 23.
- the sludge 41 is discharged from the nozzles 23a so as to be in direct contact with the large number of biofouling carriers 22 constituting the fixed layer 28.
- the temperature of the sludge 41 in the treatment tank 21 is preferably adjusted to 30 to 38 ° C.
- the temperature of the sludge 41 may be 50 to 55 ° C.
- the supply of the sludge 41 from the outside of the fixed bed 20 is stopped.
- a part of the sludge 41 supplied to the fixed bed 20 is extracted from the upper layer of the fixed bed 20 through the sludge circulation pipe 25, and the extracted sludge 41 is fixed through the sludge circulation pipe 25 and the sludge supply pipe 23.
- the sludge 41 is circulated in the fixed bed 20. That is, the sludge 41 in the treatment tank 21 is circulated in the order of the fixed layer 28, the upper layer of the fixed floor 20, the sludge circulation pipe 25, the sludge supply pipe 23, and the fixed layer 28.
- the sludge 41 passes through the fixed layer 28. More specifically, the sludge 41 passes between a large number of biofouling carriers 22 constituting the fixed layer 28. As the sludge 41 passes between the large number of biological adhesion carriers 22, the solid matter contained in the sludge 41 is refined.
- the circulation of the sludge 41 in the fixed bed 20 is performed very slowly so that the biofouling carrier 22 does not flow due to the flow of the sludge 41. That is, the speed (superficial speed) for circulating the sludge 41 from the upper layer of the fixed bed 20 to the fixed bed 28 is preferably 0.1 m / hr to 10 m / hr, more preferably 0.12 m / hr to 3 m. / Hr. If the speed at which the sludge 41 is circulated is within this range, the sludge 41 does not normally block the fixed layer 28 in the bioadhesive carrier 22 having a particle size (details will be described later) used in the present invention.
- the sludge 41 is almost uniformly dispersed in the fixed layer 28 and hardly causes a drift (channeling). Therefore, the contact efficiency between the sludge 41 and the methane bacteria held by the bioadhesive carrier 22 is improved, and the digestion efficiency of the sludge 41 is improved. In addition, since the bioadhesive carrier 22 does not flow, peeling of the methane bacterium from the bioadhesive carrier 22 due to the contact between the many bioadhesive carriers 22 is prevented. Therefore, the growth of methane bacteria on the bioadhesion carrier 22 is promoted, and the methane bacteria are held at a high concentration on the bioadhesion carrier 22.
- the digestion efficiency of the sludge 41 in the fixed bed 28 in which methane bacteria are held at a high concentration is improved. Furthermore, since the biofouling carrier 22 does not flow due to the flow of the sludge 41, the biofouling carriers 22 are not rubbed with each other and the biofouling carrier 22 is not worn. Since the bioadhesive carriers 22 do not come into contact with each other, the strength condition required for the carriers can be relaxed, and a carrier having a large porosity can be used. Therefore, it becomes possible to hold many methane bacteria by the carrier.
- rate which circulates the sludge 41 is less than 0.1 m / hr, the flow rate of the sludge 41 which passes the inside of the fixed bed 28 will become very slow. Therefore, the sludge 41 does not pass through the entire fixed layer 28, causing drift (channeling), which may reduce digestion efficiency.
- the speed at which the sludge 41 is circulated exceeds 10 m / hr, the amount of methane bacteria peeled off from the bioadhesive carrier 22 increases, making it difficult for the methane bacteria to be maintained at a high concentration and reducing the digestion efficiency of the sludge 41. There is sex.
- the bioadhesive carrier 22 flows due to the flow of the sludge 41, the bioadhesive carriers 22 may rub against each other and the bioadhesive carrier 22 may be worn. Furthermore, the energy consumption of the circulation pump 26 increases.
- the filling rate of the bioadhesive carrier 22 with respect to the total volume of the fixed bed 20, that is, the total volume of the treatment tank 21, is preferably 30 to 70%, and more preferably 40 to 60%. If the filling rate of the biofouling carrier 22 is within this range, the sludge 41 and the biofouling carrier 22 in the treatment tank 21 are completely separated at the upper part of the treatment tank 21, and the biofouling carrier 22 is placed in the sludge circulation pipe 25. Inflow is prevented. Further, the contact efficiency between the sludge 41 and the methane bacteria held on the bioadhesive carrier 22 is improved, and the digestion efficiency of the sludge 41 is improved.
- the filling rate of the biofouling carrier 22 is less than 30%, the contact efficiency between the sludge 41 in the treatment tank 21 and the methane bacteria held in the biofouling carrier 22 may be reduced, and the digestion efficiency of the sludge 41 may be reduced. There is.
- the filling rate of the biofouling carrier 22 exceeds 70%, the sludge 41 and the biofouling carrier 22 are not completely separated at the upper part of the treatment tank 21, and the biofouling carrier 22 flows into the sludge circulation pipe 25, and the circulation pump. There is a possibility that the biofouling carrier 22 is damaged at 26.
- a spherical porous body formed by sintering a clay-based material is used as the bioadhesive carrier 22.
- clay-based materials include kaolin, bentonite, and barley stone.
- the bioadhesive carrier 22 preferably has a true specific gravity of 1.5 to 4.0 g / cm 3 , more preferably 1.6 to 2.7 g / cm 3 . If the true specific gravity of the bioadhesion carrier 22 is within this range, the bioadhesion carrier 22 will not flow due to the flow of the sludge 41, and the bioadhesion carriers 22 will rub against each other and wear out. There is no. Moreover, since the porosity of the bioadhesive carrier 22 can be set within a predetermined range, methane bacteria can be held in the bioadhesive carrier 22 at a high concentration.
- the biofouling carrier 22 is completely separated from the sludge 41 in the treatment tank 21 at the upper part of the treatment tank 21, and the biofouling carrier 22 is prevented from flowing into the sludge circulation pipe 25.
- the adhesion carrier 22 is not damaged.
- the sludge 41 and the biofouling carrier 22 are completely separated at the upper part of the treatment tank 21 and the biofouling carrier 22 does not flow out into the complete mixing tank 30, the methane bacteria can be kept at a high concentration in the treatment tank 21. .
- the biofouling carrier 22 may flow due to the flow of the sludge 41, and the biofouling carriers 22 may rub against each other to wear the biofouling carrier 22. is there. Further, the bioadhesion carrier 22 is not completely separated from the sludge 41 in the treatment tank 21 at the upper part of the treatment tank 21, and the bioadhesion carrier 22 flows into the sludge circulation pipe 25, and the biofouling carrier 22 is supplied by the circulation pump 26. May be damaged. On the other hand, if the true specific gravity of the bioadhesive carrier 22 exceeds 4 g / cm 3 , it cannot be manufactured with a normal clay-based inexpensive material, and is not practical from an economical viewpoint.
- the bioadhesive carrier 22 preferably has an average particle size of 4.0 mm to 15.0 mm, more preferably 5.0 mm to 10.0 mm. If the average particle diameter of the biofouling carrier 22 is within this range, the sludge 41 can be uniformly dispersed in the fixed layer 28 without the sludge 41 blocking the fixed layer 28. Therefore, the contact efficiency between the sludge 41 in the treatment tank 21 and the methane bacteria retained on the biological adhesion carrier 22 is improved, and the digestion efficiency of the sludge 41 is improved.
- the biofouling carrier 22 is completely separated from the sludge 41 in the treatment tank 21 at the upper part of the treatment tank 21, and the biofouling carrier 22 is prevented from flowing into the sludge circulation pipe 25. Thus, the biofouling carrier 22 is not damaged.
- the sludge 41 may block the fixed layer 28 and bridging may occur, or the sludge 41 may cause a drift (channeling) in the fixed layer 28. .
- the bioadhesion carrier 22 is not completely separated from the sludge 41 in the treatment tank 21 at the upper part of the treatment tank 21, and the bioadhesion carrier 22 wraps around the sludge circulation pipe 25, and the biofouling carrier 22 is circulated by the circulation pump 26. May be damaged.
- the surface area of the bioadhesive carrier 22 becomes small, and the sludge 41 in the treatment tank 21 contacts the methane bacteria held in the bioadhesive carrier 22. Efficiency may fall and the digestion efficiency of the sludge 41 may fall. Moreover, even if the solid matter contained in the sludge 41 passes between the biofouling carriers 22, the interval between the biofouling carriers 22 is too large, and thus the solid matter may not be refined.
- the bioadhesive carrier 22 preferably has a porosity of 30 to 70%, more preferably 40 to 60%. If the porosity of the bioadhesive carrier 22 is within this range, the bioadhesive carrier 22 retains methane bacteria at a high concentration, and the digestion efficiency of the sludge 41 is improved. If the porosity of the bioadhesive carrier 22 is less than 30%, it is difficult for the bioadhesive carrier 22 to hold methane bacteria at a high concentration, and the digestion efficiency of the sludge 41 may be reduced. On the other hand, if the porosity of the bioadhesive carrier 22 exceeds 70%, the strength of the bioadhesive carrier 22 is reduced, and the bioadhesive carrier 22 may be worn or damaged over time. .
- the sludge 41 is normally circulated continuously at all times. However, preferably, when the supply of sludge from the outside into the treatment tank 21 is short, the circulation of the sludge 41 is stopped. The reason is that when the sludge 41 is circulated in the treatment tank 21, the sludge 41 in the treatment tank 21 is very well mixed and is almost completely mixed. In this case, when the sludge is newly supplied into the treatment tank 21, the amount that can be accommodated in the treatment tank 21 is constant. Therefore, a sludge amount equal to the supplied sludge amount flows out of the treatment tank 21 and is completely mixed. It is supplied to the tank 30.
- the sludge 41 in the upper layer of the fixed bed 20 is stirred intermittently by the stirrer 27 during the sludge digestion process.
- sponge cake-like sludge called scum formed in the upper layer of the fixed floor 20 can be destroyed, and gas generated by digestion of the sludge 41 can be easily removed.
- the frequency of stirring the sludge 41 with the stirrer 27 is preferably every 5 minutes to 1 hour. Further, the stirring time per one time is preferably 1 minute to 5 minutes. Further, when the circulation of the sludge 41 is stopped during the supply of sludge from the outside to the treatment tank 21, the stirring by the stirrer 27 may be stopped in order to maintain the pushing flow of the treatment tank 21. preferable.
- the sludge 41 circulation in the fixed bed 20 that is, the digestion of the sludge 41 has progressed
- the sludge 41 flows out from the fixed bed 20 and the sludge 41 is introduced into the treatment tank 31 of the complete mixing tank 30.
- the sludge 42 in the treatment tank 31 is uniformly stirred and mixed by the stirrer 33 so that the sludge is partially separated from the methane bacteria held at a high concentration in the fixed layer 28 in the treatment tank 21. 42 is biologically processed.
- the temperature of the sludge 42 in the treatment tank 31 is preferably adjusted to 30 to 38 ° C. However, the temperature of the sludge 42 may be 50 to 55 ° C. In the treatment tank 31, the sludge 42 is constantly stirred uniformly.
- a part of the sludge 41 is extracted from the upper layer of the fixed bed 20, and the extracted sludge 41 is composed of the bioadhesive carrier 22 constituting the lower layer of the fixed bed 20.
- the sludge 41 is circulated in the fixed bed 20. For this reason, the contact efficiency between the sludge 41 and the methane bacteria held at a high concentration in the bioadhesive carrier 22 is improved, and the solid matter contained in the sludge 41 is further refined when passing through the fixed layer 28.
- the digestion reaction speed of the sludge 41 is improved.
- the sludge 41 can be uniformly dispersed in the fixed layer 28 without blocking the fixed layer 28. . Therefore, a high concentration of methane bacteria can be retained on the bioadhesive carrier 22, the concentration of methane bacteria that is the rate-limiting factor for methane fermentation is increased, the digestion efficiency of the sludge 41 is improved, and the digestion reaction of the sludge 41 is eventually achieved. Increases speed. Therefore, the digestion time can be shortened to 1 to 2 days in the present embodiment, whereas the digestion of sludge conventionally takes 4 to 30 days. Thereby, the installation cost of a digester can be reduced significantly.
- the capacity of the circulation pump 26 can be reduced to 1/50 to 1/100 of the conventional one. Therefore, the initial cost and running cost of the circulation pump can be significantly reduced. Further, since the sludge 41 is circulated very slowly and the bioadhesive carrier 22 does not flow due to the flow of the sludge 41, it is possible to prevent the bioadhesive carriers 22 from rubbing against each other and wearing out the bioadhesive carrier 22. .
- digestion can be performed more efficiently by treating the sludge 41 treated in the fixed bed 20 in the complete mixing tank 30.
- the sludge which consists of sedimentation sludge obtained by carrying out precipitation operation of sewage or a waste liquid, or livestock waste sludge was used as a process target, it is not limited to these.
- Organic sludge containing 5000 mg / L or more of other sludge or suspended solids (SS) may be treated using the anaerobic digestion method of the present embodiment.
- Example 1 Sludge was digested using the same device as the digester 10 shown in FIG.
- a tank having a capacity of 2L (liter) was used as the processing tank 21 of the fixed bed 20.
- a spherical porous ceramic ball having a true specific gravity of 1.7 g / cm 3 , a particle size of about 10 mm, and a porosity of about 50% is sintered.
- the filling rate of the bioadhesive carrier 22 with respect to the total volume of the treatment tank 21 was set to about 50%.
- sludge 1L of sludge with a sludge concentration (TS) of 18,500mg / L and an organic substance content (VTS) of 74% is mixed with sludge (mixed sludge) of primary sludge and surplus sludge from a sewage treatment plant. (Liter) was supplied. Moreover, the temperature of the sludge 41 in the treatment tank 21 is adjusted to 35 ° C., a part of the sludge 41 is extracted from the upper layer of the fixed bed 20, and the extracted sludge 41 is supplied to the fixed layer 28. Digestion of sludge 41 was performed. Moreover, the speed
- the amount of gas per 1 L (liter) of input sludge generated during the digestion reaction of sludge 41 was measured by a wet gas meter manufactured by Shinagawa Co., and the sludge concentration (TS) of sludge 41 and the digestibility of sludge 41 were calculated. .
- Table 1 The results are shown in Table 1.
- Table 2 the average particle diameter of the solid substance contained in the sludge 41 after the process in the fixed bed 20 was measured with the wet laser diffraction scattering type particle size distribution measuring method. The results are shown in Table 2.
- the sludge 41 that has been processed in the fixed bed 20 is introduced into the treatment tank 31 of the complete mixing tank 30, the temperature of the sludge 42 in the treatment tank 31 is adjusted to 35 ° C., and the sludge 42 is removed by the stirrer 33. Uniform stirring and mixing were performed for 2 days, and the sludge 42 was digested.
- a tank having a capacity of 2L (liter) was used as the processing tank 31 of the complete mixing tank 30 a tank having a capacity of 2L (liter) was used.
- Example 1 The same sludge treated in Example 1 is supplied into the treatment tank of the complete mixing tank, the temperature of the sludge in the treatment tank is adjusted to 35 ° C., and the sludge is uniformly stirred and mixed by a stirrer. For 10 days to digest the sludge.
- a tank having a capacity of 2 L (liter) was used as the treatment tank of the complete mixing tank.
- the amount of gas per 1 liter (liter) of input sludge generated during the sludge digestion reaction was measured, and the sludge concentration (TS) and sludge digestibility were calculated.
- Table 1 Moreover, it carried out similarly to Example 1, and measured the average particle diameter of the solid substance contained in the sludge after a process. The results are shown in Table 2.
- Example 1 From the results of Table 1, the treatment time of the fixed bed 20 of Example 1 is 1/5 of the treatment time of the complete mixing type of Comparative Example 1, but the treatment of Example 1 is the same as that of Comparative Example 1. It was confirmed that the same amount of gas was generated as in the treatment, and the digestibility equivalent to that in the treatment of Comparative Example 1 was achieved. Moreover, in Example 1, by providing the complete mixing tank 30 in the subsequent stage of the fixed bed 20, the final gas generation amount becomes 3.8 L / L, which is significantly improved from 2.5 L / L in Comparative Example 1. Confirmed to do.
- Example 1 From the results shown in Table 2, it was confirmed that in Example 1, the sludge passed through the fixed layer 28 and the solids contained in the sludge were being refined. Therefore, in Example 1, it is guessed that the digestive decomposition of the sludge 41 is accelerated
- Example 2 In the treatment tank 21, sludge having a sludge concentration (TS) of 22,500 mg / L and an organic substance content (VTS) of 77% is mixed with 2 liters of sludge in a mixed sludge (mixed sludge) of primary sludge and surplus sludge from a sewage treatment plant. (Liter) was supplied. Further, a part of the sludge 41 was extracted from the upper layer of the fixed bed 20, and the extracted sludge 41 was supplied to the fixed layer 28, and the sludge 41 was digested in the same manner as in Example 1 in one day of digestion. .
- TS sludge concentration
- VTS organic substance content
- Example 2 The same sludge as that treated in Example 2 is supplied into the treatment tank of the complete mixing tank, the temperature of the sludge in the treatment tank is adjusted to 35 ° C., and the sludge is uniformly stirred and mixed by a stirrer. For 10 days to digest the sludge. In the same manner as in Example 1, the amount of gas per 1 L (liter) of input sludge generated during the sludge digestion reaction was measured. The results are shown in Table 3.
- an anaerobic digestion method that improves the digestion reaction rate of sludge and organic wastewater and prevents wear of the bioadhesive carrier.
Abstract
Description
本願は、2010年8月6日に日本に出願された特願2010-177780号に基づき優先権を主張し、その内容をここに援用する。
また、担体が流動することによって、担体同士が接触し、担体の表面で生育したメタン菌が剥離してしまい、保持されるメタン菌の濃度が低下し、消化反応が妨げられる。
さらに、担体同士が接触するため、担体自体が摩耗する。流動による担体の摩耗を低減するためには、担体に強度が求められるので、使用可能な担体が限定されてしまい、空隙率の大きな担体を用いることができない。結果として、処理効率が低下する。
なお、この実施の形態は、発明の趣旨をより良く理解させるために具体的に説明するものであり、特に指定のない限り、本発明を限定するものではない。
本実施形態の嫌気性消化装置10は、固定床20と、これに接続された完全混合槽30とから概略構成されている。
固定床20は、汚泥(処理対象)を収容して消化処理を行う処理槽21と、生物付着担体22と、汚泥供給管23(処理対象供給管)と、汚泥流出管24と、汚泥循環管25と、循環ポンプ26と、攪拌機27と、ガス供給管29とから概略構成されている。
完全混合槽30は、固定床20から流出させた汚泥を収容して消化処理を行う処理槽31と、汚泥排出管32と、攪拌機33とから概略構成されている。
汚泥供給管23は、処理槽21の外部から内部に汚泥を供給(導入)する。汚泥供給管23の先端に設けられたノズル23aは、固定層28内に配置されている。
汚泥流出管24は、固定床20の上層から、その外部(詳細には、完全混合槽30)に汚泥を流出させる。汚泥流出管24は、処理槽21の上部を基端として完全混合槽30の処理槽31まで設けられている。
また、汚泥循環管25の途中には、固定床20の上層から汚泥の一部を抜き取り、その抜き取った汚泥を固定層28に供給するための循環ポンプ26が設けられている。
攪拌機27は、固定床20の上層にある汚泥を攪拌する。攪拌機27は、処理槽21の上部に設けられている。攪拌機27の攪拌羽根27aは、処理槽21内の上部(固定床20の上層)に配置されている。
ガス供給管29は、汚泥供給管23(詳細には、ノズル23a)または固定床20の下層を構成する固定層28の下部に、固定床20で発生した消化ガス、又は固定床20とは別体のガス供給源からの窒素ガスを供給する。これらのガスは、固定層28が汚泥に含まれる固形物などで閉塞し、汚泥循環管25によって循環された汚泥(循環汚泥)が固定層28内に均一に分散せずに偏流(チャンネリング)を起こし、固定床20の処理性能が低下した場合に、ガス供給管29から供給される。これらのガスの供給により、固定層28を構成する生物付着担体22が攪拌される。
攪拌機33は、処理槽31内の汚泥を均一に攪拌する。攪拌機33は、処理槽31の上部に設けられている。攪拌機33の攪拌羽根33aは、処理槽31内の中央部に配置されている。
まず、固定床20の外部から処理対象である汚泥41を、汚泥供給管23を介して、処理槽21内に供給する。汚泥41は、下水もしくは廃液を沈殿操作して得られる沈殿汚泥、又は畜産廃棄物汚泥からなる。
汚泥供給管23を介して処理槽21内に供給される汚泥41は、汚泥供給管23の先端に設けられたノズル23aから、固定層28に均一に供給される。このとき、固定層28を構成する多数の生物付着担体22に直接、接触するように、ノズル23aから汚泥41が吐出される。
すなわち、汚泥41を、固定床20の上層から固定層28へ循環させる速度(空塔速度)は0.1m/hr~10m/hrであることが好ましく、より好ましくは0.12m/hr~3m/hrである。
汚泥41を循環させる速度がこの範囲内であれば、本発明で用いられる粒径(詳細は後述する)の生物付着担体22においては、通常、汚泥41が固定層28を閉塞することがなく、汚泥41がほぼ均一に固定層28内に分散し、ほとんど偏流(チャンネリング)を起こすことがない。そのため、汚泥41と生物付着担体22に保持されたメタン菌との接触効率が向上し、汚泥41の消化効率が向上する。
また、生物付着担体22が流動しないため、多数の生物付着担体22同士が接触することによるメタン菌の生物付着担体22からの剥離が防止される。そのため、生物付着担体22におけるメタン菌の増殖が促進され、生物付着担体22にメタン菌が高濃度に保持される。よって、メタン菌が高濃度に保持された固定層28における汚泥41の消化効率が向上する。
さらに、汚泥41の流れによって生物付着担体22が流動することがないので、生物付着担体22同士が擦れ合って、生物付着担体22が摩耗することがない。生物付着担体22同士が接触しないので、担体に求められる強度の条件を緩和でき、空隙率の大きな担体を用いることができる。よって、担体により多くのメタン菌を保持することが可能となる。
一方、汚泥41を循環させる速度が10m/hrを超えると、生物付着担体22から剥離するメタン菌量が増加し、メタン菌が高濃度に保持され難くなり、汚泥41の消化効率が低下する可能性がある。また、汚泥41の流れによって生物付着担体22が流動すると、生物付着担体22同士が擦れ合って、生物付着担体22が摩耗する可能性がある。さらに、循環ポンプ26の消費エネルギーが増大する。
生物付着担体22の充填率がこの範囲内であれば、処理槽21内の汚泥41と生物付着担体22は、完全に処理槽21上部で分離され、汚泥循環管25内に生物付着担体22が流れ込むことが防止される。また、汚泥41と、生物付着担体22に保持されたメタン菌との接触効率が向上し、汚泥41の消化効率が向上する。
生物付着担体22の充填率が30%未満では、処理槽21内の汚泥41と、生物付着担体22に保持されたメタン菌との接触効率が低下し、汚泥41の消化効率が低下する可能性がある。一方、生物付着担体22の充填率が70%を超えると、汚泥41と生物付着担体22が完全に処理槽21上部で分離されず、汚泥循環管25内に生物付着担体22が流れ込み、循環ポンプ26で生物付着担体22が破損する可能性がある。
生物付着担体22の真比重がこの範囲内であれば、汚泥41の流れによって生物付着担体22が流動することがないので、生物付着担体22同士が擦れ合って、生物付着担体22が摩耗することがない。また、生物付着担体22の空隙率を所定の範囲にすることができるので、メタン菌を生物付着担体22に高濃度に保持させることができる。
生物付着担体22は、処理槽21内の汚泥41と、完全に処理槽21の上部で分離され、汚泥循環管25内に生物付着担体22が流れ込むことが防止されるため、循環ポンプ26で生物付着担体22が破損されない。また、汚泥41と生物付着担体22が完全に処理槽21上部で分離され、完全混合槽30に生物付着担体22が流出しないので、処理槽21内にメタン菌を高濃度に保持させることができる。
生物付着担体22の平均粒径がこの範囲内であれば、汚泥41が固定層28を閉塞させることなく、汚泥41を固定層28に均一に分散させることができる。そのため、処理槽21内の汚泥41と、生物付着担体22に保持されたメタン菌との接触効率が向上し、汚泥41の消化効率が向上する。さらに、生物付着担体22は、処理槽21内の汚泥41と、完全に処理槽21の上部で分離され、汚泥循環管25内に生物付着担体22が流れ込むことが防止されるので、循環ポンプ26で生物付着担体22が破損されない。
一方、生物付着担体22の平均粒径が15.0mmを超えると、生物付着担体22の表面積が小さくなり、処理槽21内の汚泥41と、生物付着担体22に保持されたメタン菌との接触効率が低下し、汚泥41の消化効率が低下する可能性がある。また、汚泥41に含まれる固形物が、生物付着担体22の間を通過しても、生物付着担体22間の間隔が大きすぎるために、その固形物の微細化が進まなくなる可能性がある。
生物付着担体22の空隙率がこの範囲内であれば、生物付着担体22にメタン菌が高濃度に保持され、汚泥41の消化効率が向上する。
生物付着担体22の空隙率が30%未満では、生物付着担体22にメタン菌が高濃度に保持され難くなり、汚泥41の消化効率が低下する可能性がある。一方、生物付着担体22の空隙率が70%を超えると、生物付着担体22の強度が低下し、時間の経過に伴って、生物付着担体22が摩耗したり、破損したりする可能性がある。
その理由は、処理槽21において、汚泥41が循環されている時、処理槽21内の汚泥41は非常に良く混合されており、完全混合状態に近い。この場合、新たに処理槽21内へ汚泥が供給されると、処理槽21の収容可能量は一定であるので、供給された汚泥量と等しい汚泥量が、処理槽21から流出し、完全混合槽30に供給される。この時、処理槽21における汚泥の滞留時間が非常に短いため、ほとんど処理されない汚泥の一部が処理槽21から流出する。これに対して、汚泥41の循環を停止すると、固定層28に供給された汚泥41が、処理槽21の上部へ上昇する速度が遅いため、汚泥41の攪拌が緩やかとなり、処理槽21では押し出し流れ(ピストン流れ)の状態になる。そのため、処理槽21で処理された汚泥のみが処理槽21の上部から流出するので、ほとんど処理されていない汚泥の流出が防止され、処理効率を向上できる。
また、1回当たりの攪拌時間は、1分~5分であることが好ましい。さらに、処理槽21への外部からの汚泥の供給中に、汚泥41の循環が停止されている場合には、処理槽21の押し出し流れを維持するために、攪拌機27による攪拌を停止することが好ましい。
処理槽31内において、汚泥42を常時、均一に攪拌する。
また、汚泥41を非常にゆっくりと循環させ、汚泥41の流動によって生物付着担体22が流動することがないので、生物付着担体22同士が擦れ合って、生物付着担体22が摩耗するのを防止できる。
図1に示した消化装置10と同様の装置を用いて、汚泥の消化を行った。
固定床20の処理槽21としては、容量が2L(リットル)の槽を用いた。
固定床20における生物付着担体22としては、粘土系の材料を焼結し、真比重が1.7g/cm3、粒径が約10mm、空隙率が約50%の球状の多孔性セラミックスボールを用いた。
固定床20において、処理槽21の全容積に対する生物付着担体22の充填率を約50%とした。
処理槽21に、下水処理場の初沈汚泥と余剰汚泥の混合汚泥(混生汚泥)で、汚泥濃度(TS)18,500mg/L、有機物含有量(VTS)74%の汚泥を、1日当たり1L(リットル)供給した。また、処理槽21内の汚泥41の温度を35℃に調節し、固定床20の上層から汚泥41の一部を抜き取り、その抜き取った汚泥41を固定層28に供給し、消化日数2日で、汚泥41の消化を行った。
また、処理槽21内において、汚泥41を循環させる速度を、4L/hrとした。
シナガワ社製の湿式ガスメーターにより、汚泥41の消化反応中に発生した、投入汚泥1L(リットル)当たりのガスの量を測定し、汚泥41の汚泥濃度(TS)、汚泥41の消化率を算出した。結果を表1に示す。
また、湿式のレーザ回折散乱式粒径分布測定法により、固定床20での処理後の汚泥41に含まれる固形物の平均粒径を測定した。結果を表2に示す。
完全混合槽30の処理槽31としては、容量が2L(リットル)の槽を用いた。
シナガワ社製の湿式ガスメーターにより、汚泥42の消化反応中に発生した、投入汚泥1L(リットル)当たりのガスの量を測定し、汚泥42の汚泥濃度(TS)、汚泥42の消化率を算出した。結果を表1に示す。
実施例1で処理したのと同様の汚泥を、完全混合槽の処理槽内に供給し、処理槽内の汚泥の温度を35℃に調節し、攪拌機によって、汚泥を均一に攪拌、混合することを10日間行い、汚泥の消化を行った。
完全混合槽の処理槽としては、容量が2L(リットル)の槽を用いた。
実施例1と同様にして、汚泥の消化反応中に発生した、投入汚泥1L(リットル)当たりのガスの量を測定し、汚泥の汚泥濃度(TS)、汚泥の消化率を算出した。結果を表1に示す。
また、実施例1と同様にして、処理後の汚泥に含まれる固形物の平均粒径を測定した。結果を表2に示す。
また、実施例1では、固定床20の後段に完全混合槽30を設けることにより、最終的なガス発生量が3.8L/Lとなり、比較例1の2.5L/Lよりも大幅に向上することが確認された。
処理槽21に、下水処理場の初沈汚泥と余剰汚泥の混合汚泥(混生汚泥)で、汚泥濃度(TS)22,500mg/L、有機物含有量(VTS)77%の汚泥を、1日当たり2L(リットル)供給した。また、固定床20の上層から汚泥41の一部を抜き取り、その抜き取った汚泥41を固定層28に供給し、消化日数1日で、実施例1と同様にして、汚泥41の消化を行った。
実施例1と同様にして、汚泥の消化反応中に発生した、投入汚泥1L(リットル)当たりのガスの量を測定し、汚泥の汚泥濃度(TS)、汚泥の消化率を算出した。結果を表3に示す。
実施例2で処理したのと同様の汚泥を、完全混合槽の処理槽内に供給し、処理槽内の汚泥の温度を35℃に調節し、攪拌機によって、汚泥を均一に攪拌、混合することを10日間行い、汚泥の消化を行った。
実施例1と同様にして、汚泥の消化反応中に発生した、投入汚泥1L(リットル)当たりのガスの量を測定した。結果を表3に示す。
また、比較例2の方法による限界消化日数(最短の消化日数)は5日程度である。これに対して、実施例2の方法では、反応時間が1日であっても、生物付着担体22に保持されたメタン菌によって、良好なメタン発酵を維持できることが判明した。
20・・・固定床
21・・・処理槽
22・・・生物付着担体
23・・・汚泥供給管
24・・・汚泥流出管
25・・・汚泥循環管
26・・・循環ポンプ
27・・・攪拌機
28・・・固定層
29・・・ガス供給管
30・・・完全混合槽
31・・・処理槽
32・・・汚泥排出管
33・・・攪拌機
41,42・・・汚泥。
Claims (10)
- 下水もしくは廃液を沈殿操作して得られる沈殿汚泥、もしくは畜産廃棄物汚泥からなる汚泥、又は浮遊固形物を5000mg/L以上含んだ有機性排水を処理対象として、球状の多孔質体からなる生物付着担体を用いた固定床により生物学的処理する嫌気性消化方法であって、
前記固定床に供給された処理対象の一部を、前記固定床の上層から抜き取り、その抜き取った処理対象を、前記固定床の下層を構成する生物付着担体からなる固定層へ供給し、平均粒径が4.0mm以上の球状の多孔質体からなる生物付着担体を用いることによって、前記生物付着担体を流動させず、また前記固定層を閉塞させることなく、処理対象を均一に分散させるように、前記固定床において処理対象を循環させる嫌気性消化方法。 - 前記固定床の全容積に対する前記生物付着担体の充填率は30~70%である請求項1に記載の嫌気性消化方法。
- 前記生物付着担体は、真比重が1.5~4.0g/cm3である請求項1または2に記載の嫌気性消化方法。
- 前記生物付着担体は、平均粒径が4.0mm~15.0mmである請求項1~3のいずれか1項に記載の嫌気性消化方法。
- 前記生物付着担体は、空隙率が40~70%である請求項1~4のいずれか1項に記載の嫌気性消化方法。
- 前記固定床において処理対象を循環させる速度は0.1m/hr~10m/hrである請求項1~5のいずれか1項に記載の嫌気性消化方法。
- 前記固定床の上層にある処理対象を間欠的に攪拌する請求項1~6のいずれか1項に記載の嫌気性消化方法。
- 前記固定床から前記生物付着担体と接触した処理対象を流出させて、その処理対象を、後段の完全混合槽に導入し、前記完全混合槽において処理対象を均一に攪拌、混合することにより、処理対象を生物学的処理する請求項1~7のいずれか1項に記載の嫌気性消化方法。
- 前記固定床の処理対象供給管または前記固定層の下部に、前記固定床で発生した消化ガスまたは窒素ガスを供給し、前記消化ガスまたは前記窒素ガスにより前記生物付着担体を攪拌する請求項1~8のいずれか1項に記載の嫌気性消化方法。
- 前記処理対象供給管または前記固定層の下部に供給する、前記消化ガスまたは前記窒素ガスの供給速度は5~40m/hrである請求項9に記載の嫌気性消化方法。
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US (1) | US20130130357A1 (ja) |
EP (1) | EP2602230A4 (ja) |
JP (1) | JP5620188B2 (ja) |
KR (1) | KR20130132746A (ja) |
CN (1) | CN103097308B (ja) |
WO (1) | WO2012017834A1 (ja) |
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CN103304028A (zh) * | 2013-06-26 | 2013-09-18 | 哈尔滨工业大学 | 一种厌氧处理的氮气搅拌方法 |
US11802065B2 (en) * | 2016-08-31 | 2023-10-31 | Conly L. Hansen | Induced sludge bed anaerobic reactor system |
CN112321114B (zh) * | 2020-10-30 | 2021-08-27 | 上海市政工程设计研究总院(集团)有限公司 | 厌氧消化池及污水处理厂 |
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- 2011-07-21 WO PCT/JP2011/066611 patent/WO2012017834A1/ja active Application Filing
- 2011-07-21 EP EP11814464.1A patent/EP2602230A4/en not_active Withdrawn
- 2011-07-21 KR KR20137003827A patent/KR20130132746A/ko not_active Application Discontinuation
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KR20130132746A (ko) | 2013-12-05 |
JP2012035197A (ja) | 2012-02-23 |
CN103097308B (zh) | 2015-08-12 |
CN103097308A (zh) | 2013-05-08 |
EP2602230A4 (en) | 2015-09-09 |
EP2602230A1 (en) | 2013-06-12 |
JP5620188B2 (ja) | 2014-11-05 |
US20130130357A1 (en) | 2013-05-23 |
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