US20150068977A1 - Integrated membrane system for distributed water treatment - Google Patents
Integrated membrane system for distributed water treatment Download PDFInfo
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- US20150068977A1 US20150068977A1 US14/543,837 US201414543837A US2015068977A1 US 20150068977 A1 US20150068977 A1 US 20150068977A1 US 201414543837 A US201414543837 A US 201414543837A US 2015068977 A1 US2015068977 A1 US 2015068977A1
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/04—Feed pretreatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
- C02F1/4674—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation with halogen or compound of halogens, e.g. chlorine, bromine
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/025—Biological purification using sources of oxygen other than air, oxygen or ozone
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/12—Addition of chemical agents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/001—Upstream control, i.e. monitoring for predictive control
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/03—Pressure
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/42—Liquid level
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/44—Time
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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
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
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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
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
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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
- C02F3/005—Combined electrochemical biological processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/08—Aerobic processes using moving contact bodies
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
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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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- Embodiments of the invention relate to water and wastewater treatment and more particularly to integrated membrane treatment systems.
- Bio treatment is the most widely used technology. It utilizes metabolism of microorganisms to remove organic matter, as well as other dissolved nutrients including nitrogen and phosphorus. Biological mass (biomass) is also known to adsorb heavy metals, suspended solids, and other sorts of contaminants which do not undergo biological degradation. Biomass is separated from the treated liquid, thus allowing for discharge of treated water (effluent) and disposal of the excess of the biomass (sludge).
- two biological treatment methods are typically used separately or in combination. A first is anaerobic treatment, which does not require aeration (addition of dissolved oxygen). The other is aerobic treatment, utilizing dissolved oxygen in the biological treatment.
- the activated sludge method is an example of an aerobic biological treatment for municipal wastewater containing a relatively low level of organic impurities using biomass mixed with the treated liquid.
- RO membranes effectively remove suspended solids (including viruses and bacteria), often with higher efficiency and reliability than MBR.
- RO membranes also remove inorganic matter (including dissolved salts, thus providing softening effect).
- RO can also remove high molecular weight dissolved organics, which is typically a main fraction of the biological treatment effluent.
- Deficiencies in conventional RO implementations include high-energy consumption and high pretreatment cost.
- Another problem with treating MBR effluent by RO is bio-fouling of RO membranes. Controlling bio-fouling by disinfection is difficult due to the fact that oxidizing biocides may attack the membrane material and adversely affect membrane performance. Disinfection also typically entails a use of chemicals which require special permits and adds operational complexity
- Embodiments of the present invention integrated membrane systems which when operated independently are comparatively less efficient.
- the integrated systems enable efficient operation across a wide range of volumetric flows for scalability that is well-suited to a distributed treatment model.
- the integrated treatment systems described herein are implemented for distributed treatment within a framework of an existing sewerage system.
- RO is integrated with other components of a water treatment system, such as a biological unit, or an MBR, to recover energy from the RO unit, for example from the RO concentrate (reject), to operate the other components.
- a single hydraulic pump is harnessed to operate the majority of the treatment system.
- RO is integrated with other components of a water treatment system, such as a biological unit, or an MBR, to leverage the RO's ability to remove inorganic nitrogen.
- removal of nitrogen by RO enables biological treatment to be performed incompletely, thereby advantageously reducing retention times.
- reliance on the RO for nitrogen removal enables biological treatment to be performed with only partial nitrification (oxidation of ammonia to nitrate) further enabling the biological treatment to be performed with no pH control.
- pH freely varies as a function of the wastewater influent quality and level of biological activity sustainable with no active pH control.
- ammonia may exist in the treated water with the pH most likely dropping below 7.
- chemical use and handling is reduced.
- synergy between the RO and other components of the system simplify operation and maintenance of the water treatment system.
- RO is integrated with a chlorine generator to convert chlorides present in the RO concentrate for an in-situ source of oxidizing biocides for disinfection purposes.
- residual inorganic nitrogen in the RO concentrate (present because of the partial nitrification) is further utilized, along with the chlorides to derive chloramines for disinfection purposes.
- the pressurized RO concentrate is utilized to drive service flows employing the disinfectant so that a separate metering system is not required. As such, a synergy between the RO and other components of the system reduces system complexity, chemical use, and improves membrane lifetimes.
- carrier media is employed in a membrane tank to improve effectiveness of membrane scouring through mechanical agitation by the carrier media and potentially enhance removal of residual organics by the MBR.
- FIG. 1 illustrates a flow path diagram for water treatment system with an energy recovery system for integrated treatment and/or filtration of an aqueous solution, in accordance with an embodiment of the present invention
- FIG. 2 illustrates a water treatment method which may be performed by water treatment system illustrated in FIG. 1 to employ RO and recover energy there from for integrated treatment and/or filtration of an aqueous solution, in accordance with an embodiment of the present invention
- FIG. 3A illustrates a flow path diagram for a water treatment system with an RO salt electrolysis system for integrated disinfection of the system and aqueous solution treated by the system, in accordance with an embodiment of the present invention
- FIG. 3B illustrates an isometric view of a membrane filter, scouring elements, and scouring element retainer, in accordance with an embodiment of the present invention
- FIG. 4 illustrates a water treatment method which may be performed by water treatment system illustrated in FIG. 3A to convert salts recovered from an RO concentrate into oxidizing biocides for integrated disinfection of the system and the aqueous solution treated by the system, in accordance with an embodiment of the present invention
- FIG. 5 illustrates a flow path diagram for a water treatment system integrating treatment, membrane filtration, and RO with energy recovery and disinfection systems, in accordance with an embodiment of the present invention
- FIG. 6 illustrates a water treatment method which may be performed by water treatment system illustrated in FIG. 5 to integrate treatment, membrane filtration, and RO with energy recovery and disinfection, in accordance with an embodiment of the present invention
- FIG. 7A illustrates a cross-sectional side view of a water treatment and membrane filtration apparatus which may be utilized in the water treatment system illustrated in the FIG. 5 , in accordance with embodiments of the present invention
- FIG. 7B illustrates a plan view of the water treatment and membrane filtration apparatus illustrated in FIG. 7A , in accordance with embodiments of the present invention
- FIG. 8 illustrates a water treatment method which may be performed by the water treatment and membrane filtration apparatus illustrated in FIGS. 7A , 7 B to implement the treatment and filtration operations illustrated in FIG. 6 , in accordance with an embodiment of the present invention.
- FIG. 9 is a water treatment system architecture in which the integrated water treatment system illustrated in FIG. 5 may be implemented within an existing sewer or industrial treatment system, in accordance with an embodiment of the present invention.
- Described herein are integrated membrane water treatment systems and water treatment methods which may be performed by such systems.
- numerous specific details are set forth, such as exemplary treatment and filtration apparatuses to describe embodiments of the present invention.
- embodiments of the present invention may be practiced without such specific details.
- well-known aspects such as specific biological treatment techniques, solids separation techniques, etc. and associated hardware, are not described in detail to avoid unnecessarily obscuring embodiments of the present invention.
- Coupled and “in fluid communication,” are used herein to describe structural and functional relationships between components, respectively. Two components “coupled” together are in either direct or indirect (with other intervening components between them) physical contact with each other. Two components “in fluid communication” are coupled in a manner such that a fluid from one component is capable of flowing to the other component.
- water treatment is employed herein in its broadest sense to mean removal of a contaminant, be it by solids separation, chemical, physical, biological treatment, etc.
- any reference to “wastewater” is to be understood as a label for any aqueous solution having an impurity level which is to be improved, be it domestic sewage effluent, industrial effluent, or non-point source runoff, etc. Exemplary embodiments describing the treatment of any specific classes or types of wastewater are therefore merely to emphasize the broad applicability of the present invention.
- FIG. 1 illustrates a flow path diagram for a water treatment system 100 with an energy recovery system for integrated treatment and/or filtration of an aqueous solution, in accordance with an embodiment of the present invention.
- FIG. 1 is described in the context of FIG. 2 , illustrating operations of an exemplary water treatment method 200 that may be performed by the water treatment system 100 .
- an aqueous solution having impurities of any type is received as the influent stream 101 ( FIG. 1 ) to a vessel 105 .
- the wastewater is preferably with a brackish salinity level to provide a source of salts which are employed as an in-situ source of biocides, as described further herein.
- At operation 205 at least one of filtration, aerobic or anaerobic biological treatment, chemical treatment (e.g., oxidation of Mn and Fe, etc. or chemical precipitation such as HF waste with CaCl 2 , etc.), or physical-chemical treatment (e.g., coagulation or flocculation) of the aqueous solution is performed within the vessel 105 .
- chemical treatment e.g., oxidation of Mn and Fe, etc. or chemical precipitation such as HF waste with CaCl 2 , etc.
- physical-chemical treatment e.g., coagulation or flocculation
- processed effluent from the vessel 105 is utilized to drive one or more activities occurring in the vessel 105 .
- the processed effluent is driven downstream by a hydraulic pump 120 disposed downstream from the vessel 105 .
- Energy may be recovered from the hydraulic pump 120 utilized to drive one or more activities performed in the vessel 105 .
- the processed effluent is supplied into an influent side of an RO unit 110 .
- the RO unit is drawn in dashed line to emphasize, that the energy recovery illustrated in FIG. 1 is not dependent on RO being performed downstream, though additional synergies are to be had for those embodiments employing an RO unit, as described elsewhere herein.
- the RO unit 110 may be of any design known in the art with many variants being commercially available to filter via a diffusive mechanism with separation efficiency being dependent on solute concentration, pressure, and flux rate rather than size exclusion as for membrane filtration.
- Effluent from the RO includes a permeate stream 116 and concentrate (reject) stream 114 .
- the permeate stream 116 as the product of the water treatment system 100 is provided to a downstream application, be it further purification or consumption.
- the hydraulic pump 120 is in fluid communication with both the vessel 105 and the RO unit 110 , the breaks in the effluent stream 107 denote that one or more intervening process vessels, process controls, etc. may be disposed there between.
- a motor 130 is driven with the pressurized vessel effluent at operation 230 .
- the hydraulically driven motor 130 may be of any design known in the art, with an exemplary system being the HydroDrive, commercially available from Hastec HydroDrives, Inc. of St. Catharines, Ontario, Canada.
- the drive side of the motor 130 is in fluid communication with either or both the RO concentrate stream 114 or an RO bypass stream 112 disposed downstream of the hydraulic pump 120 and upstream of the RO unit 110 , each of which provides a pressurized source with an associated pressure head and volumetric flow rate.
- At least some portion of effluent from the pump 120 is utilized to drive one or more motor 130 as coupled to either or both the compressor 140 (to provide aeration and/or pressurization gas stream 142 ) and mixer 150 .
- the motor effluent stream 135 may be either reintroduced into the system upstream of the hydraulic pump 120 (e.g., returned vessel effluent stream 107 where RO bypass stream 112 drives the motor 130 ) or discharged to a waste drain (e.g., where the RO concentrate stream 114 drives the motor 130 ).
- the motor 130 provides a means of recovery residual energy remaining downstream of the RO unit.
- the motor 130 provides a means to enable the hydraulic pump 120 to be a single energy source for the treatment system 100 .
- the hydraulic pump 120 is therefore to be sized to accommodate the additional load associated with driving the motor 130 .
- a driven side of the motor 130 is harnessed at operation 240 ( FIG. 2 ) to power one or more action performed in the vessel 105 .
- any processing action conventional in the art may be powered by the motor 130
- exemplary embodiments include one or more of mixing, aerating, or pressurizing a filtration or biological, chemical, or physical-chemical treatment with at least some portion of effluent from the vessel 105 .
- the driven side of the motor 130 coupled to a compressor 140 having an inlet coupled to a gas source, such as ambient air, and an outlet coupled into the vessel 105 to pressurize the vessel (e.g., in the case of a filtration process occurring in the vessel 105 , as described further elsewhere herein) or aerate processes performed in the vessel with the gas (e.g., air) introduced.
- a gas source such as ambient air
- the drive side of the motor 130 is to be in fluid communication with the RO bypass stream 112 for a larger pressure head and volumetric flow rate.
- the motor 130 has the driven side coupled to a mechanical mixer 150 disposed within the vessel 105 .
- the vessel 105 may be operated as a CSTR with the mixer shaft 152 driven by the motor 130 .
- the drive side of the motor 130 may be in fluid communication with either concentrate outlet of the RO unit 110 (to be driven by the concentrate stream 114 ) or in fluid communication with the RO bypass stream 112 .
- multiple motors 130 may be driven by the pressurized vessel effluent. For example, and as further described elsewhere herein, a first motor 130 drives the mixer 150 with the RO concentrate stream 114 while a second motor 130 drives the compressor 140 with the RO bypass stream 112 .
- FIG. 3A illustrates a flow path diagram for a water treatment system 300 with an RO salt electrolysis system for integrated disinfection of the system and of the aqueous solution treated by the system, in accordance with an embodiment of the present invention.
- FIG. 3A is described in the context of FIG. 4 illustrating an exemplary operation of a water treatment method 400 that may be performed by the water treatment system 300 .
- an aqueous solution having biodegradable impurities is received as the influent stream 304 ( FIG. 3A ) to a filtration vessel 305 .
- a porous membrane filter 306 is submerged within the filtration vessel 305 with an effluent side of the filter 306 passing through a wall of the filtration vessel 305 for solid separation in addition to biological treatment, for example in the case of an MBR.
- biological treatment at operation 404 is performed incompletely, such that nitrogen (e.g., ammonia) is not completely removed.
- operation 404 may have a corresponding solids retention time of between 1 and 15 days whereas in conventional systems designed for complete nitrogen removal retention time is typically 20 to 40 days.
- operation 404 is performed without pH control.
- operation 404 and indeed all the operations in the entire treatment system 300 , is operated at whatever steady-state pH naturally occurs (e.g., as a function of the biological treatment process performed at operation 404 ). With nitrification occurring to some extent, steady-state pH is lowered, for example to be below 7. A lower pH inhibits biological processes as well as further nitrification. Allowing pH to drop freely to a relatively low level has the advantage of avoiding caustic addition, reduced oxygen demand and therefore a lower energy consumption for aeration, and reduced bio-fouling of the membrane filter 306 .
- Effluent from the filtration vessel 305 is driven into an influent side of the RO unit 110 by the hydraulic pump 120 disposed downstream from the filtration vessel 305 .
- RO permeate stream 116 as the product of the water treatment system 300 is provided to a downstream application, be it further purification or consumption. For those embodiments where pH is allowed to drop freely (e.g., upon partial nitrification), scaling of the RO membrane will be advantageously reduced.
- the hydraulic pump 120 is in fluid communication with both the filtration vessel 305 and the RO unit 110 , the breaks in the effluent stream 307 denote one or more intervening process vessels, process controls, etc. may be disposed there between.
- a chlorine generator is integrated with the RO unit 110 for in-situ generation of biocides for disinfection.
- an electrolytic cell 365 is in fluid communication with the concentrate outlet of the RO unit 110 .
- the electrolytic cell 365 is to decompose by electrolysis at least some of the salts present in the RO concentrate into more reactive species which are either oxidizing biocides or can be further reacted into oxidizing biocides.
- the electrolytic cell 365 may be any known in the art designed for electrolysis of aqueous salt solutions, such as those commercially available for brine/seawater processing. Exemplary systems are available under the trade name SEACLOR® from Severn Trent De Nora located in Sugarland, Tex.
- the electrolytic cell 365 is integrated into the water treatment system 300 for in-situ derivation of oxidizing species from the RO concentrate stream 114 which is high in salts separated from the vessel effluent stream 307 .
- Chlorides concentration in the RO reject will be typically 4-5 times as high as that of the vessel effluent stream 307 , but 1-2 orders of magnitude lower concentration than sea water.
- chloride salts e.g., NaCl
- a reactive chlorine-containing species such as, but not limited to one or more of chlorine (Cl 2 ), hypochlorite (ClO ⁇ ), chlorine dioxide (ClO 2 ), and chloride ions (CO with byproducts including aqueous sodium hydroxide (NaOH).
- the reactive chlorine-containing species may be further reacted with one or more constituents in the RO concentrate stream 114 .
- nitrogen sources e.g. ammonia (NH 3 )
- NH 3 ammonia
- the treatment system 300 is disinfected by the oxidizing biocides derived from the RO and electrolysis processes.
- Operation 470 may be performed continuously during operation of the treatment system 300 or intermittently as a service flow method.
- the electrolytic cell 365 is coupled to at least one of the filtration vessel 305 and RO unit 110 .
- a backwash apparatus 362 is coupled to both the electrolytic cell effluent stream 368 and the RO bypass stream 112 .
- the backwash apparatus 362 intermittently provides a liquid back-pulse 372 from an effluent side to an influent side of the membrane filter 306 to clean the membrane pores (e.g., when MBR permeation is not pressurized).
- the backwash apparatus 362 may be of any design in the art with many variants being commercially available for this purpose. Because the liquid back-pulse contains the oxidizing species (biocides), the membrane filter 306 is also disinfected by the liquid back-pulse with the biocide concentration determined by mixture of the electrolytic cell effluent stream 368 and the RO bypass stream 112 , both of which are pressurized by the hydraulic pump 120 .
- the filtration vessel 305 may also be disinfected by a periodic supply of oxidizing species provided by the backwash apparatus 362 .
- the liquid back-pulse being pressurized by the hydraulic pump 120 , overall system design is simplified and capital costs reduced since a separate, dedicated metering system is not required.
- the electrolytic cell 365 has an outlet coupled downstream of the filtration vessel 305 for conduction of the oxidizing species (biocide) to an inlet or outlet (not depicted) of the RO unit 110 , as driven by the pressure of the RO concentrate stream 514 .
- an electrolytic cell effluent stream 369 is introduced into the filtered effluent stream 307 upstream of the hydraulic pump 120 (low pressure side) for injection into the RO unit 110 .
- RO membranes are therefore also disinfected at the operation 470 ( FIG. 4 ), either continuously or by periodic feed from the electrolytic cell 365 .
- chloramines are generated by the system 300 , negative effects of chlorination to the RO membrane(s) in the RO unit 110 may be reduced.
- FIG. 5 illustrates a flow path diagram for a water treatment system 500 integrating treatment, membrane filtration, and RO with energy recovery and disinfection systems, in accordance with an embodiment of the present invention.
- FIG. 5 is described in the context of FIG. 6 , illustrating operations of an exemplary water treatment method 600 that may be performed by the water treatment system 500 .
- an aqueous solution having impurities of any type is received as the influent stream 101 ( FIG. 5 ) to a solids separator 503 for pretreatment.
- a solids separator 503 upstream of the solids separator 503 is a diversion valve, allowing discharge of any non-treated wastewater into a municipal sewer 502 , for example when the treatment system 500 is taken out of service or when influent exceeds capacity of the system. This guarantees full reliability of the installation.
- the aqueous solution continuously flows by gravity into the solids separator 503 .
- the solids separator 503 removes course particulates and/or grease etc. that may otherwise interfere with subsequent treatment processes. Any solids separator known in the art to have this functionality may be employed as the present invention is not limited in this context.
- the solids separator 503 is equipped with a drain connected to the municipal sewer 502 (or a retention vessel, etc.) to prevent excessive solids and grease accumulation.
- Separator effluent stream 504 overflows to the reactor 505 .
- at least one of biological, chemical (e.g., oxidation or chemical precipitation, etc.), or physical-chemical (e.g., flocculation) treatment of the aqueous solution is performed within the reactor 605 as the main treatment operation, depending on the quality of the separator effluent stream 504 , process requirements, etc.
- the reactor 505 may operate as energy efficient anaerobic digester.
- the reactor 505 may operate as flocculation tank.
- the reactor 505 is a first vessel of an MBR where organics are biologically decomposed and ammonia partially oxidized.
- carrier media are disposed in the reactor 505 for support of attached biomass to prevent biomass from being washed-out. Sufficient biomass concentration may therefore be maintained without recycling during operation even if solids are drained from reactor 505 to municipal sewer 502 .
- Any carrier media known art for moving bed bioreactors (MBBR) may be utilized as the embodiments of the present invention are not limited in this respect.
- Treated effluent 507 flows into the filtration vessel 305 which includes the membrane filter 306 .
- the treated effluent 507 is polished in the filtration vessel 305 .
- aerobic biologic treatment is performed in the filtration vessel 305 .
- biological treatment performed in the reactor 505 and/or the filtration vessel 305 may be without any pH control and with the biological treatment leaving residual nitrogen in the treated effluent 507 .
- the membrane filter 306 is submerged within the filtration vessel 305 with an effluent side of the filter 306 passing through a wall of the filtration vessel 305 to filter the treated effluent at operation 608 .
- scouring elements 353 are also disposed within the filtration vessel 305 .
- the scouring elements 353 are displaceable within the filtration vessel 305 , for example by gas introduced into the filtration vessel 305 . Displacement of the scouring elements 353 is to mechanically scour an influent side of the membrane filter 306 . Additionally, any suspended biomass present in the filtration vessel 305 may also utilize the scouring elements as a support media to further enhance biological treatment and improve biomass retention.
- the scouring elements 353 are inert particles freely suspendable within the filtration vessel 305 and may be, for example, plastic beads, silica slurry, or the like.
- the scouring elements 353 are to be too large to pass through the membrane filter 306 and indeed may be many orders of magnitude larger and sufficiently large and of a shape to avoid becoming packed into a cake by flux across the membrane filter 306 and to avoid damaging the membrane file 306 through abrasion.
- aeration of the vessel 305 is performed in proximity to the influent side of the membrane filter, for example in any manner known in the art capable of air scouring the membrane filter 306 and this aeration provides motive force to the scouring elements 353 .
- Contact induced by the displacement of the scouring particles provides the mechanical scouring of the membrane filter 306 .
- the membrane filter 306 is surrounded by a retainer which is to retain the scouring elements 353 in proximity to the influent side of the filter 306 and thereby improve their scouring efficiency. Absent such a retainer limiting the displacement of the scouring elements to within a confined subregion of the filtration vessel 305 , the scouring elements 353 may tend to collect in locales away from the membrane filter 306 (e.g., in the relatively stagnant regions of the filtration vessel 305 ).
- FIG. 3B depicts an expanded isometric view of the membrane filter 306 with a scouring element retainer 326 .
- a conventional columnar membrane filter 306 includes fibers 316 which are exposed to the bulk liquid (e.g., in the filtration vessel 305 ).
- the retainer 326 Surrounding the columnar filter is the cylindrically-shaped scouring element retainer 326 .
- the retainer 326 has a diameter larger than that of the membrane filter 306 to provide an annular region surrounding the membrane filter 306 inside of which the scouring elements 353 are to be retained.
- the retainer 326 may be of any material (e.g., PTFE, ceramic, stainless steel, etc.) and any structure (e.g., meshed, gridded, windowed, etc.) which allows for air/liquid exchange while still serving to confine the scouring elements 353 .
- the souring elements 353 are to be disposed loosely within the annular space between the membrane fibers 316 and the retainer 326 so as to be movable by an external motive force, such as the aeration and/or pressurization gas stream 142 .
- the filtered effluent stream 307 is collected in an RO feed tank 509 , providing volume equalization and a pressure head for the hydraulic pump 120 to drive the filtered effluent stream 511 through the RO unit 110 (and one or more scale abatement systems 587 disposed there between).
- the RO feed tank 509 may also serve to separate gas bubbles from the MBR, reducing cavitation at the hydraulic pump 120 .
- the treatment system 500 relies on the single hydraulic pump 120 for operation.
- integration of the RO unit 110 is such that energy is recovered from the RO unit 110 at operation 650 substantially as was described for FIGS. 1 and 2 and is applied to affect processing in any or all of the operations 605 , 607 and 608 , as denoted by the dashed lines in FIG. 6 .
- Disinfectant derived in-situ from operation of the RO unit 110 is also applied, substantially as described in the context of FIGS. 3 and 4 , to affect processing in any or all of the operations 608 and 610 , as denoted by the dashed lines in FIG. 6 .
- FIG. 1 energy is recovered from the RO unit 110 at operation 650 substantially as was described for FIGS. 1 and 2 and is applied to affect processing in any or all of the operations 605 , 607 and 608 , as denoted by the dashed lines in FIG. 6 .
- Disinfectant derived in-situ from operation of the RO unit 110 is also applied, substantially as described in the context of FIGS. 3 and 4 , to affect processing
- the electrolytic cell 365 has an effluent stream 369 coupled the RO feed tank 509 such that generated biocides (e.g., chloramines where the concentrate stream 514 includes residual inorganic nitrogen) are provided downstream of the filtration vessel 305 and upstream of the hydraulic pump 120 to introduce the biocides to an influent side of the RO unit without a separate metering system.
- generated biocides e.g., chloramines where the concentrate stream 514 includes residual inorganic nitrogen
- pressurized RO permeate stream 514 drives a hydraulic mixer 550 (which is drawn to represent both the motor 130 and mixer 150 ), as previously described for the mixer 150 in system 100 .
- Mixer effluent stream 537 may then be reintroduced as a stream 538 to the solids separator 503 or discharged to the municipal sewer 502 .
- An RO bypass stream 512 drives a hydraulic air compressor 540 substantially as previously described for the compressor 140 in system 100 with the hydraulic air compressor 540 aerating the aerobic biological process performed in the (MBR) filtration vessel 305 via air inlet 536 .
- air may also be similarly introduced into the reactor 505 .
- the air introduced by the hydraulic air compressor 540 also displaces any scouring elements disposed in the filtration vessel 305 to mechanically scour the influent side of the filter 306 .
- the filtration vessel 305 may also be intermittently pressurized above ambient conditions by the air introduced from the hydraulic air compressor 540 to drive the treated effluent 507 through the membrane filter 306 .
- FIG. 7A illustrates a cross-sectional side view of an exemplary water treatment and membrane filtration apparatus 700 which may be utilized in the water treatment system illustrated in the FIG. 5 , in accordance with embodiments of the present invention.
- FIG. 7B illustrates a plan view of the water treatment and membrane filtration apparatus 700 .
- the reactor 505 is defined by an inner chamber wall 733 with lines disposed therein for receiving the separator effluent stream 504 and a drain line, for example to the municipal sewer 502 .
- the exemplary reactor 505 is sized to provide a hydraulic retention time (HRT) of between 2 and 4 hr.
- the hydraulic mixer 550 is disposed on a top of the apparatus 700 with the mixing shaft 552 attached thereto.
- the filtration vessel 305 defined as an annular space between the inner chamber wall 733 and an outer chamber wall 734 and sized to provide an exemplary HRT 0.5-1 hr.
- a plurality of the membrane filter 306 are equally spaced within the annularly shaped filtration vessel.
- the reactor 505 includes carrier media 757 disposed therein while the filtration vessel 305 includes scouring elements 753 .
- Coupled to an effluent side of the membrane filter 306 are lines for conducting the filtered effluent stream 307 to the RO feed tank 509 further having line out for the filtered effluent stream 511 .
- Air inlets 536 A and 536 B couple air from the hydraulic compressor 540 ( FIG. 5 ) into the reactor 505 and filtration vessel 305 , respectively.
- a backflow prevention mechanism 762 e.g., a plurality of check valves embedded in the inner wall 733 ) separates the reactor 505 from the filtration vessel 305 to prevent backflow of the treated effluent 507 when a pressure control device 534 (e.g., an automated air vent) causes the filtration vessel 305 to be pressurized above that of the reactor 505 via the air inlet 536 B.
- a pressure control device 534 e.g., an automated air vent
- FIG. 8 is a flow diagram illustrating a water treatment method 800 which may be performed by the water treatment and membrane filtration apparatus 700 .
- the method 800 should therefore be considered an exemplary sequence of operations implementing an advantageous mode of the treatment and filtration operations generally described in reference to FIGS. 5 and 6 .
- Method 800 begins with operation 601 where, as previously described, aqueous solution for treatment is received by the reactor 505 (inner vessel).
- the reactor 505 operates between low and high level sensors 752 A, for example corresponding to approximately 15% of the reactor volume.
- the reactor 505 is continuously mixed, for example via the hydraulic mixer 550 , and aerated, for example via the hydraulic air compressor 540 .
- biomass is grown on the surface of the plastic carriers 757 as well as freely suspended in the reactor.
- the pressure control device 534 is actuated (e.g., opened) at operation 863 to equilibrate the pressure between the reactor 505 and filtration vessel 305 , allowing for solution levels between the reactor 505 and filtration vessel 305 to equilibrate at operation 865 via the backflow prevention mechanism 762 . Screening retains biomass carriers 757 in the reactor 505 .
- method 800 returns to operation 266 where the pressure control device 534 actuates (e.g., closes) to allow pressure in the filtration vessel 305 to increase via air introduced through air inlet 636 B. The increased pressure drives flux across the (microfiltration) membrane filter 306 at operation 857 .
- the level in the filtration vessel decreases due to permeation through the membrane filter 306 with the filtered effluent stream 307 being output to the RO feed tank 509 at operation 859 . While the pressure control device 534 operates to elevate the filtration vessel pressure, the level in the reactor 505 will continue to increase due to influent stream 101 .
- level sensors 752 B actuate the pressure control device 534 to reduce pressure to ambient. Solution flux through the membranes(s) 306 is thereby reduced to avoid drying out the membranes or forming a biomass cake.
- permeate flux may be zero and utilized for the membrane back-pulse described elsewhere herein (i.e., flux reversed).
- the RO feed tank 509 also operates between low and high level sensors 752 C.
- the tank is elevated by height H relative to the filtration vessel 305 to provide sufficient minimum head to the hydraulic pump 120 .
- an RO feed valve downstream of the RO feed tank 509 FIG. 5
- downstream of the RO bypass, 513 A and 513 B, respectively close at operation 872 .
- RO bypass return 521 recirculates the RO bypass stream 512 after driving the hydraulic air compressor 540 back to the filtered effluent (permeate) stream 511 , downstream the RO feed valve 513 A.
- the pressure control device 534 Upon the level reaching the high level sensor (e.g., permeate flow from filtration vessel 305 exceeds capacity of the RO unit 110 ), the pressure control device 534 is actuated at operation 874 to reduce filtration vessel pressure and thereby interrupt permeate flow.
- the RO feed tank level is between the level sensors, the RO feed valves 513 A and 513 B are open, allowing permeation (generating final quality permeate stream 595 ) at operation 685 .
- the hydraulic pump 120 drives permeation through the RO unit 110 and also supplies hydraulic power to drive the aeration, mixing, and pressurization of the filtration vessel, as well as other maintenance operations, when the RO feed is interrupted, the hydraulic pump 120 continues to recirculate RO feed quality water through the RO bypass stream 512 and back to an inlet of the hydraulic pump 120 (through the return 521 ).
- the pressure at the pump inlet is adjusted to be equal to the low level head of the RO feed tank, allowing both streams to feed the pump simultaneously when filtered effluent (permeate) stream 511 is available.
- a number of service flows may also be performed either simultaneously or cyclically with the method 800 .
- the electrolytic cell 365 generates a low-level of oxidizing species (e.g., chlorine) from the RO concentrate stream 514 , as described elsewhere herein.
- the electrolytic cell 365 operates continuously with the retention time (and as a result the chlorine concentration) controlled by timer. Injection of the oxidizing species (biocide) may be triggered upon activating the RO feed valve.
- the back-pulse as described elsewhere herein is injected into the membrane regularly when the pressure control device 534 is actuated to reduce filtration vessel pressure. The duration of the back-pulse may be controlled by timer or pressure regulated.
- excess sludge from the reactor 505 will overflow to the filtration vessel 305 .
- Other system rinses may also be performed periodically.
- the pressurized RO concentrate stream 514 may be used for the rinses in the solids separator 503 , discharging into the municipal sewer 502 .
- rinses downstream of the filtration vessel 305 may use pressurized recirculation flow via the RO bypass stream 512 .
- Uninterrupted processing of the influent stream 101 occurs when the treatment system 500 operates normally. However, one or more of a number interlocks may be triggered in response to a system malfunction. For example, in the absence of the influent stream 101 , the level in both the reactor 505 and filtration vessel 305 will reach the respective low levels with aeration continued to maintain biomass activity. Interruption of a sufficient duration will lead to interruption of the RO unit 110 . An absence of the RO concentrate stream 514 will halt the hydraulic mixer 550 . In this case, mixing is provided by aeration only. In the event of a toxic feed, pH meter 583 will register a change in the reactor 505 and/or filtration vessel 305 , generating an alarm and/or operator response.
- FIG. 9 is a water treatment system architecture 900 in which the integrated water treatment system 500 may be implemented within an existing POTW, in accordance with an embodiment of the present invention.
- the water treatment system 500 receives the influent stream 101 from one or more upstream commercial water uses 910 A, 910 B and/or household water uses 920 A, 920 B and returns a processed effluent for one or more downstream commercial water uses 940 A, 940 B or household water uses 950 A.
- the downstream uses may be the same as the upstream uses (e.g., a car wash) or may be downgraded (e.g., laundry upstream, car wash downstream, etc.).
- the treatment system 500 is scaled to be completely contained within a conventional tractor trailer/shipping container 599 .
- the treatment system 500 is capable of mobile, distributed point of use treatment which can reduce loading on the primary municipal treatment facilities and differentia water qualities based on use.
- the treatment system 500 can accommodate an average influent stream volumetric flow rate of up to 10,000 gal per day, depending on the quality of the influent stream 101 .
- connection to the municipal sewer 502 provides a failsafe as well as a means to dispose of separated solids, etc. in a more concentrated form.
Abstract
Integrated membrane treatment systems for treatment of an aqueous solution. In embodiments, components, such as an MBR, are integrated with means to recover energy from the system, for example from an RO concentrate, to operate the other components. In embodiments including biological treatment, RO is integrated with other components, such as an MBR with the ROs ability to remove inorganic nitrogen enabling biological treatment to be performed with only partial nitrification and the MBR operated without active pH control. In embodiments, RO is integrated with a chlorine generator to convert chlorides present in the RO concentrate for an in-situ source of oxidizing biocides for disinfection purposes. Chloramines may be generated in-situ from residual ammonia and chlorides in the RO reject. In embodiments, carrier media is employed in a membrane tank to enhance removal of residual organics by the MBR and to also improve effectiveness of membrane scouring.
Description
- This is a Divisional application of Ser. No. 13/195,746 filed Aug. 1, 2011, which is hereby incorporated by reference.
- Embodiments of the invention relate to water and wastewater treatment and more particularly to integrated membrane treatment systems.
- There are many technologies for water/wastewater treatment with practically no limit to water quality achievable when treating a majority of the existing water/wastewater streams. Biological treatment is the most widely used technology. It utilizes metabolism of microorganisms to remove organic matter, as well as other dissolved nutrients including nitrogen and phosphorus. Biological mass (biomass) is also known to adsorb heavy metals, suspended solids, and other sorts of contaminants which do not undergo biological degradation. Biomass is separated from the treated liquid, thus allowing for discharge of treated water (effluent) and disposal of the excess of the biomass (sludge). Depending on the quality of the water for treatment (influent), two biological treatment methods are typically used separately or in combination. A first is anaerobic treatment, which does not require aeration (addition of dissolved oxygen). The other is aerobic treatment, utilizing dissolved oxygen in the biological treatment.
- For concentrated wastewater streams, anaerobic treatment is commonly used to achieve partial degradation of the contamination. Although aerobic treatment consumes more energy than anaerobic treatment, aerobic treatment is often used to achieve a more rapid and complete removal of the organic pollutants. The activated sludge method is an example of an aerobic biological treatment for municipal wastewater containing a relatively low level of organic impurities using biomass mixed with the treated liquid.
- Recent development in wastewater treatment technology have demonstrated integration of a filtration membrane (micro or ultra) with activated sludge or anaerobic treatment provides effective method of sludge separation and process control, achieving more efficient treatment. Such a combination is called a Membrane Bioreactor (MBR). However, the effluent produced by biological treatment and microfiltration is insufficient for significant number of uses as the effluent contains bacteria, viruses, and residual amounts of organic and inorganic contaminants. Therefore additional treatment, such as chemical disinfection, UV disinfection, ion exchange, sorption, etc. is common. Because of limitations in treatment efficiency, these technologies are often used in combination, resulting in high treatment cost.
- Reverse Osmosis (RO) technology is another commonly used process which provides high treatment efficiency. RO membranes effectively remove suspended solids (including viruses and bacteria), often with higher efficiency and reliability than MBR. RO membranes also remove inorganic matter (including dissolved salts, thus providing softening effect). RO can also remove high molecular weight dissolved organics, which is typically a main fraction of the biological treatment effluent.
- However, conventional implementations of both MBR and RO technologies have significant drawbacks resulting in high treatment cost. For example, MBR requires a long retention time to ensure efficient nitrogen removal. This long retention time translates into large footprint and higher capital cost. Also, conventional MBR implementations require a large number of units of mechanical equipment, including hydraulic pumps, blowers, compressors, vacuum pumps, etc. This again increases capital cost and maintenance cost, and raises reliability concerns.
- Deficiencies in conventional RO implementations include high-energy consumption and high pretreatment cost. Another problem with treating MBR effluent by RO is bio-fouling of RO membranes. Controlling bio-fouling by disinfection is difficult due to the fact that oxidizing biocides may attack the membrane material and adversely affect membrane performance. Disinfection also typically entails a use of chemicals which require special permits and adds operational complexity
- In view of recent trends in environmental/health regulations, as well as greater public awareness of the importance of clean water, decentralized small-scale treatment technologies are expected to become more important. Generally, when scaling the typical applications down, the cost of each volumetric unit of the treated water increases exponentially. More particularly, the operational difficulties, permitting, and concomitant costs described above have thus far limited application of these treatment technologies to large treatment plants of a size of the POTW (publicly owned treatment works). Furthermore, systems designed to overcome the constraints typical of smaller scale systems may also prove to be cost competitive for implementations at the POTW scale.
- Embodiments of the present invention integrated membrane systems which when operated independently are comparatively less efficient. The integrated systems enable efficient operation across a wide range of volumetric flows for scalability that is well-suited to a distributed treatment model. In certain embodiments, the integrated treatment systems described herein are implemented for distributed treatment within a framework of an existing sewerage system.
- In embodiments, RO is integrated with other components of a water treatment system, such as a biological unit, or an MBR, to recover energy from the RO unit, for example from the RO concentrate (reject), to operate the other components. In one such embodiment, a single hydraulic pump is harnessed to operate the majority of the treatment system. As such, synergy between the RO and other components of the system simplify operation and maintenance of the water treatment system.
- In embodiments, RO is integrated with other components of a water treatment system, such as a biological unit, or an MBR, to leverage the RO's ability to remove inorganic nitrogen. In certain such embodiments, removal of nitrogen by RO enables biological treatment to be performed incompletely, thereby advantageously reducing retention times. In further embodiments, reliance on the RO for nitrogen removal enables biological treatment to be performed with only partial nitrification (oxidation of ammonia to nitrate) further enabling the biological treatment to be performed with no pH control. In embodiments with no pH control, pH freely varies as a function of the wastewater influent quality and level of biological activity sustainable with no active pH control. As such, ammonia may exist in the treated water with the pH most likely dropping below 7. With no active pH control, chemical use and handling is reduced. As such, synergy between the RO and other components of the system simplify operation and maintenance of the water treatment system.
- In embodiments, RO is integrated with a chlorine generator to convert chlorides present in the RO concentrate for an in-situ source of oxidizing biocides for disinfection purposes. In certain such embodiments, where biological treatment is performed incompletely, residual inorganic nitrogen in the RO concentrate (present because of the partial nitrification) is further utilized, along with the chlorides to derive chloramines for disinfection purposes. In further embodiments, the pressurized RO concentrate is utilized to drive service flows employing the disinfectant so that a separate metering system is not required. As such, a synergy between the RO and other components of the system reduces system complexity, chemical use, and improves membrane lifetimes.
- In embodiments, carrier media is employed in a membrane tank to improve effectiveness of membrane scouring through mechanical agitation by the carrier media and potentially enhance removal of residual organics by the MBR.
- Embodiments of the present invention are illustrated by way of example, and not limitation, in the figures of the accompanying drawings in which:
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FIG. 1 illustrates a flow path diagram for water treatment system with an energy recovery system for integrated treatment and/or filtration of an aqueous solution, in accordance with an embodiment of the present invention; -
FIG. 2 illustrates a water treatment method which may be performed by water treatment system illustrated inFIG. 1 to employ RO and recover energy there from for integrated treatment and/or filtration of an aqueous solution, in accordance with an embodiment of the present invention; -
FIG. 3A illustrates a flow path diagram for a water treatment system with an RO salt electrolysis system for integrated disinfection of the system and aqueous solution treated by the system, in accordance with an embodiment of the present invention; -
FIG. 3B illustrates an isometric view of a membrane filter, scouring elements, and scouring element retainer, in accordance with an embodiment of the present invention; -
FIG. 4 illustrates a water treatment method which may be performed by water treatment system illustrated inFIG. 3A to convert salts recovered from an RO concentrate into oxidizing biocides for integrated disinfection of the system and the aqueous solution treated by the system, in accordance with an embodiment of the present invention; -
FIG. 5 illustrates a flow path diagram for a water treatment system integrating treatment, membrane filtration, and RO with energy recovery and disinfection systems, in accordance with an embodiment of the present invention; -
FIG. 6 illustrates a water treatment method which may be performed by water treatment system illustrated inFIG. 5 to integrate treatment, membrane filtration, and RO with energy recovery and disinfection, in accordance with an embodiment of the present invention; -
FIG. 7A illustrates a cross-sectional side view of a water treatment and membrane filtration apparatus which may be utilized in the water treatment system illustrated in theFIG. 5 , in accordance with embodiments of the present invention; -
FIG. 7B illustrates a plan view of the water treatment and membrane filtration apparatus illustrated inFIG. 7A , in accordance with embodiments of the present invention; -
FIG. 8 illustrates a water treatment method which may be performed by the water treatment and membrane filtration apparatus illustrated inFIGS. 7A , 7B to implement the treatment and filtration operations illustrated inFIG. 6 , in accordance with an embodiment of the present invention; and -
FIG. 9 is a water treatment system architecture in which the integrated water treatment system illustrated inFIG. 5 may be implemented within an existing sewer or industrial treatment system, in accordance with an embodiment of the present invention. - Described herein are integrated membrane water treatment systems and water treatment methods which may be performed by such systems. In the following description, numerous specific details are set forth, such as exemplary treatment and filtration apparatuses to describe embodiments of the present invention. However, it will be apparent to one skilled in the art that embodiments of the present invention may be practiced without such specific details. In other instances, well-known aspects, such as specific biological treatment techniques, solids separation techniques, etc. and associated hardware, are not described in detail to avoid unnecessarily obscuring embodiments of the present invention.
- Reference throughout this specification to “an embodiment” means that a particular system component or operative sequence described in connection with the embodiment is included in at least one embodiment of the invention. Thus, use of the phrase “in an embodiment” in various places throughout this specification are not necessarily referring to the same embodiment of the invention. Furthermore, exemplary system components or operative sequences may be combined in any suitable manner in one or more embodiments. Also, it is to be understood that the various exemplary embodiments shown in the Figures are merely illustrative representations, are not to scale, and are not exclusive of additional hardware and/or operations which remain otherwise consistent with system operation. In the figures, reference numbers are retained where convenient for the sake of avoiding duplicative description of components shared between embodiments.
- The terms “coupled” and “in fluid communication,” are used herein to describe structural and functional relationships between components, respectively. Two components “coupled” together are in either direct or indirect (with other intervening components between them) physical contact with each other. Two components “in fluid communication” are coupled in a manner such that a fluid from one component is capable of flowing to the other component.
- Generally, the systems described herein are for the removal of any contaminant from any aqueous solution. Therefore, the term “water treatment” is employed herein in its broadest sense to mean removal of a contaminant, be it by solids separation, chemical, physical, biological treatment, etc. Similarly, any reference to “wastewater” is to be understood as a label for any aqueous solution having an impurity level which is to be improved, be it domestic sewage effluent, industrial effluent, or non-point source runoff, etc. Exemplary embodiments describing the treatment of any specific classes or types of wastewater are therefore merely to emphasize the broad applicability of the present invention.
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FIG. 1 illustrates a flow path diagram for awater treatment system 100 with an energy recovery system for integrated treatment and/or filtration of an aqueous solution, in accordance with an embodiment of the present invention.FIG. 1 is described in the context ofFIG. 2 , illustrating operations of an exemplarywater treatment method 200 that may be performed by thewater treatment system 100. - Beginning at
operation 201, an aqueous solution having impurities of any type (i.e., “wastewater”) is received as the influent stream 101 (FIG. 1 ) to avessel 105. In certain embodiments, the wastewater is preferably with a brackish salinity level to provide a source of salts which are employed as an in-situ source of biocides, as described further herein. - At operation 205 (
FIG. 2 ), at least one of filtration, aerobic or anaerobic biological treatment, chemical treatment (e.g., oxidation of Mn and Fe, etc. or chemical precipitation such as HF waste with CaCl2, etc.), or physical-chemical treatment (e.g., coagulation or flocculation) of the aqueous solution is performed within thevessel 105. The term “filtration” is employed here, as well as throughout the remainder description, to refer to either microfiltration or ultrafiltration, as the present invention is not limited in that respect. - In an embodiment, processed effluent from the
vessel 105 is utilized to drive one or more activities occurring in thevessel 105. In the exemplary implementation, the processed effluent is driven downstream by ahydraulic pump 120 disposed downstream from thevessel 105. Energy may be recovered from thehydraulic pump 120 utilized to drive one or more activities performed in thevessel 105. In the depicted embodiment, the processed effluent is supplied into an influent side of anRO unit 110. The RO unit is drawn in dashed line to emphasize, that the energy recovery illustrated inFIG. 1 is not dependent on RO being performed downstream, though additional synergies are to be had for those embodiments employing an RO unit, as described elsewhere herein. - For embodiments herein employing RO, the
RO unit 110 may be of any design known in the art with many variants being commercially available to filter via a diffusive mechanism with separation efficiency being dependent on solute concentration, pressure, and flux rate rather than size exclusion as for membrane filtration. Effluent from the RO includes apermeate stream 116 and concentrate (reject)stream 114. Thepermeate stream 116, as the product of thewater treatment system 100 is provided to a downstream application, be it further purification or consumption. Although thehydraulic pump 120 is in fluid communication with both thevessel 105 and theRO unit 110, the breaks in theeffluent stream 107 denote that one or more intervening process vessels, process controls, etc. may be disposed there between. - As illustrated in
FIG. 1 , amotor 130 is driven with the pressurized vessel effluent atoperation 230. The hydraulically drivenmotor 130 may be of any design known in the art, with an exemplary system being the HydroDrive, commercially available from Hastec HydroDrives, Inc. of St. Catharines, Ontario, Canada. Depending on the embodiment, and as illustrated inFIG. 1 , the drive side of themotor 130 is in fluid communication with either or both theRO concentrate stream 114 or anRO bypass stream 112 disposed downstream of thehydraulic pump 120 and upstream of theRO unit 110, each of which provides a pressurized source with an associated pressure head and volumetric flow rate. - For embodiments where no RO is employed, at least some portion of effluent from the
pump 120 is utilized to drive one ormore motor 130 as coupled to either or both the compressor 140 (to provide aeration and/or pressurization gas stream 142) andmixer 150. Depending on the stream employed to drive themotor 130, themotor effluent stream 135 may be either reintroduced into the system upstream of the hydraulic pump 120 (e.g., returnedvessel effluent stream 107 whereRO bypass stream 112 drives the motor 130) or discharged to a waste drain (e.g., where theRO concentrate stream 114 drives the motor 130). For embodiments in which the drive side of themotor 130 is in fluid communication with theRO concentrate stream 114, themotor 130 provides a means of recovery residual energy remaining downstream of the RO unit. For embodiments in which the drive side of themotor 130 is in fluid communication with theRO bypass stream 112, themotor 130 provides a means to enable thehydraulic pump 120 to be a single energy source for thetreatment system 100. Thehydraulic pump 120 is therefore to be sized to accommodate the additional load associated with driving themotor 130. - With the
motor 130 having a drive side in fluid communication with thehydraulic pump 120, a driven side of themotor 130 is harnessed at operation 240 (FIG. 2 ) to power one or more action performed in thevessel 105. Although any processing action conventional in the art may be powered by themotor 130, exemplary embodiments include one or more of mixing, aerating, or pressurizing a filtration or biological, chemical, or physical-chemical treatment with at least some portion of effluent from thevessel 105. In one embodiment, the driven side of themotor 130 coupled to acompressor 140 having an inlet coupled to a gas source, such as ambient air, and an outlet coupled into thevessel 105 to pressurize the vessel (e.g., in the case of a filtration process occurring in thevessel 105, as described further elsewhere herein) or aerate processes performed in the vessel with the gas (e.g., air) introduced. Typically, for such an application, the drive side of themotor 130 is to be in fluid communication with theRO bypass stream 112 for a larger pressure head and volumetric flow rate. - In another embodiment, the
motor 130 has the driven side coupled to amechanical mixer 150 disposed within thevessel 105. For one such an embodiment, thevessel 105 may be operated as a CSTR with themixer shaft 152 driven by themotor 130. Depending on the load, the drive side of themotor 130 may be in fluid communication with either concentrate outlet of the RO unit 110 (to be driven by the concentrate stream 114) or in fluid communication with theRO bypass stream 112. In further embodiments,multiple motors 130 may be driven by the pressurized vessel effluent. For example, and as further described elsewhere herein, afirst motor 130 drives themixer 150 with theRO concentrate stream 114 while asecond motor 130 drives thecompressor 140 with theRO bypass stream 112. -
FIG. 3A illustrates a flow path diagram for awater treatment system 300 with an RO salt electrolysis system for integrated disinfection of the system and of the aqueous solution treated by the system, in accordance with an embodiment of the present invention.FIG. 3A is described in the context ofFIG. 4 illustrating an exemplary operation of awater treatment method 400 that may be performed by thewater treatment system 300. - Beginning at
operation 401, an aqueous solution having biodegradable impurities is received as the influent stream 304 (FIG. 3A ) to afiltration vessel 305. For the exemplary embodiment illustrated inFIG. 3A , aporous membrane filter 306 is submerged within thefiltration vessel 305 with an effluent side of thefilter 306 passing through a wall of thefiltration vessel 305 for solid separation in addition to biological treatment, for example in the case of an MBR. - In the exemplary embodiment, biological treatment at
operation 404 is performed incompletely, such that nitrogen (e.g., ammonia) is not completely removed. For example,operation 404 may have a corresponding solids retention time of between 1 and 15 days whereas in conventional systems designed for complete nitrogen removal retention time is typically 20 to 40 days. In further embodiments,operation 404 is performed without pH control. As such,operation 404, and indeed all the operations in theentire treatment system 300, is operated at whatever steady-state pH naturally occurs (e.g., as a function of the biological treatment process performed at operation 404). With nitrification occurring to some extent, steady-state pH is lowered, for example to be below 7. A lower pH inhibits biological processes as well as further nitrification. Allowing pH to drop freely to a relatively low level has the advantage of avoiding caustic addition, reduced oxygen demand and therefore a lower energy consumption for aeration, and reduced bio-fouling of themembrane filter 306. - Effluent from the
filtration vessel 305 is driven into an influent side of theRO unit 110 by thehydraulic pump 120 disposed downstream from thefiltration vessel 305. Inorganic nitrogen (ammonia, ammonium salt, etc.) remaining after thetreatment operation 404 is removed by the RO atoperation 406. RO permeatestream 116, as the product of thewater treatment system 300 is provided to a downstream application, be it further purification or consumption. For those embodiments where pH is allowed to drop freely (e.g., upon partial nitrification), scaling of the RO membrane will be advantageously reduced. Although thehydraulic pump 120 is in fluid communication with both thefiltration vessel 305 and theRO unit 110, the breaks in theeffluent stream 307 denote one or more intervening process vessels, process controls, etc. may be disposed there between. - In an embodiment of the present invention a chlorine generator is integrated with the
RO unit 110 for in-situ generation of biocides for disinfection. As further illustrated inFIG. 3A , anelectrolytic cell 365 is in fluid communication with the concentrate outlet of theRO unit 110. Theelectrolytic cell 365 is to decompose by electrolysis at least some of the salts present in the RO concentrate into more reactive species which are either oxidizing biocides or can be further reacted into oxidizing biocides. Theelectrolytic cell 365 may be any known in the art designed for electrolysis of aqueous salt solutions, such as those commercially available for brine/seawater processing. Exemplary systems are available under the trade name SEACLOR® from Severn Trent De Nora located in Sugarland, Tex. While such systems are typically designed to generate biocides from a seawater influent or high concentration sodium chloride solution, for embodiments of the present invention theelectrolytic cell 365 is integrated into thewater treatment system 300 for in-situ derivation of oxidizing species from theRO concentrate stream 114 which is high in salts separated from thevessel effluent stream 307. Chlorides concentration in the RO reject will be typically 4-5 times as high as that of thevessel effluent stream 307, but 1-2 orders of magnitude lower concentration than sea water. - In the exemplary method illustrated in
FIG. 4 , chloride salts (e.g., NaCl) in theRO concentrate stream 114 are decomposed atoperation 465 to produce a reactive chlorine-containing species, such as, but not limited to one or more of chlorine (Cl2), hypochlorite (ClO−), chlorine dioxide (ClO2), and chloride ions (CO with byproducts including aqueous sodium hydroxide (NaOH). Depending on the other constituents in theRO concentrate stream 114, the reactive chlorine-containing species may be further reacted with one or more constituents in theRO concentrate stream 114. As further illustrated inFIG. 4 , atoperation 466, nitrogen sources (e.g. ammonia (NH3)) inRO concentrate stream 114 react with the reactive chlorine-containing species form chloramines, such as, but not limited to, monochloramine ClNH2. - At
operation 470, thetreatment system 300, as well as the filteredeffluent stream 307 itself in certain embodiments (e.g., in generation of drinking water), is disinfected by the oxidizing biocides derived from the RO and electrolysis processes.Operation 470 may be performed continuously during operation of thetreatment system 300 or intermittently as a service flow method. As further illustrated inFIG. 3A , theelectrolytic cell 365 is coupled to at least one of thefiltration vessel 305 andRO unit 110. In one embodiment, abackwash apparatus 362 is coupled to both the electrolyticcell effluent stream 368 and theRO bypass stream 112. Thebackwash apparatus 362 intermittently provides a liquid back-pulse 372 from an effluent side to an influent side of themembrane filter 306 to clean the membrane pores (e.g., when MBR permeation is not pressurized). Thebackwash apparatus 362 may be of any design in the art with many variants being commercially available for this purpose. Because the liquid back-pulse contains the oxidizing species (biocides), themembrane filter 306 is also disinfected by the liquid back-pulse with the biocide concentration determined by mixture of the electrolyticcell effluent stream 368 and theRO bypass stream 112, both of which are pressurized by thehydraulic pump 120. Similarly, thefiltration vessel 305 may also be disinfected by a periodic supply of oxidizing species provided by thebackwash apparatus 362. In the preferred embodiment, with the liquid back-pulse being pressurized by thehydraulic pump 120, overall system design is simplified and capital costs reduced since a separate, dedicated metering system is not required. - In another embodiment, the
electrolytic cell 365 has an outlet coupled downstream of thefiltration vessel 305 for conduction of the oxidizing species (biocide) to an inlet or outlet (not depicted) of theRO unit 110, as driven by the pressure of theRO concentrate stream 514. In the illustrative embodiment, an electrolyticcell effluent stream 369 is introduced into the filteredeffluent stream 307 upstream of the hydraulic pump 120 (low pressure side) for injection into theRO unit 110. RO membranes are therefore also disinfected at the operation 470 (FIG. 4 ), either continuously or by periodic feed from theelectrolytic cell 365. For embodiments where chloramines are generated by thesystem 300, negative effects of chlorination to the RO membrane(s) in theRO unit 110 may be reduced. - In further embodiments, the components illustrated in the
treatment systems FIG. 5 illustrates a flow path diagram for awater treatment system 500 integrating treatment, membrane filtration, and RO with energy recovery and disinfection systems, in accordance with an embodiment of the present invention.FIG. 5 is described in the context ofFIG. 6 , illustrating operations of an exemplarywater treatment method 600 that may be performed by thewater treatment system 500. - Beginning at
operation 601, an aqueous solution having impurities of any type (i.e., “wastewater”) is received as the influent stream 101 (FIG. 5 ) to asolids separator 503 for pretreatment. In the exemplary embodiment of municipal wastewater treatment, upstream of thesolids separator 503 is a diversion valve, allowing discharge of any non-treated wastewater into amunicipal sewer 502, for example when thetreatment system 500 is taken out of service or when influent exceeds capacity of the system. This guarantees full reliability of the installation. - In the exemplary embodiment, the aqueous solution continuously flows by gravity into the
solids separator 503. Atoperation 603, thesolids separator 503 removes course particulates and/or grease etc. that may otherwise interfere with subsequent treatment processes. Any solids separator known in the art to have this functionality may be employed as the present invention is not limited in this context. The solids separator 503 is equipped with a drain connected to the municipal sewer 502 (or a retention vessel, etc.) to prevent excessive solids and grease accumulation. -
Separator effluent stream 504 overflows to thereactor 505. At operation 605 (FIG. 2 ), at least one of biological, chemical (e.g., oxidation or chemical precipitation, etc.), or physical-chemical (e.g., flocculation) treatment of the aqueous solution is performed within thereactor 605 as the main treatment operation, depending on the quality of theseparator effluent stream 504, process requirements, etc. For embodiments where theseparator effluent stream 504 has a high organics content thereactor 505 may operate as energy efficient anaerobic digester. For embodiments where theseparator effluent stream 504 has low organics content with high solids content, thereactor 505 may operate as flocculation tank. For the illustrative embodiment of municipal wastewater treatment, thereactor 505 is a first vessel of an MBR where organics are biologically decomposed and ammonia partially oxidized. In one MBR embodiment, carrier media are disposed in thereactor 505 for support of attached biomass to prevent biomass from being washed-out. Sufficient biomass concentration may therefore be maintained without recycling during operation even if solids are drained fromreactor 505 tomunicipal sewer 502. Any carrier media known art for moving bed bioreactors (MBBR) may be utilized as the embodiments of the present invention are not limited in this respect. -
Treated effluent 507 flows into thefiltration vessel 305 which includes themembrane filter 306. Atoperation 607, the treatedeffluent 507 is polished in thefiltration vessel 305. For a municipal wastewater treatment embodiment for example, aerobic biologic treatment is performed in thefiltration vessel 305. As previously described in the context of thesystem 300, biological treatment performed in thereactor 505 and/or thefiltration vessel 305 may be without any pH control and with the biological treatment leaving residual nitrogen in the treatedeffluent 507. Themembrane filter 306 is submerged within thefiltration vessel 305 with an effluent side of thefilter 306 passing through a wall of thefiltration vessel 305 to filter the treated effluent atoperation 608. - In advantageous embodiments, scouring
elements 353 are also disposed within thefiltration vessel 305. The scouringelements 353 are displaceable within thefiltration vessel 305, for example by gas introduced into thefiltration vessel 305. Displacement of the scouringelements 353 is to mechanically scour an influent side of themembrane filter 306. Additionally, any suspended biomass present in thefiltration vessel 305 may also utilize the scouring elements as a support media to further enhance biological treatment and improve biomass retention. - In embodiments, the scouring
elements 353 are inert particles freely suspendable within thefiltration vessel 305 and may be, for example, plastic beads, silica slurry, or the like. The scouringelements 353 are to be too large to pass through themembrane filter 306 and indeed may be many orders of magnitude larger and sufficiently large and of a shape to avoid becoming packed into a cake by flux across themembrane filter 306 and to avoid damaging themembrane file 306 through abrasion. In the exemplary embodiment, aeration of thevessel 305 is performed in proximity to the influent side of the membrane filter, for example in any manner known in the art capable of air scouring themembrane filter 306 and this aeration provides motive force to the scouringelements 353. Contact induced by the displacement of the scouring particles provides the mechanical scouring of themembrane filter 306. - In advantageous embodiments employing the scouring
elements 353, themembrane filter 306 is surrounded by a retainer which is to retain the scouringelements 353 in proximity to the influent side of thefilter 306 and thereby improve their scouring efficiency. Absent such a retainer limiting the displacement of the scouring elements to within a confined subregion of thefiltration vessel 305, the scouringelements 353 may tend to collect in locales away from the membrane filter 306 (e.g., in the relatively stagnant regions of the filtration vessel 305).FIG. 3B depicts an expanded isometric view of themembrane filter 306 with a scouringelement retainer 326. As shown, a conventionalcolumnar membrane filter 306 includesfibers 316 which are exposed to the bulk liquid (e.g., in the filtration vessel 305). Surrounding the columnar filter is the cylindrically-shaped scouringelement retainer 326. Theretainer 326 has a diameter larger than that of themembrane filter 306 to provide an annular region surrounding themembrane filter 306 inside of which the scouringelements 353 are to be retained. Theretainer 326 may be of any material (e.g., PTFE, ceramic, stainless steel, etc.) and any structure (e.g., meshed, gridded, windowed, etc.) which allows for air/liquid exchange while still serving to confine the scouringelements 353. The souringelements 353 are to be disposed loosely within the annular space between themembrane fibers 316 and theretainer 326 so as to be movable by an external motive force, such as the aeration and/orpressurization gas stream 142. - The filtered
effluent stream 307 is collected in anRO feed tank 509, providing volume equalization and a pressure head for thehydraulic pump 120 to drive the filteredeffluent stream 511 through the RO unit 110 (and one or morescale abatement systems 587 disposed there between). TheRO feed tank 509 may also serve to separate gas bubbles from the MBR, reducing cavitation at thehydraulic pump 120. Again, in the preferred embodiment thetreatment system 500 relies on the singlehydraulic pump 120 for operation. - With the
permeate stream 595 provided for use atoperation 685, integration of theRO unit 110 is such that energy is recovered from theRO unit 110 atoperation 650 substantially as was described forFIGS. 1 and 2 and is applied to affect processing in any or all of theoperations FIG. 6 . Disinfectant derived in-situ from operation of theRO unit 110 is also applied, substantially as described in the context ofFIGS. 3 and 4 , to affect processing in any or all of theoperations FIG. 6 . For example, as shown inFIG. 5 , theelectrolytic cell 365 has aneffluent stream 369 coupled theRO feed tank 509 such that generated biocides (e.g., chloramines where theconcentrate stream 514 includes residual inorganic nitrogen) are provided downstream of thefiltration vessel 305 and upstream of thehydraulic pump 120 to introduce the biocides to an influent side of the RO unit without a separate metering system. - As illustrated in
FIG. 5 , pressurizedRO permeate stream 514 drives a hydraulic mixer 550 (which is drawn to represent both themotor 130 and mixer 150), as previously described for themixer 150 insystem 100.Mixer effluent stream 537 may then be reintroduced as astream 538 to thesolids separator 503 or discharged to themunicipal sewer 502. AnRO bypass stream 512 drives ahydraulic air compressor 540 substantially as previously described for thecompressor 140 insystem 100 with thehydraulic air compressor 540 aerating the aerobic biological process performed in the (MBR)filtration vessel 305 viaair inlet 536. - Though not depicted in
FIG. 5 , air may also be similarly introduced into thereactor 505. The air introduced by thehydraulic air compressor 540 also displaces any scouring elements disposed in thefiltration vessel 305 to mechanically scour the influent side of thefilter 306. In a preferred embodiment, thefiltration vessel 305 may also be intermittently pressurized above ambient conditions by the air introduced from thehydraulic air compressor 540 to drive the treatedeffluent 507 through themembrane filter 306. -
FIG. 7A illustrates a cross-sectional side view of an exemplary water treatment andmembrane filtration apparatus 700 which may be utilized in the water treatment system illustrated in theFIG. 5 , in accordance with embodiments of the present invention.FIG. 7B illustrates a plan view of the water treatment andmembrane filtration apparatus 700. - In
FIG. 7A , thereactor 505 is defined by aninner chamber wall 733 with lines disposed therein for receiving theseparator effluent stream 504 and a drain line, for example to themunicipal sewer 502. Theexemplary reactor 505 is sized to provide a hydraulic retention time (HRT) of between 2 and 4 hr. Thehydraulic mixer 550 is disposed on a top of theapparatus 700 with the mixingshaft 552 attached thereto. Thefiltration vessel 305 defined as an annular space between theinner chamber wall 733 and anouter chamber wall 734 and sized to provide an exemplary HRT 0.5-1 hr. As show inFIG. 7B , a plurality of themembrane filter 306 are equally spaced within the annularly shaped filtration vessel. - As shown in
FIG. 7A , thereactor 505 includescarrier media 757 disposed therein while thefiltration vessel 305 includes scouringelements 753. Coupled to an effluent side of themembrane filter 306 are lines for conducting the filteredeffluent stream 307 to theRO feed tank 509 further having line out for the filteredeffluent stream 511. -
Air inlets FIG. 5 ) into thereactor 505 andfiltration vessel 305, respectively. As further illustrated inFIGS. 7A and 7B , a backflow prevention mechanism 762 (e.g., a plurality of check valves embedded in the inner wall 733) separates thereactor 505 from thefiltration vessel 305 to prevent backflow of the treatedeffluent 507 when a pressure control device 534 (e.g., an automated air vent) causes thefiltration vessel 305 to be pressurized above that of thereactor 505 via theair inlet 536B. -
FIG. 8 is a flow diagram illustrating awater treatment method 800 which may be performed by the water treatment andmembrane filtration apparatus 700. Themethod 800 should therefore be considered an exemplary sequence of operations implementing an advantageous mode of the treatment and filtration operations generally described in reference toFIGS. 5 and 6 . -
Method 800 begins withoperation 601 where, as previously described, aqueous solution for treatment is received by the reactor 505 (inner vessel). Thereactor 505 operates between low andhigh level sensors 752A, for example corresponding to approximately 15% of the reactor volume. Atoperation 860 thereactor 505 is continuously mixed, for example via thehydraulic mixer 550, and aerated, for example via thehydraulic air compressor 540. Atoperation 862, biomass is grown on the surface of theplastic carriers 757 as well as freely suspended in the reactor. - If the
reactor 505 reaches the high level, then thepressure control device 534 is actuated (e.g., opened) at operation 863 to equilibrate the pressure between thereactor 505 andfiltration vessel 305, allowing for solution levels between thereactor 505 andfiltration vessel 305 to equilibrate atoperation 865 via thebackflow prevention mechanism 762. Screening retainsbiomass carriers 757 in thereactor 505. Upon equalization of solution levels,method 800 returns to operation 266 where thepressure control device 534 actuates (e.g., closes) to allow pressure in thefiltration vessel 305 to increase via air introduced through air inlet 636B. The increased pressure drives flux across the (microfiltration)membrane filter 306 atoperation 857. The level in the filtration vessel decreases due to permeation through themembrane filter 306 with the filteredeffluent stream 307 being output to theRO feed tank 509 atoperation 859. While thepressure control device 534 operates to elevate the filtration vessel pressure, the level in thereactor 505 will continue to increase due toinfluent stream 101. - Upon the
filtration vessel 305 reaching a low level located at the top of themembrane filter 306,level sensors 752B actuate thepressure control device 534 to reduce pressure to ambient. Solution flux through the membranes(s) 306 is thereby reduced to avoid drying out the membranes or forming a biomass cake. During all or a portion of the time while at the low level, permeate flux may be zero and utilized for the membrane back-pulse described elsewhere herein (i.e., flux reversed). - The
RO feed tank 509 also operates between low andhigh level sensors 752C. The tank is elevated by height H relative to thefiltration vessel 305 to provide sufficient minimum head to thehydraulic pump 120. When level in theRO feed tank 509 reaches the low level (e.g., insufficient MBR product), an RO feed valve downstream of the RO feed tank 509 (FIG. 5 ) and downstream of the RO bypass, 513A and 513B, respectively, close atoperation 872. RO bypass return 521 recirculates theRO bypass stream 512 after driving thehydraulic air compressor 540 back to the filtered effluent (permeate)stream 511, downstream theRO feed valve 513A. Upon the level reaching the high level sensor (e.g., permeate flow fromfiltration vessel 305 exceeds capacity of the RO unit 110), thepressure control device 534 is actuated atoperation 874 to reduce filtration vessel pressure and thereby interrupt permeate flow. When the RO feed tank level is between the level sensors, theRO feed valves operation 685. - As the
hydraulic pump 120 drives permeation through theRO unit 110 and also supplies hydraulic power to drive the aeration, mixing, and pressurization of the filtration vessel, as well as other maintenance operations, when the RO feed is interrupted, thehydraulic pump 120 continues to recirculate RO feed quality water through theRO bypass stream 512 and back to an inlet of the hydraulic pump 120 (through the return 521). The pressure at the pump inlet is adjusted to be equal to the low level head of the RO feed tank, allowing both streams to feed the pump simultaneously when filtered effluent (permeate)stream 511 is available. - A number of service flows may also be performed either simultaneously or cyclically with the
method 800. For example, theelectrolytic cell 365 generates a low-level of oxidizing species (e.g., chlorine) from theRO concentrate stream 514, as described elsewhere herein. In the exemplary embodiment, theelectrolytic cell 365 operates continuously with the retention time (and as a result the chlorine concentration) controlled by timer. Injection of the oxidizing species (biocide) may be triggered upon activating the RO feed valve. Also during themethod 800, the back-pulse as described elsewhere herein is injected into the membrane regularly when thepressure control device 534 is actuated to reduce filtration vessel pressure. The duration of the back-pulse may be controlled by timer or pressure regulated. Duringmethod 800, excess sludge from thereactor 505 will overflow to thefiltration vessel 305. Periodically (e.g., once a day) aeration of thereactor 505 is halted, and after short settling of the scouringelements 753, the content of the reactor will be drained, for example from the upper portion of thefiltration vessel 305 and discharged intomunicipal sewer 502. Other system rinses may also be performed periodically. For example, the pressurizedRO concentrate stream 514 may be used for the rinses in thesolids separator 503, discharging into themunicipal sewer 502. Similarly, rinses downstream of thefiltration vessel 305 may use pressurized recirculation flow via theRO bypass stream 512. - Uninterrupted processing of the
influent stream 101 occurs when thetreatment system 500 operates normally. However, one or more of a number interlocks may be triggered in response to a system malfunction. For example, in the absence of theinfluent stream 101, the level in both thereactor 505 andfiltration vessel 305 will reach the respective low levels with aeration continued to maintain biomass activity. Interruption of a sufficient duration will lead to interruption of theRO unit 110. An absence of theRO concentrate stream 514 will halt thehydraulic mixer 550. In this case, mixing is provided by aeration only. In the event of a toxic feed,pH meter 583 will register a change in thereactor 505 and/orfiltration vessel 305, generating an alarm and/or operator response. In the event of a surge in theinfluent stream 101, the high level in thereactor 505 is exceeded and a bypass valve diverts theseparator effluent stream 504 to themunicipal sewer 502. In the event thefiltration vessel 305 becomes clogged,hydraulic pump 120 stops, or a membrane in theRO unit 110 becomes clogged, both thefiltration vessel 305 andreactor 505 reach the high level, and the bypass valve to themunicipal sewer 502 is activated triggering an alarm for operator response. In the event theelectrolytic cell 365 fails, membranes in theRO unit 110 will become clogged, again triggering the high levels in both thefiltration vessel 305 andreactor 505 resulting in an alarm. -
FIG. 9 is a watertreatment system architecture 900 in which the integratedwater treatment system 500 may be implemented within an existing POTW, in accordance with an embodiment of the present invention. As shown, thewater treatment system 500 receives theinfluent stream 101 from one or more upstream commercial water uses 910A, 910B and/or household water uses 920A, 920B and returns a processed effluent for one or more downstream commercial water uses 940A, 940B or household water uses 950A. The downstream uses may be the same as the upstream uses (e.g., a car wash) or may be downgraded (e.g., laundry upstream, car wash downstream, etc.). In the illustrative embodiment, thetreatment system 500 is scaled to be completely contained within a conventional tractor trailer/shipping container 599. As such, thetreatment system 500 is capable of mobile, distributed point of use treatment which can reduce loading on the primary municipal treatment facilities and differentia water qualities based on use. At this exemplary scale, it is expected that thetreatment system 500 can accommodate an average influent stream volumetric flow rate of up to 10,000 gal per day, depending on the quality of theinfluent stream 101. With thetreatment system 500 being a distributed treatment resource inserted into a municipal treatment framework proximate the point of use, connection to themunicipal sewer 502 provides a failsafe as well as a means to dispose of separated solids, etc. in a more concentrated form. - The above description of illustrative embodiments of the invention, including what is described in the Abstract, is not intended to be exhaustive or to limit the invention to the precise forms disclosed. While specific implementations of, and examples for, the invention are described herein for illustrative purposes, various equivalent modifications are possible within the scope of the invention, as those skilled in the relevant art will recognize. The scope of the invention is therefore to be determined entirely by the following claims, which are to be construed in accordance with established doctrines of claim interpretation.
Claims (15)
1. A water treatment system, comprising:
a vessel for filtration or treatment of an aqueous solution;
a reverse osmosis (RO) unit; and
an electrolytic cell in fluid communication with an RO concentrate outlet, the electrolytic cell operative to convert a salt in the RO concentrate into an oxidizing species, wherein the electrolytic cell is coupled to at least one of the vessel and RO unit for disinfection by the oxidizing species or reaction products thereof.
2. The water treatment system of claim 1 , wherein the oxidizing species comprises chlorine and wherein the reaction product comprises a chloramine product of a reaction between residual ammonia in the RO concentrate and the oxidizing species.
3. The water treatment system of claim 1 , wherein the electrolytic cell has an outlet coupled downstream of the vessel for conduction of the oxidizing species to the RO inlet.
4. The water treatment system of claim 1 , further comprising a backwash apparatus to intermittently provide a liquid back-pulse from an effluent side to an influent side of a membrane filter in the vessel, the liquid back-pulse containing the oxidizing species.
5. The water treatment system of claim 4 , further comprising a hydraulic pump with a high pressure side in fluid communication with the RO inlet and an RO bypass upstream of the RO inlet, wherein the backwash apparatus is in fluid communication with both the electrolytic cell and with the RO bypass, the liquid back-pulse to be pressurized by the pump.
6. A water treatment method, comprising:
performing an incomplete biological treatment of an aqueous solution leaving residual ammonia in the treated effluent, wherein performing the incomplete biological treatment further comprises performing treatment without adding a caustic to control pH; and
removing the ammonia from the treated effluent by driving the treated effluent through a reverse osmosis (RO) unit with a hydraulic pump.
7. The water treatment method of claim 6 , further comprising
electrolytically converting a chloride in a RO concentrate of the RO unit into a chlorine-containing oxidizing species;
reacting the chlorine-containing oxidizing species with the residual ammonia in the RO concentrate to generate chloramines; and
disinfecting at least a portion of a system performing the water treatment method with the generated chloramines.
8. The water treatment method of claim 7 , the method further comprising filtering the treated effluent with a membrane filter, and wherein disinfecting at least a portion of the system further comprises, at least one of:
intermittently backwashing the membrane filter with a liquid back-pulse from an effluent side to an influent side, the liquid back-pulse pressurized by the hydraulic pump and carrying the chloramines,
introducing the generated chloramines to a feed tank disposed downstream of the filtration vessel and upstream of the hydraulic pump to expose an influent side of the RO unit to the chloramines, or
introducing the generated chloramines into the RO permeate.
9. A water treatment method, comprising:
performing at least one of filtration or biological, chemical, or physical-chemical treatment of an aqueous solution;
removing salts from the filtered or treated effluent by driving the effluent through a reverse osmosis (RO) unit with a hydraulic pump;
electrolytically converting a salt in the RO concentrate into a chlorine-containing oxidizing species; and
disinfecting at least a portion of the system performing the water treatment method with the chlorine-containing oxidizing species.
10. The water treatment method of claim 9 , the method further comprising filtering the treated effluent with a membrane filter, and wherein disinfecting at least a portion of the system further comprises, at least one of:
intermittently backwashing the membrane filter with a liquid back-pulse from an effluent side to an influent side, the liquid back-pulse pressurized by the hydraulic pump and carrying the chlorine-containing oxidizing species,
introducing the generated chloramines to a feed tank disposed downstream of the filtration vessel and upstream of the hydraulic pump to expose an influent side of the RO unit to the chlorine-containing oxidizing species, or
introducing the generated chlorine-containing oxidizing species into the RO permeate.
11. A water treatment method, comprising:
providing a waste water comprising ammonia and having a first pH;
treating the waste water by oxidizing the ammonia to provide a treated effluent, the treated effluent having a second pH lower than the first pH; and
driving the treated effluent through a reverse osmosis (RO) unit, the second pH sufficient to reduce scaling of the RO unit.
12. The water treatment method of claim 11 , wherein the treated effluent comprises residual ammonia, the method further comprising:
removing the residual ammonia with the RO unit.
13. The water treatment method of claim 2 , further comprising:
electrolytically converting a chloride in a RO concentrate of the RO unite into a chlorine-containing oxidizing species;
reacting the chlorine-containing oxidizing species with the residual ammonia in the RO concentrate to generate chloramines; and
disinfecting at least a portion of A system performing the water treatment method with the generated chloramines.
14. The water treatment method of claim 13 , the method further comprising:
filtering the treated effluent with a membrane filter, and wherein disinfecting at least a portion of the system further comprises, at least one of:
intermittently backwashing the membrane filter with a liquid back-pulse from an effluent side to an influent side, the liquid back-pulse pressurized by the hydraulic pump and carrying the chloramines,
introducing the generated chloramines to a feed tank disposed downstream of the filtration vessel and upstream of the hydraulic pump to expose an influent side of the RO unit to the chloramines, or
introducing the generated chloramines into the RO permeate.
15. The water treatment method of claim 11 , wherein the treating the waste water is performed without adding a caustic.
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CN107601654B (en) * | 2016-07-12 | 2020-09-15 | 中国石油化工股份有限公司 | Ultrasonic treatment method for preventing wet air regeneration system from scaling |
CN106698865B (en) * | 2017-03-22 | 2023-04-07 | 贵州大学 | Industrial sewage purification device |
CN107129115B (en) * | 2017-06-29 | 2020-09-29 | 长安大学 | Integrated small sewage treatment device and process for treating carbon, nitrogen and phosphorus and sludge |
CN108862507A (en) * | 2018-06-26 | 2018-11-23 | 深圳市雷凌广通技术研发有限公司 | A kind of coagulative precipitation device of highly effective and safe |
CN108996837A (en) * | 2018-08-22 | 2018-12-14 | 陈立波 | Oil removal cleaning treatment system for sanitary sewage |
US10851005B2 (en) * | 2018-11-20 | 2020-12-01 | Vector Innovative Products, L.L.C. | Water provision apparatuses and related methods |
CN110104762A (en) * | 2019-05-22 | 2019-08-09 | 江苏中百洲环境科技有限公司 | A kind of floatation type sewage water treatment method |
WO2020264153A1 (en) * | 2019-06-27 | 2020-12-30 | De Nora Water Technologies, LLC | Methods and systems for marine wastewater treatment |
CN112237847A (en) * | 2020-09-02 | 2021-01-19 | 重庆电子工程职业学院 | Acid pickling device for preparing nanofiltration membrane |
Family Cites Families (48)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3662890A (en) * | 1970-10-19 | 1972-05-16 | Environmental Services Inc | Waste treatment system |
US5639373A (en) | 1995-08-11 | 1997-06-17 | Zenon Environmental Inc. | Vertical skein of hollow fiber membranes and method of maintaining clean fiber surfaces while filtering a substrate to withdraw a permeate |
US5248424A (en) | 1990-08-17 | 1993-09-28 | Zenon Environmental Inc. | Frameless array of hollow fiber membranes and method of maintaining clean fiber surfaces while filtering a substrate to withdraw a permeate |
US5151187A (en) | 1991-11-19 | 1992-09-29 | Zenon Environmental, Inc. | Membrane bioreactor system with in-line gas micronizer |
US5403479A (en) | 1993-12-20 | 1995-04-04 | Zenon Environmental Inc. | In situ cleaning system for fouled membranes |
US5501798A (en) | 1994-04-06 | 1996-03-26 | Zenon Environmental, Inc. | Microfiltration enhanced reverse osmosis for water treatment |
US6863823B2 (en) | 2001-03-23 | 2005-03-08 | Zenon Environmental Inc. | Inverted air box aerator and aeration method for immersed membrane |
US5944997A (en) | 1995-08-11 | 1999-08-31 | Zenon Environmental Inc. | System for maintaining a clean skein of hollow fibers while filtering suspended solids |
US7087173B2 (en) | 1995-08-11 | 2006-08-08 | Zenon Environmental Inc. | Inverted cavity aerator for membrane module |
WO1997006880A2 (en) | 1995-08-11 | 1997-02-27 | Zenon Environmental Inc. | Vertical skein of hollow fiber membranes and method of maintaining clean fiber surfaces |
FR2741280B1 (en) | 1995-11-22 | 1997-12-19 | Omnium Traitement Valorisa | METHOD FOR CLEANING A FILTER SYSTEM OF THE SUBMERSIBLE MEMBRANE TYPE |
US6258278B1 (en) | 1997-03-03 | 2001-07-10 | Zenon Environmental, Inc. | High purity water production |
NL1008425C2 (en) | 1998-02-26 | 1999-08-30 | Waterleiding Friesland Nv | A method for treating aqueous flows in a bioreactor and an ultrafiltration unit, as well as a device for treating aqueous flows in a bioreactor and an ultrafiltration unit. |
US6235196B1 (en) | 1998-04-23 | 2001-05-22 | Alliedsignal Inc. | Biological wastewater treatment system |
US6550747B2 (en) | 1998-10-09 | 2003-04-22 | Zenon Environmental Inc. | Cyclic aeration system for submerged membrane modules |
PL214717B1 (en) | 1998-10-09 | 2013-09-30 | Zenon Technology Partnership | Cyclic aeration system for submerged membrane modules |
US6616843B1 (en) | 1998-12-18 | 2003-09-09 | Omnium De Traitement Et De Valorisation | Submerged membrane bioreactor for treatment of nitrogen containing water |
US6547968B1 (en) | 1999-07-30 | 2003-04-15 | Zenon Environmental Inc. | Pulsed backwash for immersed membranes |
AU6257000A (en) | 1999-07-29 | 2001-02-19 | Zenon Environmental Inc. | Chemical cleaning backwash for immersed filtering membranes |
US6470683B1 (en) * | 1999-08-30 | 2002-10-29 | Science Applications International Corporation | Controlled direct drive engine system |
US6324898B1 (en) | 1999-12-21 | 2001-12-04 | Zenon Environmental Inc. | Method and apparatus for testing the integrity of filtering membranes |
US20050218074A1 (en) | 2004-04-06 | 2005-10-06 | Pollock David C | Method and apparatus providing improved throughput and operating life of submerged membranes |
US6451201B1 (en) | 2001-04-25 | 2002-09-17 | Zenon Environmental Inc. | Distributed on-line integrity testing for immersed membranes |
US6814868B2 (en) | 2001-06-28 | 2004-11-09 | Zenon Environmental Inc. | Process for reducing concentrations of hair, trash, or fibrous materials, in a waste water treatment system |
WO2003002468A1 (en) | 2001-06-28 | 2003-01-09 | Zenon Environmental Inc. | A process for reducing concentrations of hair, trash, or fibrous materials in a waste water |
US20040168980A1 (en) | 2002-01-04 | 2004-09-02 | Musale Deepak A. | Combination polymer treatment for flux enhancement in MBR |
US6767455B2 (en) | 2002-08-21 | 2004-07-27 | Ceramem Corporation | Airlift membrane device and membrane bioreactor and bioreactor process containing same |
US6863817B2 (en) | 2002-12-05 | 2005-03-08 | Zenon Environmental Inc. | Membrane bioreactor, process and aerator |
KR20050102115A (en) | 2003-02-13 | 2005-10-25 | 제논 인바이런멘탈 인코포레이티드 | Supported biofilm apparatus and process |
CN100361907C (en) | 2003-02-13 | 2008-01-16 | 泽农技术合伙公司 | Supported biofilm apparatus and process |
WO2005082498A1 (en) | 2004-02-27 | 2005-09-09 | Zenon Environmental Inc. | Water filtration using immersed membranes |
AU2005233102A1 (en) | 2004-04-06 | 2005-10-27 | Vost Environmental Technologies | Method and apparatus providing improved throughput and operating life of submerged membranes |
AU2005240524C1 (en) | 2004-04-22 | 2009-12-24 | Evoqua Water Technologies Llc | Filtration apparatus comprising a membrane bioreactor and a treatment vessel for digesting organic materials |
WO2006002529A1 (en) | 2004-07-01 | 2006-01-12 | Zenon Technology Partnership | Screening apparatus for water treatment with membranes |
US20060065597A1 (en) * | 2004-09-29 | 2006-03-30 | Sisyan, R.L. De C.V. | Hybrid, reverse osmosis, water desalinization apparatus and method with energy recuperation assembly |
US7591950B2 (en) | 2004-11-02 | 2009-09-22 | Siemens Water Technologies Corp. | Submerged cross-flow filtration |
EP1852175A4 (en) * | 2005-02-25 | 2009-08-05 | Ngk Insulators Ltd | Method of cleaning membrane in membrane separation activated-sludge process |
US20080017558A1 (en) | 2005-03-31 | 2008-01-24 | Pollock David C | Methods and Devices for Improved Aeration From Vertically-Orientated Submerged Membranes |
US7396453B1 (en) * | 2005-04-19 | 2008-07-08 | Procorp Enterprises, Llc | Hydraulically integrated solids/liquid separation system for wastewater treatment |
ES2599640T3 (en) | 2005-07-12 | 2017-02-02 | Zenon Technology Partnership | Procedure control for a submerged membrane system |
WO2007044345A2 (en) | 2005-10-05 | 2007-04-19 | Siemens Water Technologies Corp. | Method and apparatus for treating wastewater |
US7527736B2 (en) * | 2006-09-01 | 2009-05-05 | Anticline Disposal, Llc | Method for generating fracturing water |
US8105488B2 (en) | 2006-09-01 | 2012-01-31 | Anticline Disposal, Llc | Waste water treatment method |
US7731847B2 (en) * | 2007-05-25 | 2010-06-08 | Huy Ton That | Submersible reverse osmosis desalination apparatus and method |
US20090050561A1 (en) | 2007-08-20 | 2009-02-26 | Jon Inman Sattler | System and method for processing wastewater |
US8273251B2 (en) | 2007-09-07 | 2012-09-25 | Clearwater Systems Corporation | Use of electromagnetic pulses in cross-flow filtration systems |
EP2226115B1 (en) | 2007-12-14 | 2017-02-15 | Beijing Ecojoy Water Technology Co., Ltd | A hollow fiber membrane module |
US20100096327A1 (en) | 2008-09-19 | 2010-04-22 | Gin Douglas L | Polymer coatings that resist adsorption of proteins |
-
2011
- 2011-08-01 US US13/195,746 patent/US8910799B2/en not_active Expired - Fee Related
-
2014
- 2014-11-17 US US14/543,837 patent/US20150068977A1/en not_active Abandoned
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106946347A (en) * | 2017-05-03 | 2017-07-14 | 上海世浦泰膜科技有限公司 | A kind of external MBR reactors agitating device of reflux formula and its method of work |
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CN108706835A (en) * | 2018-06-16 | 2018-10-26 | 江苏吉隆环保科技有限公司 | A kind of sewage-treatment plant using internal lining pipe |
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US20130032533A1 (en) | 2013-02-07 |
US8910799B2 (en) | 2014-12-16 |
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