US20020192809A1 - Anaerobic digestion apparatus methods for anaerobic digestion and for minimizing the use of inhibitory polymers in digestion - Google Patents

Anaerobic digestion apparatus methods for anaerobic digestion and for minimizing the use of inhibitory polymers in digestion Download PDF

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US20020192809A1
US20020192809A1 US10/161,387 US16138702A US2002192809A1 US 20020192809 A1 US20020192809 A1 US 20020192809A1 US 16138702 A US16138702 A US 16138702A US 2002192809 A1 US2002192809 A1 US 2002192809A1
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digester
mixed liquor
nozzle
anaerobic
digestion apparatus
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Jelte Lanting
John Murphy
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Biothane Corp
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Biothane Corp
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Publication of US20020192809A1 publication Critical patent/US20020192809A1/en
Priority to US12/228,136 priority patent/US7708885B2/en
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/282—Anaerobic digestion processes using anaerobic sequencing batch reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C02F3/2873—Particular arrangements for anaerobic reactors with internal draft tube circulation
    • 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
    • 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
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • 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
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/18—Flow directing inserts
    • C12M27/20—Baffles; Ribs; Ribbons; Auger vanes
    • 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
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/18—Flow directing inserts
    • C12M27/24—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
    • 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
    • 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
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/10—Temperature conditions for biological treatment
    • C02F2301/106—Thermophilic treatment
    • 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
    • Y02W10/10—Biological treatment of water, waste water, or sewage
    • 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 invention relates to anaerobic biological treatment of waste streams with high solids content.
  • Anaerobic biological treatment has traditionally been applied to the digestion of primary and secondary sludge at municipal sewage treatment facilities, but is also applicable to municipal solid waste, agricultural manures and crop residues, or industrial solid wastes and slurries where a significant portion of the solids material is potentially biodegradable.
  • Additives such as polymers
  • additives have been mixed with the sludge stream to enhance the thickening process.
  • These polymers are known in the art and include, for example, cationic polyacrylamides in a water-in-oil emulsion, solution mannich polymers—nonionic polyacrylamide polymers made cationic by reacting the amide groups along the polyacrylamide backbone with both a dialkylamine and a formaldehyde source, and cationic water-soluble polymers in emulsions, for example polyamine or poly (diallyldialkylammonium halides).
  • cationic polyacrylamides in a water-in-oil emulsion
  • solution mannich polymers nonionic polyacrylamide polymers made cationic by reacting the amide groups along the polyacrylamide backbone with both a dialkylamine and a formaldehyde source
  • cationic water-soluble polymers in emulsions, for example polyamine or poly (diallyl
  • Digesters for the anaerobic digestion of municipal publicly-owned treatment works (POTW) sludge are generally large tanks of relatively low height providing for 20-40 days of HRT. Proper treatment of municipal POTW sludge requires a sufficient inventory of active digesting bacteria and contact of those bacteria with the biodegradable fraction of the sludge. Contact is achieved by mixing digester contents. Optimally, the digester contents are mixed thoroughly. Conventional mixing methods include mixing by mechanical methods and mixing by using gas. However, the large and low design of conventional digesters typically results in “dead zones” which are not mixed and which could reach or exceed approximately 15% of the digester.
  • Loop digesters have a continuous circulating flow which may be around a draft tube configuration.
  • a mixing method used in the field of aerobic digestion is the concept of an eductor nozzle immersed in a liquid filled vessel. The pressure on the pumped side of the nozzle can be used to accelerate the flow of liquid at the nozzle outlet thus releasing energy into the liquid filled vessel and disturbing the vessel contents to effect mixing. Additionally, this acceleration creates a suction effect (similar to a Venturi) which can be used to draw a secondary fluid or gas into the flow stream.
  • Eductor nozzles to fragment biological solids have been used in the treatment of wastewaters using high rate aerobic digesters that apply a shearing force to the mixed liquor in the digester. With the supplemental addition of oxygen in the form of air injection, these digesters rely on contact between wastewater and biomass particles in an oxygen-rich environment to promote aerobic bacterial digestion of soluble components contained in the wastewater.
  • the invention includes an anaerobic solids digestion apparatus comprising a digester; a mixing device in the digester capable of directing a flow of a mixed liquor within the digester; and a shearing device in communication with a mixed liquor inlet to the digester, the shearing device being capable of imparting shear to a mixed liquor within the digester.
  • the invention also includes an anaerobic solids digestion apparatus comprising a digester comprising a shear source capable of imparting shear to a mixed liquor within the digester and a concentrator in fluid communication with a mixed liquor inlet of the digester and at least one mixed liquor outlet of the digester, wherein the concentrator and digester are configured to allow for concurrent concentration and digestion of a mixed liquor.
  • the invention also includes an anaerobic solids digestion apparatus comprising a digester; at least one draft tube positioned in the digester and capable of directing a flow of a mixed liquor and comprising an upper inlet and a lower outlet; at least one nozzle comprising a gas inlet, a liquid inlet, an outlet and an interior surface, the nozzle further comprising a gas tube having an exterior surface, the tube extending from the nozzle gas inlet to the nozzle outlet, wherein a generally annular space is defined between the exterior surface of the gas tube and the interior surface of the nozzle; and a biogas source in communication with the gas inlet of the nozzle.
  • the invention additionally includes a method for digesting a waste stream in an anaerobic solids digestion apparatus, the method comprising feeding a waste stream comprising anaerobically biodegradable solids to a digester; reacting the anaerobically biodegradable solids in the waste stream with anaerobic bacteria in the digester to reduce an amount of the biodegradable solids, thereby producing a mixed liquor and a biogas; introducing a mixed liquor to the digester through a shearing device; and mixing the mixed liquor within the digester.
  • the invention includes a method for improving the efficiency of an anaerobic solids digestion apparatus comprising feeding a waste stream comprising anaerobically biodegradable solids to a digester; reacting the anaerobically biodegradable solids in the waste stream with anaerobic bacteria in the digester to reduce an amount of the biodegradable solids, thereby producing a mixed liquor and a biogas; imparting a shearing force to the mixed liquor in the digester; and concentrating the mixed liquor, wherein the steps of reacting the anaerobically biodegradable solids and concentrating the mixed liquor occur concurrently.
  • the invention additionally includes a method for minimizing the need for use of a polymer that inhibits biological activity in a waste stream in a digestion apparatus, the method comprising feeding a waste stream to a digester, wherein a portion of the waste stream is biodegradable; reacting the biodegradable portion in the waste stream with bacteria in the digester to produce a mixed liquor and gas; and concentrating the mixed liquor with a membrane separator, wherein the steps of reacting the biodegradable portion in the waste stream and concentrating the mixed liquor occur concurrently.
  • FIG. 1 is a schematic representation of the features of a shear enhanced anaerobic digestion apparatus according to the invention
  • FIG. 2 is a schematic representation of a two-phase mixing and shearing nozzle.
  • FIG. 2 a is a schematic representation of a single phase mixing and shearing nozzle.
  • FIG. 3 is a schematic representation of a conventional sludge treatment process
  • FIG. 4 is a schematic representation of a sludge treatment process according to an embodiment of the invention which includes a membrane concentrator;
  • FIG. 5 is a schematic representation of an anaerobic digestion apparatus and a membrane concentrator
  • FIG. 6 is a schematic representation of an alternative anaerobic digestion apparatus and a concentrator.
  • the present invention relates to an apparatus, designated generally in the drawings as 100 , and process for the anaerobic digestion of solids in a waste stream using a shear enhanced anaerobic digestion apparatus (SEAD).
  • SEAD shear enhanced anaerobic digestion apparatus
  • the invention also relates to an apparatus and method for concurrently concentrating and digesting the degradable solids fraction of a waste stream.
  • the invention additionally relates to a method of minimizing the need for use of a polymer(s) that can inhibit biological activity in a waste stream.
  • a shearing nozzle may be used in the apparatus to impart energy to the digester contents so as to fracture solids particles and expose the maximum reactable surface area.
  • Entrained biogas is dispersed throughout the circulating mixed liquor providing for maximum turbulence in the mixed liquor to ensure optimal contact of the biodegradable organics with the anaerobic bacteria.
  • a fraction of the digester contents can be concentrated by using membrane separation or other conventional concentration process in combination, and preferably concurrently, with the digestion apparatus.
  • a concentrator is in fluid communication with an inlet and an outlet of the digester, so that the concentrator and digester may operate concurrently.
  • digestion acts on the degradable waste material in the digester, the hydrophilic components are being digested, and the digester contents are more easily concentrated.
  • the apparatus can work alongside a concentrator, they can be operated concurrently and the thickening of the waste is significantly improved.
  • the design of the apparatus including a concentrator as described herein enhances separation performance over conventional concentration processes with the result that the feed stock to the digester is effectively concentrated.
  • the performance of the digester is enhanced because the concentration can be performed without the need for the use of polymers that can inhibit biological activity or other additives that can negatively impact an optimized digester such as the digester described herein.
  • Applicants have additionally discovered that concurrently concentrating while digesting the feed stock for other types of digesters, including, for example, non-shear enhanced anaerobic digesters, egg-shaped anaerobic digesters, and aerobic digesters, can also minimize the need for additives, such as thickening polymers that may act to inhibit biological activity in those digesters when optimized.
  • waste streams to be treated according to the various embodiments and aspects of the present invention may be any waste streams containing material that is at least partially biodegradable by anaerobic or aerobic bacteria.
  • the principle aspects of the invention are directed to anaerobic bacteria unless otherwise specified herein.
  • waste streams are primary and/or waste-activated sludge from municipal sewage treatment plants or industrial aerobic wastewater treatment plants, but may also include wastewater streams from solid waste agricultural manures, crop residues, industrial solid wastes, sludge, and slurries or any other high solids waste streams where a significant portion of the solids material is potentially biodegradable.
  • the present invention can process streams with high concentrations of total suspended solids (TSS) and/or fat, oil and grease (FOG), as well as the slurries or solid waste having anaerobically digestible material.
  • TSS total suspended solids
  • FOG fat, oil and grease
  • the waste stream is preferably a waste slurry. More preferably, the waste slurry is a mixture of primary and secondary sludge in a ratio of about 70:30 to about 30:70, most preferably about 60:40 to 40:60.
  • a total solids concentration of about 2 to about 20 wt % is preferred for embodiments of the digester of the invention without the concentrator based on the weight of solids divided by the weight of the sample.
  • the total solids concentration is preferably about 1 to about 10 wt %, more preferably about 1 to about 5%.
  • waste sludge will also preferably have an inlet chemical oxygen demand (COD) level of at least 20,000 mg/l for the embodiments of the digester of the invention without the concentrator and at least 5,000 mg/l, more preferably at least 10,000 mg/l, for embodiments of the invention with concentrator.
  • COD levels are preferred. It will be understood, however, based on the disclosure that the anaerobically digestible stream processed by the invention can have varied characteristics.
  • FIGS. 1 - 6 are representative and not drawn to scale. Certain terminology is used in the following description for convenience only and is not considered to be limiting.
  • the words “lower” and “upper”, “top” and “bottom”, “upward” and “downward” and “left” and “right” designate directions in the drawings to which reference is made.
  • the terminology includes the words specifically mentioned, derivatives thereof and words of similar import.
  • a waste stream can be introduced into a digester 30 , as shown in FIG. 1, through one or more inlets 2 located around the periphery of the digester vessel or through the digester recirculation conduit 60 , 64 as described herein.
  • the digester 30 also preferably includes one or more mixed liquor outlets 50 around the periphery of the digester vessel, one of which may serve as a main outlet for discharging digester effluent or the digested liquor or sludge for disposal or further processing.
  • the digester may also include one or more sample ports 44 around the periphery of the digester.
  • the digester 30 additionally may include one or more drains 40 for emptying the vessel when not in use.
  • mixed liquor in this specification includes, but is not limited to a mixed liquor, a mixture of solids, liquids and gas and the biodegradable portion therein and bacteria therein, which in the preferred embodiment are anaerobic bacteria.
  • the mixed liquor may be within the digester, fed into the digester as a recycle stream from the digester and any effluent from the digester.
  • the digester volume is selected such that the sludge retention time SRT within the digester is about 2 to about 20 days, preferably about 6 to about 12 days.
  • the configuration of the digester may vary, however, preferably it is a generally cylindrical vessel with a height as measured along the longitudinal axis A of the digester of preferably about 25 feet (8 m) to about 75 feet (23 m), and more preferably about 45 feet (14 m) to about 55 feet (17 m), with a height to diameter ratio of about 0.2 to about 20, and more preferably about 1 to about 4, wherein the diameter is measured in a transverse direction along the largest transverse dimension of the digester.
  • the digester can be constructed of any conventional material that is consistent with the materials handling and structural requirements of the particular materials to be digested and digester design chosen. However, it is preferable that the digester is constructed of concrete, steel or fiberglass.
  • the waste stream is preferably fed to the digester upstream of a recirculation pump 6 .
  • the digester inlet 2 is preferably upstream of the digester recirculation pump 6 so that the feed immediately and intensely contacts with the digesting bacteria existing in the preferred recirculated stream flowing through conduit 60 and is mixed proportionately with that stream.
  • the waste stream is fed continuously to the digester 30 , although a batch feeding operation may also be utilized.
  • the rate of feed of waste stream into the digester may vary, but the maximum feed rate can generally be determined by dividing the volume of the digester employed by the design hydraulic retention time (HRT).
  • the digester is operated at a controlled mixed liquor volume, which is a substantially constant volume, subject to typical control fluctuations.
  • a controlled mixed liquor volume which is a substantially constant volume, subject to typical control fluctuations.
  • an amount of mixed liquor substantially equal to the flow rate of the waste stream feed is extracted from the digester 30 via a mixed liquor outlet 50 , preferably one located to extend generally transversely from a side 32 of the digester vessel.
  • a control valve 4 such as a gravity overflow or control valve, or any other appropriate flow control mechanism can be used to control the mixed liquor discharge so as to maintain the liquid volume in the digester at a substantially constant volume.
  • the apparatus further includes a recirculation system 46 , including the recirculation pump 6 and recirculation conduit 60 , 64 .
  • the recirculation system provides fluid communication for the mixed liquor L within the digester 30 from a mixed liquor outlet 50 , which in this instance serves as a mixed liquor recirculation outlet, preferably in the bottom 52 of the digester vessel, to a liquid inlet 65 of at least one preferred two-phase nozzle 18 as best shown in FIG. 2.
  • the rate of recirculation through the recirculation system is controlled to be substantially constant such that the digester volume divided by the digester volume recirculation rate is about 15 to about 150 minutes, and more preferably about 45 to about 75 minutes. Similar digester recirculation rates would be preferred in the processing of other waste slurries such as agricultural or industrial slurries. However, recirculation rates can be altered or optimized for varying systems.
  • a first conduit 60 conveys liquid from pump 6 , which may be a pump or any liquid pumping apparatus that moves the liquid through the conduit 60 , 64 , to the liquid inlet 65 of the nozzle 18 .
  • a second conduit 64 conveys liquid from the mixed liquor outlet 50 that serves as the mixed liquor recirculation outlet to the pump 6 . It is understood that the term “conduit”, as described in this specification, may be any pipe, conduit, tube, conveyance mechanism, valve, or indirect or direct connection or the like which provides fluid communication as described herein.
  • the recirculation system 46 provides a continuous blend of waste stream feed and recirculated mixed liquor from the digester to the liquid inlet 65 of the preferred two-phase nozzle 18 which would then discharge fresh waste stream and recirculated mixed liquor and biogas from a biogas source into the digester 30 .
  • the nozzle 18 includes a nozzle gas inlet 13 in fluid communication with a biogas source, a nozzle liquid inlet 65 and a nozzle outlet 20 .
  • the nozzle further has a gas flow tube 15 extending from the nozzle gas inlet 13 to the gas tube outlet 33 in proximity to the nozzle outlet 20 .
  • a nozzle space 56 which is generally annular is defined by the exterior surface 35 of the gas flow tube 15 and the interior surface 54 of the nozzle 18 , through which recirculated mixed liquor is passed.
  • the pump 6 circulates the recirculation stream and/or feed stream and pressurizes the slurry upstream of the preferred two-phase nozzle 18 .
  • the pump energy is transferred to the digester contents at the fluid outlet 20 of the preferred two-phase nozzle 18 .
  • the fluid outlet 20 of the preferred two-phase nozzle 18 is configured such that the nozzle annular space 56 narrows at the nozzle outlet causing an acceleration of the mixed liquor at the outlet.
  • the velocity gradient generated via the nozzle outlet 20 is preferably maintained at a level of about 50 to about 500 sec ⁇ 1 , as defined by formula (I)
  • G is the mean velocity gradient
  • sec ⁇ 1 P is the power requirement in Watts
  • V is the digester volume in cubic meters
  • ⁇ is the dynamic viscosity of the digester contents in Ns/m 2 .
  • the energy transferred to the mixed liquor at nozzle outlet 20 imparts a shearing force on the solids in the stream which breaks the solids into smaller particles and increases the surface area.
  • the increase in surface area exposes more unreacted organics making them accessible to the anaerobic bacteria.
  • the shearing occurs both inside the nozzle 18 as the fluid is accelerated and in the mixing zone 66 outside the nozzle outlet 20 where the energy of the mixed liquor is transferred to the digester contents.
  • the nozzle is a two-phase nozzle which can provide a shearing force as well as educting a gas.
  • a single phase nozzle 72 as shown in FIG. 2 a , would also be suitable for the providing shear to the mixed liquor in the digester.
  • the nozzle in FIG. 2 a includes a liquid inlet 73 having a diameter d 2 , which would be in fluid communication with a mixed liquor outlet 50 of the digester 30 shown in FIG.
  • the narrower outlet 74 causes acceleration of the mixed liquor at the outlet 74 .
  • Recirculated liquor passes through an interior space 75 of the nozzle 72 defined by interior walls 76 of the nozzle 72 .
  • the single-phase nozzle 72 does not include a gas tube.
  • nozzles of the present invention may also be used within the scope of the invention.
  • shearing devices for example a Venturi valve or nozzle, or an impeller, capable of fracturing the solids and introducing them into the digester while not as preferred as the nozzles of the present invention may also be used within the scope of the invention.
  • the number of nozzles used can vary depending upon the volume of the digester and/or the desired optimized process. For example, two nozzles are shown in the preferred embodiment of FIG. 5. Preferably, about one nozzle to about 150 to about 1,500 cubic meters of digester volume is preferred, and more preferably about one nozzle to about 600 to about 900 cubic meters of digester volume.
  • a “mixing device” which is preferably a draft tube but may be any mixing device including impellers, injected gas, vacuum pumping, mixing blades and the like capable of inducing mixing within the digester are within the scope of the invention. It will be recognized by one skilled in the art that other forms of mixing such as mechanical mixers or gas injection or other mixing methods in the presence of a shear enhanced medium would contribute to an improvement in mass transfer rates and, accordingly, be suitable for use in the invention.
  • the nozzle outlet 20 discharges proximate to the inlet 22 of a draft tube 28 positioned below the level 48 of the mixed liquor in the digester. The fluid exiting the nozzle flows downwardly through the inner area 26 defined by the draft tube 28 .
  • the diameter d 1 of the draft tube 28 as measured transversely through the tube is preferably constant and is preferably about 40 to 200 centimeters.
  • the length l 1 of the draft tube 28 as measured along a longitudinal axis B of the draft tube should be such that the draft tube inlet 22 is sufficiently far below the surface of the liquid level to allow circulation of the contents of the digester into the draft tube inlet 22 , as shown in FIG. 1, and the draft tube outlet 43 is sufficiently far above the bottom of the digester to minimize flow restriction or excessive pressure drop.
  • the length 11 of the draft tube 28 ranges from about 50% to about 90% of the digester liquid depth Q as measured longitudinally from the bottom 52 of the digester to the surface 48 of the mixed liquor, with the depth of the liquid above the draft tube inlet being no greater than the liquid depth below the draft tube outlet 43 . It is understood that more than one draft tube may be employed according to the considerations discussed above with respect to the number of nozzles employed. A 1:1 relationship between the number of nozzles employed and the number of draft tubes employed is preferred. However, there may be more than one nozzle per draft tube in the anaerobic digestion apparatus according to the invention.
  • the continuing downward flow of the nozzle effluent into the draft tube 28 induces a generally downward flow inside the draft tube.
  • a circulation pattern is developed within the digester 30 in which liquid flows back up around the exterior surface 24 of the draft tube 28 and then is pulled and/or pushed downwardly again into the draft tube 28 through the upper inlet 22 .
  • This induced circulation pattern around the draft tube preferably exceeds the volumetric flow rate discharged from the nozzle and is beneficial to the mixing of the mixed liquor, and more preferably the enhanced circulation is about 5 to about 25 times the discharge volumetric flow rate of the nozzle.
  • the enhanced mixing provided by the preferred circulation around the draft tube contributes to an increased mass transfer rate.
  • the degree of anaerobic digestion of a particular biodegradable solid substrate is limited by the organic makeup of that substrate. However the rate at which this digestion can be achieved is affected by the mass transfer rate. By improving the mass transfer rate, a reduction in the time for achieving digestion can be effected.
  • the induced circulation of the mixed liquor within the digester 30 provides enhanced mixing of the digester contents thoroughly dispersing the feed material and exposing the unreacted organics to the digesting bacteria. Because the shearing effect of the nozzle 18 has increased the exposed surface area of the unreacted organics, the mass transfer rates of the anaerobic digestion process are improved over conventional anaerobic digesters. Under the influence of the energy imparted to the digester by the discharge from nozzle 18 , these conditions increase the mass transfer rate.
  • the anaerobically biodegradable material contained in the waste stream is digested through reactions in the digester 30 , where anaerobic bacteria convert the biodegradable material to a biogas which substantially is made up of methane and carbon dioxide, with lesser amounts of other gases, such as hydrogen sulfide. These gaseous components and other similar anaerobic gas byproducts are generally referred to herein as “biogas”.
  • biogas may also contain small amounts of water vapor, nitrogen and traces of other volatile compounds which may be present in the feed or formed during biodegradation.
  • the composition of the biogas by volume percent will vary depending on the particular digestible organics being processed.
  • Preferred methane levels in biogas formed in the digester of the invention are in the range of about 50 to about 90 volume percent.
  • Preferred carbon dioxide levels are in the range of about 5 to about 45 volume percent and hydrogen sulfide levels can range from about 200 parts per million (volume) to about 6 volume percent.
  • Action of the anaerobic bacteria on the digestible organics also results in multiplication of the anaerobic bacteria.
  • This apparatus preferably has a biogas source in fluid communication with the nozzle 18 to provide biogas to the nozzle 18 .
  • a preferred biogas source is a biogas recycle system generally designated 27 which uses a portion of the gas generated in digestion as gas feed to the nozzle.
  • biogas or other anaerobic digestion feed gas can be introduced independently through inlet 37 and/or used together with a biogas recycle system as shown in FIG. 1.
  • the level 48 of the mixed liquor is such that there is an area 3 above the liquor to allow for collection of the biogas that de-entrains from the mixed liquor at its upper surface 48 .
  • the volume of the area 3 above the mixed liquor may vary, but there is preferably a distance of about 4 feet (1 m) to about 7 feet (2.5 m), more preferably about 5 feet (1.5 m) to about 6 feet (2 m), of space between the upper surface 48 of the mixed liquor and the upper surface 34 of the digester 30 to prevent any foam that is generated from impeding circulation or gas collection.
  • This biogas collection area 3 is preferably in fluid communication with nozzle 18 in a biogas recycle system.
  • the biogas recycle system is provided for recycling a portion of the biogas from the collection area 3 to the nozzle 18 .
  • this biogas recycle system 27 comprises a conduit 5 .
  • the conduit provides an outlet at one end 7 for biogas in the collection area 3 .
  • the other end 11 of the conduit is in communication with the gas inlet to the nozzle.
  • the conduit preferably has a control valve 4 for adjusting the rate of flow of the biogas in the conduit 5 .
  • Biogas is also preferably vented from the collection area, for example via a defoaming hood 17 through biogas outlet 29 , with such venting preferably being controlled, for example by a further valve 67 , to maintain a gas pressure in the area 3 of about atmospheric pressure to about 50 inches water at 35° C. (12,400 Pa). More preferably, the pressure range will be about 10 inches water at 35° C. (2,500 Pa) to about 20 inches water at 35° C. (5,000 Pa). Any biogas not recycled through the biogas recycle system 27 may be discharged and may subsequently be burned as fuel or utilized for other purposes.
  • additional gases may be introduced to the nozzle 18 through inlet 37 .
  • nitrogen feed gas may be routed to the nozzle 18 , either for control of strippable toxins, or for altering the carbon dioxide equilibrium between the biogas and the mixed liquor, thereby affecting the pH of the mixed liquor in the digester.
  • small amounts of air or oxygen may be routed to the nozzle 18 through inlet 37 or a separate gas inlet (not shown) to modulate the oxidation-reduction potential (ORP) of the mixed liquor. This is desirable since the tendency of undesirable anaerobic bacterial reactions to produce hydrogen sulfide is favored by particular ranges of oxidation-reduction potential.
  • Hydrogen sulfide is malodorous, corrosive to certain materials, and toxic to humans and the digesting bacteria.
  • the level of hydrogen sulfide present in the mixed liquor may be reduced, thereby mitigating one of the less desirable features associated with anaerobic digestion.
  • This may be facilitated by an ORP meter or gauge 14 coupled to the SEAD system 100 , preferably somewhere along the recirculation system 46 , most preferably along the conduit 60 .
  • This ORP meter or gauge 14 may signal a motorized control valve such as valve 16 to adjust the flow of gas from inlet 37 .
  • the mixed liquor is accelerated as it exits the nozzle 18 , which is in close proximity to the outlet 33 of the gas flow tube 15 .
  • As the mixed liquor and the biogas exit the nozzle 18 further mixing occurs between the portion of biogas and the recirculating mixed liquor at the nozzle outlet 20 and the outlet 33 of the gas flow tube with the gas creating increased turbulence at the nozzle discharge.
  • This turbulence exerts an additional shearing force on the solid particles in the mixed liquor, further fracturing particles and thereby providing additional surface area of degradable organics.
  • This additional shearing mechanism further enhances the performance of the invention by providing for increased mass transfer rates as described above when more of the degradable organics are exposed.
  • the entrained gas promotes a high degree of turbulence on the sheared particles in the mixed liquor.
  • this entrained gas turbulence further promotes an increase in the mass transfer rate that is beneficial to the optimum performance of the invention.
  • the eduction effect of the nozzle draws biogas into the mixed liquor from a biogas source, preferably the biogas recycle system 27 . It is preferred to control the amount of biogas recycled into the mixed liquor, for example by control valve 4 on conduit 5 .
  • the volume ratio of biogas to liquid in the nozzle will be up to about 0.5 of the volume of biogas per volume of liquid that flows through the nozzle.
  • the characteristics of each mixed liquor will vary for many reasons including the characteristics of the feed waste stream and it is further recognized that these characteristics will impact the rate at which entrained gas generated within or injected into the mixed liquor is released.
  • the biogas recycle may be shut off by closing control valve 4 .
  • the concentration of solids in the waste stream feed is expressed in percent total suspended solids (TSS).
  • TSS percent total suspended solids
  • the TSS of the feed before thickening is typically less than 1.0% TSS.
  • this sludge is thickened to about 5% TSS by utilizing polymers in the thickening process.
  • performance of an optimized digester such as the apparatus of the invention, can be negatively impacted by the presence of such thickening polymers in the waste stream. Digesting the unthickened waste stream would effect this, but the digester volume would become proportionally larger which is not desirable. Thus a method to thicken the waste feed without the need for polymer addition is desired.
  • concentration or thickening of the feed into the digester occurs upstream of the digester.
  • conventional methods typically do not digest the hydrophilic compounds in the waste stream.
  • the hydrophilic compounds typically present in the solids in the waste stream make it difficult to thicken.
  • the performance of any concentration system, and in particular a membrane concentrator can be improved if the hydrophilic compounds can be removed from the medium as these compounds reduce the tendency of the medium to release water.
  • the digester apparatus of the present invention will digest these hydrophilic compounds and, when operated concurrently with the concentrator, enhances the performance of the concentrator by removing these hydrophilic compounds that make it difficult for the concentrator to thicken.
  • a concentrator 62 conveys a portion of the mixture of solids and liquid from a mixed liquor outlet 50 of the digester, preferably the mixed liquor recirculation outlet, to the concentrator and back to an inlet 77 of the digester.
  • the concentrator 62 is in fluid communication with an inlet 77 and with a mixed liquor outlet 50 of the digester.
  • the concentrator comprises a pump 70 , which may be the pump 6 of the recirculation system, but is preferably one or more separate pumps, and a separator 58 having an outlet 53 which is in fluid communication with an inlet 77 of the digester and an inlet 68 in communication with a mixed liquor outlet 50 of the digester.
  • the concentrator also preferably includes a conduit 55 with a first end 57 connected to the outlet 53 of the separator 58 , and a second end 59 connected to the inlet 77 of the digester. This conduit preferably conveys the concentrate from a concentrate side 69 of the separator 58 back to the digester 30 .
  • the separator is a water-permeable membrane including and preferably manufactured of a material suitable for processing a liquid with various concentrations of suspended solids and suspended solid particles of varying sizes.
  • a suitable membrane is an ultra-porous, asymmetric, polymeric ultra-filtration membrane.
  • Commonly used polymers include cellulose acetates, polyamides, polysulfones, poly (vinylchloride-co-acrylonitrile)s, and poly (vinylidene fluoride).
  • Membrane separation is an effective concentrating method, however, other concentration methods such as a lamella separators, dissolved air flotation, gravity belt filter, decanter, rotating screen, or others are suitable separators.
  • the permeate from the concentrator and any unused concentrate may be discharged from the system or routed to one or more heat exchangers 8 as discussed below.
  • a flow control meter(s) or gauge(s) 51 and preferably a motorized valve 16 may be provided to control the flow of mixed liquor to and from the concentrator.
  • any control mechanism is acceptable for controlling the flow of liquor to and from the concentrator.
  • a pressure meter or gauge 63 coupled with a motorized valve 16 may be employed to control the pressure of mixed liquor conveyed to the digester 30 from the separator 58 .
  • any pressure control mechanism is suitable for controlling the pressure of the mixed liquor conveyed to the digester.
  • the digester configuration described previously allows for improved rates of digestion due to increased mass transfer rates but the volatile solids destruction is limited by the fraction of biodegradable solids available in said waste stream and is a function of solids retention time (SRT).
  • SRT solids retention time
  • the process performance in the same apparatus can be further improved if the SRT of the digester can be extended without increasing the digester volume. This can be achieved by further increasing the solids concentration in the digester.
  • concurrent concentration and digestion allows for adjustment of the mixed liquor concentration resulting in increased SRT in the digester at a fixed waste stream feed rate.
  • the design SRT can be targeted to achieve a particular goal such as, for example, to increase volatile solids destruction or to achieve specific effluent solids concentration.
  • the preferred embodiment is illustrated for the case of a municipal POTW waste sludge or a waste slurry. Similar digester designs and use of this method are envisioned for digesting other waste slurries from agricultural and industrial sources by the present invention. It is recognized that the percent fraction of biodegradable material in the slurry will vary based on the source and also that the concentration of solids in the slurry could be in the range of about 0.5% to about 12% TSS, but is preferably above 1% TSS. It is further recognized that the treatment objectives or economics of a given application might make it preferable to operate the digester 30 or concentrator 62 at parameters outside of the preferred ranges.
  • concentration of the feed may not be required and, in fact, a dilution stream might instead be preferred to achieve the desired mixed liquor TSS in the digester. It is also recognized that this anaerobic digestion process will also digest the soluble biodegradable organics present in the fluid stream. These and other variations in the present invention are contemplated.
  • An optional gas de-entrainment zone 45 can be provided within the digester 30 , as shown in FIG. 5.
  • the gas de-entrainment zone is preferably in the form of a vertical cylinder defined by a wall(s) 47 with an open top and a closed bottom 61 , preferably contiguous with the bottom 52 of the digester, except for an opening in the bottom 52 which is in communication with a mixed liquor outlet 50 of the digester, preferably the mixed liquor recycle outlet.
  • the shape of the wall(s) 47 of the zone may be generally cylindrical or otherwise configured so that the transverse cross sectional area of the zone is sufficient such that the downward velocity of the mixed liquor in the zone caused by the suction of the recirculation pump 6 is less than the rate of rise of gas bubbles of less than about 1 mm in diameter, in order to allow for such bubbles to de-entrain from the mixed liquor.
  • the preferred cross sectional area varies, but should be sufficient such that the downward velocity of the mixed liquor in the entrainment zone may range from 0.02 to 0.2 m/s, more preferably 0.05 to 0.1 m/s. This gas de-entrainment zone is preferred to avoid any potential for such gas bubbles to contribute to possible cavitation at the recirculation pump or the concentrate pump 6 , which could result in mechanical damage.
  • an optional gas deflector plate 25 depicted in FIGS. 1 and 5 is preferably positioned between the lower outlet 43 of the draft tube 28 and the digester bottom 52 to minimize the entrainment of gas bubbles in the mixed liquor at the point where it enters the conduit 50 of the recirculation system 46 or the concentrator 62 .
  • the gas deflector plate 25 has a shape that is larger than the outlet of the draft tube but smaller than a size that would cause the downward velocity of the mixed liquor flowing around the plate 25 to be increased above the rise rate of gas bubbles less than about 1 mm in diameter, in order to allow for such bubbles to de-entrain from the mixed liquor. It is understood however that, optional gas de-entrainment zone and deflector plate may used each alone or in combination in varying SEAD systems according to the invention.
  • Performance of the system can be further enhanced by operating the system at optimal levels of pH.
  • Any conventional manual or automated pH control mechanism can be used to control and optimize these conditions inside the digester.
  • a conventional pH control system 10 can be included, preferably in the recirculation conduit 60 , to measure pH and dose appropriate amounts of adjusting chemicals.
  • the preferred pH level of the digester for the anaerobic digestion is about 6 to about 8.
  • COD chemical oxygen demand
  • adjustment of the pH may be required to maintain the optimum level in the digester.
  • Performance of the system can also be further enhanced by operating the system at optimal levels of temperature.
  • Any conventional temperature control mechanism may be used to control the temperature of the mixed liquor in the digester.
  • One mechanism, shown in FIG. 1, includes a temperature meter or gauge 12 and a heat exchanger 8 , preferably in the recirculation system 46 of the invention.
  • a preferred method, shown in FIG. 5, includes the use of a heat exchanger 8 and a steam injector 9 upstream of recirculation pump 6 .
  • the heat exchanger 8 may serve as a recovery heat exchanger to capture heat from the permeate from concentrator 62 .
  • the waste heat may also be recovered from the digester effluent or the excess concentrate using a separate heat exchanger (not shown).
  • the temperature control mechanism preferably heats the feed into the digester (or into the recirculation conduit) to a temperature at or slightly above the preferred reaction temperature prior to the entry of the mixed liquor and/or feed into an inlet 2 of the digester.
  • the preferred temperature level of the digester for mesophilic anaerobic digestion is about 80° F. (25° C.) to about 105° F. (40° C.).
  • the digester may also be operated in the thermophilic range of about 125° F. (50° C.) to about 145° F. (60° C.).
  • the feed into the digester may be heated to any temperature that does not damage the anaerobic bacteria to a degree that negatively impacts the digestion process. In the case where it is preferred to destroy pathogens in the slurry, such as for the purpose of producing Class A municipal sludge, operation in the thermophilic range would allow for achievement of this objective simultaneously with digestion of the degradable organics.
  • the recirculation of mixed liquor through the nozzle 18 induces a circulation pattern around the draft tube 28 , which provides for mixing of the digester contents.
  • the biogas entrained in the mixed liquor enhances the mixing.
  • mixing provides a more uniform pH and temperature profile across the digester, thereby maintaining stable reaction conditions within the digester vessel.
  • the liquid circulation would be supplied by pump 6 and a conduit 36 in fluid communication with the discharge of the pump 6 and a nozzle 38 on the digester 30 , and would be directed below the deflector plate(s) 25 or otherwise in the area above and in proximity to the digester bottom 52 .
  • This liquid circulation may have any shape that sufficiently disturbs the layer of built up solids.
  • an additional biogas recycle system 21 may be utilized.
  • the biogas recycle system 21 preferably includes internal gas nozzles 23 , in communication with a conduit 19 , to force a gas upwardly around and into the draft tube 28 so as to dislodge the solids, before beginning normal operation of the nozzle 18 .
  • the system may also be further facilitated by an optional pump 49 to accelerate the flow of gas to nozzles 23 .
  • a defoaming spray system for the optimum operation of the anaerobic digester in the present invention.
  • Such a system prevents the buildup of foam inside the digester 30 by spraying liquid preferably continuously onto the upper surface of the mixed liquor in the digester.
  • Such spray preferably covers the majority or substantially all of the liquid surface.
  • the impact of the sprayed liquid on the surface of the liquid level serves to collapse the foam and inhibit foam buildup.
  • the liquid sprayed would be mixed liquor from the digester 30 .
  • at least one spray head 31 is used, and preferably many such spray heads.
  • This defoaming spray system can be supplemented if necessary with conventional chemical defoamer injection, activated through an appropriate foam sensor, and/or with conventional mechanical methods for foam destruction.
  • the apparatus according to the invention is operable when generally comprising a digester; any suitable mixing device capable of inducing a circulation and contributing to an improved mass transfer rate, including but not limited to the examples discussed above; and any suitable shearing device capable of fracturing the solids and introducing them into the digester, including but not limited to the examples discussed above.
  • FIG. 6 is directed to an alternative embodiment of the invention comprising a digester, preferably an anaerobic and shear enhanced digester, coupled with a concentrator.
  • the apparatus has improved efficiency due to concurrent operation of the digester and a concentrator.
  • the apparatus includes a digester 30 ′ preferably including a shear source 71 ′, such as a shearing nozzle, a Venturi nozzle, an impeller, or some other device capable of imparting shear to the mixed liquor within the digester, and a concentrator 62 ′ in fluid communication with a mixed liquor inlet 77 ′ of the digester and at least one mixed liquor outlet 50 ′ of the digester 30 ′.
  • the digester 30 ′ may be the digester 30 above or any digester preferably with a source for imparting shear to the mixed liquor in the digester.
  • the shear source 71 ′ may be either within or outside of the digester 30 ′ or in fluid communication with the digester 30 ′ so long as it is configured to impart shear to the mixed liquor within the digester.
  • the concentrator 62 ′ may be any concentrator that reduces the amount of water in the waste stream, including any of the concentrators 62 described above with respect to FIG. 5.
  • the concentrator 62 ′ and the digester 30 ′ can be configured as described above with respect to FIG. 5 to effect concurrent concentration and digestion of the mixed liquor.
  • the apparatus may further comprise any of the devices and adopt any configuration described above and will optimize the efficiency, particularly of the anaerobic digestion apparatus.
  • the concentrator 62 ′ may comprise a pump 70 ′ and a separator 58 ′ having an outlet 53 ′ which is in fluid communication with an inlet 77 ′ of the digester and an inlet 68 ′ in communication with a mixed liquor outlet 50 ′ of the digester.
  • the concentrator may also include a conduit 55 ′ with a first end 57 ′ connected to the outlet 53 ′ of the separator 58 ′, and a second end 59 ′ connected to the inlet 77 ′ of the digester 30 ′.
  • This conduit preferably conveys the concentrate from a concentrate side 69 ′ of the separator 58 ′ back to the digester 30 ′.
  • a waste stream may be digested in various embodiments of an anaerobic digestion apparatus, as described herein, by feeding the waste stream into the digester, preferably taking into consideration the parameters discussed above.
  • the biodegradable material in the waste stream may be reacted with anaerobic bacteria to produce a mixed liquor and a biogas.
  • This reaction may be further optimized by any of the methods described above, if desired, including controlling temperature and pH, concentrating the mixed liquor, minimizing the entrainment of gas bubbles, etc.
  • the mixed liquor may be introduced to the digester and any shearing device or method may be used, preferably in communication with an inlet of the digester, and the mixed liquor within the digester may be mixed by any mixing device or method, including those described herein.
  • the data in Table 1 illustrate the improved mass transfer rates of the digester apparatus of the present invention.
  • the pilot apparatus for this study was generally the embodiment of the digester apparatus as depicted in FIG. 1 of the attached drawings, hereinafter referred to as a shear-enhanced anaerobic digester (SEAD digester).
  • the apparatus included one two-phase nozzle, a draft tube, and a gas impingement plate, but not the concentrator.
  • the data additionally indicate the impact of typical polymers on the anaerobic digestion process.
  • the data is taken from a pilot study at a POTW wherein the feed to the SEAD digester was a mixture of primary and secondary sludge that had been thickened using a conventional belt thickener with the addition of polymers.
  • Chemical A is a cationic water soluble polymer in emulsion.
  • Chemical B is a solution mannich polymer.
  • the feed concentration is expressed in percent total solids (% TS), i.e. lbs. of solids per 100 lbs. of liquid sludge.
  • the HRT is hydraulic retention time in days, which in a once-through system equals the solids retention time (SRT).
  • SRT solids retention time
  • the bioactivity is a measure of the volatile solids conversion capacity of the anaerobic biomass and is expressed as kilograms of volatile solids digested per kilogram of digesting bacteria (volatile solids) per day.
  • Rx VFA is the concentration of volatile fatty acids in the digester expressed in milliequivalents per liter (meq/L).
  • Rx VFA is a measure of the process stability in the digester. Rx VFA readings of less than 1.0 indicate that the digesting environment is very stable and could likely perform at even higher mass transfer rates.
  • the first column indicates the data for the last month wherein Polymer A was added.
  • the SRT is roughly equivalent to that of an aggressively designed conventional digester.
  • the VFA indicates less than optimal stability.
  • the second column indicates the data for the subsequent month of operation when the POTW switched to a more economical polymer. Performance of the SEAD digester deteriorated as indicated by the much longer SRT as well as the elevated VFA indicating that Polymer B was significantly more inhibitory than Polymer A.
  • the first column indicates the performance obtained on the unthickened feed without the concentrator in operation.
  • the SRT again indicates that the improved mass transfer rates of the SEAD apparatus according to the invention are beneficial to the digestion process.
  • the low VFA indicates that further reductions in SRT might be possible.
  • the concentrator was then activated and the same sludge feed was concurrently concentrated and digested. Concentration was achieved with a membrane separation system without the addition of polymers as indicated in the preferred embodiment.
  • the second column indicates the performance with the concentrator operating during a transition period as the mixed liquor TSS is increasing. As the quantity of digesting bacteria accumulated in the digester, increased demand on the existing bacteria is indicated by the increase in Bioactivity and slightly elevated VFA.
  • Sludge digester systems are typically once through systems designed based on SRT and HRT.
  • the solids concentration of raw sludge is typically about 1% TS.
  • sludge is often thickened to about 5% TS before digestion.
  • Table 2 shows that the embodiment of the digester of the apparatus of the present invention including a shearing device and a mixing device can achieve the same process performance with prethickened sludge as a conventional high rate or egg-shaped digester, but at a considerably reduced SRT and HRT.
  • Table 1 shows that thickening polymers can be moderately to severely inhibitory to the anaerobic bacteria in the applicants' digester having a shearing device and a mixing device, and that elimination of such polymers improves process stability and bacterial activity.
  • Mere removal of the polymer is not a practical way in which to improve such process stability and bacterial activity because it would require treatment of dilute sludge in such a digester apparatus, which even at reduced SRT and HRT would require a large digester volume.
  • prethickening raw sludge from 1% TS to 5% TS with a membrane separator upstream of the digester is difficult, as discussed above, because the presence of hydrophilic compounds in sludge can prevent efficient performance of the upstream membrane.
  • applicants' embodiment further including concurrent digestion and concentration of the mixed liquor permits control of SRT independently of HRT, making it possible to digest dilute sludge without use of inhibitory polymers and using a digester volume similar to or less than the digester volumes associated with the prethickened sludge as used in Table 2.
  • Table 3 illustrates that for a given digester volume, applicants digester embodiment using the addition of a membrane concentrator according to the invention permits maintaining an SRT of 11 days while increasing the digester throughput by a factor of 11, as shown by the decrease in HRT from 11 days to 1 day.

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Cited By (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050077238A1 (en) * 2003-10-09 2005-04-14 Clark Sidney E. Anaerobic sludge digester
US20060138046A1 (en) * 2003-04-11 2006-06-29 Enviro Control Limited Apparatus for and a method of treating organic waste
US20060196829A1 (en) * 2004-12-14 2006-09-07 Sutton Paul M System for wastewater treatment and digestion having aerobic and anaerobic treatment zones
US20080283468A1 (en) * 2007-05-15 2008-11-20 John William Logan Method, composition and apparatus for high temperature production of methane from poultry waste
WO2009092821A1 (fr) * 2008-01-25 2009-07-30 David Ulmert Traitement de boues biologiques
WO2007058557A3 (fr) * 2005-11-18 2010-11-11 Universidade Do Minho Reacteur anaerobie pour extraire des acides gras a chaine longue d'eaux usees contenant des graisses
WO2011020000A2 (fr) * 2009-08-14 2011-02-17 The Ohio State University Research Foundation Co-digestion anaérobie de liquides-phases solides pour la production d'un biogaz à partir de déchets municipaux et agricoles
US20110042307A1 (en) * 2009-04-23 2011-02-24 Ghd, Inc. Methods and apparatuses to reduce hydrogen sulfide in a biogas
WO2011055092A1 (fr) * 2009-11-06 2011-05-12 Veolia Water Solutions & Technologies Support Procede de traitement anaerobie d'une eau usee et dispositif associe
WO2011130392A1 (fr) 2010-04-14 2011-10-20 Veolia Water Solutions & Technolgies Support Bioréacteur à membrane anaérobie pour traiter un courant de déchets
US20120145627A1 (en) * 2009-02-18 2012-06-14 Anaergia Inc. Anaerobic fermentation to produce biogas
US20130213883A1 (en) * 2010-08-13 2013-08-22 Anaergia Inc. Treatment of municipal wastewater with anaerobic digestion
US20130327694A1 (en) * 2009-08-12 2013-12-12 Kristinn G. Drewry Digester gas mixer for liquid waste treatment
US20140004589A1 (en) * 2011-03-28 2014-01-02 Rainbowtec Environmental Solutions 2010 Ltd. Apparatus for waste separation
US20140027374A1 (en) * 2010-02-25 2014-01-30 Siemens Water Technologies Llc Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
US20140299541A1 (en) * 2013-03-15 2014-10-09 John Armour Water filtration and sewage system
US8894857B2 (en) 2008-03-28 2014-11-25 Evoqua Water Technologies Llc Methods and systems for treating wastewater
ITBO20130362A1 (it) * 2013-07-11 2015-01-12 Walther Simonini Sistema per la produzione di biogas
US20150259639A1 (en) * 2012-10-08 2015-09-17 Calysta Energy, Llc Gas-fed fermentation systems
US9359236B2 (en) 2010-08-18 2016-06-07 Evoqua Water Technologies Llc Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle
AU2014200009B2 (en) * 2013-01-03 2016-08-04 Council Of Scientific & Industrial Research Anaerobic gas lift reactor for treatment of organic waste
EP3054000A1 (fr) * 2015-02-06 2016-08-10 Francesco Natta Digesteur à poussée de gaz pour la digestion anaérobie de déchets provenant de la chaîne alimentaire
US9771292B2 (en) 2011-02-03 2017-09-26 Anaergia Inc. Treatment of waste products with anaerobic digestion
US9809481B2 (en) 2015-01-27 2017-11-07 Anaergia Inc. Treatment of waste products with anaerobic digestion
US10131550B2 (en) 2013-05-06 2018-11-20 Evoqua Water Technologies Llc Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle
US20190152820A1 (en) * 2016-06-16 2019-05-23 Evoqua Water Technologies Llc Method of Combining Recuperative Digestion with a Contact Tank and Dissolved Air Flotation
WO2019156442A1 (fr) * 2018-02-09 2019-08-15 Hyun Yong Shin Bioréacteur pour la conversion de co2 gazeux
US10982233B2 (en) 2016-11-07 2021-04-20 Eagle Green Energy Ii Llc Method of processing organic matter

Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4218504B2 (ja) * 2003-11-13 2009-02-04 富士電機ホールディングス株式会社 メタン発酵処理方法
JP2006205030A (ja) * 2005-01-27 2006-08-10 Fuji Electric Holdings Co Ltd メタン発酵処理方法及び装置
JP2006314896A (ja) * 2005-05-11 2006-11-24 Nishihara Environment Technology Inc 汚泥処理槽の撹拌装置
CN100473615C (zh) * 2006-02-10 2009-04-01 中国科学院生态环境研究中心 用于废水处理的一体式膜固定化生物反应器及废水处理方法
JP2007245002A (ja) * 2006-03-16 2007-09-27 Ngk Insulators Ltd 膜分離型生物処理槽の運転方法
EP2028162B1 (fr) * 2007-08-03 2011-03-16 ACEA Pinerolese Industriale S.p.A. Reacteur pour la production anaérobique de biogaz d'ordures humides prétraités et procédé d' agitation dans cette reacteur
US8366932B1 (en) * 2008-10-08 2013-02-05 Iowa State University Research Foundation, Inc. Micro-aeration of sulfide removal from biogas
US8728801B2 (en) * 2009-01-21 2014-05-20 Daritech, Inc. Composter mechanism
JP5166337B2 (ja) * 2009-03-30 2013-03-21 メタウォーター株式会社 メタン発酵処理方法及びメタン発酵処理装置
DE102009016397A1 (de) * 2009-04-07 2010-10-14 Wilo Se Verfahren zur Verwirbelung von Aufwuchskörpern in einem Klärbecken und zugehöriges Klärbecken
FR2948355B1 (fr) * 2009-07-21 2011-09-02 Ondeo Ind Solutions Procede de methanisation, a partir d'effluents industriels ou urbains, liquides ou solides
JP5265588B2 (ja) * 2010-01-22 2013-08-14 メタウォーター株式会社 メタン発酵方法
US9090496B2 (en) 2010-07-27 2015-07-28 WISErg Corporation Methods and systems for processing organic material
US9751787B1 (en) 2011-08-23 2017-09-05 Daritech, Inc. Anaerobic digesting systems and methods for processing animal waste
CH705866A2 (de) * 2011-11-28 2013-05-31 Pdx Technologies Ag Verfahren für die behandlung von biologisch abbaubaren abfallströmen.
US9157058B2 (en) * 2011-12-14 2015-10-13 Kiverdi, Inc. Method and apparatus for growing microbial cultures that require gaseous electron donors, electron acceptors, carbon sources, or other nutrients
DE102012002964B3 (de) * 2012-02-16 2013-04-25 Technocon Gmbh Vorrichtung zur Gewinnung von Biogas
RU2505490C2 (ru) * 2012-04-10 2014-01-27 Государственное научное учреждение Всероссийский научно-исследовательский институт электрификации сельского хозяйства Российской академии сельскохозяйственных наук (ГНУ ВИЭСХ Россельхозакадемии) Устройство для утилизации органических субстратов с влажностью 92-99% с получением органических удобрений и электроэнергии
DE102012025027A1 (de) * 2012-12-20 2014-06-26 Reiflock Abwassertechnik Gmbh Vorrichtung und Verfahren zur Behandlung von Biomasse
DE102013001637B4 (de) * 2013-01-31 2022-05-05 Uwe Peters Verfahren und Vorrichtung zum Herstellen von Biogas
US9181138B2 (en) 2013-03-12 2015-11-10 WISErg Corporation Methods and systems for stabilizing organic material
CN104743659A (zh) * 2013-12-30 2015-07-01 易百皓源（北京）环保科技有限公司 新型水解酸化污水处理工艺
CA2963406A1 (fr) 2016-04-05 2017-10-05 Daritech, Inc. Systeme de digesteur anaerobique autonettoyant
CN108996680A (zh) * 2018-09-30 2018-12-14 中国环境科学研究院 模块组装式厌氧发酵塔装置及其处理有机废水的方法
CN109453722A (zh) * 2018-12-29 2019-03-12 天津天元伟业化工技术有限公司 一种串级喷射环流式反应装置
CN109825423B (zh) * 2019-01-09 2022-04-29 德沃（苏州）环境科技有限公司 内循环式生物反应器
IT202200001427A1 (it) * 2022-01-28 2023-07-28 D T A Srl Reattore a doppia camera di trattamento

Citations (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US32597A (en) * 1861-06-18 Fruit-drying apparatus
US3787316A (en) * 1970-01-29 1974-01-22 Fmc Corp Foam flotation concentration of sewage
US4165285A (en) * 1976-06-24 1979-08-21 N.V. Centrale Suiker Maatschappij Combined anaerobic reactor and settler
US4267038A (en) * 1979-11-20 1981-05-12 Thompson Worthington J Controlled natural purification system for advanced wastewater treatment and protein conversion and recovery
US4284510A (en) * 1978-05-11 1981-08-18 Canadian Liquid Air Ltd./Air Liquide Canada Ltee. Two zone process for biological treatment of waste water
US4290884A (en) * 1978-08-25 1981-09-22 Clevepak Corporation Nitrification-denitrification system
US4301007A (en) * 1979-11-08 1981-11-17 Canadian Liquid Air Ltd./Air Liquide Canada Ltee. Two zone apparatus for biological treatment of waste water
US4377066A (en) * 1980-05-27 1983-03-22 Dickinson Norman L Pollution-free pressurized fluidized bed combustion utilizing a high concentration of water vapor
US4446018A (en) * 1980-05-01 1984-05-01 Armco Inc. Waste treatment system having integral intrachannel clarifier
US4488960A (en) * 1982-08-06 1984-12-18 Utb Umwelttechnik Buchs Ag Biological reactor apparatus for biological decomposition of organic refuse
US4609460A (en) * 1984-07-24 1986-09-02 Paques B.V. Anaerobic purification equipment for waste water
US4618418A (en) * 1982-03-29 1986-10-21 Gist-Brocades N.V. Fluidized bed reactor
US4659464A (en) * 1984-09-14 1987-04-21 Long Enterprises, Inc. Apparatus for dispersing sludge with gas impingement
US4749494A (en) * 1985-04-01 1988-06-07 Mitsui Sekiyu Kagaku Kogyo Kabushiki Kaisha Treatment of waste water by the activated sludge process
US4885094A (en) * 1988-03-09 1989-12-05 Micro Pure Systems, Inc. Anaerobic digestion process, and forced fed fast rate digester
US4940546A (en) * 1987-09-03 1990-07-10 Tecon Gmbh Installation for aerobic biological purification of pollutant-containing water
US4954257A (en) * 1987-09-03 1990-09-04 Tecon Gmbh Biological purification loop device and method having deflector plate within guide pipe
US5116505A (en) * 1987-10-08 1992-05-26 Gist-Brocades N.V. Fluidized bed process
US5120442A (en) * 1987-02-07 1992-06-09 Dr. Karl Thomae Gmbh Process for the simultaneous chemical and biological elimination of solid and liquid organic waste
US5230794A (en) * 1987-10-08 1993-07-27 Biothane Corporation Fluidized-bed apparatus
US5360546A (en) * 1992-04-01 1994-11-01 Ngk Insulators, Ltd. Method for treating organic sludge
US5409610A (en) * 1991-03-13 1995-04-25 Clark; Sidney E. Method for anaerobic sludge digestion
US5454949A (en) * 1994-01-03 1995-10-03 Davis; Harold E. Sewage treatment system and method
US5505862A (en) * 1991-06-14 1996-04-09 Sonnenrein; Uwe Method for sewage clarification
US5518618A (en) * 1992-06-10 1996-05-21 Paques B.V. System and process for purifying waste water which contains nitrogenous compounds
US5565098A (en) * 1992-06-03 1996-10-15 Paques B.V. Reactor for the biological treatment of water
US5616288A (en) * 1995-06-26 1997-04-01 Mcdonald; Stephen J. Aeration apparatus and method of aerating liquids
US5739031A (en) * 1994-02-02 1998-04-14 Eco Soil Systems, Inc. Soil and water remediation and enhancement process and apparatus therefor
US5811259A (en) * 1997-07-29 1998-09-22 Ecomat, Inc. Biochemical reactor
US5837141A (en) * 1995-10-26 1998-11-17 Technische Consult Tecon Gmbh Process for the biological treatment of waste water
US5942118A (en) * 1996-10-04 1999-08-24 Besten; Hans-Werner Method and arrangement for decomposing organic waste water pollutants
US5945039A (en) * 1996-09-06 1999-08-31 Kojima; Hisao Gas-liquid processing apparatus
US5948261A (en) * 1998-02-05 1999-09-07 Pressley; Richard L. Process for treating biosolids from wastewater treatment
US5993650A (en) * 1995-10-27 1999-11-30 Sam Kwang Aqua-Clear, Inc. Granular carrier for treating sewage or waste water, method for producing the same and apparatus for treating sewage or waste water by using the granular carriers
US6030534A (en) * 1999-06-10 2000-02-29 De Lima; Daniel Three dimensional continuous loop reactor
US6059971A (en) * 1995-01-30 2000-05-09 Vit; Robert Device and process for thickening and conveying waste water sludge
US6224769B1 (en) * 1997-06-05 2001-05-01 Shinko Pantec Co., Ltd. Method and apparatus for treating organic waste water

Family Cites Families (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2991983A (en) * 1956-09-21 1961-07-11 Dorr Oliver Inc Sludge treatment
US4111808A (en) * 1975-12-11 1978-09-05 Fair John H Apparatus for sludge digestion
NL173738C (nl) 1978-05-23 1988-10-17 Gist Brocades Nv Anaerobe zuiveringsinrichting.
US4337152A (en) * 1978-09-27 1982-06-29 Frebar Holding Ag Aeration apparatus and method
DE3102435A1 (de) 1981-01-26 1982-10-07 Zenith-Maschinenfabrik Gmbh, 5908 Neunkirchen Klaeranlage
DE3117462A1 (de) 1981-05-02 1982-11-25 Zenith-Maschinenfabrik Gmbh, 5908 Neunkirchen "verfahren und einrichtung zur belueftung des abwasser-belebtschlamm-gemisches beim belebungsverfahren in klaeranlagen"
DE3117461A1 (de) 1981-05-02 1982-11-25 Zenith-Maschinenfabrik Gmbh, 5908 Neunkirchen Verfahren zur behandlung des abwasserschlamms in klaeranlagen durch einen anaeroben faulprozess sowie zum betrieb der klaeranlagen mit der beim faulprozess anfallenden gas- und waermeenergie
DE3131917C2 (de) * 1981-08-12 1995-07-13 Marker Int Fersenstrammer für eine Skibindung mit integrierter Skibremse
DE3144487A1 (de) 1981-11-09 1983-05-19 Zenith-Maschinenfabrik Gmbh, 5908 Neunkirchen Umwaelzvorrichtung fuer faulraeume
JPS58214396A (ja) * 1982-06-08 1983-12-13 Hiroshi Yoshimoto 畜舎糞尿の処理装置
DE3231234A1 (de) 1982-08-23 1984-03-01 Martin Dipl.-Ing. 6349 Breitscheid Menges Verfahren und anlage zur vorpasteurisierung von fluessigkeiten insbesondere klaerschlamm
DE3244577A1 (de) 1982-12-02 1984-06-07 Martin Dipl.-Ing. 6349 Breitscheid Menges Verfahren und maschine zur mechanisch biologischen abwasserbehandlung fuer kompaktanlagen
DE3323514A1 (de) 1983-06-30 1985-01-10 Menges, Martin, Dipl.-Ing., 6349 Breitscheid Kompaktreaktor zur biologischen intensivbehandlung von abwasser, bei gleichzeitiger bindung der leichtfluechtigen c-verbindungen (poc)
DE3413537A1 (de) 1983-06-30 1985-10-24 Martin Dipl.-Ing. 6349 Breitscheid Menges Reaktor zur biologischen abwasserreinigung
DE3326939A1 (de) * 1983-07-26 1985-02-07 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zur anaeroben biologischen reinigung von abwasser
JPS614598A (ja) * 1984-06-19 1986-01-10 Matsushita Electric Ind Co Ltd メタン発酵装置
JPS61178016A (ja) * 1985-02-01 1986-08-09 Takuma Sogo Kenkyusho:Kk 消化槽におけるメタンガス回収方法
US5185079A (en) * 1991-05-16 1993-02-09 Iowa State University Research Foundation, Inc. Anaerobic sequencing batch reactor
JP2976772B2 (ja) * 1993-09-28 1999-11-10 日本鋼管株式会社 消化タンクの運転方法
GB9323870D0 (en) 1993-11-19 1994-01-05 Ea Tech Ltd Methods and apparatus for using micro-organisms to treat organic material found in waste water
US6059972A (en) * 1995-07-18 2000-05-09 Mahrer; Francois-Regis Apparatus for receiving and conditioning organic waste by anaerobic bioconversion
ATE219469T1 (de) 1996-05-22 2002-07-15 Va Tech Wabag Schweiz Ag Verfahren und reaktor zur anaeroben abwasserreinigung in einem schlammbett
US6203701B1 (en) * 1998-02-05 2001-03-20 Thermal Process Systems, Llc Process and apparatus for treating biosolids from wastewater treatment
US6153099A (en) * 1998-12-21 2000-11-28 Smith & Loveless, Inc. Biological waste treatment process and apparatus

Patent Citations (39)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US32597A (en) * 1861-06-18 Fruit-drying apparatus
US3787316A (en) * 1970-01-29 1974-01-22 Fmc Corp Foam flotation concentration of sewage
US4165285A (en) * 1976-06-24 1979-08-21 N.V. Centrale Suiker Maatschappij Combined anaerobic reactor and settler
US4284510A (en) * 1978-05-11 1981-08-18 Canadian Liquid Air Ltd./Air Liquide Canada Ltee. Two zone process for biological treatment of waste water
US4290884A (en) * 1978-08-25 1981-09-22 Clevepak Corporation Nitrification-denitrification system
US4301007A (en) * 1979-11-08 1981-11-17 Canadian Liquid Air Ltd./Air Liquide Canada Ltee. Two zone apparatus for biological treatment of waste water
US4267038A (en) * 1979-11-20 1981-05-12 Thompson Worthington J Controlled natural purification system for advanced wastewater treatment and protein conversion and recovery
US4446018A (en) * 1980-05-01 1984-05-01 Armco Inc. Waste treatment system having integral intrachannel clarifier
US4377066A (en) * 1980-05-27 1983-03-22 Dickinson Norman L Pollution-free pressurized fluidized bed combustion utilizing a high concentration of water vapor
US4618418A (en) * 1982-03-29 1986-10-21 Gist-Brocades N.V. Fluidized bed reactor
US4488960A (en) * 1982-08-06 1984-12-18 Utb Umwelttechnik Buchs Ag Biological reactor apparatus for biological decomposition of organic refuse
US4609460A (en) * 1984-07-24 1986-09-02 Paques B.V. Anaerobic purification equipment for waste water
US4659464A (en) * 1984-09-14 1987-04-21 Long Enterprises, Inc. Apparatus for dispersing sludge with gas impingement
US4749494A (en) * 1985-04-01 1988-06-07 Mitsui Sekiyu Kagaku Kogyo Kabushiki Kaisha Treatment of waste water by the activated sludge process
US5120442A (en) * 1987-02-07 1992-06-09 Dr. Karl Thomae Gmbh Process for the simultaneous chemical and biological elimination of solid and liquid organic waste
US4954257A (en) * 1987-09-03 1990-09-04 Tecon Gmbh Biological purification loop device and method having deflector plate within guide pipe
US4940546A (en) * 1987-09-03 1990-07-10 Tecon Gmbh Installation for aerobic biological purification of pollutant-containing water
US5855785A (en) * 1987-10-08 1999-01-05 Biothane Corporation Three-phase separator for a fluidized bed apparatus
US5116505A (en) * 1987-10-08 1992-05-26 Gist-Brocades N.V. Fluidized bed process
US5230794A (en) * 1987-10-08 1993-07-27 Biothane Corporation Fluidized-bed apparatus
US4885094A (en) * 1988-03-09 1989-12-05 Micro Pure Systems, Inc. Anaerobic digestion process, and forced fed fast rate digester
US5409610A (en) * 1991-03-13 1995-04-25 Clark; Sidney E. Method for anaerobic sludge digestion
US5505862A (en) * 1991-06-14 1996-04-09 Sonnenrein; Uwe Method for sewage clarification
US5616240A (en) * 1991-06-14 1997-04-01 Sonnenrein; Uwe Device for sewage clarification
US5360546A (en) * 1992-04-01 1994-11-01 Ngk Insulators, Ltd. Method for treating organic sludge
US5565098A (en) * 1992-06-03 1996-10-15 Paques B.V. Reactor for the biological treatment of water
US5518618A (en) * 1992-06-10 1996-05-21 Paques B.V. System and process for purifying waste water which contains nitrogenous compounds
US5454949A (en) * 1994-01-03 1995-10-03 Davis; Harold E. Sewage treatment system and method
US5739031A (en) * 1994-02-02 1998-04-14 Eco Soil Systems, Inc. Soil and water remediation and enhancement process and apparatus therefor
US6059971A (en) * 1995-01-30 2000-05-09 Vit; Robert Device and process for thickening and conveying waste water sludge
US5616288A (en) * 1995-06-26 1997-04-01 Mcdonald; Stephen J. Aeration apparatus and method of aerating liquids
US5837141A (en) * 1995-10-26 1998-11-17 Technische Consult Tecon Gmbh Process for the biological treatment of waste water
US5993650A (en) * 1995-10-27 1999-11-30 Sam Kwang Aqua-Clear, Inc. Granular carrier for treating sewage or waste water, method for producing the same and apparatus for treating sewage or waste water by using the granular carriers
US5945039A (en) * 1996-09-06 1999-08-31 Kojima; Hisao Gas-liquid processing apparatus
US5942118A (en) * 1996-10-04 1999-08-24 Besten; Hans-Werner Method and arrangement for decomposing organic waste water pollutants
US6224769B1 (en) * 1997-06-05 2001-05-01 Shinko Pantec Co., Ltd. Method and apparatus for treating organic waste water
US5811259A (en) * 1997-07-29 1998-09-22 Ecomat, Inc. Biochemical reactor
US5948261A (en) * 1998-02-05 1999-09-07 Pressley; Richard L. Process for treating biosolids from wastewater treatment
US6030534A (en) * 1999-06-10 2000-02-29 De Lima; Daniel Three dimensional continuous loop reactor

Cited By (47)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060138046A1 (en) * 2003-04-11 2006-06-29 Enviro Control Limited Apparatus for and a method of treating organic waste
US7150832B2 (en) * 2003-04-11 2006-12-19 Enviro Control Limited Apparatus for and a method of treating organic waste
US20050077238A1 (en) * 2003-10-09 2005-04-14 Clark Sidney E. Anaerobic sludge digester
US7172698B2 (en) * 2003-10-09 2007-02-06 Chicago Bridge & Iron Company Anaerobic sludge digester
US20060196829A1 (en) * 2004-12-14 2006-09-07 Sutton Paul M System for wastewater treatment and digestion having aerobic and anaerobic treatment zones
US7402247B2 (en) * 2004-12-14 2008-07-22 Shaw Intellectual Property Holdings, Inc. System for wastewater treatment and digestion having aerobic and anaerobic treatment zones
WO2007058557A3 (fr) * 2005-11-18 2010-11-11 Universidade Do Minho Reacteur anaerobie pour extraire des acides gras a chaine longue d'eaux usees contenant des graisses
US7785467B2 (en) * 2007-05-15 2010-08-31 Eagle Green Energy, LLC Method, composition and apparatus for high temperature production of methane from poultry waste
US20080283468A1 (en) * 2007-05-15 2008-11-20 John William Logan Method, composition and apparatus for high temperature production of methane from poultry waste
WO2009092821A1 (fr) * 2008-01-25 2009-07-30 David Ulmert Traitement de boues biologiques
US9359239B2 (en) 2008-03-28 2016-06-07 Evoqua Water Technologies Llc Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
US8894857B2 (en) 2008-03-28 2014-11-25 Evoqua Water Technologies Llc Methods and systems for treating wastewater
US8894856B2 (en) 2008-03-28 2014-11-25 Evoqua Water Technologies Llc Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
US10144664B2 (en) 2009-02-18 2018-12-04 Anaergia Inc. Anaerobic fermentation to produce biogas
US9416372B2 (en) * 2009-02-18 2016-08-16 Anaergia Inc. Anaerobic fermentation to produce biogas
US20120145627A1 (en) * 2009-02-18 2012-06-14 Anaergia Inc. Anaerobic fermentation to produce biogas
US20110042307A1 (en) * 2009-04-23 2011-02-24 Ghd, Inc. Methods and apparatuses to reduce hydrogen sulfide in a biogas
US20130327694A1 (en) * 2009-08-12 2013-12-12 Kristinn G. Drewry Digester gas mixer for liquid waste treatment
WO2011020000A2 (fr) * 2009-08-14 2011-02-17 The Ohio State University Research Foundation Co-digestion anaérobie de liquides-phases solides pour la production d'un biogaz à partir de déchets municipaux et agricoles
WO2011020000A3 (fr) * 2009-08-14 2011-05-26 The Ohio State University Research Foundation Co-digestion anaérobie de liquides-phases solides pour la production d'un biogaz à partir de déchets municipaux et agricoles
AU2010316835B2 (en) * 2009-11-06 2015-09-10 Veolia Water Solutions & Technologies Support Method for anaerobic treatment of wastewater and associated device
WO2011055092A1 (fr) * 2009-11-06 2011-05-12 Veolia Water Solutions & Technologies Support Procede de traitement anaerobie d'une eau usee et dispositif associe
FR2952369A1 (fr) * 2009-11-06 2011-05-13 Otv Sa Procede de traitement anaerobie d'une eau usee et dispositif associe
US20140027374A1 (en) * 2010-02-25 2014-01-30 Siemens Water Technologies Llc Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
US8801931B2 (en) * 2010-02-25 2014-08-12 Evoqua Water Technologies Llc Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
WO2011130392A1 (fr) 2010-04-14 2011-10-20 Veolia Water Solutions & Technolgies Support Bioréacteur à membrane anaérobie pour traiter un courant de déchets
US9181120B2 (en) * 2010-08-13 2015-11-10 Anaergia Inc. Treatment of municipal wastewater with anaerobic digestion
US9845260B2 (en) 2010-08-13 2017-12-19 Anaergia Inc. Treatment of municipal wastewater with anaerobic digestion
US20130213883A1 (en) * 2010-08-13 2013-08-22 Anaergia Inc. Treatment of municipal wastewater with anaerobic digestion
US9359236B2 (en) 2010-08-18 2016-06-07 Evoqua Water Technologies Llc Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle
US9783440B2 (en) 2010-08-18 2017-10-10 Evoqua Water Technologies Llc Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle
US9771292B2 (en) 2011-02-03 2017-09-26 Anaergia Inc. Treatment of waste products with anaerobic digestion
US20140004589A1 (en) * 2011-03-28 2014-01-02 Rainbowtec Environmental Solutions 2010 Ltd. Apparatus for waste separation
US20150259639A1 (en) * 2012-10-08 2015-09-17 Calysta Energy, Llc Gas-fed fermentation systems
JP2015535692A (ja) * 2012-10-08 2015-12-17 キャリスタ， インコーポレイテッド Ｇａｓ−ｆｅｄ発酵システム
US10889793B2 (en) 2012-10-08 2021-01-12 Calysta, Inc. C1 substrate-fed fermentation systems and methods for producing C4 compounds
US10501714B2 (en) * 2012-10-08 2019-12-10 Calysta Energy, Inc. Gas-fed fermentation systems
AU2014200009B2 (en) * 2013-01-03 2016-08-04 Council Of Scientific & Industrial Research Anaerobic gas lift reactor for treatment of organic waste
US20140299541A1 (en) * 2013-03-15 2014-10-09 John Armour Water filtration and sewage system
US10131550B2 (en) 2013-05-06 2018-11-20 Evoqua Water Technologies Llc Enhanced biosorption of wastewater organics using dissolved air flotation with solids recycle
ITBO20130362A1 (it) * 2013-07-11 2015-01-12 Walther Simonini Sistema per la produzione di biogas
US9809481B2 (en) 2015-01-27 2017-11-07 Anaergia Inc. Treatment of waste products with anaerobic digestion
EP3054000A1 (fr) * 2015-02-06 2016-08-10 Francesco Natta Digesteur à poussée de gaz pour la digestion anaérobie de déchets provenant de la chaîne alimentaire
US20190152820A1 (en) * 2016-06-16 2019-05-23 Evoqua Water Technologies Llc Method of Combining Recuperative Digestion with a Contact Tank and Dissolved Air Flotation
US10654735B2 (en) * 2016-06-16 2020-05-19 Evoqua Water Technologies Llc Method of combining recuperative digestion with a contact tank and dissolved air flotation
US10982233B2 (en) 2016-11-07 2021-04-20 Eagle Green Energy Ii Llc Method of processing organic matter
WO2019156442A1 (fr) * 2018-02-09 2019-08-15 Hyun Yong Shin Bioréacteur pour la conversion de co2 gazeux

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