WO2018215040A1 - Méthode et appareil de récupération de matières organiques solides à partir d'un flux d'un effluent de biomasse partiellement digérée - Google Patents

Méthode et appareil de récupération de matières organiques solides à partir d'un flux d'un effluent de biomasse partiellement digérée Download PDF

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Publication number
WO2018215040A1
WO2018215040A1 PCT/DK2018/050116 DK2018050116W WO2018215040A1 WO 2018215040 A1 WO2018215040 A1 WO 2018215040A1 DK 2018050116 W DK2018050116 W DK 2018050116W WO 2018215040 A1 WO2018215040 A1 WO 2018215040A1
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Prior art keywords
riser pipe
flotation tank
flotation
mixture
microbubbles
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PCT/DK2018/050116
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English (en)
Inventor
Erik JESSEN JÜRGENSEN
Tore Christian SVENDSEN
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Bio-Aqua A/S
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Application filed by Bio-Aqua A/S filed Critical Bio-Aqua A/S
Priority to DKPA201970806A priority Critical patent/DK201970806A1/en
Priority to EP18728029.2A priority patent/EP3630938A1/fr
Publication of WO2018215040A1 publication Critical patent/WO2018215040A1/fr

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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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0205—Separation of non-miscible liquids by gas bubbles or moving solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1412—Flotation machines with baffles, e.g. at the wall for redirecting settling solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/1475—Flotation tanks having means for discharging the pulp, e.g. as a bleed stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1493—Flotation machines with means for establishing a specified flow pattern
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/24—Pneumatic
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/04—Apparatus for enzymology or microbiology with gas introduction means
    • C12M1/08—Apparatus for enzymology or microbiology with gas introduction means with draft tube
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/04—Apparatus for enzymology or microbiology with gas introduction means
    • C12M1/09—Flotation apparatus
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/107—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane
    • 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
    • C12M1/00—Apparatus for enzymology or microbiology
    • C12M1/107—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane
    • C12M1/113—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane with transport of the substrate during the fermentation
    • 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
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/58—Reaction vessels connected in series or in parallel
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
    • C12M29/08—Air lift
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/24—Recirculation of gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2203/00—Specified materials treated by the flotation agents; specified applications
    • B03D2203/001—Agricultural products, food, biogas, algae
    • 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
    • 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

  • a method and an apparatus for recovering a solid organics from a flow of an effluent of partly digested biomass is provided.
  • the present invention relates to a method of continuously recovering at least solid organics from a flow of an effluent from a biogas plant and re-circulating the recovered substances to the biogas plant.
  • the invention further relates to an apparatus for performing the method.
  • a biogas plant converts biomasses, such as manure, waste and other organic feedstock into biogas by anaerobic digestion in a digester with anaerobic organisms, which digest material inside a closed system, or by fermentation of biodegradable materials.
  • biomasses such as manure, waste and other organic feedstock
  • anaerobic digestion in a digester with anaerobic organisms, which digest material inside a closed system, or by fermentation of biodegradable materials.
  • methane gas is created.
  • the biogas is primarily methane and carbon dioxide that can subsequently be combusted or oxidized with oxygen to be used as a fuel and to make electricity, or be used as a chemical feedstock for producing petrochemicals .
  • an average retention time of 20 days in a fully stirred digester is assumed typical.
  • one twentieth of the biomass is replaced every day by the daily in- and outflow.
  • About 20% of the biomass pumped into the digester on day 1 will have been pumped out again already after five days. This biomass will therefore not be fully digested.
  • about one third of the biomass will still be in the reactor after 20 days. This relationship is decisive of how much of the theoretically potential gas production of the biomass can be achieved before the biomass is pumped out again.
  • the digester effluent from the biogas plant may for some readily digested biomass have a content of organic solids as little as about 2 - 5 wt/vol %, the rest being water. However, the digester effluent is often much higher in suspended organics.
  • a centrifuge can be used to recover organics.
  • the filtrate from the centrifugation can be subjected to lime clarification, additional centrifugation, ammonia stripping, and a spiral reverse osmosis (RO) unit.
  • RO reverse osmosis
  • a known method for recovering product from an effluent from a biogas plant is disclosed in International patent application no. W02011 / 19373.
  • the separation method utilizes an aerated inlet mixture of fluid and solids together with one or both of a coagulating agent and a flocculating agent.
  • This aerated inlet mixture is fed into a cylindrical, upright, separation vessel at four spaced-apart locations at a center part of said vessel, so as to be injected tangentially along the cylinder wall and force aggregates towards the top of the vessel. Tangentially injection of the inlet mixture promotes the formation of solid aggregates so that the inlet mixture becomes separated into an upper float layer and a lower clarified layer.
  • the aerating gas that contributes in the gas flotation separation of the solid contaminant by attaching to the solid particles aids in forming an aggregate mass of solids and gas microbubbles .
  • the density difference between the aggregate mass and the fluid medium provides a buoyant force to drive the separation process.
  • the aerating gas e.g. methane
  • the aerating gas is generally added to the inlet fluid as a dissolved gas at an elevated pressure relative to the operating pressure of the separation vessel.
  • the aerated gas leaves solution and forms the aerated gas micro-bubbles.
  • the upper float layer is withdrawn from the vessel when the height of the upper float layer exceeds the height of an overflow conduit and forms a concentrated solids effluent.
  • the lower clarified layer is withdrawn from the separation vessel as a clarified fluid effluent.
  • the separation process is performed continuously using a control process that maintains a relatively stable distribution between the lower clarified layer and the upper float layer.
  • the upper phase can be re-circulated as a feed substrate to a biogas plant however such re-circulated matter is polluted with the coagulating agent and a flocculating agent .
  • the inlet mixture needs to be injected tangentially at several points at a center section of the separation vessel or at an even higher location to achieve the swirl that is needed to continuously stir of the large reaction chamber to create the solid aggregates in the large reactor chamber, and move those towards the upper float layer.
  • a single injection position close to the bottom of separation vessel would only create a small or inferior swirl and limited level of aggregation.
  • this known method and apparatus are complex, and there is high need to carefully keep control of the operating parameters.
  • WO9220628 discloses a method of recovering solids organic from a flow of an effluent from a biogas plant and re-circulating the recovered solid substances to the biogas plant, wherein the recovery is performed by flotation using anoxic gases.
  • a main aspect of the present invention is to provide an efficient method and an efficient apparatus to increase and optimize the gas production from the biogas plant.
  • first flotation tank with a first flotation chamber, which first flotation tank comprises at least
  • first riser pipe erected in the first flotation chamber, which first riser pipe has a first riser pipe inlet and an opposite first riser pipe outlet,
  • microbubbles are bubbles smaller than one millimeter in diameter, but larger than one micrometer.
  • organics refers to organic matter that is capable of decay, the product of decay, or substances composed of organic compounds.
  • the terms “organics”, “organic matter” and “organic substances” are used interchangeable in the present application.
  • methane potential refers to the volume of methane biogas produced during anaerobic degradation in the presence of bacteria of a sample initially introduced, expressed under Normal conditions of Temperature and Pressure (0°C, 1013 hPa) .
  • the composition of the biomass being digested in the biogas plant may vary considerably and is not exactly known. So in all biogas plants some solid organic matter escapes the digester without having been digested and converted fully into biogas. How much organics that escape depend amongst others on the reaction conditions and the reaction parameters of the digestion process, including the composition of the biomass, the digestion time, the reaction temperature, pH, stirring, potential inhibitor concentrations, the feed speed and density of the biomass, etc. The more complicated the molecules of the biomass are the longer it takes a microorganism to break the molecule down. So normally digestion of organics in an effluent from a biogas plant are incomplete and the effluent can have a substantial residual caloric content and methane potential represented by undigested organic matter.
  • the caloric content and methane potential of said organics are still valuable to derive from the effluent.
  • the caloric content and methane potential of a larger part of the biomass can be utilized, and the need for expensive secondary storage capacity for effluent is reduced.
  • the effluent from the biogas plant is mixed with a first mixture containing microbubbles of a first gaseous flotation vehicle dispersed in a first liquid medium.
  • the first mixture is fed to the first inlet of the first flotation tank, which first inlet is in fluid communication with the first riser pipe inlet with the first nozzle means.
  • the micro-bubbles of gas in the first mixture is released in the first riser pipe upon passing the first nozzle means, which passage also reduces the feed pressure of the first mixture.
  • the first mixture with microbubbles dispersed therein then ascends the first riser pipe erected in the first flotation tank at a pressure equalized by the first nozzle means to typically about the water column pressure existing in the first flotation tank.
  • said first riser pipe serves as a confined first reaction chamber where microbubbles and organics of the first mixture are kept in a close contact to facilitate and promote formation during rising of the microbubbles through the first riser pipe of aggregates formed by the attachment of the microbubbles to the organic matter.
  • the microbubbles make the aggregated substances buoyant and carries said aggregates gently upwards through the first riser pipe directly into the first upper phase as a first flotation layer that settles, e.g. as a foam, as a top surface layer at a top zone of the first flotation tank.
  • the first liquid phase which is the first lower phase, has a lower density than the first flotation layer, which is the first upper layer, so the first liquid phase flows towards a bottom zone of the first flotation tank as a first lower phase when the reacted first mixture leaves the first riser pipe outlet.
  • the first lower phase is substantially water containing dissolved, not yet digested organic matter, inorganics and optionally some indigestible matter that cannot be attached to the microbubbles .
  • the selected gas keeps same anaerobic conditions as in the digester. No additional stirring that could disintegrate the formed aggregates or swirls for enhancing contact between gas and organics are needed, nor is any flocculation agents and coagulation agents used.
  • the first riser pipe serves as a separate temporary confined reaction and flotation chamber wherein the microbubbles induce aggregation of residual solid organic matter in the effluent from the biogas plant by attaching to said residual organics during the rising.
  • the retention time of the organics during passage of the first riser pipe suffice for creating coherent floatable aggregates containing said organics, which floatable aggregates are driven upwards due to, on the one hand the driving force of the microbubbles flowing upwards, and on the other hand due to the aggregates having a lower density than the liquid first lower phase.
  • the first riser pipe preferably has the first riser pipe inlet aligned with the first inlet and is shorter than the overall height of the first flotation tank to leave a head space for the first upper phase, and optionally also for establishing a distinctive distance between the first upper phase and the first riser pipe outlet so that aggregates can continuously float freely upwards and out through said first riser pipe outlet without plugging or clogging of the first riser pipe.
  • a thorough dispersing of microbubbles of selected gases of the first flotation vehicle in the first liquid medium is e.g. obtained by means of a pump, preferably a turbine pump.
  • the first liquid medium with its content of gas microbubbles is typically pumped to the first inlet of the first flotation tank by the pump at a pressure substantially higher than the water column pressure in the first flotation tank, e.g. a pressure about 3 - 5 bar.
  • a suitable turbine pump is e.g. the MICRO/NANO BUBBLE GENERATOR obtainable from Rotary Trading Company, Industrieterrein ' t Woud 28, 3232 LN Brielle, The Netherlands.
  • Rotary Trading Company is the European Distributor for Nikuni pumps .
  • the first nozzle means reduces the pressure of the first mixture and releases the microbubbles of gas of the first mixture into the effluent at the first riser pipe inlet.
  • the incoming pressure of the first mixture to the first flotation tank is preferably reduced at the first riser pipe inlet to a pressure close to the water column pressure in the first flotation tank so that the first mixture is not driven so fast towards the first riser pipe outlet that formation of aggregates of organics of the effluent and gas microbubbles of the first mixture are hindered and/or are limited, and so that disintegration of such floatable aggregates are prevented.
  • the first nozzle means for obtaining the reduction of the pressure of the first mixture into the first riser pipe include e.g.
  • a first nozzle positioned inside the first riser pipe at the first riser pipe inlet.
  • the orifices of the first nozzle provide restrictions for the incoming flow of the first mixture to control the pressure of the incoming gaseous first mixture when it enters the first riser pipe.
  • the outlet pressure from the first nozzle of the first mixture is balanced substantially to the pressure of the water column head as there is nothing to restrict flow on the exit side of the orifices.
  • the flow of first mixture that passes through the orifices to the exit side of the orifices at reduced pressure depends on the pressure of the first mixture when it hits the orifice (s) of the first nozzle, and of e.g. the size, shape and design of the first nozzle.
  • the first nozzle may conveniently be self-cleaning, in that the at least one slot can be opened pneumatically on a timer-controlled basis. The first nozzle means can then operate uninterrupted and under same conditions at all times.
  • the opening and size of the orifices of the first nozzle can be controlled by being subjected to pressurized gas, e.g. pressurized methane directed through the orifices.
  • pressurized gas e.g. pressurized methane directed through the orifices.
  • the pressure of the pressurized gas directed towards the orifices of the first nozzle may be adjusted in accordance with the static pressure in the first flotation tank to open, close and/or re-size the orifices.
  • the first upper phase settles at the top zone of the first flotation tank and is harvested, and optionally pressurized, and re-circulated to the biogas plant for further digestion. Thus floating matter is re-used to make more biogas.
  • the above method may further comprises the steps of
  • the first lower phase may still contain some organic matter and thus still represent a source of bio-energy and methane potential. Accordingly the first lower phase may conveniently be subjected to yet a flotation process in a second flotation tank.
  • the first flotation tank has a conical bottom zone and optionally also a conical top zone.
  • the first inlet can then be expediently located at the tapered tip of the bottom zone.
  • the second flotation tank may have the same design, but can in the alternative be of a different design, such as an oblong tank that exposes a large surface area at the top zone for accumulation of floating aggregates.
  • the first lower phase can conveniently be treated in a similar manner as the effluent was in the first flotation tank.
  • the second flotation tank can thus work and be operated in the same manner as the first flotation tank, as described in details above.
  • the first flotation vehicle and the second flotation vehicle may conveniently be the same gas and come from the same source, but can in the alternative be different gases.
  • the first inert, anoxic or low-oxygen gas and the second inert, anoxic or low-oxygen gas are selected from the group of gases including methane and nitrogen and C0 2 , wherein methane is most preferred. Combinations of the above-mentioned cases are also within the scope of the present invention.
  • the first inert or low-oxygen gas and/or the second inert or low-oxygen gas can be a product gas from the biogas plant, such as a clean gas, e.g. methane, or a gas mixture preferably containing methane.
  • the second nozzle means for obtaining the reduction of the pressure of the second mixture into the second riser pipe includes e.g. a second nozzle positioned inside the second riser pipe at the second riser pipe inlet.
  • the first nozzle means and the second nozzle may be of the same kind as the first nozzle means and the first nozzle, including the second nozzle be self-cleaning, as described above, and be subjected to a compressed gas stream to release the microbubbles of the second mixture into the first lower phase added to the second riser pipe from the first flotation tank.
  • the first and second mixtures with their content of microbubbles are preferably pumped by the same pump that created these mixtures of flotation vehicle and liquid media to the first nozzle and the second nozzle, respectively.
  • the pump puts the first and second mixture under pressure at which they arrive at the first nozzle and the second nozzle, respectively.
  • the first nozzle means and the second nozzle means, respectively are preferably of the kind being able to provide a counter pressure, whereby a pressure drop across a respective nozzle of a nozzle means is obtained, which pressure drop advantageously may serve to further reduce the size of the microbubbles .
  • microbubbles that attach to organics to obtain floating aggregates of organics are at least to some extent trapped in the first upper phase and in the second upper phase, respectively, which upper phases then contain microbubbles of gases which can come from the biogas plant itself and can be re-circulated to the biogas plant again in a closed loop. No biogas is lost to the environment in that the methane potential of the effluent is derived to the largest possible extent and biogas re-used in the flotation steps of the present invention.
  • the first liquid medium and the second liquid medium may be the same, be of the same kind or be different.
  • the first liquid medium and the second liquid medium is taken from the second lower phase that is withdrawn from the second flotation tank and pumped by a pump that adds microbubbles of a first inert, anoxic or low-oxygen gas to the liquid media and pumps the obtained mixtures into the first flotation tank and the second flotation tank, respectively.
  • a preferred pump for this purpose is a turbine pump, preferably the turbine pump from Nikuni mentioned above.
  • the vacuum at the suction side is responsible for the intake of inert, anoxic or low-oxygen gases into the pump chamber where it is mixed into the liquid media as microbubbles. The pump pressurizes the so obtained mixture.
  • a flow of a mixture of a flow of gas and a flow of lower second phase is created by one single turbine pump.
  • This flow of mixture is divided into a flow of a first mixture and a flow of a second mixture of same composition, which flow of first mixture and flow of second mixture are pumped by the pump via the respective first and second nozzles into the respective riser pipes of the first and second flotation tanks to further reduce the size of the gas microbubbles created by the pump.
  • the method of the present invention can include one or more of the further steps of
  • the entire first upper phase can be cleaned further of organics by passing the first upper phase to yet a flotation tank and re-doing the cleaning process.
  • the incoming first upper phase from the first flotation tank has been separated into a second upper phase and a second lower phase. At least some of this second lower phase can be re-used as the first liquid media.
  • the method of the present inventions can re-use methane or other gases developed from digestion of biomass in the biogas plant or derived from one or both of the flotation tanks as the flotation vehicles.
  • the method can advantageously also derive and re-use/re-circulate any water that are present in any step of the method of the present to the highest possible extent as process water e.g. to adjust viscosity and density of the raw effluent entering the first flotation tank and/or as part of a liquid media.
  • process water e.g. to adjust viscosity and density of the raw effluent entering the first flotation tank and/or as part of a liquid media.
  • process water e.g. to adjust viscosity and density of the raw effluent entering the first flotation tank and/or as part of a liquid media.
  • Both the process stream of gas for creating microbubbles and the process streams of the liquid media are not flow streams that need to come from an additional source.
  • the invention further relates to an apparatus for continuously recovering at least organics from an effluent from a biogas plant, wherein the recovering apparatus comprises a first flotation tank defining a first flotation chamber, which first flotation tank has a first bottom zone opposite a first top zone, a first center zone between the first bottom zone and the first top zone, a first upper discharge conduit at the first top zone, a first inlet provided at the first bottom zone, and a first riser pipe erected in the first flotation tank,
  • the first riser pipe has a first riser pipe inlet and an opposite first riser pipe outlet, preferably the first riser pipe inlet is aligned with the first inlet,
  • a first nozzle means at the first riser pipe inlet or at the first inlet for reducing the pressure of said first mixture that rises through the first riser pipe and for releasing the microbubbles in the effluent
  • the apparatus may according to the present invention further comprise a second flotation tank that defines a second flotation chamber, and which second flotation tank has a second bottom zone opposite a second top zone, a second center zone between the second bottom zone and the second top zone, a second upper discharge conduit at the second top zone, a second inlet provided at the second bottom zone, and a second riser pipe erected in the second flotation tank, the second riser pipe has a second riser pipe inlet and an opposite second riser pipe outlet,
  • a second nozzle means at the second riser pipe inlet for reducing the pressure of said second mixture that rises through the second riser pipe and for releasing the microbubbles in the first lower phase inside the second riser pipe
  • Re-circulating of an upper phase may include re-circulating floating aggregates for further digestion in the biogas plant and re-circulating gases of flotation vehicles to the product stream of the biogas plant or to the liquid media.
  • the second flotation tank can preferably be coupled in series with the first flotation tank so that the first lower phase directly enters the second riser pipe of the second floatation tank.
  • the first flotation tank and the second flotation tank can communicate so that liquid content in a respective flotation tank continuously is balanced in response to adding matter and removing matter in any of the flotation tanks. If e.g. a fraction of the second lower phase is taken out of the second flotation tank replenishment of first lower phase from the first flotation tank will inherently take place so that a substantial constant amount of first lower phase continues to exist in the second flotation tank. In a similar manner the feed of effluent from the biogas plant can be balanced in response to the withdrawal of first lower phase from the first flotation tank into the second flotation tank. So the apparatus and continuous method of the present invention can be self- balancing.
  • the speed of the effluent to the first flotation tank, the speed of first lower phase to the second flotation tank, the speed of gaseous first and second liquid media to the respective first and second flotation tanks, the amount of recirculated upper and lower phases and fractions thereof, and the size of the fractions of the second lower phase that is not re-circulated, but goes to waste in order not to accumulate indigestible matter in the process mass, are mutually adjusted in condition of each other.
  • An air trap can be provided in the communication line between the first flotation tank and the second riser pipe in the second flotation tank to keep gases in the first flotation tank.
  • An adjustable overflow may serve as a means to control the liquid level in one or both flotation tanks .
  • the means for mixing a liquid medium with a flotation vehicle to create microbubbles in said liquid medium includes a pump means, preferably the pump means include a turbine pump, preferably the turbine pump has an inlet gauge of between -0.02MPa - 0.03MPa and an outlet gauge of between 0.4MPa - 0.6MPa.
  • the effluent 2 is partly digested biomass still having a content of dry matter, e.g. about 2.5 - 3 wt/vol%, containing organics that still have a methane potential.
  • the flow E of effluent 2 which is indicated in the figure in fat full line, go to the first flotation tank 5 that delimits a first flotation chamber 5' within a cylindrical center zone 6, a conical bottom zone 7 and an opposite conical top zone 8, above which a collection chamber 9 collect gases rising from the content in the first flotation tank 5.
  • the collection chamber 9 prevents valuable gases from escaping to the surrounding atmosphere and serves as a temporary storage chamber for the later re-circulating of the gases to other steps of the method, to the biogas product line and/or to components of the apparatus of the present invention.
  • the flow E of effluent 2 enters the first flotation tank via a first inlet 10 in a tapering of the conical bottom zone 7.
  • a first nozzle 14 is disposed at the first riser pipe inlet 12, close to said first inlet 10, preferably the first nozzle 14 is arranged inside or just inside the first riser pipe 11.
  • a flow of a first liquid media LM1 is provided with dispersed microbubbles 15 by means of turbine pump 16.
  • the first liquid medium LM1 and a flow of first flotation vehicle FV1 which is taken from the methane-containing product stream P from the biogas plant 1, is subjected to a turbulent mixing by means of the turbine pump 16, to create a high concentration of methane- containing microbubbles in the first liquid media LM1, thereby obtaining the first mixture Ml.
  • the first mixture is pumped as a first mixture Ml at a pressure of e.g. about 4 - 5 bar by the turbine pump 16 to the first nozzle 14 and into the effluent 2 in the first riser pipe 11, whereby the pressure of the first mixture Ml is reduced and the microbubbles 15 is released, preferably at reduced size, into the effluent 2 confined in the first riser pipe 11.
  • the microbubbles 15 attach to said organic matter to form aggregates that float upwards through the first riser pipe 11 and out through the first riser pipe outlet 13 to settle as a first upper phase 17 in the conical top zone 8 of the first flotation tank 5.
  • a first lower phase 18 is then created below the first upper phase 17, which first lower phase 18 has a reduced content of organics.
  • the gases of the microbubbles 15 that rises through the first riser pipe 11 is collected in the collection chamber 9 wherefrom the gases can be re-circulated to the product stream P of the biogas plant 1, as indicated by dotted line Gl .
  • the first upper phase 17 is harvested, optionally pressurized to remove water and capture any methane or other gases of the first upper phase. Captured gases can be directed to the biogas product stream P or be used in other gas demanding steps of the method.
  • the water derived from the first upper phase can be used as process water for adjusting the density of the biomass or in any water-demanding step of the method.
  • the first upper phase whether it has been further treated or not, is pumped, by means of hose pump 19 back to the biogas plant 1 for digestion, as indicated by dash-dotted line UPl.
  • the first lower phase 18 is transferred to a second riser pipe 20 erected in the second flotation tank 21, as indicated by arrow A, e.g. via a first outlet 22 of the first flotation tank 5, and into the second flotation tank 21 via a third inlet 23a.
  • first outlet 22 and the third inlet 23a are coaxial, but in other embodiments the axis of said first outlet 22 and the third inlet 23a are not aligned.
  • Pump means may be inserted for this purpose.
  • the second flotation tank 21 is an oblong tank that delimits a second flotation chamber 21' within a second center zone 24, a second top zone 25, and a second bottom zone 26.
  • the oblong design of the second flotation tank 21 provides a large surface area for accumulation of aggregates of organics of the first lower phase 18 and microbubbles 15 at the second top zone 25.
  • the second riser pipe 20 has a second riser pipe inlet 27 and an opposite second riser pipe outlet 28, and is erected in the second flotation tank 21, so that first lower phase 18 can enter the second riser pipe inlet 27 when said first lower phase 18 enters the second flotation tank 21 via its third inlet 23a close to the second riser pipe inlet 27.
  • the third inlet 23a is located in a sidewall of the second bottom zone 26.
  • the third inlet 23a can in the alternative be located next to the second inlet 23b in the bottom wall of the second flotation tank 21 and pumped from the first outlet 22 of the first flotation tank 5.
  • the third inlet 23a is the same as the second inlet 23b.
  • the first lower phase 18 can rise through the second riser pipe 20.
  • a second nozzle 29 is disposed at a the second riser pipe inlet 27, close to said riser pipe inlet 27, preferably inside the second riser pipe 20.
  • a flow of a second liquid medium LM2 is provided with dispersed microbubbles 15 of a second flotation vehicle FV2 by means of turbine pump 16.
  • the flow of second liquid medium LM2 is the same as the flow of first liquid medium LM1 and the flow of first flotation vehicle FV1 is the same as the flow of second flotation vehicle FV2.
  • the same turbine pump thus produces first and second identical mixtures M1,M2 of liquid medium LM1,LM2 and microbubbles 15 of gas, preferably of gas derived from the method itself or directly from the biogas plant 3.
  • each flotation tank 5; 21 may in the alternative be fed by individual turbine pumps and use separate flows of flotation vehicles and liquid medium.
  • the second mixture M2 is pumped at a pressure of e.g. about 4 - 5 bar by the turbine pump 16 via the second inlet 23b at the bottom of the second flotation tank 21 to the second nozzle 29 and into the first lower phase 18 in the second riser pipe 20, whereby the pressure of the first mixture M2 is reduced and the microbubbles 15 is released, preferably at reduced size, into the first lower phase 18 confined in the second riser pipe 20.
  • the microbubbles 15 attach to said organic matter to form aggregates that float upwards through the second riser pipe 20 and out through the second riser pipe outlet 28 to settle as a second upper phase 30 in the second top zone 25 of the second flotation tank 21.
  • a fraction of about 0.5% of second lower phase 31 may continuously be discharged as waste Wl and a fraction of about 15% of same lower phase be used as liquid media LM1 ; LM2.
  • the gases of the microbubbles 15 that rises through the second riser pipe 20 may be collected in the head space 33 above the second upper phase 30 wherefrom the gases can be re-circulated to the product stream P of the biogas plant 1, as indicated by dotted line G2.
  • the second upper phase 30 is harvested, optionally pressurized to remove water and capture any methane or other gases of the second upper phase 30. Captured gases can be directed to the biogas product stream P or be used in other gas demanding steps of the method.
  • the water derived from the second upper phase 30 can e.g. be used as process water for adjusting the density of the biomass in the biogas plant 1, or of the effluent 2, or be used in any other water-demanding step of the method.
  • the second upper phase 30, whether it has been further treated or not, is pumped, by means of the same hose pump 19 used for pumping the first upper phase 17, or by means of another pump, back to the biogas plant 1 for digestion, as indicated by dash-dotted line UP2.
  • the first nozzle 14 and the second nozzle 29 may be of the same kind, preferably being self-cleaning, as described above.
  • the first nozzle 14 is subjected to compressed gas, as indicated by arrow CI, through a first valve 34 to counteract the static pressure in the first flotation tank and aid in releasing the microbubbles 15 of the first mixture Ml into the effluent 2 in the first riser pipe 11 by controlling the opening and closing of the orifices (not shown) of the first nozzle 14, whereby also the size of the microbubbles is reduced.
  • the second nozzle 29 is subjected to compressed gas, as indicated by arrow C2, through a second valve 35 to counteract the static pressure in the second flotation tank 21 and aid in releasing the microbubbles 15 of the second mixture M2 into the first lower phase 18 in the second riser pipe 11 by controlling the opening and closing of the orifices (not shown) of the second nozzle 29, whereby also the size of the microbubbles is reduced.
  • the digestion of biomass involves a lot of water and use of make-up water.
  • the majority of process water and make-up water are the same water as the effluent from the biogas plant brought along, and which is used again in the method of the present invention as dispersion water, thus as liquid media, which is water captured and re-circulated again and again until concentrations of particulates and of non -digestible matter in the second lower phase 31 reaches an upper limit beyond which the method is no longer favorable.
  • the first flotation tank 5 can be emptied completely or partly, or a first sediment phase (not shown) at the first bottom zone 7 be discharged via discharge line W2 at said first bottom zone via discharge valve 37.
  • a similar process can take place via discharge line W3 from the second flotation tank 21 through second discharge valve 38.
  • the discharge valves 37,38 are ball valves.
  • An exemplary first flotation tank may e.g. have a total height of 3.2 m, a diameter at the center diameter of 1.2 m, and a total volume of 2.5 m 3 .
  • the first riser pipe may e.g. have a total height of 1300 mm and a diameter of 315 mm.
  • the second flotation tank may e.g. have a total height of 1.8 m and a total volume of 4.9 m 3 .
  • the second riser pipe may be similar to the first riser pipe.
  • Such an apparatus can process an effluent flow of 5.5 m 3 /h.
  • the flotation vehicles are expediently gases from the biogas plant or from the apparatus developed during its operation, so separate sources of gas for formation of microbubbles in the liquid media are not needed. Accordingly, the present invention optimizes the yield of biogas from the biogas plant at minimum costs using an apparatus and method based on recovery and recirculation of products in form of water and gases for use in process streams of the apparatus and method itself.
  • This novel method and apparatus to recover, re-circulate and otherwise treat the organics in the effluent from a biogas plant is a fast and efficient way to optimize the yield of a biogas plant.
  • the method and apparatus are economical attractive, pollute the environment at a minimum, do not negatively influence the digestion process and utilize the caloric content and methane potential of a biomass at its optimum.
  • a further advantage is that the method and apparatus are easily and inexpensively implemented at existing biogas plants.
  • the apparatus can be a mobile unit that can be used at different biogas plants upon demand. Such a unit can be rented or leased, or be shared by several owners so, that e.g. a farmer not need to invest a substantial amount in such processing equipment.
  • Gases of the microbubbles taking part in the flotation reaction in any of the flotation tanks can be collected and be recirculated to the biogas plant, e.g. added to the biogas product stream of the biogas plant, wherefrom the gas(es) used as the flotation vehicles to create microbubbles in the liquid media also can be taken initially.
  • the collected gases can also be re-used in the method of the present invention.
  • a further huge advantage is that the slow growing methanogens that are attached to the organic fraction of the effluent can be re-circulated. Due to the anaerobic conditions in the flotation tank the methanogens are immediate ready for further methane production when re-circulated as included in the upper phase to the reactor of the biogas plant.
  • the biogas plant in itself is not part of the apparatus of the present invention.
  • the apparatus can be provided as a rather compact unit that can be connected to the waste and products streams of the biogas plant in a very easy and simple manner.
  • first aggregation process in the first flotation tank aggregates of organics in the effluent and microbubbles of gas from the product stream from the biogas plant float into the upper zone and are transported back for further digestion in the biogas plant thereby boosting biogas formation.
  • the effluent is thus cleaned of some further organics but may still have a content of organics worth recovering. This takes place in a similar manner in a second flotation tank in fluid connection with the first flotation tank.
  • Process gas is the gas already present in the digester of the biogas plant and dispersion water for microbubbles is water re-circulated from a second lower phase of the second flotation tank formed in the second flotation tank in response to a second formation of floating aggregates in a second aggregation process.
  • dispersion water for microbubbles is water re-circulated from a second lower phase of the second flotation tank formed in the second flotation tank in response to a second formation of floating aggregates in a second aggregation process.

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Abstract

Un appareil est utilisé dans une méthode qui comprend les étapes consistant à utiliser un premier réservoir de flottation (5) avec une première colonne montante (11) érigée dans une première chambre de flottation, à fournir un flux continu (E) d'effluent (2) vers le premier réservoir de flottation (5) par l'intermédiaire de la première entrée (10), à fournir un premier mélange (Ml) d'un premier milieu liquide (LM1) avec des microbulles (15) d'un premier véhicule de flottation (FV1) sous la forme d'un premier gaz inerte, anoxique ou pauvre en oxygène et à pomper le premier mélange (Ml) vers le premier réservoir de flottation (5), et permettre aux microbulles de se fixer à des matières organiques à l'intérieur de la première colonne montante pour former des agrégats qui peuvent flotter et se déposer au niveau de la zone supérieure du premier réservoir de flottation et peuvent être encore digérés dans le digesteur de l'installation de biogaz. Un autre traitement et raffinage d'une phase inférieure peuvent avoir lieu dans un second réservoir de flottation d'une manière similaire. Le gaz de traitement est le gaz déjà présent dans le digesteur et l'eau de dispersion pour les microbulles est recirculée dans l'eau à partir d'une seconde phase inférieure formée dans le second réservoir de flottation en réponse à une seconde formation d'agrégats flottants.
PCT/DK2018/050116 2017-05-23 2018-05-23 Méthode et appareil de récupération de matières organiques solides à partir d'un flux d'un effluent de biomasse partiellement digérée WO2018215040A1 (fr)

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DKPA201970806A DK201970806A1 (en) 2017-05-23 2018-05-23 A method and an apparatus for recovering a solid organics from a flow of an effluent of partly digested biomass
EP18728029.2A EP3630938A1 (fr) 2017-05-23 2018-05-23 Méthode et appareil de récupération de matières organiques solides à partir d'un flux d'un effluent de biomasse partiellement digérée

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DKPA201770365A DK180237B1 (en) 2017-05-23 2017-05-23 A method and an apparatus for recovering at solid organics from a flow of an effluent of partly digested biomass.

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020127918A1 (fr) * 2018-12-21 2020-06-25 Paques I.P. B.V. Procédé et dispositif de purification anaérobie
EP3962264A4 (fr) * 2019-04-29 2023-10-25 Searas AS Installation pour écumage multiple

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4948509A (en) * 1988-08-24 1990-08-14 Charles Stack & Associates, Inc. Anaerobic fermentation process
US5080802A (en) * 1990-05-09 1992-01-14 Cairo Jr John A Induced gas liquid coalescer and flotation separator
WO1992020628A1 (fr) * 1988-05-25 1992-11-26 Burke Dennis A Processus de digestion anaerobie
DE102005059723A1 (de) * 2005-12-14 2007-06-21 Fan Separator Gmbh Biogasanlagen

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1992020628A1 (fr) * 1988-05-25 1992-11-26 Burke Dennis A Processus de digestion anaerobie
US4948509A (en) * 1988-08-24 1990-08-14 Charles Stack & Associates, Inc. Anaerobic fermentation process
US5080802A (en) * 1990-05-09 1992-01-14 Cairo Jr John A Induced gas liquid coalescer and flotation separator
DE102005059723A1 (de) * 2005-12-14 2007-06-21 Fan Separator Gmbh Biogasanlagen

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020127918A1 (fr) * 2018-12-21 2020-06-25 Paques I.P. B.V. Procédé et dispositif de purification anaérobie
CN113226997A (zh) * 2018-12-21 2021-08-06 巴格知识产权有限公司 用于厌氧净化的方法和装置
US11878924B2 (en) 2018-12-21 2024-01-23 Paques I.P.B.V. Process and device for anaerobic purification
CN113226997B (zh) * 2018-12-21 2024-04-12 巴格知识产权有限公司 用于厌氧净化的方法和装置
EP3962264A4 (fr) * 2019-04-29 2023-10-25 Searas AS Installation pour écumage multiple

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DK201770365A1 (en) 2018-12-13

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