WO2013146013A1 - 嫌気性処理液の処理システムおよび処理方法 - Google Patents
嫌気性処理液の処理システムおよび処理方法 Download PDFInfo
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- WO2013146013A1 WO2013146013A1 PCT/JP2013/054912 JP2013054912W WO2013146013A1 WO 2013146013 A1 WO2013146013 A1 WO 2013146013A1 JP 2013054912 W JP2013054912 W JP 2013054912W WO 2013146013 A1 WO2013146013 A1 WO 2013146013A1
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2866—Particular arrangements for anaerobic reactors
- C02F3/2893—Particular arrangements for anaerobic reactors with biogas recycling
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
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- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
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- C02F3/006—Regulation methods for biological treatment
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
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- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/10—Separation or concentration of fermentation products
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/06—Specific process operations in the permeate stream
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2653—Degassing
- B01D2311/2657—Deaeration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2688—Biological processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/04—Backflushing
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/162—Use of acids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/164—Use of bases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/168—Use of other chemical agents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/18—Use of gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09C—RECLAMATION OF CONTAMINATED SOIL
- B09C1/00—Reclamation of contaminated soil
- B09C1/08—Reclamation of contaminated soil chemically
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/005—Black water originating from toilets
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- 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
- C02F2103/28—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof from the paper or cellulose industry
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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
- 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
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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
- C02F2209/38—Gas flow rate
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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
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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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/20—Sludge processing
Definitions
- the present invention relates to an anaerobic treatment liquid treatment system and treatment method.
- Patent Document 1 a method of filtering an anaerobic treatment liquid with an immersion membrane filter medium is known.
- the filtrate is directly applied from the filtrate extraction side of the membrane filter medium. It is common to filter by suction with a pump. Further, biogas is generated from the anaerobic treatment liquid, and Patent Document 1 discloses that the generated biogas is used for cleaning the surface of the membrane filter medium.
- the present invention has been made in view of the above circumstances, and an object of the present invention is to provide a processing system and a processing method capable of efficiently performing filtration of anaerobic processing liquid and recovery of biogas and making equipment compact. It is to provide.
- the anaerobic treatment liquid treatment system of the present invention that has solved the above problems includes a solid-liquid separator provided with a filter medium immersed in the anaerobic treatment liquid, and a filtrate that has permeated the filter medium.
- a gas-liquid separator in which gas is held in the gas phase portion above the filtrate, a filtrate flow path communicating with the filtrate extraction side of the filter medium and the gas phase portion of the gas-liquid separator, and gas-liquid separation
- a first gas flow path provided with a pressure reducing means for reducing the pressure of the gas phase portion.
- the filtrate is degassed by the gas-liquid separator, and the biogas dissolved in the filtrate is recovered.
- the filtrate flow path is provided in communication with the gas phase portion of the gas-liquid separator and the filtrate extraction side of the filter medium, the gas phase portion of the gas-liquid separator is decompressed by the decompression means, thereby Filtration with a filter medium in a liquid separator can be promoted.
- filtration with a filter medium in a solid-liquid separator and degassing of a filtrate with a gas-liquid separator can be performed by a common decompression means, and anaerobic treatment liquid is filtered and biogas is efficiently recovered. And the equipment can be made compact.
- the second gas flow path is provided in communication with the first gas flow path on the discharge side of the decompression means and the filtrate flow path on the filtrate extraction side of the filter medium.
- the processing system of the present invention includes a gas phase part of the solid-liquid separator, at least one of the first gas flow path on the suction side of the decompression means and the gas phase part of the gas-liquid separator. It is preferable that a third gas flow path is provided in communication with.
- a gas holder connected to at least one of the first gas channel on the suction side of the decompression means and the gas phase portion of the gas-liquid separator instead of or together with the third gas channel. May be provided.
- the present invention also provides a filtration step of filtering the anaerobic treatment liquid in which biogas is dissolved with an immersion filter medium to obtain a filtrate, and degassing the filtrate by introducing the filtrate into a gas-liquid separator, and collecting the biogas.
- the filtrate removal side of the filter medium communicates with the gas phase part of the gas-liquid separator, and the gas phase part of the gas-liquid separator is depressurized to depressurize the filtrate output side of the filter medium.
- the present invention provides a method for treating an anaerobic treatment liquid that promotes filtration of the anaerobic treatment liquid in a filtration step and degass the filtrate in a deaeration step.
- the filtrate extraction side of the filter medium is depressurized to promote the filtration of the anaerobic treatment liquid in the filtration step, and the deaeration step Since the filtrate can be deaerated, the filtration step and the deaeration step can be performed efficiently.
- the amount of biogas recovered can be adjusted by adjusting the degree of vacuum in the gas phase of the gas-liquid separator and / or the filtrate water depth of the gas-liquid separator. For example, if the degree of decompression of the gas phase part of the gas-liquid separator is increased (that is, the pressure of the gas phase part of the gas-liquid separator is reduced), or the filtrate water depth of the gas-liquid separator is reduced, the biogas The recovered amount can be easily increased.
- the decompression of the gas phase part of the gas-liquid separator is preferably performed by a decompression means.
- the treatment method of the present invention supplies the biogas discharged from the decompression means to the filtrate outlet side of the filter medium, You may have further the backwashing process which backwashes.
- the gas phase part of the gas-liquid separator and the supply of biogas for backwashing to the filter medium can be performed by a common decompression means.
- Such equipment costs can be reduced.
- the anaerobic processing liquid can be efficiently filtered and biogas can be recovered, and the equipment can be made compact.
- An example of the processing system of the anaerobic processing liquid of this invention is represented.
- the other example of the processing system of the anaerobic processing liquid of this invention is represented.
- the present invention relates to a processing system and a processing method for an anaerobic processing liquid, and in particular, a processing system and a processing method capable of efficiently performing filtration of an anaerobic processing liquid and degassing of a filtrate obtained by the filtration.
- a processing system and a processing method capable of efficiently performing filtration of an anaerobic processing liquid and degassing of a filtrate obtained by the filtration.
- the anaerobic treatment liquid to be treated in the present invention is not particularly limited as long as it can be obtained by anaerobic treatment of liquid substances (including slurry) containing organic substances and solid substances.
- liquids and solids containing organic substances include sewage, human waste, livestock manure, industrial wastewater generated from food factories, paper mills, etc., garbage, kitchen wastewater, vegetation, and sludge generated by these treatments. Is mentioned.
- the anaerobic treatment is not particularly limited as long as the organic matter undergoes methane fermentation by placing the liquid or solid containing the organic matter in an anaerobic state. Therefore, the anaerobic treatment liquid contains biogas such as methane gas and carbon dioxide gas which are methane fermentation products, and these biogas are generally dissolved in the anaerobic treatment liquid according to the gas phase pressure. In the present invention, the biogas only needs to contain at least methane gas.
- the anaerobic treatment liquid may be one that has been subjected to methane fermentation or may be in the middle of methane fermentation.
- Methane fermentation may be performed in equipment intended to perform methane fermentation, such as a digester (methane fermenter), and liquids and solids containing organic substances are placed in an anaerobic state during transportation and storage. It may be caused by being.
- the SS concentration (floating substance concentration) of the anaerobic treatment liquid is not particularly limited.
- the SS concentration is generally about 50 mg / L to 400 mg / L.
- the SS concentration of the anaerobic treatment liquid is, for example, about 1000 mg / L to 8,000 mg / L.
- digested sludge obtained by anaerobic digestion can also be used as an anaerobic treatment solution.
- the SS concentration is It is about 10,000 mg / L to 50,000 mg / L.
- the SS concentration is determined according to the sewage test method.
- an anaerobic treatment liquid in which biogas is dissolved is filtered with an immersion filter medium to obtain a filtrate (filtration step).
- the filter medium is provided soaked in an anaerobic treatment liquid stored in a solid-liquid separator.
- the filter medium has a supply side and a filtrate extraction side, the anaerobic treatment liquid is supplied to the supply side, and the filtrate is taken out from the filtrate extraction side.
- Filtration with a filter medium is performed using a differential pressure between the filter medium supply side and the filtrate extraction side.
- filtration is promoted by the water pressure applied to the filter medium, but in the present invention, the filtrate take-out side is depressurized by the pressure reducing means described later, thereby further promoting the filtration of the anaerobic treatment liquid by the filter medium.
- the type of filter medium is not particularly limited, and a conventionally known filter medium may be used.
- the filter medium include a sand filter medium and a membrane filter medium. Among these, a membrane filter medium is preferably used.
- the pore diameter of the membrane filter medium is not particularly limited, but is preferably a so-called microfiltration membrane (MF membrane) or ultrafiltration membrane (UF membrane).
- MF membrane microfiltration membrane
- UF membrane ultrafiltration membrane
- the membrane filter medium is a microfiltration membrane (MF membrane) from the viewpoint of efficiently removing suspended substances (SS) from the anaerobic treatment liquid.
- the type (shape) of the membrane filter medium is not particularly limited, such as a hollow fiber membrane, a tubular membrane, and a flat membrane.
- the membrane filter medium may be one in which the filter medium itself functions as a separation layer.
- the support is immersed in the anaerobic treatment liquid, and suspended substances contained in the anaerobic treatment liquid are deposited on the support, and the deposited layer is separated. It may function as a layer. The latter is commonly referred to as dynamic filtration.
- the separation layer is a layer that determines solid-liquid separation ability, and is a layer having the smallest pore diameter among the layers constituting the membrane filter medium.
- the material constituting the membrane filter medium and the support is not particularly limited, and examples thereof include plastic, metal (for example, stainless steel), ceramic, fiber material, and paper.
- the solid-liquid separator that performs filtration may be any one that can hold the anaerobic treatment liquid and is provided by immersing the filter medium in the anaerobic treatment liquid.
- the solid-liquid separator may perform only solid-liquid separation (filtration) using a filter medium, or may perform anaerobic treatment along with solid-liquid separation.
- a solid-liquid separator may be provided in communication with the digester.
- the filter medium is provided soaked in a digestion tank, or the filter medium is provided soaked in a sewage and human waste receiving tank.
- the digestion tank and the receiving tank are regarded as a solid-liquid separator.
- the solid-liquid separator has a gas phase part in which a gas is held at the upper part of the anaerobic treatment liquid.
- the anaerobic treatment liquid contains biogas, and in the solid-liquid separator, biogas can be generated from the anaerobic treatment liquid. Therefore, it is preferable that the solid-liquid separator has a gas phase part in which the gas is held above the anaerobic treatment liquid, from the viewpoint that the biogas generated in the solid-liquid separator can be recovered.
- the solid-liquid separator has a cover and a gas outlet for taking out the biogas is provided at the top of the solid-liquid separator.
- a solid-liquid separator is configured by arranging a filter medium inside a tank.
- the filtrate obtained in the filtration step is introduced into a gas-liquid separator, the filtrate is degassed, and biogas is recovered (degassing step).
- the gas-liquid separator there is a filtrate that has permeated through the filter medium, and gas is held in the gas phase portion above the filtrate.
- the filtrate is degassed by depressurizing the gas phase portion of the gas-liquid separator.
- the gas-liquid separator is not limited as long as it can hold the filtrate inside and can hold the gas above the filtrate.
- the gas-liquid separator is configured so that the gas phase portion can hold gas, and the gas phase portion of the gas-liquid separator is in communication with a first gas flow path having a decompression means.
- the gas phase portion of the gas-liquid separator is decompressed by the decompression means.
- the gas-liquid separator is not limited as long as the gas phase portion can be decompressed by the decompression means.
- the gas-liquid separator may be composed of, for example, a tank that stores filtrate, or may be composed of a pipe through which filtrate flows. However, in any case, the gas-liquid separator is provided with a gas phase portion above the filtrate.
- the gas phase part of the gas-liquid separator is depressurized by a depressurizing means. Further, as described above, filtration of the anaerobic treatment liquid in the solid-liquid separator with the filter medium is performed in the same decompression means. That is, in the present invention, the filtration of the anaerobic treatment liquid with the filter medium and the degassing of the filtrate obtained by the filtration are performed by a common decompression means. In order to realize this, in the present invention, a filtrate flow path is provided in communication with the filtrate extraction side of the filter medium and the gas phase portion of the gas-liquid separator.
- the gas phase portion of the gas-liquid separator is depressurized, whereby the filtrate is degassed in the degassing step, and the filtrate outlet side of the filter medium is depressurized.
- the filtration of the anaerobic treatment liquid in the filtration process is promoted.
- the filtrate outlet side of the filter medium is communicated with the gas phase part of the gas-liquid separator, and the gas phase part of the gas-liquid separator is decompressed and filtered by the filter medium.
- the anaerobic treatment liquid can be efficiently filtered.
- the depressurization means is not particularly limited as long as it can depressurize the gas phase part of the gas-liquid separator, but is preferably one that sucks the gas in the gas phase part of the gas-liquid separator and depressurizes the gas phase part.
- the mechanical decompression means is preferred.
- a pressure reducing pump vacuum pump
- a blower or the like can be used as such pressure reducing means.
- the filtrate flow path has one end connected to the filtrate extraction side of the filter medium and the other end connected to the gas phase part of the gas-liquid separator.
- the arrangement method of the filtrate channel is not particularly limited as long as it connects the filtrate extraction side of the filter medium and the gas phase part of the gas-liquid separator.
- the filtrate water level in the filtrate flow path is the water level of the anaerobic treatment liquid in the solid-liquid separator because the differential pressure between the filter medium supply side and the filtrate take-out side is increased to achieve efficient filtration. Is preferably not too high.
- the filtrate water level in the filtrate channel is preferably not located above 3 m or more, more preferably not located above 2 m or more, preferably 1 m or more above, based on the water level of the anaerobic treatment liquid of the solid-liquid separator. More preferably, the filtrate water level in the filtrate channel is particularly preferably the same as or lower than the water level of the anaerobic treatment liquid of the solid-liquid separator. That is, it is preferable that the filtrate flow path is not arranged so as to extend as high as possible starting from the filtrate take-out side, and more preferably, the filtrate flow path is installed so as to be horizontal or descending.
- the amount of biogas recovered can be adjusted by adjusting the degree of vacuum in the gas phase of the gas-liquid separator.
- the filtration flow rate in a filter medium can also be raised, so that the pressure reduction degree of the gaseous-phase part of a gas-liquid separator is raised. Therefore, the pressure in the gas phase part of the gas-liquid separator should be at least lower than the pressure in the gas phase part of the solid-liquid separator.
- the gas phase part of the vessel may be depressurized to be -10 kPa (gauge pressure) or less, preferably -30 kPa (gauge pressure) or less, more preferably -50 kPa (gauge pressure) or less. .
- the amount of biogas recovered can also be adjusted by adjusting the filtrate water depth of the gas-liquid separator.
- the filtrate water depth of the gas-liquid separator is shallower, degassing can be performed more efficiently.
- the filtrate water depth of the gas-liquid separator satisfies the following relationship in relation to the surface area at which the filtrate contacts the gas phase portion.
- the filtrate in the gas-liquid separator preferably has a ratio of (surface area) 1/2 / water depth of 1 or more, preferably 2 or more, and more preferably 4 or more.
- the surface area means the surface area where the filtrate comes into contact with the gas phase part
- (surface area) 1/2 is the length of one side of the square of the same area as the surface where the filtrate comes into contact with the gas phase part. Equivalent to.
- the biogas dissolved in the filtrate moves to the gas phase part of the gas-liquid separator and is discharged from the gas-liquid separator through the first gas flow path.
- the pressure reducing means provided in the first gas flow path has a suction side and a discharge side, and the biogas in the first gas flow path is sucked from the suction side of the pressure reducing means and discharged to the discharge side.
- the biogas discharged to the discharge side of the decompression means can be recovered and used as an energy source.
- energy may be recovered by supplying it to a gas turbine and burning it, or methane contained in biogas may be used as fuel for the fuel cell. Of course, you may just burn and use heat.
- the biogas discharged to the discharge side of the decompression means may be used for backwashing the filter medium.
- a second gas flow path may be provided in communication with the discharge side of the decompression means and the filtrate extraction side of the filter medium, and the biogas discharged from the decompression means through the second gas flow path is filtered.
- the filter medium can be backwashed by supplying it to the take-out side (backwashing step).
- the filter medium need not be backwashed at all times, and may be performed when the filtration flow rate of the filter medium decreases. That is, the backwash process may be performed intermittently.
- a backwashing agent for example, an oxidizing agent, an acid, an alkali, etc.
- a backwashing agent for example, an oxidizing agent, an acid, an alkali, etc.
- the biogas discharged to the discharge side of the decompression means may be used for cleaning the filter medium surface.
- the filter medium is a membrane filter medium (except for dynamic filtration)
- the surface (membrane surface) of the membrane filter medium may be subjected to cross-flow cleaning by supplying biogas from below the membrane filter medium.
- biogas dissolved in the anaerobic treatment liquid can be efficiently recovered.
- the ratio of the biogas generated by the anaerobic treatment dissolved in the anaerobic treatment liquid increases.
- biogas can be efficiently collected.
- FIGS. 1 and 2 An example of a configuration of an anaerobic treatment liquid treatment method and a treatment system according to the present invention will be described with reference to FIGS. 1 and 2.
- this invention is not limited to the embodiment shown in FIG. 1 and FIG.
- the anaerobic treatment liquid treatment system shown in FIG. 1 includes a solid-liquid separator 11 that filters the anaerobic treatment liquid, a gas-liquid separator 21 that degass the filtrate obtained by the solid-liquid separator 11,
- the gas phase section 23 of the liquid separator 21 is depressurized to promote filtration in the solid-liquid separator 11, and has a pressure reducing means 31 for degassing in the gas-liquid separator 21.
- the solid-liquid separator 11 is provided by immersing the filter medium 13 in the anaerobic treatment liquid 12, and has a gas phase part 14 in which a gas is held above the anaerobic treatment liquid 12.
- a digestion tank 15 is provided adjacent to the front stage of the solid-liquid separator 11, and the organic waste water is anaerobically treated in the digestion tank 15 to obtain an anaerobic treatment liquid.
- the anaerobic treatment liquid obtained by anaerobic digestion in the digestion tank 15 overflows from the digestion tank 15 and flows into the solid-liquid separator 11.
- a filtration process is performed.
- the anaerobic treatment liquid 12 in which biogas is dissolved is filtered by the immersion filter medium 13 to obtain a filtrate.
- the digestion tank 15 may be provided by being connected to the solid-liquid separator 11 by a pipe line (not shown).
- the gas phase part 14 of the solid-liquid separator 11 is connected to the gas phase part 16 of the digestion tank 15, and a gas flow path 43 is provided in communication with the gas phase part 16 of the digestion tank 15.
- the gas flow path 43 has one end connected to the gas phase section 16 of the digestion tank 15, the other end connected to the gas holder 41, and is provided with a transfer means 42 (blower in FIG. 1).
- biogas is generated from the organic wastewater or the anaerobic treatment liquid 12, and the generated biogas is transferred to the gas holder 41 through the gas flow path 43 by the transfer means 42 and collected.
- one end of the gas flow path 43 may be connected to the gas phase part 14 of the solid-liquid separator 11.
- a filtrate channel 17 is provided in communication with the filtrate extraction side of the filter medium 13, and the filtrate channel 17 further communicates with the gas phase portion 23 of the gas-liquid separator 21.
- the filtrate obtained by filtering with the filter medium 13 is transferred to the gas-liquid separator 21 through the filtrate channel 17.
- the filtrate 22 is present in the gas-liquid separator 21, and the gas is held in the gas phase part 23 above the filtrate 22.
- the filtrate 22 introduced into the gas-liquid separator 21 is degassed, and a degassing step for collecting biogas is performed.
- a first gas flow path 32 having a decompression means 31 communicates with the gas phase portion 23 of the gas-liquid separator 21.
- the decompression means 31 is provided on the suction side so as to communicate with the gas phase part 23 of the gas-liquid separator 21.
- the gas phase part 23 of the gas-liquid separator 21 is depressurized by the depressurization means 31, whereby the filtrate take-out side of the filter medium 13 is also depressurized, and the filtration of the anaerobic treatment liquid 12 is promoted in the filtration step, and the deaeration is performed.
- the filtrate 22 is degassed in the process.
- the biogas obtained by degassing the filtrate 22 with the gas-liquid separator 21 is discharged from the discharge side of the decompression means 31 through the first gas flow path 32.
- the discharge side of the decompression means 31 communicates with the gas holder 41, and the biogas discharged from the discharge side of the decompression means 31 is transferred to the gas holder 41 and collected.
- the biogas from the digester 15 or the solid-liquid separator 11 and the biogas from the gas-liquid separator 21 are separately collected. Comparing the composition of these biogases, the solubility in the filtrate 22 is higher for carbon dioxide gas than for methane gas, so that the biogas recovered from the gas-liquid separator 21 is the digester 15 or solid-liquid separation.
- the ratio of carbon dioxide tends to be higher than the biogas from the vessel 11. Therefore, for example, when it is desired to increase the proportion of methane gas contained in the biogas recovered in the gas holder 41, the degree of decompression of the gas phase portion 23 of the gas-liquid separator 21 may be reduced (that is, the pressure of the gas phase portion 23).
- the degree of decompression of the gas phase portion 23 of the gas-liquid separator 21 may be increased (that is, The pressure in the gas phase portion 23 may be lowered).
- the composition and amount of biogas recovered in the gas holder 41 can also be adjusted by appropriately adjusting the filtrate water depth.
- the filtrate 22 deaerated by the gas-liquid separator 21 is discharged from the filtrate outlet 24.
- a filtrate discharge flow path 25 is connected to the filtrate discharge port 24, and the filtrate discharge flow path 25 is sealed with a water seal portion 26 so that the gas-liquid separator 21 is kept airtight. It is preferable.
- the filtrate discharged from the filtrate discharge channel 25 may be discharged as it is or may be further processed separately.
- a second gas flow path 34 is provided in communication with the first gas flow path 32 on the discharge side of the decompression means 31 and the filtrate flow path 17 on the filtrate extraction side of the filter medium 13.
- a third gas flow path 36 is provided in communication with at least one of the above. If the third gas flow path 36 is provided in this way, the valve 37 provided in the third gas flow path 36 is opened at the time of backwashing, so that the gas for backwashing becomes the gas phase of the solid-liquid separator 11. It is supplied from the section 14 and it is possible to increase the backwash time.
- FIG. 2 shows a processing system different from the anaerobic processing liquid processing system shown in FIG.
- the description of the same part as the above description regarding FIG. 1 is omitted.
- the anaerobic treatment liquid treatment system shown in FIG. 2 also serves as a digestion tank in which the solid-liquid separator 11 performs anaerobic digestion. That is, anaerobic treatment liquid 12 is obtained by supplying organic wastewater to the solid-liquid separator 11 and performing anaerobic treatment.
- anaerobic digestion is obtained by performing anaerobic digestion on a relatively small scale
- the solid-liquid separator 11 may also serve as a digestion tank, and in this way, equipment costs can be kept low. .
- the gas holder 41 communicates with at least one of the first gas flow path 32 on the suction side of the decompression means 31 and the gas phase portion 23 of the gas-liquid separator 21.
- a fourth gas flow path 38 is provided. That is, the gas holder 41 is provided so as to be connected to at least one of the first gas flow path 32 on the suction side of the decompression means 31 and the gas phase portion 23 of the gas-liquid separator 21. If the fourth gas flow path 38 is provided in this way, the back-washing gas is supplied from the gas holder 41 by opening the valve 39 provided in the fourth gas flow path 38 during backwashing. It is possible to take a long backwash time.
- the present invention can be used for the treatment of sewage, human waste, livestock manure, industrial wastewater generated from food factories, paper mills, etc., raw garbage, kitchen wastewater, vegetation, and sludge generated by these treatments.
- Solid-liquid separator 12 Anaerobic treatment liquid 13: Filter medium 14: Gas phase part 17: Filtrate flow path 21: Gas-liquid separator 22: Filtrate 23: Gas phase part 31: Pressure reducing means 32: First gas Channel 34: Second gas channel 36: Third gas channel 41: Gas holder
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Abstract
Description
しく、4以上となることがさらに好ましい。前記比において、表面積は、ろ液が気相部と接触する表面積を意味し、(表面積)1/2は、ろ液が気相部と接触する表面と等面積の正方形の一辺の長さに相当する。
12: 嫌気性処理液
13: ろ材
14: 気相部
17: ろ液流路
21: 気液分離器
22: ろ液
23: 気相部
31: 減圧手段
32: 第1ガス流路
34: 第2ガス流路
36: 第3ガス流路
41: ガスホルダー
Claims (7)
- 嫌気性処理液にろ材が浸漬して設けられた固液分離器と、
前記ろ材を透過したろ液が存在し、当該ろ液の上部の気相部にガスが保持された気液分離器と、
前記ろ材のろ液取出側と、前記気液分離器の気相部とに連通したろ液流路と、
前記気液分離器の気相部に連通し、前記気相部を減圧する減圧手段を備えた第1ガス流路とを有することを特徴とする嫌気性処理液の処理システム。 - 前記減圧手段の吐出側の第1ガス流路と前記ろ材のろ液取出側のろ液流路とに連通して第2ガス流路が設けられている請求項1に記載の処理システム。
- 前記固液分離器は、嫌気性処理液の上部にガスが保持された気相部を有し、
前記固液分離器の気相部と、前記減圧手段の吸引側の第1ガス流路および前記気液分離器の気相部の少なくとも一方とに連通して第3ガス流路が設けられている請求項2に記載の処理システム。 - 前記減圧手段の吸引側の第1ガス流路および前記気液分離器の気相部の少なくとも一方に接続して、ガスホルダーが設けられている請求項2または3に記載の処理システム。
- バイオガスが溶存した嫌気性処理液を浸漬ろ材でろ過し、ろ液を得るろ過工程と、
前記ろ液を気液分離器に導入してろ液を脱気し、バイオガスを回収する脱気工程とを有し、
前記ろ材のろ液取出側が前記気液分離器の気相部に連通し、前記気液分離器の気相部を減圧することにより、前記ろ材のろ液取出側を減圧して前記ろ過工程で前記嫌気性処理液のろ過を推進するとともに、前記脱気工程で前記ろ液を脱気することを特徴とする嫌気性処理液の処理方法。 - 前記脱気工程において、前記気液分離器の気相部の減圧度および/または前記気液分離器のろ液水深を調整して、バイオガスの回収量を調整する請求項5に記載の処理方法。
- 前記気液分離器の気相部の減圧が減圧手段によって行われ、
前記処理方法が、前記減圧手段から吐出されたバイオガスを前記ろ材のろ液取出側に供給して、前記ろ材を逆洗する逆洗工程をさらに有する請求項5または6に記載の処理方法。
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US14/376,753 US20150013540A1 (en) | 2012-03-29 | 2013-02-26 | System and process for treating an anaerobically-processed liquid |
CN201380012968.XA CN104203834B (zh) | 2012-03-29 | 2013-02-26 | 嫌气性处理液的处理系统及处理方法 |
ES13768802.4T ES2621259T3 (es) | 2012-03-29 | 2013-02-26 | Sistema y procedimiento para el tratamiento de una disolución de tratamiento anaeróbico |
EP13768802.4A EP2835355B1 (en) | 2012-03-29 | 2013-02-26 | System and method for treating anaerobic treatment solution |
PH12014501764A PH12014501764A1 (en) | 2012-03-29 | 2014-08-06 | System and process for treating an anaerobically-processed liquid |
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JP2012078165A JP5867923B2 (ja) | 2012-03-29 | 2012-03-29 | 嫌気性処理液の処理システムおよび処理方法 |
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EP (1) | EP2835355B1 (ja) |
JP (1) | JP5867923B2 (ja) |
CN (1) | CN104203834B (ja) |
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DE102015109822A1 (de) * | 2015-06-19 | 2016-12-22 | Gottfried Wilhelm Leibniz Universität Hannover | Verfahren und Vorrichtung zur Gewinnung von Methan aus anaeroben Abwässern |
CN112593464A (zh) * | 2020-12-10 | 2021-04-02 | 东莞市加隆纸塑包装有限公司 | 一种无排放的鞋撑生产系统 |
JP7398601B1 (ja) * | 2023-05-30 | 2023-12-14 | 三菱化工機株式会社 | 有機性排水処理装置および有機性排水処理方法 |
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2012
- 2012-03-29 JP JP2012078165A patent/JP5867923B2/ja active Active
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2013
- 2013-02-26 WO PCT/JP2013/054912 patent/WO2013146013A1/ja active Application Filing
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US20150013540A1 (en) | 2015-01-15 |
ES2621259T3 (es) | 2017-07-03 |
CN104203834B (zh) | 2016-08-24 |
CN104203834A (zh) | 2014-12-10 |
JP2013202602A (ja) | 2013-10-07 |
PH12014501764A1 (en) | 2014-11-10 |
EP2835355A4 (en) | 2015-12-16 |
EP2835355A1 (en) | 2015-02-11 |
EP2835355B1 (en) | 2017-01-18 |
JP5867923B2 (ja) | 2016-02-24 |
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