US20130341271A1 - Mechanical axial vibration in membrane separation treatment of effluents - Google Patents
Mechanical axial vibration in membrane separation treatment of effluents Download PDFInfo
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- US20130341271A1 US20130341271A1 US13/987,738 US201313987738A US2013341271A1 US 20130341271 A1 US20130341271 A1 US 20130341271A1 US 201313987738 A US201313987738 A US 201313987738A US 2013341271 A1 US2013341271 A1 US 2013341271A1
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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
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0036—Flash degasification
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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
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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
- B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
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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
- B01D61/029—Multistep processes comprising different kinds of membrane processes selected from reverse osmosis, hyperfiltration or nanofiltration
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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
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
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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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
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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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
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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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/008—Mobile apparatus and plants, e.g. mounted on a vehicle
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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
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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
- C02F2209/005—Processes using a programmable logic controller [PLC]
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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
- C02F2209/005—Processes using a programmable logic controller [PLC]
- C02F2209/006—Processes using a programmable logic controller [PLC] comprising a software program or a logic diagram
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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
- C02F2209/005—Processes using a programmable logic controller [PLC]
- C02F2209/008—Processes using a programmable logic controller [PLC] comprising telecommunication features, e.g. modems or antennas
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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
- C02F3/082—Rotating biological contactors
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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
- This invention relates to effluent treatment, and, more particularly, relates to membrane separation treatment of effluents.
- Membrane elements in such use require constant maintenance and frequent cleaning or replacement.
- Vibratory means have been heretofore known and/or utilized in membrane separation to reduce maintenance requirements. These have employed horizontal vibratory torsional motion, and often require use of proprietary one source only custom membrane modules. Further improvements could thus still be utilized.
- This invention provides methods for mechanical (motorized, electromagnetic or hydrodynamic) axial vibration in membrane separation treatment of effluents.
- the methods allow use of readily available, and thus less costly, conventional membrane elements and/or modules.
- Axial, linear operation allows mounting of membrane modules in a vertical flow gravity assisted position, with adjustable crossflow operation accommodated.
- the methods are adapted to apparatus including a separation membrane element having an axial dimension, a membrane support structure having the element therein, and means for vibrating the membrane element in the axial dimension.
- Crossflow pumping is connected with the support structure.
- the support structure includes a membrane housing, the vibrating means including a fluid pump and spring arrangement for oscillating the membrane element.
- the support structure includes a tube for receiving and securing the membrane element, the tube and element together defining a membrane cartridge, the cartridge axially mounted in a containment housing and movable axially therein by the vibrating means (hydrodynamically or electromagnetically, for example).
- the vibrating means are motors for vibrating a plurality of elements on a common platform.
- the methods of this invention include the steps of locating a membrane element in a support structure and feeding effluent for treatment into the support structure.
- Axial vibration of the membrane element in the support structure is initiated without securement of the membrane element to a source of vibration, and treated effluent is withdrawn from the support structure.
- the membrane element is located in the support structure without attachment to the support structure or other structure outside the support structure. Vibration of the membrane element in the support structure in the axial dimension is accomplished using any of hydrodynamic, electromagnetic and mechanical methods.
- the membrane module is positioned in a containment housing configured for free axial movement of the membrane module therein, extent of axial movement being adjustably limitable.
- Axial vibration is hydrodynamically activated in the containment housing as limited.
- Vibration direction is axial and preferably perpendicular to the floor of the installation for gravity assisted membrane separation systems.
- the shear wave produced by axial vertical membrane vibration causes solids and foulants to be lifted off membrane surfaces and remixed with retentate flowing through the parallel or tunnel spacer or other specially designed spacers of spirally wound elements or through flow channels of tubular or capillar membrane elements. Movement continuity is maintained through adjustable crossflow, reducing further additional membrane fouling tendency.
- the vibration curve is preferably a regular curve, which corresponds mathematically to a zero centered sine or cosine, a sinusoidal or simple harmonic.
- the amplitude is preferably steady and frequency high.
- FIG. 1 is a block diagram illustrating phased functions in an effluent treatment regime
- FIG. 2 is a diagram illustrating a first membrane technology of this invention utilizable in steps directed to the primary (effluent polishing) treatment of effluents;
- FIG. 3 is a diagram illustrating a second membrane technology of this invention utilizable in steps directed to the primary treatment of effluents
- FIGS. 4 a and 4 b are illustrations of coil structures utilizable in the technology of FIGS. 2 and 3 ;
- FIG. 5 is a detailed view illustrating coil cooling utilizable in the technology of FIGS. 2 through 4 ;
- FIG. 6 is a diagram illustrating apparatus for internal concentration polarization control in the technology of FIGS. 2 through 4 ;
- FIG. 7 is a diagram illustrating one membrane deployment option utilizable in primary treatment steps of this invention.
- FIG. 8 is a sectional illustration of a crossflow pump of this invention utilized in various membrane separation technologies
- FIG. 9 is a sectional illustration of an improved degasser column used with the membrane systems of this invention.
- FIG. 10 is a flow distributor and discharge equalizer deployed, for example, with the membrane systems of this invention.
- FIGS. 11 a and 11 b are diagrams illustrating a high frequency oscillating membrane system utilizable in primary treatment of this invention.
- FIG. 12 is a sectional diagram illustrating a second embodiment of the high frequency oscillating membrane system
- FIG. 13 is a partial sectional illustration of the oscillating membrane system of FIG. 12 ;
- FIG. 14 is a detailed sectional illustration of the upper part of the oscillating membrane system of FIG. 13 ;
- FIG. 15 is a detailed sectional illustration of the lower part of the oscillating membrane system of FIG. 13 ;
- FIG. 16 is an illustration showing function of the spirally wound membrane elements of the oscillating membrane system of FIG. 13 (also employable in other oscillating systems shown herein);
- FIG. 17 is a diagram illustrating an alternative deployment of the oscillating membrane system of FIG. 13 ;
- FIG. 18 is a sectional illustration of a vibratory seal arrangement for the oscillating membrane system of FIGS. 13 and 14 ;
- FIG. 19 is a sectional illustration of a high shear embodiment of the oscillating membrane system of FIGS. 12 through 17 ;
- FIG. 20 is a sectional illustration of a draw-off utilizable in the high shear embodiment of FIG. 19 .
- FIG. 1 shows steps of an effluent treatment regime.
- the option numbers located at three-way valves 401 refer to automated or override manual flow control options for different treatment regimes.
- Stage 403 (step 1 ) is a dual strainer receiving feed effluent and removing particulates down to about 500 ⁇ m (for example, the model 120 dual strainer produced by Plenty Products, Inc.).
- Stage 405 (step 2 ) provides oil separation from the feed flow utilizing a separator (for example, a Highland Tank & Mfg. Co. R-HTC Oil/Water Separator with Petro-Screen and parallel corrugated plate coalescers).
- a separator for example, a Highland Tank & Mfg. Co. R-HTC Oil/Water Separator with Petro-Screen and parallel corrugated plate coalescers.
- Stage 407 is an automatic backflush filter providing particle removal down to the 100 ⁇ m range or better (a TEKLEEN self cleaning bell filter setup with GB6 electric controller by Automatic Filters, Inc., or similar filter setups by Amiad Filtration Systems, could be utilized for example).
- a TEKLEEN self cleaning bell filter setup with GB6 electric controller by Automatic Filters, Inc. or similar filter setups by Amiad Filtration Systems, could be utilized for example).
- Stage 409 provides inline direct feed effluent (water) heating.
- Feed water heating is required in many treatment settings due to seasonal operations, and further benefits many downpipe treatment options by breaking feed water alkalinity, enhancing CH 4 gas removal, ensuring proper membrane (where present) permeate flux for an overall constant permeate flow yield, and the like.
- Either of two types of inline heating systems may be utilized, as more fully detailed below.
- Stage 411 is a first suite of pre-treatment apparatus including eight apparatus (all eight are preferred, but fewer could be provided in some applications). These apparatus provide, as more fully detailed below, on-line diffusive effect (ODE) membrane aeration, fluid density reduction, modified vacuum tower or cascade series waterfall degassing, air stone degassing, modified venturi gas evacuation, fine filtration, lamella plate clarification, and sludge chamber concentration.
- ODE on-line diffusive effect
- Stage 413 is a second suite of pre-treatment apparatus including ten apparatus (all ten are preferred, but fewer could be provided in some applications).
- This stage provides pH adjustment (via an injection pump 302 ), chemical dosing (via an injection pump 304 , ODE/IDI (inline diffusive ionization) membrane aeration, ionized air/gas treatment, electrocoagulation, dissolved air/gas flotation, vacuum introduced cyclone separation, vacuum degassing, lamella plate clarification, and sludge chamber concentration.
- Stage 415 (step 7 ) provides a bag filter and/or belt filter assembly (for example, fabric filtration systems sold by SERFILCO) for filtration down to about the 1 ⁇ m range.
- Stage 417 (step 8 ) is a homogenizing and buffer tank with pH adjustment and chemical dosing (at injection pumps 306 and 308 , respectively).
- Stage 419 (step 9 ) is the first of the primary, effluent polishing treatment array (stages 419 through 433 , steps 9 through 16 ), and may include any of several membrane treatment apparatus in accord with this invention as more fully detailed hereinafter providing nanofiltration, and/or known ion-exchange treatment technology. Stage 419 , as is apparent, is an option for up-concentrating effluent to increase overall flow yield.
- Stage 421 (step 10 ) provides antifouling and antiscaling chemical treatment to prevent fouling and scaling of membranes by keeping low molecular weight components in solution (foremost of which are divalent and multivalent cations).
- Known variable speed tubing pumps could be utilized for insertion.
- Stage 423 (step 11 ) provides filtration for removal of low molecular weight components (Al, Fe, Mg and Mn, for example) and/or colloidals utilizing membrane treatment nanofiltration and/or ion-exchange treatment.
- Stage 425 (step 12 ) provides a buffer tank for step 14 for process flow control (for example a Snyder horizontal leg tank by Harrington).
- Stage 427 (step 13 ) provides antiscaling chemical treatment addressing monovalent and a few divalent cations and anions (Ba, Ca, Na, Sr, CO 3 F, HCO 3 , and SO 4 for example). Again, known variable speed tubing pumps could be utilized for insertion.
- Stage 429 addresses removal of low molecular weight components (salts, for example) utilizing reverse osmosis membrane treatment and/or ion-exchange treatment.
- Stage 431 (step 15 ) is a high pressure buffer tank providing flow control for step 9 and/or 16 .
- Stage 433 (step 16 ) provides up-concentration of concentrate flow from stage 429 to further increase flow yield, and may utilize reverse osmosis membrane treatment, ion-exchange treatment and/or high efficiency electrodialysis technology (for example, a HEED assembly by EET Corporation), a hybrid process including both electrodialysis and reverse osmosis approaches.
- Stage 435 is a suite of four post-treatment apparatus as more fully detailed herein below, and including activated carbon filtration for gas absorption (Ametic filter chambers by Harrington, for example), sodium absorption ratio compensation, utilizing a dolomite filter for example, UV treatment (for example, an SP or SL series unit from Aquafine Corporation), and membrane aeration for O 2 saturation (preferably utilizing an ODE system in accord with yet another aspect of this invention).
- activated carbon filtration for gas absorption Ametic filter chambers by Harrington, for example
- sodium absorption ratio compensation utilizing a dolomite filter for example, UV treatment (for example, an SP or SL series unit from Aquafine Corporation), and membrane aeration for O 2 saturation (preferably utilizing an ODE system in accord with yet another aspect of this invention).
- Stage 437 (step 18 ) provides bio-monitoring utilizing a 10 gallon aquarium with the operating volume passing through either a sterilizer or other aquarium device to prevent in situ bio-contamination from waste and nutrients.
- the sterilizer or other device must match the maximum produced permeate flow of at the rate of approximately one gallon per minute for real time bio-monitoring. Since the sterilized water is typically being mixed with unsterilized water, it is not possible to completely purify it, but a sterilized percentage exceeding 99.9% is acceptable for the bio-monitoring step sensitivity.
- Stage 439 (step 19 ) conventionally provides waste collection and purified feed return.
- this process is a well known water treatment process for removing ions from solution by exchanging cations or anions between the dissolved phase and counter ions on a matrix such as organic zeolite, in which Ca 2 + ions in solution displace Na ions in the zeolite, montmorillonite (a colloidal bentonite clay) or synthetically produced organic resins, for example.
- a matrix such as organic zeolite, in which Ca 2 + ions in solution displace Na ions in the zeolite, montmorillonite (a colloidal bentonite clay) or synthetically produced organic resins, for example.
- An organic ion exchange resin is composed of high molecular-weight polyelectrolytes that can exchange their mobile ions for ions of similar charge from the surrounding medium. Each resin has a distinct number of mobile sites that set the maximum quantity of exchanges per unit of resin. Ion exchange reactions are stoichiometric and reversible.
- ion-exchange treatment technology can be utilized alone as an alternative to the hereinafter detailed membrane treatment technology or may supplement specific membrane technology.
- the implementation of ion-exchange technology depends on the specific application and project economics (the less complex and labor-intensive state of the art ion exchange technology may be used as a single polishing step instead of membrane treatment where cost is a factor and desired treatment outcomes warrant the tradeoff).
- the produced permeate is fed into a strongly acidic cation exchanger followed by a strongly basic anion exchanger (substituting for both steps 15 and 16 ).
- a strongly acidic cation exchanger followed by a strongly basic anion exchanger (substituting for both steps 15 and 16 ).
- Such systems are commercially available from KINETICO, REMCO ENGINEERING and others.
- Membrane treatment and other treatment systems may be realized by deployment of various types of apparatus and systems, particularly at steps 9 , 11 , 14 and 16 (steps 8 , 10 , 12 , 13 and 15 are primarily directed to homogenization and process buffering and/or chemical metering, and have been addressed hereinabove). Ion-exchange treatment and HEED systems utilizable herein have already been addressed. In addition V-SEP series L/P systems, while not preferred, could be utilized at stages 419 , 423 , 429 and 433 for analytics as well as nanofiltration and reverse osmosis filter installations.
- FIGS. 2 through 5 illustrate an axial (linear) vibratory membrane separation apparatus and methods for forward osmosis.
- This aspect of the invention relates to low amplitude, axial vibratory membrane separation apparatus (both nanofiltration and reverse osmosis filtration) called quaking recycle membrane separation technology employed with forward osmosis technology.
- Forward osmosis technology is employed to supplement the quaking membrane nanofiltration and/or reverse osmosis technology, the hybrid application incorporated into an integrated apparatus (high frequency forward nanofiltration or high frequency forward reverse osmosis apparatus).
- Draw solutions typically used include ammonium bicarbonate (NH 4 HCO 3 ), ammonium carbonate (NH 4 ) 2 CO 3 , ammonium carbamate NH 4 NH 2 CO 2 ; (H 4 NO)(CONH 2 ; H 2 N—CO—O—NH 4 ), and can preferably include magnetoferritin in solution.
- the concentration of solutes in the thermally recyclable draw is required to have a higher osmotic pressure than the osmotic pressure of the concentration of solutes in the feed water (often brackish).
- Common spiral-wound membranes have not been heretofore utilized for forward osmosis because a liquid stream cannot be forced to flow on the support side (permeate side) inside the envelope, where the porous polymer layer further increases the internal concentration polarization.
- the apparatus of this aspect of the invention employs tubular or hollow fiber membrane modules, rather than spiral-wound membrane elements.
- the hybrid quaking membrane plus forward osmosis process and apparatus of this invention secure permeate continuity of the present art forward osmosis technology (generating extreme turbulence on both sides of the forward osmosis membrane (feed side and draw side) to support permeate continuity), provide nondestructive, vibratory membrane separation for commercially available forward osmosis membranes, and reduce the potential tendencies of concentration polarization, scaling and fouling of forward osmosis membranes.
- FIGS. 2 to 5 the hybrid quaking membrane plus forward osmosis process and apparatus is illustrated with the quaking membrane assembly at 2401 and recycle and reconcentrating closed loop system at 2501 .
- self-supported, semi-permeable or hollow fiber tubular membrane 2403 is used as a forward osmosis membrane operating in a quaking membrane process.
- Such tubular and hollow fiber membranes have no thick support layer as in spiral-wound, flat sheet, asymmetric membranes, thus minimizing internal concentration polarization. Membranes of this type are commercially available.
- the quaking membrane process is low amplitude and high quaking frequency, generating low shear energy and therefore a gentle treatment in the epoxy potting compound of tubular or hollow fiber membrane 2403 .
- the quaking energy significantly lowers already low external concentration polarization, and has a positive effect on internal concentration polarization as well.
- Sufficient turbulence is generated on both sides of tubular or hollow fiber membrane 2403 (external and internal) for securing continuation of increased flux performance required by the forward osmosis process.
- the process thus yields a higher permeate production with less concentrate for disposal and requires less up front pre-treatment for the feed, while using less energy compared to conventional reverse osmosis/nanofiltration technology because little or no hydraulic pressure is needed as a driving force for separation.
- membrane module design allows liquids to flow freely on both sides of membrane elements.
- Cellulose triacetate is the preferred material used in membrane 2403 (TOYOBO Hollosep hollow fiber membranes, for example).
- Low pressurized, recirculating feed water flows inside of the hollow fiber tubes of the membrane module 2403 from low pressure feed recirculation pump 2405 .
- the gravity-assisted feed flow is induced at the top of the axial vibrating, hollow fiber module 2403 .
- Quaking membrane module 2403 can either be operated in a vertical or inclined position, quaking membrane movement is provided by means of quake generator such as high pressure diaphragm pump 2407 .
- the low pressurized, draw solution flows counter currently to the feed on the outside of the hollow fiber tubes.
- the draw enters at the bottom of membrane module 2403 and exits at the top.
- Forced draw circulation flow is provided by vacuum and compressor pump 2503 ( FIG. 3 ).
- the concentration of the draw solution is diluted as the high osmotic pressure of the solution draws water through the semi-permeable membrane from the feed medium of lesser osmotic pressure. This, in turn, requires a reconcentration of the draw solution for the continuous desalination process.
- the diluted draw solution is thermally recycled and reconcentrated in a closed loop system, which yields potable water.
- the closed loop system consists of two heat exchangers 2505 and 2507 , a stripper column 2509 , and buffer tank 2511 .
- the draw solution diluted with water is first lightly heated to 30° to 50° C. in heat exchanger 2505 .
- the heated draw exits heat exchanger 2505 from the top and is siphoned into stripper column 2509 .
- Stripper column 2509 packing includes either raschig rings or berl saddles. Stripping takes place the column, the packing providing the necessary increased area and turbulence to achieve a desired draw solution conversion from a liquid to a vapor phase with the nonvolatile water precipitating out of the draw solution.
- the lightly heated, liquefied and diluted influent (consisting of water and its soluble light volatile draw components) is distributed (at spray head 2512 , for example) at the top of packed column bed 2513 , flowing down through the bed where the large transfer area and the vacuum assistance of pump 2503 allows the volatile components of the diluted draw to convert into an effluent vapor phase in the upper column portion and yielding potable water dilution water from the lower column portion (the treatment product of this apparatus).
- Vacuum and compressor pump 2503 is configured to handle a large vapor volume on its suction side and compressing the vapor on its pressure side, and transfers the pressurized vapor from stripper column 2509 into the top of second heat exchanger 2507 for compression heat removal from the compressed vapor mixture. Cooling is provided by means of fresh cold feed water.
- the cooling the vapor phase yields a condensate of a highly concentrated solute mixture and thus generates a recycled draw solution of initial concentration strength.
- the vapor mixture condensate is discharged from exchanger 2507 into buffer tank 2511 .
- Tank 2511 includes automatic aeration and de-aeration device 2517 to avoid the passage of residual vapor into hollow fiber module 2403 .
- Treated water is transferred out of column 2509 by centrifugal-vacuum pump 2519 while retentate particle separation is achieved via hydrocyclone separator 2409 ( FIG. 2 ).
- the upper module suction provides motive force to the recycled draw solution for flowing continuously from the lower permeate suction connection of module 2403 upwards and towards the upper permeate discharge connection, while the feed flows counter current to the draw downwards inside of hollow fiber module 2403 .
- the apparatus of FIGS. 2 and 3 is adapted for use not only with commercially available semi-permeable tubular and/or hollow fiber membranes modules, but also for forward osmosis specialized spiral-wound membranes when and if they become commercially available.
- the apparatus and processes can be used in applications for any brackish water treatment, higher contaminated CBM water treatment, overflow treatment of biological, defecated, municipal waste water for irrigation, cleaning processes for airplane and other public transportation wash water recycling, processing of bilge water, processing of wash water for combat vehicles after active and practice missions, and waste water processing for the pharmaceutical and chemical industry.
- the quaking membrane coupled with the forward osmosis process allows a substantial concentration upgrading at stage 419 at a significantly reduced energy requirement compared to conventional membrane separation processes, and could be employed as well at stages 423 , 429 and/or 433 .
- quaking membrane technology provides high recovery relative to conventional nanofiltration and/or reverse osmosis technology. Reduced scaling and fouling tendencies of the apparatus and processes reduce costs associated with pre-treatment stages used in conventional nanofiltration and reverse osmosis technology.
- Quaking frequency is variable in the range of 1 to 100 Hz depending on configuration. Quake amplitude has a relatively wide adjustable range of 0.2 to 2.0 mm. Quaking membrane movement can be generated either by any of electrical, hydraulic or mechanical means through an adjustable high frequency generator. Electrical means can include electromagnetic linear reciprocating membrane motion apparatus through a frequency-controlled, modified linear motion motor assembly wherein frequency and amplitude can be adjusted dynamically over a greater range (from 1 to 100 Hz.—see FIGS. 4 and 5 ).
- Modified motor assembly 2601 is shown in FIGS. 4 a and 4 b having an upper stator coil section 2603 and lower stator coil section 2605 , upper and lower (upper components only being shown in FIG. 4 b ) fluid transferring end pieces 2607 being equipped with encapsulated, high-energy neodymium, iron-boron, reciprocating permanent magnet sleeves 2609 .
- the nonmagnetic outer housing 2610 has upper (and lower, not shown) stator 2611 thereat between retainers 2613 .
- the stators contain the electromagnetic coils, which utilizes 3-phase direct drive, brushless technology.
- the stator's length and diameter set the force level, while the sleeve length determines the amplitude height.
- Motor 2601 uses a dual synchronous design wherein two stators and two permanent magnet sleeves are spaced over the entire length of the membrane. These dual linear motors are operated synchronously thus providing positive linear reciprocating motion over the entire length of the membrane. Quaking membrane cartridge at 2403 floats and is supported between an upper recoil spring system and the lower support structure spring system (both at 2403 ), thus isolating membrane cartridge movement therebetween. Spring rate is adjustable for equalization of the stator coil force requirement between upper and lower stator coils 2611 , with force requirements based on the chosen operational quaking frequency and amplitude.
- the membrane cartridge rides up and down between two resilient spring isolation systems within a stationary (housing also at 2403 ), whereas the motive reciprocating forces are provided by means of dual synchronously operating linear motor assembly 2601 .
- the two spring systems are configured to be adjustable for vibration transmissibility and damping efficiency (the spring system's ability to dissipate oscillatory energy and thus not transfer the energy to the entire quaking membrane module 2403 ).
- the modified linear motor assembly 2601 is essentially an electric motor that has its stator configured and positioned so that, instead of producing rotation, it produces a linear force along its length.
- stator coil cooling can be accomplished utilizing a cold feed water stream (for example, from the same cold feed stream feeding heat exchanger 2507 ) fed by appropriate piping to port 2701 of ring-shaped cooler 2703 mounted between retainer disks 2705 adjacent to stator coil 2411 . Feed at port 2701 is constantly replenished and recycled out at port 2707 connected at heat exchanger 2505 .
- Three-way ball valve 2521 functions as a selector valve for quaking membrane plus forward osmosis mode operations or quaking membrane mode operations only.
- FIG. 6 shows an ultrasonically active draw solution dispersion system in accord with yet another aspect of this invention.
- Alternating electrical energy from ultrasonic generator 2801 is converted to an alternating magnetic field at coil 2803 in protective housing 2805 held around the outer housing of membrane module 2403 by retaining disks 2807 .
- Coil 2803 extends substantially the entire length of module 2403 .
- Generator 2801 is adjustable.
- the oscillating magnetic field induces hydrodynamic dispersion forces (turbulence) at ultrasonic frequencies in the ultrasonically active draw solution including magnetoferritin.
- the turbulence is at the internal boundary layer of the membrane thus minimizing internal concentration polarization.
- External concentration polarization is controlled by using a low pressure magnetically coupled centrifugal feed pump with an elevated output rate for producing external feed flow turbulence.
- FIG. 7 shows one arrangement of components in a polishing treatment array 205 using membrane treatment systems especially concentrating on the integration of the membrane treatment systems of stages 423 (step 11 using the nanofiltration membrane treatment option) and 429 (step 14 using the reverse osmosis membrane treatment option). These two stages (implementing membrane processes) separate dissolved solids from the pre-treated water.
- the selection of specific membranes and spacer material are based on test results (for example, from on-site three-dimensional test cells such as those shown in U.S. Pat. No. 6,059,970).
- the systems are set to operate at moderately to high pressures and typically employ high speed gravity assisted geometries with selected variable crossflow capabilities.
- Nanofiltration membrane implementation of stage 423 is a multistage configuration, operating in series.
- the array includes, for example, three pressure vessels 2901 each having a single membrane.
- the primary function of nanofiltration membrane treatment is the removal of the finest colloidal matter.
- the separated colloidal matter is removed with the nanofiltration concentrate.
- the produced nanofiltration permeate serves as feed the next membrane and, ultimately, for reverse osmosis implementation of stage 429 .
- the reverse osmosis implemented array of stage 429 includes, for example, two stages, with two membranes 2903 operating in parallel in the first stage feeding a third membrane 2905 in the second stage. As shown, each stage thus implemented has its own pressure pump and crossflow pump 2907 , 2909 and 2911 and 2913 , respectively.
- Nanofiltration stage 423 has a maximum operating pressure of 35 bar (508 psi), and a crossflow pump maximum rating of 50 gpm at a maximum of 60 psi in a 750 psi environment.
- Reverse osmosis stage 429 has a maximum operating pressure of 70 bar (1015 psi), and a crossflow pump rating of maximum rating of 10 gpm at a maximum of 45 psi in a 1,200 psi environment.
- System operating pressure is regulated through bypass regulators 2914 and 2920 .
- the most economical ready-made nanofiltration membrane shape is a flat membrane sheet in a spiral wound membrane element.
- a spiral wound element consists of multiple membrane pockets (for example 4-16 pockets), the spiral wound pockets terminating into a centralized collecting pipe.
- Special parallel polypropylene spacers of 80 mil thickness are preferred and complete the membrane (spiral wound nanofiltration membrane elements from Nadir with a practical neutral surface voltage (zeta potential), for example).
- the nanofiltration special spacing materials are especially effective in applications with high suspended solids (colloidal) concentration. Since the primary purpose of the nanofiltration is to remove all suspended solids rather than dissolved solids (such as salts), these types of spacers with their larger spacing between the membrane surfaces are preferred. A smaller membrane spacer for other applications could be use (for example, having 33 mil diamond spacer).
- low and ultra-low pressure reverse osmosis membranes could be used (where total dissolved salts are an issue). If nanofiltration membranes are employed, crossflow pump 2909 output flow must be turned down at bypass valve 2915 for a lesser brine to permeate ratio to achieve a more desirable permeate quality.
- Reverse osmosis and/or HEED assembly buffer tank and at stages 425 and 431 can be any suitable tank and containment basin (for example, a three leg tank by SNYDER).
- Stage 427 (step 13 ) is interposed to reduce scalants in reverse osmosis processes.
- Bicarbonate (HCO 3 ) is present in many post production waters presented for treatment (such as CBM water, for example). Many produced CBM waters are near saturation in dissolved bicarbonate. When these waters are concentrated in a reverse osmosis system, calcium carbonate will be one of the first salts to precipitate. Calcium Carbonate scaling potential can be estimated using stability index calculations.
- a fouling and scaling inhibitor such as VITECH 3000
- a scaling inhibitor such as VITECH 4000
- VITECH 4000 a scaling inhibitor
- Common scale inhibitors consist of molecules that contain carboxylic or phosphate functional groups. Lower molecular weight polyacrylate molecules contain multiple carboxylic functional groups.
- membranes 2903 and 2905 are preferably spiral wound polyamide skin layer composite membranes with a zeta potential of approximately ⁇ 7 mV and a polysulfone support layer and standard 31 mil diamond spacers (since prefiltered feed water will be used).
- seawater polyamide membranes with a spacer thickness of 27 mil could be utilized.
- the polyamide thin layer membranes are constructed with an aromatic polyamide extruded onto a less dense polysulfone substrate.
- the optional seawater membrane elements use a denser polyamide membrane layer with better rejection characteristics.
- Polyamide membranes are sensitive to oxidizing agents such as free chlorine or iodine. This requires that chlorine or iodine present in the feedwater be removed by a reducing agent (such as sodium bisulfite in the case of chlorine injected upstream of the reverse osmosis modules). To avoid fouling in such case, a non-oxidizing biocide like BUSAN (150 to 1500 ppm) can be continuously injected in-line with the reverse osmosis feed stream. This mixture which kills bacteria, fungi and algae is compatible with the membrane material as well as the other injection chemicals used.
- a reducing agent such as sodium bisulfite in the case of chlorine injected upstream of the reverse osmosis modules.
- a non-oxidizing biocide like BUSAN (150 to 1500 ppm) can be continuously injected in-line with the reverse osmosis feed stream. This mixture which kills bacteria, fungi and algae is compatible with the membrane material as well as the other injection chemicals used.
- stage 429 A number of parameters can affect reverse osmosis permeate flowrate at stage 429 (or stage 425 if used there also). These include water temperature, salt concentration and membrane pressure as the feed water flows through the system. Stage 429 is preferably configured to work within a minimum and maximum range of 1,000 ppm to 20,000 ppm TDS, as well as a temperature range of 40° to 80° F. The system's maximum design pressure is around 1,000 psig.
- Membrane 2903 housings are arranged vertically rather than horizontally, and all are top fed. This operating geometry provides gravitational assistance to the high speed crossflow turbulence.
- Crossflow (recirculation flow) is provided by pump 2913 and flow controlled by bypass valve 2919 .
- System pressure is controlled by pressure regulator 2920 .
- Pressure pump 2911 operates at a maximum flowrate of 2.65 GPM at a maximum 1,029 psi.
- membrane systems are working with an unconventional high crossflow velocity, and the membrane housings are geometrically arranged in a vertical top feed position. Therefore, it allows the feed water crossing the membrane with the assist of gravity, whereby the chosen array minimizes the pressure differential across the membrane system. This differential would otherwise take away from the net driving pressure at the tail end of the individual membrane system.
- a portion of the concentrate is recycled back to the overall membrane system feed to increase recovery beyond the 75% it may have already achieved. For example, by recycling only 1 ⁇ 5 of the concentrate back to the feed, recovery can be increased to an 80% permeate recovery. This results into a 20% reduction of disposable concentrate production.
- the concentrate recirculation (retentate) flow rate for the pilot unit operation is provided through the crossflow pumps 2909 for the nanofiltration at stage 423 and 2913 for the reverse osmosis at stage 429 .
- separate high flow, low pressure crossflow pumps are utilized. Since pressure pumps 2907 and 2911 of the membrane system cannot fulfill these requirements, separate low pressure but high flow crossflow pumps operating in a high pressure environment with flowrate adjustment capability are needed. These pumps are magnetically driven with no seals and are equipped with high pressure stainless steel housings to contain a feed pressure of up to 1200 psi. The relatively small, low energy, high pressure feed pumps provide the system operating pressure. The feed pressure and flow rate is preferably regulated by a vector drive.
- the feed achieves sufficient pressure through the high pressure feed pumps for membrane separation.
- These high flow crossflow pumps provide sufficient turbulence and hydrodynamic shear to flush down and clean out the membrane flow channels of contaminated matter to minimize any fouling/scaling potential of the specific membrane system.
- the low operating pressure of the crossflow pump does not create excessive pressure even when operated at full flow capacity.
- Crossflow meters are preferably utilized to measure, control, and obtain optimum crossflow and crossflow velocity to achieve sufficient turbulence to minimize fouling/scaling potential. Turbine meters with magnetic pickups and transmitter/read-out units are preferred.
- the preferred pumps here are magnetically driven centrifugal pumps.
- the high flowrate is needed to cover a large crossflow rate range. The flowrate is easily adjustable through a valve controlled by-pass.
- FIG. 8 the preferred magnetically driven centrifugal pump 3001 (used, for example, for pumps 2909 and/or 2913 ) of this aspect of the invention is illustrated, such pumps being heretofore commercially unavailable that can operate in a high pressure environment (over 500 psi for the nanofiltration, and in excess of 1,000 psi for reverse osmosis). All high pressure parts are manufactured from compatible nonmagnetic stainless steel series 316 or 312, 316L or Hastelloy C4 (casing sections 3005 , 3013 and 3016 , for example). Nonmagnetic stainless steel is required to contain the high operating system pressure, to offer corrosion resistance in a chloride rich environment and to allow a magnetic field transfer, from drive magnet 3007 to magnet capsule 3021 , to facilitate the no touch magnetic coupling process.
- Another novel element of the pump design herein is use of off-the-shelf plastic low pressure internal pump parts (for example, impeller 3009 , mouth ring 3011 , spindle 3015 , rear thrust 3018 , front thrust 3019 and magnet capsule 3021 ). Since pump shavings from plastic impellers have been known to foul the lead end elements of membrane systems, an optional discharge screen downstream of the pump is recommended.
- a chemically resistant coating such as Ceramic, PVDF, PP, PE, HPE, PTFE or PFA is utilized to prevent pitting and is applied to the inside of high pressure pump components.
- the magnetic pump is otherwise of convention design.
- Ceramic spindle 3015 is mounted rigidly on one end onto stationary, high pressure resisting rear casing 3016 which is made from non-magnetic stainless alloy.
- Main bearing 3017 rotates on the protruding end of spindle 3015 , bearing 3017 press fitted into magnet capsule 3021 which is counter-rotationally twist-locked onto impeller 3009 .
- Pointed conical rear thrust 3018 is mounted on impeller 3009 and limits rearward movement of magnet capsule 3021 and impeller 3009 .
- Thrust 3018 rides against the front face of stationary spindle 3015 thus limiting the rear thrust.
- front thrust of magnet capsule 3021 and impeller 3009 is limited by impeller mounted mouth ring 3011 riding against the front face of stationary front thrust 3019 .
- the feed medium itself provides lubrication between moving and stationary thrust contact areas.
- in-line degasser and degasser column assemblies 3101 are shown in FIGS. 7 and 9 .
- Assemblies 3101 are specifically adapted for air and/or CO 2 removal or reduction in the produced membrane permeate flow stages 423 and 429 in order to improve flow rates and flow data acquisition in the permeate production process.
- the design, use and application of these assemblies are an improvement over prior art designs and methods.
- Assemblies 3101 condition flow of produced permeate by air/gas removal prior to processing through flow instrumentation and recording devices for the generation of real time liquid flow data without error producing air or gas content.
- Assemblies 3101 are adaptable in any setting where enhanced flow process stabilization is required in a liquid system with entrained and unwanted air or gas and where in-line degassing is needed for flowmeter applications. No packing material is needed for optimum surface area contact between the water and the air as is used in conventional tall column forced-draft degassifier designs.
- Assemblies 3101 include inline degasser 3103 and attached degasser column 3105 , and has no moving parts. Head back pressure control can be adjustable by height adjustment of elbow 3107 relative to the top of column 3105 (at cap 3109 ). Visual inspection of ongoing degassification processes can be monitored through clear column tube 3111 . Ball-valve 3113 controls flow to degasser 3103 of assembly 3101 , flowmeter 3115 following degasser 3103 . Gas supersaturated concentrate flows into the bottom of expansion chamber 3117 of degasser 3103 providing atmospheric pressure release through top connected hose 3119 . Hose 3119 is connected at the other end to degasser column 3105 .
- column 3105 provides proper back-head, back-pressure control, the column's horizontal swivel capability at cantilever arm 3121 providing dead leg free hose transfer. Head is adjusted to match individual concentrate draw-off by keeping enough column head on column 3105 , which is open to the atmosphere. As a result, a spilling out of concentrate flow is avoided. Through controlled release of back-pressure, concentrate discharge gas pressure is lowered in expansion chamber 3117 .
- Equalizer 3201 in accord with another aspect of this invention is shown in FIG. 10 .
- the method of use of equalizer 3201 is novelly adapted to use with high speed crossflow membrane systems operating in a gravity assisted mode.
- Equalizer 3201 is hydrodynamically designed for flow direction from a horizontal entry flow at port 3203 to a vertical flow in housing 3205 , and a flow directional change back from a vertical flow to a horizontal side exit flow to enhance operation of the vertically mounted high speed membrane systems.
- Flow altering distribution cones 3207 at product tube extension 3209 provide favorable hydromechanical loading and unloading for spirally wound membranes by distributing the in-rushing high crossflow of high operating pressure more evenly into the leading portion of the vertically arranged membranes. Since favorable membrane hydromechanics extends useful membrane life expectancy, cost savings are realized.
- Equalizers 3201 are mounted in place of long sweeping mounting elbows usually used for top entry and bottom exit of conventional high speed, vertical membrane system designs (at 3211 , for example, in FIG. 7 , other utilization nodes being identifiable in the drawings).
- This improved hydrodynamic design adapted for side entry operation is a practical method for reducing overall height and footprint requirements of a vertically mounted, high speed membrane system.
- FIGS. 11 a and 11 b a first embodiment of a high frequency membrane separation apparatus and method utilizable with membrane systems of this invention is shown in FIGS. 11 a and 11 b .
- This invention relates to apparatus and methods for fluid filtering utilizing membrane separation (for example nanofiltration and/or reverse osmosis filtration) that combines vibratory shear techniques with adjustable crossflow techniques.
- membrane separation for example nanofiltration and/or reverse osmosis filtration
- This and further embodiments of the high frequency membrane separation apparatus and methods are particularly well adapted to treatment stages 419 , 423 , 429 and/or 433 when membrane treatment options are applied (generically referred to hereinafter as membrane treatment systems).
- High frequency membrane separation herein refers to vibrating, oscillatory motion of the membrane support structure. Vibration direction is perpendicular to the floor of the installation for gravity assisted membrane separation systems.
- the vibration curve is preferably a regular curve, which corresponds mathematically to a zero centered sine or cosine, a sinusoidal or simple harmonic.
- the amplitude is preferably steady and frequency high.
- This hybrid does not depend solely on vibratory induced shearing forces to prevent fouling and thus does not require total shut down of the membrane separation process during preventive maintenance on the vibrators.
- the shear wave produced by axial vertical membrane vibration causes solids and foulants to be lifted off membrane surfaces and remixed with retentate flowing through the parallel or tunnel spacer or other specially designed spacers of spirally wound elements or through flow channels of tubular or capillar membrane elements. Movement continuity is maintained through the adjustable crossflow, reducing further additional membrane fouling tendency.
- each membrane module requires its own vibratory energy source. Only a single vibratory engine 3303 is utilized for a multi-membrane module design herein (up to thirty-two 2.5′′, sixteen 4′′ or eight 8′′ membrane modules).
- high frequency membrane separation apparatus of this invention can be operated at an incline using center pivot 3304 for adjustment of swivel framework 3305 (from standard vertical position to a maximum 15° incline orientation) in swivel support 3306 .
- center pivot 3304 for adjustment of swivel framework 3305 (from standard vertical position to a maximum 15° incline orientation) in swivel support 3306 .
- this approach is more flexible.
- conventional membrane modules can be used, and mounting of membrane modules in a vertical flow gravity assisted position with adjustable crossflow operation is accommodated.
- This embodiment of the high frequency membrane separation apparatus uses twin motors connected at shaft/eccentric and weight assemblies 3307 and 3309 of the motors in vibratory engine 3303 to provide shear enhanced fouling reducing membrane separation (these vibrator motors are well known structures).
- the motors are preferably 3-phase 1800-3600 RPM induction motors delivering high speed synchronized centrifugal force, one motor rotating shaft/eccentric and weight 3307 counter-clockwise and the other rotating shaft/eccentric and weight 3309 in a clockwise direction.
- the vibrator motors are capable of producing net centrifugal forces that change direction in space as the motor rotates. Such a force acts upward at one instant and downward a half-rotation later, thus producing a force that acts sinusoidal at a frequency that corresponds to shaft/eccentric/weight assemblies' 3307 / 3309 rotation.
- Adjustable eccentric weight provides variable force output (from 0% to 100%) at a synchronized mode of operation (i.e., the adjustable weights are aligned with each other at 90° for clockwise rotation and 270° for counter-clockwise rotation).
- a vibratory high-speed linear motion through center of gravity thus impacts swivel framework 3305 having the vibrating motors mounted on the inside thereof and the membrane modules mounted on the outside thereof.
- Support box frame structure 3310 is preferably square tubing 2 ′′ ⁇ 2′′ with a 1 ⁇ 8′′ wall.
- Frame structure 3310 carries membrane modules (hereinafter 3311 , generally applied, for example, to modules 2901 or 2903 / 2905 of FIG. 7 or other membrane modules disclosed herein and related to the various nanofiltration and reverse osmosis options) and includes frame uprights 3312 mounted via rubber dampeners 3313 (preferably eight) at swivel framework 3305 (one upright per corner of the support structure).
- Swivel frame uprights 3315 of support 3306 are preferably made from fabricated 1 ⁇ 4′′ steel material, and are connected to seismic absorbing mass at fabricated steel base frame 3317 .
- Base frame 3317 is preferably at least partially filled with concrete to add mass.
- Two springs 3319 are located in-line at the top of support structure box frame 3310 (supporting panel structure not shown) and between horizontal top frame members 3321 of the open swivel framework 3305 .
- Dampeners 3323 are located adjacent to bottom frame member 3325 of swivel framework 3305 .
- urethane springs/dampeners are preferred for their high load-carrying capability, longer life, abrasion resistance, low noise, and vibration damping and shock absorbency.
- the springs themselves are cylindrical, and four connecting bolts 3327 fasten support structure 3310 to swivel framework 3305 .
- the fine-threaded connecting bolts allow for vibratory amplitude adjustment in a range up to about 1′′. If combined with conventional coil springs, the vibratory amplitude adjustment range increases up to 1.5′′.
- adjustable frequency drive or inverter drive
- FIGS. 12 through 16 A second embodiment of the high frequency membrane separation apparatus and methods of this invention is shown in FIGS. 12 through 16 .
- vibration is hydrodynamically controlled.
- This embodiment is specially applicable whenever a homogen disperse fluid substance with a lower concentration polarization layer has to be treated—for instance, organic and inorganic colloidal solution as well as fine disperse suspensions and higher concentrations of salt solutions (TDS 1,000-50,000 mg/L). Since high shear rates are not required in high frequency membrane separation apparatus 3401 , apparatus 3401 can be configured to operated at a lower amplitude. System 3403 can operate efficiently at a lower amplitude.
- Vibratory impulse energy is provided through the primary feed pump (for example, pumps 2907 / 2911 as shown in FIG. 7 ), no secondary vibratory energy source is required. Furthermore, only the membrane, fluid column (preferably pre-filtered as taught herein, generally represented at 3404 ) and some associated internal components of apparatus 3401 are vibrated (not the entire unit including support mass).
- One feed pump 2907 / 2911 can serve one or many modules in parallel feed array.
- hydrodynamic vibration herein provides axial vibration of amplitude “Y” to enhance the sinusoidal flow pattern between transverse spacer rods 3801 in membrane media 3802 (see FIG. 16 ). Vibration amplitude is controlled through stroke adjustment.
- the system operates with low vibratory energy waves which are scaled to provide effective agitation.
- Axial vibration with a maximum amplitude Y of only about 2 mm for a spirally wound membrane is sufficient to maintain proper permeate continuity.
- Apparatus 3401 provides sinusoidal meandering turbulent cleaning action by high frequency vibration up to 180 Hz in a tangential direction to the surface of the membranes (see FIG. 16 ).
- membrane element 3405 is oscillated within the membrane housing 3407 (see FIGS. 13 through 15 ).
- the bulk stream containing the returned suspended particles between the membrane leaves of spirally wound membrane elements (generally at 3803 in FIG. 16 ), and in the flow channels of tubular and/or capillary membrane elements, is continuously flushed out of the membrane module by means of the gravity assisted low crossflow. Since apparatus 3401 does not depend on crossflow induced turbulence, feed of a homogen fluid substance with a lower concentration polarization layer can be concentrated at a higher level.
- Crossflow pressure can be maintained in a low range between 35 and 140 kPa (utilizing crossflow pump 2902 / 2913 , for example) thus producing an adjustable low crossflow velocity in the range of 0.075 to 1 m/s and requiring low operating energy.
- Sufficiency of turbulence for anti-fouling/scaling is maintained by high frequency of the vibration.
- Produced are low vibratory energy waves scaled to provide a nonstagnant membrane area environment with effective sinusoidal meandering turbulence to the boundary layer 3805 area, settling of suspended particles thus inhibited.
- Feed activated hydrodynamic impulse system 3501 is best illustrated in FIGS. 13 through 15 .
- a pulsating high pressure water jet is receive from plunger pump 2907 / 2911 through inlet port 3503 through lower retainer ring 3504 and feed ring-room housing 3505 at lower section 3506 .
- Housing 3407 holding filter module 3405 is ported as required for feed input and concentrate and permeate output and is constructed accordingly.
- Upper section 3601 ( FIG. 14 ) includes permeate discharge connector 3603 , upper retainer plate 3605 , spring rings 3606 , bolt retainer plate 3607 , spring adjustment plate 3609 , return spring 3611 and lantern ring 3613 .
- Variously sized O-rings seals 3615 seal the unit.
- Membrane coupling 3617 couples connector 3603 to membrane 3405 .
- Lower section 3506 ( FIG. 15 ) further includes permeate tube plug 3703 , ring piston 3705 , retentate discharge connector 3707 , and spring rings 3709 and 3711 . Again, various sized o-rings 3713 seal the apparatus. As can be appreciated the pulsating jet of water received through port 3503 vibrates module 3405 at ring piston 3705 at the rate of pulsation. Reciprocation is limited and maintained by spring 3611 operating against ring 3613 (held in adjustment by adjustment plate 3609 ).
- FIGS. 17 and 18 Self-contained, vibratory spring, seal and transfer conduit apparatus and methods, in accord with yet another aspect of this invention, are illustrated in FIGS. 17 and 18 .
- the self contained, vibratory spring, seal and transfer conduit apparatus and methods of this invention provide a flexible sealing connection between an oscillating and a stationary object by means of a fluid conveying elastomeric conduit connection.
- the flexible fluid conveying conduit is equipped with nonflexing end connectors to provide motionless sealing surfaces for the associated o-ring seals which are housed in the respective objects.
- Self contained apparatus 3901 is adapted for (but not limited to) use with vibrating membrane technology of the type shown herein in FIG. 13 (and numbers therein common to both embodiments are carried forward).
- Apparatus 3901 is preloaded under tension by a polyurethane based permeate transfer conduit 4003 (also referred to herein as polyurethane spring conduit 4003 ).
- the material used has a durometer of about 60 A and has high rebound values (greater than 65%) sufficient to withstand high frequency vibrations.
- the materials is selected to have high load bearing properties in both tension and compression). All machine elements thus remain in alignment and remain stationary (relative to one another) thereby preserving sealing surfaces while the vibratory load is operating.
- Springs 4005 generate a portion of the compressive force counter reacting the tension load of polyurethane spring conduit 4003 .
- Pre-load retainers 4007 preferably stainless steel retainer rings or spring clips
- Springs 4005 are held between upper and lower load guides 4009 and center load guides 4011 , load transfer spacer 4013 spanning center guides 4011 spacing the two spring columns (formed by a spring 4005 and one each of load guides 4009 and 4013 ). This arrangement equally distributes the low value tension and compression loads.
- Spring 4015 further supports polyurethane spring conduit 4003 .
- Conduit 4003 is mounted at the upper end with a modified plate 4016 , abutting modified permeate discharge connector 4004 , and at the lower end to a modified lantern ring 4017 .
- Load transfer spacer 4013 has a length selected so that maximum urethane spring conduit 4003 deflection is less than 2%.
- Urethane spring manufacturers suggest a maximum deflection of 25% and a maximum cycle rate of 700 cycles per hour for intermittent operation. For continuous operations and a maximum deflection of 15%, a maximum cycle rate of 12,000 cycles per hour is suggested. Because apparatus such as apparatus 3901 has a cycle rate of between 216,000 and 648,000 cycles per hour, the deflection percentage needs to be significantly reduced.
- Apparatus 3901 provides wear and leak-free operation for permeate fluid transfer between oscillating membrane element 3405 and its stationary housing 3407 components, thus effectively avoiding contamination of the produced permeate with feed water.
- Apparatus 3901 accommodates either high frequency membrane separation housing designs (side port entry and the top port entry) and serves as a return spring for apparatus 3401 as well as a permeate transfer conduit and seal unit. Modular design accommodates ease of maintenance.
- lower spring 4005 column oscillates simultaneously with the module 3405 , while at the upper side of apparatus 3901 upper spring 4005 column remains steadier so that the connecting end of conduit 4003 remains motionless in its sealing seat 4019 . This is due to the return spring pressure acting upon the upper retainer which keeps the upper male connecting end securely in its sealing seat.
- FIGS. 19 and 20 illustrate a high shear and high amplitude internal membrane separation apparatus and methods.
- This invention relates to permeate continuity in water treatment processes. More particularly, the purpose of this aspect of the invention is to achieve high shear in such processes to increase permeate continuity while treating high load of colloidal and slimy matter (polysaccharide, etc.) in treatment station feed water.
- Apparatus 4101 illustrated in FIG. 19 offers high shear operation for internally vibrating membrane separation systems of the types heretofore disclosed.
- This high shear option is provided by means of a high vibration amplitude in the range of 1/32′′ to 3 ⁇ 8′′.
- such high amplitude vibration could damage membrane element 3405 .
- an all-surrounding membrane support tube 4103 with upper and lower connecting end pieces 4105 and 4107 which are rigidly coupled and locked to support tube 4103 by split tongue and groove rings 4109 are provided, thus converting membrane element 3405 into membrane cartridge 4111 having element 3405 therein.
- Membrane cartridge 4111 provides a backlash free, non-load bearing and non-force transmitting, hardened operating environment for membrane element 3405 .
- End pieces 4105 and 4107 also provide means for membrane fluid transfer.
- Upper end piece 4105 has two conduits 4113 for crossflow feed influent and 4115 for produced permeate effluent.
- Lower end piece 4107 has multiple inclined conduits 4117 (at least four conduits for smaller membranes) all merging into large retentate effluent conduit 4119 of venturi nozzle 4121 .
- Nozzle 4121 has an outside cone angle of about 21° to support venturi function and enhance rapid transfer of the pulsating, make up feed flow at elevated operating frequencies.
- High pressure vibrating pulsating feed input 4123 through lower flange and injector body assembly 4124 is positioned to operate against surface 4125 of lower end piece 4107 to vibrate cartridge 4111 .
- a containment housing 4127 is welded to transfer flange assemblies 4129 (upper) and outer flange 4130 of assembly 4124 , the lower flange assembly bolted together by bolt and nut sets 4131 through lower inner flange 4132 and outer flange 4130 of assembly 4124 .
- Upper flange assembly is bolted together with bolt and nut sets 4133 having recoil springs 4135 thereover for recoil adjustment.
- Safety guard 4137 is mounted at the top of apparatus 4101 and includes a window for on-site amplitude inspection.
- the structural integrity of the membrane element 3405 needs to be strong enough to sustain its own vibratory mass acceleration forces within its hardened enclosure.
- the preferred spirally-wound membrane element design for all high frequency membrane separation applications in high shear mode includes fiberglassed outside for holding element 3405 together.
- amplitudes greater than 3 ⁇ 8′′ are not recommended for the spirally-wound membrane elements under any circumstances since adhesive membrane joints fatigue prematurely at higher operating frequencies (60 Hz).
- Apparatus 4101 allows operation of vibratory membrane implementations at higher shear at moderate frequency (20 to 60 Hz).
- Membrane cartridge 4111 is relatively light and vibrates internally at an adjustable up to a relatively high frequency within housing 4127 (rather than vibrating the entire heavy membrane module as is common in conventional vibratory membrane separation processes).
- a primary application for this high shear option for high frequency membrane separation systems is the effluent treatment of dewatered electrocoagulation sludge. This is an important treatment step whenever a required electrocoagulation process generates sludge and the produced sludge requires dewatering prior to disposal. Any other application where an elevated shear energy requirement for treatment of a specific feed water is diagnosed would benefit from use of apparatus 4101 .
- End pieces 4105 and 4107 are preferably machined out of any suitable material such as metal alloys or engineering plastic materials (selected to keep the vibratory mass low).
- antichanneling flow distribution plug 4139 having splash dome 4141 blocks direct throughflow and guides the feed flow into ring room flow distribution channel 4143 defined at end piece 4105 .
- Splash dome plug 4139 rests on a shoulder in the lower section of feed conduit 4113 and is secured in its upper position by stainless steel retainer ring 4142 .
- a flared fluid transfer opening from ring room 4143 faces towards the anti-telescoping device at the lead end of membrane element 3405 .
- Step bore 4145 in end piece 4105 seals (at o-ring 4147 ) the upper end of permeate collection tube 4149 .
- the outside of upper end piece 4105 includes groove structures, the first to receive upper reciprocating groove ring seal 4151 to seal the upper portion of membrane cartridge 4111 .
- a second high and shallow groove 4153 receives the overlapping split tongue ring 4109 (connectable at its other end in groove 4155 of tube 4103 .
- the split tongue ring halves can be held together by dual spring rings or other suitable means.
- O-ring 4157 seal upper end piece 4105 and support tube 4103 .
- shims can be added to flow distribution and screen plate 4159 sandwiched between upper end piece 4105 and the anti-telescoping device at the lead end of membrane element 3405 . (and where applicable, at the permeate collection tube). Membrane element backlash is thus virtually eliminated.
- Plate 4159 provides the necessary pressure drop for proper crossflow feed distribution around the feed ring room. In conjunction with anti channeling flow distribution plug 4139 , plate 4159 minimizes localized feed channeling, thus utilizing more efficiently the available membrane area for diffusive fluid transfer. Plate 4159 also acts as a crossflow pump discharge filter screen to catch any particles and foreign objects.
- Support tube 4103 can be made from a thin-walled metal alloy a heavier walled, suitable plastic material in order to reduce the vibratory mass. Support tube 4103 is grooved at it bottom end (at 4155 ) to provide a connection sites for tongue and groove ring 4109 thereat. U-cup seal gasket 4161 is placed around the outside (in a concentrate seal holder 4162 ) of the lead end of the membrane element 3405 . This gasket seals membrane element 3405 to external support tube 4103 and prevents the crossflow feed influent from bypassing the membrane element.
- membrane element 3405 Downstream, membrane element 3405 is equipped with an anti-telescoping device that is connected to lower end piece 4107 by means of the extended lower end of its permeate collection tube 4162 .
- Tube 4162 is sealed at o-ring 4163 at lower end piece 4107 .
- Lower end piece 4107 itself is rigidly coupled and sealed to support tube 4103 in the same manner as upper end piece 4105 .
- the top face of lower end piece 4107 is equipped with a tapered, shallow ring groove 4165 .
- Groove 4165 collects and distributes concentrate/retentate fluid through multiple inclined fluid transfer conduits 4117 which are distributed around groove 4165 .
- Venturi nozzle 4121 Protruding venturi nozzle 4121 , is fitted in inlet chamber 4166 which is defined by injector body 4167 of assembly 4124 protruding into lower end piece 4107 leaving a small ring room 4169 adjacent surface 4145 of end piece 4107 for the distribution of the high pressure, pulsating make up feed flow. Venturi nozzle 4121 has an effective sealing length equivalent to the maximum operating amplitude.
- End piece 4107 has a dual purpose concentric guide shroud 4171 providing a close fit concentricity between the axially vibrating lower end piece 4107 and non-vibrating injector body 4167 .
- Shroud 4171 defines a reasonable operating clearance between end piece 4107 and external housing 4127 to ensure proper operation of reciprocating seal 4172 sealing housing 4127 and vibrating membrane cartridge 4111 from potential fluid loss.
- Shroud 4171 also provides impact surface 4173 contacting amplitude regulating impact ring 4175 .
- Ring 4175 is preferably made from polyether-based urethane (60 on the Shore A scale), providing shock deadening. Ring 4175 is configured and positioned for highly resilient operation providing quick recovery in high-frequency vibration applications (rebound values from 50 to 70%). Vibration amplitude ranges can be regulated by ring height selection. An increase in ring height increases the volume of the distribution ring room 4169 while reducing the effective height of the cylindrical shaped section of nozzle 4121 .
- the unchanged volume of the displacement stroke of high pressure piston pump ( 2907 or 2911 , for example, in FIG. 7 ) first fills the volume of ring room 4169 with feed liquid before it starts to initiate an axial, upward movement of membrane cartridge 4111 .
- a fluid transfer passage around nozzle 4121 (from ring room 4169 to chamber 4166 ) opens and passes the liquid which then flows by the 21° cone-shaped end of nozzle 4121 of lower end piece 4107 .
- Injector body 4167 is also preferably a unitary structure, machined, for example, from either suitable metallic alloys or plastic material. Injector body 4167 has large conduit 4177 and smaller conduit 4179 , conduit 4177 for transfer of concentrated retentate and the pulsating, make up feed influent to crossflow recirculation pump as discussed hereinabove. Conduit 4179 is the input for the vibration inducing feed. Injector body 4167 is sealed at outer housing 4127 with o-ring 4181 . Camber 4166 tapers down at conduit 4177 to funnel the flow into recirculation suction connector pipe 4183 maintained through inner lower flange 4132 .
- Injector body 4167 is positioned and kept in place inside external housing 4127 by flange 4132 .
- the weldment of flange 4130 and housing 4127 could be replaced by an integral structure such as a pipe spool.
- An upper impact and buffering ring 4185 (made from a polyurethane material) is located between upper end piece 4105 and upper inner flange 4186 of flange assembly 4129 (the weldment of flange 4187 of assembly 4129 to housing 4127 could also be replaced by an integral structure such as a pipe spool).
- FIG. 20 While not preferred, a potentially useful alternative draw off arrangement for apparatus 4101 as illustrated in FIG. 20 could be utilized.
- This arrangement provides secondary retentate conduit 4201 in conduit 4183 and through injector body 4167 and chamber 4166 defined by lower end piece 4107 so that its inlet 4203 resides above venturi nozzle 4121 in conduit 4119 .
- draw off received through cartridge 4111 can be at least partially segregated from mixed retentate and feed received during operations from ring room 4169 .
Abstract
Apparatus and methods are disclosed for mechanical axial vibration in membrane separation treatment processes. The apparatus includes a separation membrane element having an axial dimension, a membrane support structure having the element therein, and means for vibrating the membrane element (hydrodynamically or using motors) in the axial dimension.
Description
- This application is a Division of now pending U.S. patent application Ser. No. 12/452,778 filed Jan. 22, 2010 by the inventors herein and entitled Mechanical Axial Vibration In Membrane Separation Treatment of Effluents, which prior application is a continuation of U.S. patent application Ser. No. 11/888,512 filed Aug. 1, 2007 by inventors including the inventors herein.
- This invention relates to effluent treatment, and, more particularly, relates to membrane separation treatment of effluents.
- Most industrial and municipal processes require water treatment facilities to treat effluents returned to the environment. Such facilities typically represent a significant investment by the business/community, and the performance of the facility (or failure thereof) can seriously impact ongoing operations financially and in terms of operational continuity.
- Moreover, not all effluent treatment requires the same technologies. Industrial effluents (such as is found at coal bed methane facilities or oil production sites, for example) all have different particulate, pollutant and/or biomass content inherent to both the industrial processes as well as the particular water and soil conditions found at the site. Municipal requirements would likewise vary depending on desired end-of-pipe quality and use (and again depending on the feed water present at the site).
- Filtering by membrane separation techniques is known. Membrane elements in such use require constant maintenance and frequent cleaning or replacement. Vibratory means have been heretofore known and/or utilized in membrane separation to reduce maintenance requirements. These have employed horizontal vibratory torsional motion, and often require use of proprietary one source only custom membrane modules. Further improvements could thus still be utilized.
- This invention provides methods for mechanical (motorized, electromagnetic or hydrodynamic) axial vibration in membrane separation treatment of effluents. The methods allow use of readily available, and thus less costly, conventional membrane elements and/or modules. Axial, linear operation allows mounting of membrane modules in a vertical flow gravity assisted position, with adjustable crossflow operation accommodated.
- The methods are adapted to apparatus including a separation membrane element having an axial dimension, a membrane support structure having the element therein, and means for vibrating the membrane element in the axial dimension. Crossflow pumping is connected with the support structure. In one embodiment, the support structure includes a membrane housing, the vibrating means including a fluid pump and spring arrangement for oscillating the membrane element. In another embodiment, the support structure includes a tube for receiving and securing the membrane element, the tube and element together defining a membrane cartridge, the cartridge axially mounted in a containment housing and movable axially therein by the vibrating means (hydrodynamically or electromagnetically, for example). In yet another embodiment, the vibrating means are motors for vibrating a plurality of elements on a common platform.
- The methods of this invention include the steps of locating a membrane element in a support structure and feeding effluent for treatment into the support structure. Axial vibration of the membrane element in the support structure is initiated without securement of the membrane element to a source of vibration, and treated effluent is withdrawn from the support structure. The membrane element is located in the support structure without attachment to the support structure or other structure outside the support structure. Vibration of the membrane element in the support structure in the axial dimension is accomplished using any of hydrodynamic, electromagnetic and mechanical methods.
- In one embodiment, the membrane module is positioned in a containment housing configured for free axial movement of the membrane module therein, extent of axial movement being adjustably limitable. Axial vibration is hydrodynamically activated in the containment housing as limited.
- Vibration direction is axial and preferably perpendicular to the floor of the installation for gravity assisted membrane separation systems. The shear wave produced by axial vertical membrane vibration causes solids and foulants to be lifted off membrane surfaces and remixed with retentate flowing through the parallel or tunnel spacer or other specially designed spacers of spirally wound elements or through flow channels of tubular or capillar membrane elements. Movement continuity is maintained through adjustable crossflow, reducing further additional membrane fouling tendency. The vibration curve is preferably a regular curve, which corresponds mathematically to a zero centered sine or cosine, a sinusoidal or simple harmonic. The amplitude is preferably steady and frequency high.
- It is therefore an object of this invention to provide methods for mechanical axial vibration in membrane separation treatment of effluents.
- It is another object of this invention to provide methods for mechanical axial vibration in membrane separation treatment of effluents that accommodates use of readily available, conventional membrane elements and/or modules.
- It is another object of this invention to provide a method for axial vibration in membrane separation treatment of effluents that includes the steps of locating a membrane element in a support structure, feeding effluent for treatment into the support structure, initiating axial vibration of the membrane element in the support structure without securement of the membrane element to a source of vibration, and withdrawing treated effluent from the support structure.
- It is still another object of this invention to provide a method for axial vibration in membrane separation treatment of effluents including the steps of locating a membrane element having an axial dimension in a membrane support structure without any direct attachment of the membrane element to the support structure or other structure outside the support structure, and vibrating the membrane element in the support structure in the axial dimension one of hydrodynamically, electromagnetically and mechanically.
- It is yet another object of this invention to provide a method for axial vibration in membrane separation treatment of effluents which includes the steps of positioning a membrane module in a containment housing configured for free axial movement of the membrane module therein, adjustably limiting extent of axial movement of the membrane module in the containment housing, and hydrodynamically activating axial vibration of the membrane module in the containment housing as limited.
- With these and other objects in view, which will become apparent to one skilled in the art as the description proceeds, this invention resides in the novel construction, combination, and arrangement of parts and methods substantially as hereinafter described, and more particularly defined by the appended claims, it being understood that changes in the precise embodiment of the herein disclosed invention are meant to be included as come within the scope of the claims.
- The accompanying drawings illustrate a complete embodiment of the invention according to the best mode so far devised for the practical application of the principles thereof, and in which:
-
FIG. 1 is a block diagram illustrating phased functions in an effluent treatment regime; -
FIG. 2 is a diagram illustrating a first membrane technology of this invention utilizable in steps directed to the primary (effluent polishing) treatment of effluents; -
FIG. 3 is a diagram illustrating a second membrane technology of this invention utilizable in steps directed to the primary treatment of effluents; -
FIGS. 4 a and 4 b are illustrations of coil structures utilizable in the technology ofFIGS. 2 and 3 ; -
FIG. 5 is a detailed view illustrating coil cooling utilizable in the technology ofFIGS. 2 through 4 ; -
FIG. 6 is a diagram illustrating apparatus for internal concentration polarization control in the technology ofFIGS. 2 through 4 ; -
FIG. 7 is a diagram illustrating one membrane deployment option utilizable in primary treatment steps of this invention; -
FIG. 8 is a sectional illustration of a crossflow pump of this invention utilized in various membrane separation technologies; -
FIG. 9 is a sectional illustration of an improved degasser column used with the membrane systems of this invention; -
FIG. 10 is a flow distributor and discharge equalizer deployed, for example, with the membrane systems of this invention; -
FIGS. 11 a and 11 b are diagrams illustrating a high frequency oscillating membrane system utilizable in primary treatment of this invention; -
FIG. 12 is a sectional diagram illustrating a second embodiment of the high frequency oscillating membrane system; -
FIG. 13 is a partial sectional illustration of the oscillating membrane system ofFIG. 12 ; -
FIG. 14 is a detailed sectional illustration of the upper part of the oscillating membrane system ofFIG. 13 ; -
FIG. 15 is a detailed sectional illustration of the lower part of the oscillating membrane system ofFIG. 13 ; -
FIG. 16 is an illustration showing function of the spirally wound membrane elements of the oscillating membrane system ofFIG. 13 (also employable in other oscillating systems shown herein); -
FIG. 17 is a diagram illustrating an alternative deployment of the oscillating membrane system ofFIG. 13 ; -
FIG. 18 is a sectional illustration of a vibratory seal arrangement for the oscillating membrane system ofFIGS. 13 and 14 ; -
FIG. 19 is a sectional illustration of a high shear embodiment of the oscillating membrane system ofFIGS. 12 through 17 ; and -
FIG. 20 is a sectional illustration of a draw-off utilizable in the high shear embodiment ofFIG. 19 . - As background,
FIG. 1 shows steps of an effluent treatment regime. The option numbers located at three-way valves 401 refer to automated or override manual flow control options for different treatment regimes. Stage 403 (step 1) is a dual strainer receiving feed effluent and removing particulates down to about 500 μm (for example, the model 120 dual strainer produced by Plenty Products, Inc.). Stage 405 (step 2) provides oil separation from the feed flow utilizing a separator (for example, a Highland Tank & Mfg. Co. R-HTC Oil/Water Separator with Petro-Screen and parallel corrugated plate coalescers). Stage 407 (step 3) is an automatic backflush filter providing particle removal down to the 100 μm range or better (a TEKLEEN self cleaning bell filter setup with GB6 electric controller by Automatic Filters, Inc., or similar filter setups by Amiad Filtration Systems, could be utilized for example). - Stage 409 (step 4) provides inline direct feed effluent (water) heating. Feed water heating is required in many treatment settings due to seasonal operations, and further benefits many downpipe treatment options by breaking feed water alkalinity, enhancing CH4 gas removal, ensuring proper membrane (where present) permeate flux for an overall constant permeate flow yield, and the like. Either of two types of inline heating systems may be utilized, as more fully detailed below.
- Stage 411 (step 5) is a first suite of pre-treatment apparatus including eight apparatus (all eight are preferred, but fewer could be provided in some applications). These apparatus provide, as more fully detailed below, on-line diffusive effect (ODE) membrane aeration, fluid density reduction, modified vacuum tower or cascade series waterfall degassing, air stone degassing, modified venturi gas evacuation, fine filtration, lamella plate clarification, and sludge chamber concentration.
- Stage 413 (step 6) is a second suite of pre-treatment apparatus including ten apparatus (all ten are preferred, but fewer could be provided in some applications). This stage provides pH adjustment (via an injection pump 302), chemical dosing (via an
injection pump 304, ODE/IDI (inline diffusive ionization) membrane aeration, ionized air/gas treatment, electrocoagulation, dissolved air/gas flotation, vacuum introduced cyclone separation, vacuum degassing, lamella plate clarification, and sludge chamber concentration. - Stage 415 (step 7) provides a bag filter and/or belt filter assembly (for example, fabric filtration systems sold by SERFILCO) for filtration down to about the 1 μm range. Stage 417 (step 8) is a homogenizing and buffer tank with pH adjustment and chemical dosing (at injection pumps 306 and 308, respectively). Stage 419 (step 9) is the first of the primary, effluent polishing treatment array (
stages 419 through 433,steps 9 through 16), and may include any of several membrane treatment apparatus in accord with this invention as more fully detailed hereinafter providing nanofiltration, and/or known ion-exchange treatment technology.Stage 419, as is apparent, is an option for up-concentrating effluent to increase overall flow yield. - Stage 421 (step 10) provides antifouling and antiscaling chemical treatment to prevent fouling and scaling of membranes by keeping low molecular weight components in solution (foremost of which are divalent and multivalent cations). Known variable speed tubing pumps could be utilized for insertion. Stage 423 (step 11) provides filtration for removal of low molecular weight components (Al, Fe, Mg and Mn, for example) and/or colloidals utilizing membrane treatment nanofiltration and/or ion-exchange treatment. Stage 425 (step 12) provides a buffer tank for
step 14 for process flow control (for example a Snyder horizontal leg tank by Harrington). Stage 427 (step 13) provides antiscaling chemical treatment addressing monovalent and a few divalent cations and anions (Ba, Ca, Na, Sr, CO3F, HCO3, and SO4 for example). Again, known variable speed tubing pumps could be utilized for insertion. - Stage 429 (step 14) addresses removal of low molecular weight components (salts, for example) utilizing reverse osmosis membrane treatment and/or ion-exchange treatment. Stage 431 (step 15) is a high pressure buffer tank providing flow control for
step 9 and/or 16. Stage 433 (step 16) provides up-concentration of concentrate flow fromstage 429 to further increase flow yield, and may utilize reverse osmosis membrane treatment, ion-exchange treatment and/or high efficiency electrodialysis technology (for example, a HEED assembly by EET Corporation), a hybrid process including both electrodialysis and reverse osmosis approaches. - Stage 435 (step 17) is a suite of four post-treatment apparatus as more fully detailed herein below, and including activated carbon filtration for gas absorption (Ametic filter chambers by Harrington, for example), sodium absorption ratio compensation, utilizing a dolomite filter for example, UV treatment (for example, an SP or SL series unit from Aquafine Corporation), and membrane aeration for O2 saturation (preferably utilizing an ODE system in accord with yet another aspect of this invention).
- Stage 437 (step 18) provides bio-monitoring utilizing a 10 gallon aquarium with the operating volume passing through either a sterilizer or other aquarium device to prevent in situ bio-contamination from waste and nutrients. The sterilizer or other device must match the maximum produced permeate flow of at the rate of approximately one gallon per minute for real time bio-monitoring. Since the sterilized water is typically being mixed with unsterilized water, it is not possible to completely purify it, but a sterilized percentage exceeding 99.9% is acceptable for the bio-monitoring step sensitivity. Stage 439 (step 19) conventionally provides waste collection and purified feed return.
- Regarding the ion-exchange treatment alternative at
stages steps - An organic ion exchange resin is composed of high molecular-weight polyelectrolytes that can exchange their mobile ions for ions of similar charge from the surrounding medium. Each resin has a distinct number of mobile sites that set the maximum quantity of exchanges per unit of resin. Ion exchange reactions are stoichiometric and reversible.
- Commercially available ion-exchange treatment technology can be utilized alone as an alternative to the hereinafter detailed membrane treatment technology or may supplement specific membrane technology. The implementation of ion-exchange technology depends on the specific application and project economics (the less complex and labor-intensive state of the art ion exchange technology may be used as a single polishing step instead of membrane treatment where cost is a factor and desired treatment outcomes warrant the tradeoff).
- In some settings, primarily depending on the intended use of the purified water, complete deionization (replacement of all cations by the hydrogen ion as well as replacement of all anions by the hydroxide ion) may be required. In such case, commercial cation- and anion-exchange technology will be employed as a polishing treatment step alone or in addition to membrane treatment (again depending on the end-of-pipe outcomes desired). For example, feed water with total dissolved solids of less than about 500 mg/L is ideally suited for ion exchange technology in combination with reverse osmosis membrane treatment. In other words, after membrane treatment at step 14 (429), the produced permeate is fed into a strongly acidic cation exchanger followed by a strongly basic anion exchanger (substituting for both
steps 15 and 16). Such systems are commercially available from KINETICO, REMCO ENGINEERING and others. - Membrane treatment and other treatment systems (205 in some of the FIGURES), including
stages 419 through 433 (steps 8 through 16), may be realized by deployment of various types of apparatus and systems, particularly atsteps steps stages - At
stage 419, high frequency nanofiltration systems as discussed hereinbelow could be employed. However, in accordance with one aspect of this invention,FIGS. 2 through 5 illustrate an axial (linear) vibratory membrane separation apparatus and methods for forward osmosis. This aspect of the invention relates to low amplitude, axial vibratory membrane separation apparatus (both nanofiltration and reverse osmosis filtration) called quaking recycle membrane separation technology employed with forward osmosis technology. Forward osmosis technology is employed to supplement the quaking membrane nanofiltration and/or reverse osmosis technology, the hybrid application incorporated into an integrated apparatus (high frequency forward nanofiltration or high frequency forward reverse osmosis apparatus). - Heretofore known forward osmosis technology uses the osmotic pressure differential across a membrane, rather than the hydraulic pressure differential, for filtration. The osmotic pressure differential is provided by a recyclable solute composed of a mixture of salts, the thermally recyclable salt solution called “draw solution”. Draw solutions typically used include ammonium bicarbonate (NH4HCO3), ammonium carbonate (NH4)2CO3, ammonium carbamate NH4NH2CO2; (H4NO)(CONH2; H2N—CO—O—NH4), and can preferably include magnetoferritin in solution. The concentration of solutes in the thermally recyclable draw is required to have a higher osmotic pressure than the osmotic pressure of the concentration of solutes in the feed water (often brackish). Common spiral-wound membranes have not been heretofore utilized for forward osmosis because a liquid stream cannot be forced to flow on the support side (permeate side) inside the envelope, where the porous polymer layer further increases the internal concentration polarization. The apparatus of this aspect of the invention employs tubular or hollow fiber membrane modules, rather than spiral-wound membrane elements.
- The hybrid quaking membrane plus forward osmosis process and apparatus of this invention secure permeate continuity of the present art forward osmosis technology (generating extreme turbulence on both sides of the forward osmosis membrane (feed side and draw side) to support permeate continuity), provide nondestructive, vibratory membrane separation for commercially available forward osmosis membranes, and reduce the potential tendencies of concentration polarization, scaling and fouling of forward osmosis membranes.
- Turning to
FIGS. 2 to 5 , the hybrid quaking membrane plus forward osmosis process and apparatus is illustrated with the quaking membrane assembly at 2401 and recycle and reconcentrating closed loop system at 2501. In the combined apparatus, self-supported, semi-permeable or hollowfiber tubular membrane 2403 is used as a forward osmosis membrane operating in a quaking membrane process. Such tubular and hollow fiber membranes have no thick support layer as in spiral-wound, flat sheet, asymmetric membranes, thus minimizing internal concentration polarization. Membranes of this type are commercially available. - The quaking membrane process is low amplitude and high quaking frequency, generating low shear energy and therefore a gentle treatment in the epoxy potting compound of tubular or
hollow fiber membrane 2403. The quaking energy significantly lowers already low external concentration polarization, and has a positive effect on internal concentration polarization as well. Sufficient turbulence is generated on both sides of tubular or hollow fiber membrane 2403 (external and internal) for securing continuation of increased flux performance required by the forward osmosis process. The process thus yields a higher permeate production with less concentrate for disposal and requires less up front pre-treatment for the feed, while using less energy compared to conventional reverse osmosis/nanofiltration technology because little or no hydraulic pressure is needed as a driving force for separation. - For a continuously operated forward osmosis process, it is necessary that the membrane module design allows liquids to flow freely on both sides of membrane elements. Cellulose triacetate is the preferred material used in membrane 2403 (TOYOBO Hollosep hollow fiber membranes, for example). Low pressurized, recirculating feed water flows inside of the hollow fiber tubes of the
membrane module 2403 from low pressurefeed recirculation pump 2405. The gravity-assisted feed flow is induced at the top of the axial vibrating,hollow fiber module 2403. - Quaking
membrane module 2403 can either be operated in a vertical or inclined position, quaking membrane movement is provided by means of quake generator such as highpressure diaphragm pump 2407. The low pressurized, draw solution flows counter currently to the feed on the outside of the hollow fiber tubes. The draw enters at the bottom ofmembrane module 2403 and exits at the top. Forced draw circulation flow is provided by vacuum and compressor pump 2503 (FIG. 3 ). The concentration of the draw solution is diluted as the high osmotic pressure of the solution draws water through the semi-permeable membrane from the feed medium of lesser osmotic pressure. This, in turn, requires a reconcentration of the draw solution for the continuous desalination process. - The diluted draw solution is thermally recycled and reconcentrated in a closed loop system, which yields potable water. The closed loop system consists of two
heat exchangers stripper column 2509, andbuffer tank 2511. In the closed loop, the draw solution diluted with water is first lightly heated to 30° to 50° C. inheat exchanger 2505. The heated draw exitsheat exchanger 2505 from the top and is siphoned intostripper column 2509.Stripper column 2509 packing includes either raschig rings or berl saddles. Stripping takes place the column, the packing providing the necessary increased area and turbulence to achieve a desired draw solution conversion from a liquid to a vapor phase with the nonvolatile water precipitating out of the draw solution. - The lightly heated, liquefied and diluted influent (consisting of water and its soluble light volatile draw components) is distributed (at
spray head 2512, for example) at the top of packedcolumn bed 2513, flowing down through the bed where the large transfer area and the vacuum assistance ofpump 2503 allows the volatile components of the diluted draw to convert into an effluent vapor phase in the upper column portion and yielding potable water dilution water from the lower column portion (the treatment product of this apparatus). Vacuum andcompressor pump 2503 is configured to handle a large vapor volume on its suction side and compressing the vapor on its pressure side, and transfers the pressurized vapor fromstripper column 2509 into the top ofsecond heat exchanger 2507 for compression heat removal from the compressed vapor mixture. Cooling is provided by means of fresh cold feed water. - The cooling the vapor phase yields a condensate of a highly concentrated solute mixture and thus generates a recycled draw solution of initial concentration strength. The vapor mixture condensate is discharged from
exchanger 2507 intobuffer tank 2511.Tank 2511 includes automatic aeration andde-aeration device 2517 to avoid the passage of residual vapor intohollow fiber module 2403. Treated water is transferred out ofcolumn 2509 by centrifugal-vacuum pump 2519 while retentate particle separation is achieved via hydrocyclone separator 2409 (FIG. 2 ). The upper module suction provides motive force to the recycled draw solution for flowing continuously from the lower permeate suction connection ofmodule 2403 upwards and towards the upper permeate discharge connection, while the feed flows counter current to the draw downwards inside ofhollow fiber module 2403. - The apparatus of
FIGS. 2 and 3 is adapted for use not only with commercially available semi-permeable tubular and/or hollow fiber membranes modules, but also for forward osmosis specialized spiral-wound membranes when and if they become commercially available. The apparatus and processes can be used in applications for any brackish water treatment, higher contaminated CBM water treatment, overflow treatment of biological, defecated, municipal waste water for irrigation, cleaning processes for airplane and other public transportation wash water recycling, processing of bilge water, processing of wash water for combat vehicles after active and practice missions, and waste water processing for the pharmaceutical and chemical industry. - The quaking membrane coupled with the forward osmosis process allows a substantial concentration upgrading at
stage 419 at a significantly reduced energy requirement compared to conventional membrane separation processes, and could be employed as well atstages - Quaking frequency is variable in the range of 1 to 100 Hz depending on configuration. Quake amplitude has a relatively wide adjustable range of 0.2 to 2.0 mm. Quaking membrane movement can be generated either by any of electrical, hydraulic or mechanical means through an adjustable high frequency generator. Electrical means can include electromagnetic linear reciprocating membrane motion apparatus through a frequency-controlled, modified linear motion motor assembly wherein frequency and amplitude can be adjusted dynamically over a greater range (from 1 to 100 Hz.—see
FIGS. 4 and 5 ). -
Modified motor assembly 2601 is shown inFIGS. 4 a and 4 b having an upperstator coil section 2603 and lower stator coil section 2605, upper and lower (upper components only being shown inFIG. 4 b) fluid transferringend pieces 2607 being equipped with encapsulated, high-energy neodymium, iron-boron, reciprocatingpermanent magnet sleeves 2609. The nonmagneticouter housing 2610 has upper (and lower, not shown) stator 2611 thereat betweenretainers 2613. The stators contain the electromagnetic coils, which utilizes 3-phase direct drive, brushless technology. The stator's length and diameter set the force level, while the sleeve length determines the amplitude height. -
Motor 2601 uses a dual synchronous design wherein two stators and two permanent magnet sleeves are spaced over the entire length of the membrane. These dual linear motors are operated synchronously thus providing positive linear reciprocating motion over the entire length of the membrane. Quaking membrane cartridge at 2403 floats and is supported between an upper recoil spring system and the lower support structure spring system (both at 2403), thus isolating membrane cartridge movement therebetween. Spring rate is adjustable for equalization of the stator coil force requirement between upper andlower stator coils 2611, with force requirements based on the chosen operational quaking frequency and amplitude. - As can be appreciated, the membrane cartridge rides up and down between two resilient spring isolation systems within a stationary (housing also at 2403), whereas the motive reciprocating forces are provided by means of dual synchronously operating
linear motor assembly 2601. The two spring systems are configured to be adjustable for vibration transmissibility and damping efficiency (the spring system's ability to dissipate oscillatory energy and thus not transfer the energy to the entire quaking membrane module 2403). - The modified
linear motor assembly 2601 is essentially an electric motor that has its stator configured and positioned so that, instead of producing rotation, it produces a linear force along its length. As shown inFIG. 5 stator coil cooling can be accomplished utilizing a cold feed water stream (for example, from the same cold feed stream feeding heat exchanger 2507) fed by appropriate piping to port 2701 of ring-shaped cooler 2703 mounted betweenretainer disks 2705 adjacent to stator coil 2411. Feed atport 2701 is constantly replenished and recycled out atport 2707 connected atheat exchanger 2505. - Feedback in the forward osmosis system can be bypassed, if operations in quaking membrane mode only is preferred, by simple valving preventing re-osmosis of clean permeate. Three-
way ball valve 2521 functions as a selector valve for quaking membrane plus forward osmosis mode operations or quaking membrane mode operations only. - Osmotic pressure differential in the foregoing quaking membrane forward osmosis apparatus and methods is preferable provided by a magnetically recyclable solute composed of magnetic mixture of soluble salts. The use of magnetoferritin is known but requires removal from the aqueous stream by means of electromagnetic separation. To minimize problems associated therewith and with the problem of concentration polarization,
FIG. 6 shows an ultrasonically active draw solution dispersion system in accord with yet another aspect of this invention. - Alternating electrical energy from
ultrasonic generator 2801 is converted to an alternating magnetic field atcoil 2803 inprotective housing 2805 held around the outer housing ofmembrane module 2403 by retainingdisks 2807.Coil 2803 extends substantially the entire length ofmodule 2403.Generator 2801 is adjustable. The oscillating magnetic field induces hydrodynamic dispersion forces (turbulence) at ultrasonic frequencies in the ultrasonically active draw solution including magnetoferritin. The turbulence is at the internal boundary layer of the membrane thus minimizing internal concentration polarization. External concentration polarization is controlled by using a low pressure magnetically coupled centrifugal feed pump with an elevated output rate for producing external feed flow turbulence. -
FIG. 7 shows one arrangement of components in a polishing treatment array 205 using membrane treatment systems especially concentrating on the integration of the membrane treatment systems of stages 423 (step 11 using the nanofiltration membrane treatment option) and 429 (step 14 using the reverse osmosis membrane treatment option). These two stages (implementing membrane processes) separate dissolved solids from the pre-treated water. The selection of specific membranes and spacer material are based on test results (for example, from on-site three-dimensional test cells such as those shown in U.S. Pat. No. 6,059,970). The systems are set to operate at moderately to high pressures and typically employ high speed gravity assisted geometries with selected variable crossflow capabilities. - Nanofiltration membrane implementation of
stage 423 is a multistage configuration, operating in series. The array includes, for example, threepressure vessels 2901 each having a single membrane. The primary function of nanofiltration membrane treatment is the removal of the finest colloidal matter. The separated colloidal matter is removed with the nanofiltration concentrate. The produced nanofiltration permeate serves as feed the next membrane and, ultimately, for reverse osmosis implementation ofstage 429. - The reverse osmosis implemented array of
stage 429 includes, for example, two stages, with twomembranes 2903 operating in parallel in the first stage feeding a third membrane 2905 in the second stage. As shown, each stage thus implemented has its own pressure pump andcrossflow pump Nanofiltration stage 423 has a maximum operating pressure of 35 bar (508 psi), and a crossflow pump maximum rating of 50 gpm at a maximum of 60 psi in a 750 psi environment.Reverse osmosis stage 429 has a maximum operating pressure of 70 bar (1015 psi), and a crossflow pump rating of maximum rating of 10 gpm at a maximum of 45 psi in a 1,200 psi environment. System operating pressure is regulated throughbypass regulators - At this time, the most economical ready-made nanofiltration membrane shape is a flat membrane sheet in a spiral wound membrane element. A spiral wound element consists of multiple membrane pockets (for example 4-16 pockets), the spiral wound pockets terminating into a centralized collecting pipe. Special parallel polypropylene spacers of 80 mil thickness are preferred and complete the membrane (spiral wound nanofiltration membrane elements from Nadir with a practical neutral surface voltage (zeta potential), for example).
- The nanofiltration special spacing materials (spacers) are especially effective in applications with high suspended solids (colloidal) concentration. Since the primary purpose of the nanofiltration is to remove all suspended solids rather than dissolved solids (such as salts), these types of spacers with their larger spacing between the membrane surfaces are preferred. A smaller membrane spacer for other applications could be use (for example, having 33 mil diamond spacer).
- Alternatively, to maintain maximum processing flexibility at
stage 423, low and ultra-low pressure reverse osmosis membranes could be used (where total dissolved salts are an issue). If nanofiltration membranes are employed,crossflow pump 2909 output flow must be turned down atbypass valve 2915 for a lesser brine to permeate ratio to achieve a more desirable permeate quality. - Reverse osmosis and/or HEED assembly buffer tank and at
stages - Prevention of calcium carbonate precipitation in nanofiltration or reverse osmosis systems is aided by injection of sulfuric acid at
pump 306 into a homogenizing buffer tank atstage 417 to condition nanofiltration and/or reverse osmosis feed water. This will convert much of the bicarbonate to carbonic acid and dissolved carbon dioxide as well as increase the solubility of calcium carbonate due to the lower pH. In estimating the acid concentrations for pH adjustment, the rule of thumb is that lowering the feedwater pH to between 6.0 and 6.5 will reduce the bicarbonate concentration by about 80%. For most CBM waters and typical pilot program nanofiltration and/or reverse osmosis permeate recoveries, an 80% reduction of bicarbonate will be sufficient to prevent calcium precipitation. - By inline injection of a fouling and scaling inhibitor (such as VITECH 3000) at
stage 421 into the nanofiltration feed stream, colloidal and scale crystal growth is slowed, colloidal formation inhibited, and the crystalline shape of the scale crystal is modified. By inline injection of a scaling inhibitor (such as VITECH 4000) atstage 427 into the reverse osmosis feed stream, scale crystal growth is slowed and crystalline shape is modified. It should be realized that scaling by other salt types can occur simultaneously (for instance, BaSO4). Therefore, it is necessary for the hybrid dosing to catch the remaining scaling causing salts with an antiscaling medium. Common scale inhibitors consist of molecules that contain carboxylic or phosphate functional groups. Lower molecular weight polyacrylate molecules contain multiple carboxylic functional groups. - At reverse osmosis implementation of
stage 429,membranes 2903 and 2905 are preferably spiral wound polyamide skin layer composite membranes with a zeta potential of approximately −7 mV and a polysulfone support layer and standard 31 mil diamond spacers (since prefiltered feed water will be used). Optionally, seawater polyamide membranes with a spacer thickness of 27 mil could be utilized. The polyamide thin layer membranes are constructed with an aromatic polyamide extruded onto a less dense polysulfone substrate. The optional seawater membrane elements use a denser polyamide membrane layer with better rejection characteristics. - Polyamide membranes are sensitive to oxidizing agents such as free chlorine or iodine. This requires that chlorine or iodine present in the feedwater be removed by a reducing agent (such as sodium bisulfite in the case of chlorine injected upstream of the reverse osmosis modules). To avoid fouling in such case, a non-oxidizing biocide like BUSAN (150 to 1500 ppm) can be continuously injected in-line with the reverse osmosis feed stream. This mixture which kills bacteria, fungi and algae is compatible with the membrane material as well as the other injection chemicals used.
- A number of parameters can affect reverse osmosis permeate flowrate at stage 429 (or
stage 425 if used there also). These include water temperature, salt concentration and membrane pressure as the feed water flows through the system.Stage 429 is preferably configured to work within a minimum and maximum range of 1,000 ppm to 20,000 ppm TDS, as well as a temperature range of 40° to 80° F. The system's maximum design pressure is around 1,000 psig. - Higher pressures result in higher permeate flowrates and better salt rejection characteristics. Higher pressures also require more power and can result in higher membrane fouling rates and reduced membrane life expectancy. These considerations are important considerations for programming at steps related to upsizing (to full size plant). In addition, higher pressure operation may require stainless steel, fiberglass/epoxy or carbon fiber/epoxy membrane housings and piping material to handle the higher pressure. To maximize flexibility, reverse osmosis systems configured for high pressure operating capabilities are often preferred.
-
Membrane 2903 housings are arranged vertically rather than horizontally, and all are top fed. This operating geometry provides gravitational assistance to the high speed crossflow turbulence. Crossflow (recirculation flow) is provided bypump 2913 and flow controlled bybypass valve 2919. System pressure is controlled bypressure regulator 2920.Pressure pump 2911 operates at a maximum flowrate of 2.65 GPM at a maximum 1,029 psi. - In facilities that employ high speed gravity assisted geometries in their system design, membrane systems are working with an unconventional high crossflow velocity, and the membrane housings are geometrically arranged in a vertical top feed position. Therefore, it allows the feed water crossing the membrane with the assist of gravity, whereby the chosen array minimizes the pressure differential across the membrane system. This differential would otherwise take away from the net driving pressure at the tail end of the individual membrane system.
- A portion of the concentrate is recycled back to the overall membrane system feed to increase recovery beyond the 75% it may have already achieved. For example, by recycling only ⅕ of the concentrate back to the feed, recovery can be increased to an 80% permeate recovery. This results into a 20% reduction of disposable concentrate production. The concentrate recirculation (retentate) flow rate for the pilot unit operation is provided through the crossflow pumps 2909 for the nanofiltration at
stage stage 429. - In order to provide the desired high crossflow velocity over the membranes, and in accord with another aspect of this invention, separate high flow, low pressure crossflow pumps are utilized. Since pressure pumps 2907 and 2911 of the membrane system cannot fulfill these requirements, separate low pressure but high flow crossflow pumps operating in a high pressure environment with flowrate adjustment capability are needed. These pumps are magnetically driven with no seals and are equipped with high pressure stainless steel housings to contain a feed pressure of up to 1200 psi. The relatively small, low energy, high pressure feed pumps provide the system operating pressure. The feed pressure and flow rate is preferably regulated by a vector drive.
- Through this arrangement, the feed achieves sufficient pressure through the high pressure feed pumps for membrane separation. These high flow crossflow pumps provide sufficient turbulence and hydrodynamic shear to flush down and clean out the membrane flow channels of contaminated matter to minimize any fouling/scaling potential of the specific membrane system. The low operating pressure of the crossflow pump does not create excessive pressure even when operated at full flow capacity. Crossflow meters are preferably utilized to measure, control, and obtain optimum crossflow and crossflow velocity to achieve sufficient turbulence to minimize fouling/scaling potential. Turbine meters with magnetic pickups and transmitter/read-out units are preferred. The preferred pumps here are magnetically driven centrifugal pumps. The high flowrate is needed to cover a large crossflow rate range. The flowrate is easily adjustable through a valve controlled by-pass.
- Turning to
FIG. 8 , the preferred magnetically driven centrifugal pump 3001 (used, for example, forpumps 2909 and/or 2913) of this aspect of the invention is illustrated, such pumps being heretofore commercially unavailable that can operate in a high pressure environment (over 500 psi for the nanofiltration, and in excess of 1,000 psi for reverse osmosis). All high pressure parts are manufactured from compatible nonmagnetic stainless steel series 316 or 312, 316L or Hastelloy C4 (casing sections drive magnet 3007 tomagnet capsule 3021, to facilitate the no touch magnetic coupling process. - Another novel element of the pump design herein is use of off-the-shelf plastic low pressure internal pump parts (for example,
impeller 3009,mouth ring 3011,spindle 3015,rear thrust 3018,front thrust 3019 and magnet capsule 3021). Since pump shavings from plastic impellers have been known to foul the lead end elements of membrane systems, an optional discharge screen downstream of the pump is recommended. A chemically resistant coating such as Ceramic, PVDF, PP, PE, HPE, PTFE or PFA is utilized to prevent pitting and is applied to the inside of high pressure pump components. - The magnetic pump is otherwise of convention design.
Ceramic spindle 3015 is mounted rigidly on one end onto stationary, high pressure resistingrear casing 3016 which is made from non-magnetic stainless alloy.Main bearing 3017 rotates on the protruding end ofspindle 3015, bearing 3017 press fitted intomagnet capsule 3021 which is counter-rotationally twist-locked ontoimpeller 3009. Pointed conicalrear thrust 3018 is mounted onimpeller 3009 and limits rearward movement ofmagnet capsule 3021 andimpeller 3009.Thrust 3018 rides against the front face ofstationary spindle 3015 thus limiting the rear thrust. Likewise, front thrust ofmagnet capsule 3021 andimpeller 3009 is limited by impeller mountedmouth ring 3011 riding against the front face ofstationary front thrust 3019. The feed medium itself provides lubrication between moving and stationary thrust contact areas. - In accordance with another aspect of this invention, in-line degasser and
degasser column assemblies 3101 are shown inFIGS. 7 and 9 .Assemblies 3101 are specifically adapted for air and/or CO2 removal or reduction in the produced membrane permeate flowstages Assemblies 3101 condition flow of produced permeate by air/gas removal prior to processing through flow instrumentation and recording devices for the generation of real time liquid flow data without error producing air or gas content.Assemblies 3101 are adaptable in any setting where enhanced flow process stabilization is required in a liquid system with entrained and unwanted air or gas and where in-line degassing is needed for flowmeter applications. No packing material is needed for optimum surface area contact between the water and the air as is used in conventional tall column forced-draft degassifier designs. -
Assemblies 3101 includeinline degasser 3103 and attacheddegasser column 3105, and has no moving parts. Head back pressure control can be adjustable by height adjustment ofelbow 3107 relative to the top of column 3105 (at cap 3109). Visual inspection of ongoing degassification processes can be monitored throughclear column tube 3111. Ball-valve 3113 controls flow todegasser 3103 ofassembly 3101,flowmeter 3115 followingdegasser 3103. Gas supersaturated concentrate flows into the bottom ofexpansion chamber 3117 ofdegasser 3103 providing atmospheric pressure release through topconnected hose 3119.Hose 3119 is connected at the other end todegasser column 3105. - Vertical adjustment of
column 3105 provides proper back-head, back-pressure control, the column's horizontal swivel capability atcantilever arm 3121 providing dead leg free hose transfer. Head is adjusted to match individual concentrate draw-off by keeping enough column head oncolumn 3105, which is open to the atmosphere. As a result, a spilling out of concentrate flow is avoided. Through controlled release of back-pressure, concentrate discharge gas pressure is lowered inexpansion chamber 3117. - The in-rushing expanding CO2 bubbles towards the lower pressure level of upper
expansion chamber outlet 3123. The rising bubbles accelerate during their ascent due to the simultaneous decline of available head pressure inassembly 3101. Since the ascending bubbles are shielded from entering the lower water transfer openings inpipe riser 3125 byshield 3127, only the descending, saturated but bubble-free water enters the transfer openings. The now transformed water from the supersaturated to the saturated stage is calm enough to allow for meaningful flowmeter readings and control. - Flow distributor and
discharge equalizer 3201 in accord with another aspect of this invention is shown inFIG. 10 . The method of use ofequalizer 3201 is novelly adapted to use with high speed crossflow membrane systems operating in a gravity assisted mode.Equalizer 3201 is hydrodynamically designed for flow direction from a horizontal entry flow atport 3203 to a vertical flow inhousing 3205, and a flow directional change back from a vertical flow to a horizontal side exit flow to enhance operation of the vertically mounted high speed membrane systems. - Flow altering
distribution cones 3207 atproduct tube extension 3209 provide favorable hydromechanical loading and unloading for spirally wound membranes by distributing the in-rushing high crossflow of high operating pressure more evenly into the leading portion of the vertically arranged membranes. Since favorable membrane hydromechanics extends useful membrane life expectancy, cost savings are realized. -
Equalizers 3201 are mounted in place of long sweeping mounting elbows usually used for top entry and bottom exit of conventional high speed, vertical membrane system designs (at 3211, for example, inFIG. 7 , other utilization nodes being identifiable in the drawings). This improved hydrodynamic design adapted for side entry operation is a practical method for reducing overall height and footprint requirements of a vertically mounted, high speed membrane system. - In accordance with another aspect of this invention, a first embodiment of a high frequency membrane separation apparatus and method utilizable with membrane systems of this invention is shown in
FIGS. 11 a and 11 b. This invention relates to apparatus and methods for fluid filtering utilizing membrane separation (for example nanofiltration and/or reverse osmosis filtration) that combines vibratory shear techniques with adjustable crossflow techniques. This and further embodiments of the high frequency membrane separation apparatus and methods (set forth hereinafter) are particularly well adapted totreatment stages - High frequency membrane separation herein refers to vibrating, oscillatory motion of the membrane support structure. Vibration direction is perpendicular to the floor of the installation for gravity assisted membrane separation systems. The vibration curve is preferably a regular curve, which corresponds mathematically to a zero centered sine or cosine, a sinusoidal or simple harmonic. The amplitude is preferably steady and frequency high.
- This hybrid does not depend solely on vibratory induced shearing forces to prevent fouling and thus does not require total shut down of the membrane separation process during preventive maintenance on the vibrators. The shear wave produced by axial vertical membrane vibration causes solids and foulants to be lifted off membrane surfaces and remixed with retentate flowing through the parallel or tunnel spacer or other specially designed spacers of spirally wound elements or through flow channels of tubular or capillar membrane elements. Movement continuity is maintained through the adjustable crossflow, reducing further additional membrane fouling tendency.
- This hybrid approach using adjustable crossflow and high shear processing exposes membrane surfaces for maximum flux (volume of permeate per unit area and time) that is typically higher than the flux of conventional vibratory membrane technology alone. In the conventional vibratory membrane design, each membrane module requires its own vibratory energy source. Only a single vibratory engine 3303 is utilized for a multi-membrane module design herein (up to thirty-two 2.5″, sixteen 4″ or eight 8″ membrane modules).
- To suit certain operating environments, where height restrictions and/or leveling problems are encountered, high frequency membrane separation apparatus of this invention can be operated at an incline using
center pivot 3304 for adjustment of swivel framework 3305 (from standard vertical position to a maximum 15° incline orientation) inswivel support 3306. Unlike other vibratory membrane separation technology which employs horizontal vibratory torsional motion in the axis plane of abscissa (x), and which require use of proprietary one source only custom membrane modules, this approach is more flexible. Readily available, and thus less costly, conventional membrane modules can be used, and mounting of membrane modules in a vertical flow gravity assisted position with adjustable crossflow operation is accommodated. - This embodiment of the high frequency membrane separation apparatus uses twin motors connected at shaft/eccentric and
weight assemblies weight 3307 counter-clockwise and the other rotating shaft/eccentric andweight 3309 in a clockwise direction. - The vibrator motors are capable of producing net centrifugal forces that change direction in space as the motor rotates. Such a force acts upward at one instant and downward a half-rotation later, thus producing a force that acts sinusoidal at a frequency that corresponds to shaft/eccentric/weight assemblies' 3307/3309 rotation.
- Adjustable eccentric weight provides variable force output (from 0% to 100%) at a synchronized mode of operation (i.e., the adjustable weights are aligned with each other at 90° for clockwise rotation and 270° for counter-clockwise rotation). A vibratory high-speed linear motion through center of gravity thus impacts
swivel framework 3305 having the vibrating motors mounted on the inside thereof and the membrane modules mounted on the outside thereof. - Support
box frame structure 3310 is preferablysquare tubing 2″×2″ with a ⅛″ wall.Frame structure 3310 carries membrane modules (hereinafter 3311, generally applied, for example, tomodules FIG. 7 or other membrane modules disclosed herein and related to the various nanofiltration and reverse osmosis options) and includes frame uprights 3312 mounted via rubber dampeners 3313 (preferably eight) at swivel framework 3305 (one upright per corner of the support structure). Swivel frame uprights 3315 ofsupport 3306 are preferably made from fabricated ¼″ steel material, and are connected to seismic absorbing mass at fabricatedsteel base frame 3317.Base frame 3317 is preferably at least partially filled with concrete to add mass. - Two
springs 3319 are located in-line at the top of support structure box frame 3310 (supporting panel structure not shown) and between horizontaltop frame members 3321 of theopen swivel framework 3305. Dampeners 3323 are located adjacent to bottom frame member 3325 ofswivel framework 3305. As compared to conventional springs, urethane springs/dampeners are preferred for their high load-carrying capability, longer life, abrasion resistance, low noise, and vibration damping and shock absorbency. - The springs themselves are cylindrical, and four connecting bolts 3327 fasten
support structure 3310 to swivelframework 3305. The fine-threaded connecting bolts allow for vibratory amplitude adjustment in a range up to about 1″. If combined with conventional coil springs, the vibratory amplitude adjustment range increases up to 1.5″. Together with the adjustable frequency drive (or inverter drive), customization of axial vibratory linear motion for shear enhanced fouling reducing membrane separation is accommodated. - A second embodiment of the high frequency membrane separation apparatus and methods of this invention is shown in
FIGS. 12 through 16 . In the embodiment shown inFIG. 12 , vibration is hydrodynamically controlled. This embodiment is specially applicable whenever a homogen disperse fluid substance with a lower concentration polarization layer has to be treated—for instance, organic and inorganic colloidal solution as well as fine disperse suspensions and higher concentrations of salt solutions (TDS 1,000-50,000 mg/L). Since high shear rates are not required in high frequencymembrane separation apparatus 3401,apparatus 3401 can be configured to operated at a lower amplitude.System 3403 can operate efficiently at a lower amplitude. - Vibratory impulse energy is provided through the primary feed pump (for example, pumps 2907/2911 as shown in
FIG. 7 ), no secondary vibratory energy source is required. Furthermore, only the membrane, fluid column (preferably pre-filtered as taught herein, generally represented at 3404) and some associated internal components ofapparatus 3401 are vibrated (not the entire unit including support mass). Onefeed pump 2907/2911 can serve one or many modules in parallel feed array. - In combination with heretofore described crossflow characteristics, hydrodynamic vibration herein provides axial vibration of amplitude “Y” to enhance the sinusoidal flow pattern between
transverse spacer rods 3801 in membrane media 3802 (seeFIG. 16 ). Vibration amplitude is controlled through stroke adjustment. The system operates with low vibratory energy waves which are scaled to provide effective agitation. Axial vibration with a maximum amplitude Y of only about 2 mm for a spirally wound membrane is sufficient to maintain proper permeate continuity.Apparatus 3401 provides sinusoidal meandering turbulent cleaning action by high frequency vibration up to 180 Hz in a tangential direction to the surface of the membranes (seeFIG. 16 ). - To affect the benefits of
hybrid apparatus 3401membrane element 3405 is oscillated within the membrane housing 3407 (seeFIGS. 13 through 15 ). The bulk stream containing the returned suspended particles between the membrane leaves of spirally wound membrane elements (generally at 3803 inFIG. 16 ), and in the flow channels of tubular and/or capillary membrane elements, is continuously flushed out of the membrane module by means of the gravity assisted low crossflow. Sinceapparatus 3401 does not depend on crossflow induced turbulence, feed of a homogen fluid substance with a lower concentration polarization layer can be concentrated at a higher level. - Crossflow pressure can be maintained in a low range between 35 and 140 kPa (utilizing crossflow pump 2902/2913, for example) thus producing an adjustable low crossflow velocity in the range of 0.075 to 1 m/s and requiring low operating energy. Sufficiency of turbulence for anti-fouling/scaling is maintained by high frequency of the vibration. Produced are low vibratory energy waves scaled to provide a nonstagnant membrane area environment with effective sinusoidal meandering turbulence to the
boundary layer 3805 area, settling of suspended particles thus inhibited. - Feed activated
hydrodynamic impulse system 3501 is best illustrated inFIGS. 13 through 15 . A pulsating high pressure water jet is receive fromplunger pump 2907/2911 throughinlet port 3503 throughlower retainer ring 3504 and feed ring-room housing 3505 atlower section 3506.Housing 3407 holdingfilter module 3405 is ported as required for feed input and concentrate and permeate output and is constructed accordingly. Upper section 3601 (FIG. 14 ) includespermeate discharge connector 3603,upper retainer plate 3605, spring rings 3606, boltretainer plate 3607,spring adjustment plate 3609,return spring 3611 andlantern ring 3613. Variously sized O-rings seals 3615 seal the unit.Membrane coupling 3617couples connector 3603 tomembrane 3405. - Lower section 3506 (
FIG. 15 ) further includespermeate tube plug 3703,ring piston 3705,retentate discharge connector 3707, and spring rings 3709 and 3711. Again, various sized o-rings 3713 seal the apparatus. As can be appreciated the pulsating jet of water received throughport 3503 vibratesmodule 3405 atring piston 3705 at the rate of pulsation. Reciprocation is limited and maintained byspring 3611 operating against ring 3613 (held in adjustment by adjustment plate 3609). - Self-contained, vibratory spring, seal and transfer conduit apparatus and methods, in accord with yet another aspect of this invention, are illustrated in
FIGS. 17 and 18 . The self contained, vibratory spring, seal and transfer conduit apparatus and methods of this invention provide a flexible sealing connection between an oscillating and a stationary object by means of a fluid conveying elastomeric conduit connection. The flexible fluid conveying conduit is equipped with nonflexing end connectors to provide motionless sealing surfaces for the associated o-ring seals which are housed in the respective objects. As a result, positive nonreciprocating sealing in a dynamic operating environment is provided. - Self contained
apparatus 3901 is adapted for (but not limited to) use with vibrating membrane technology of the type shown herein inFIG. 13 (and numbers therein common to both embodiments are carried forward).Apparatus 3901 is preloaded under tension by a polyurethane based permeate transfer conduit 4003 (also referred to herein as polyurethane spring conduit 4003). The material used has a durometer of about 60 A and has high rebound values (greater than 65%) sufficient to withstand high frequency vibrations. The materials is selected to have high load bearing properties in both tension and compression). All machine elements thus remain in alignment and remain stationary (relative to one another) thereby preserving sealing surfaces while the vibratory load is operating. - Springs (preferably Belleville or disc springs) 4005 generate a portion of the compressive force counter reacting the tension load of
polyurethane spring conduit 4003.Pre-load retainers 4007 preferably stainless steel retainer rings or spring clips) contain and secure preload, connectingurethane spring conduit 4003 with the upper and lower load guides 4009.Springs 4005 are held between upper and lower load guides 4009 and center load guides 4011,load transfer spacer 4013 spanning center guides 4011 spacing the two spring columns (formed by aspring 4005 and one each of load guides 4009 and 4013). This arrangement equally distributes the low value tension and compression loads. -
Spring 4015 further supportspolyurethane spring conduit 4003.Conduit 4003 is mounted at the upper end with a modifiedplate 4016, abutting modifiedpermeate discharge connector 4004, and at the lower end to a modifiedlantern ring 4017.Load transfer spacer 4013 has a length selected so that maximumurethane spring conduit 4003 deflection is less than 2%. Urethane spring manufacturers suggest a maximum deflection of 25% and a maximum cycle rate of 700 cycles per hour for intermittent operation. For continuous operations and a maximum deflection of 15%, a maximum cycle rate of 12,000 cycles per hour is suggested. Because apparatus such asapparatus 3901 has a cycle rate of between 216,000 and 648,000 cycles per hour, the deflection percentage needs to be significantly reduced. -
Apparatus 3901 provides wear and leak-free operation for permeate fluid transfer between oscillatingmembrane element 3405 and itsstationary housing 3407 components, thus effectively avoiding contamination of the produced permeate with feed water.Apparatus 3901 accommodates either high frequency membrane separation housing designs (side port entry and the top port entry) and serves as a return spring forapparatus 3401 as well as a permeate transfer conduit and seal unit. Modular design accommodates ease of maintenance. - On the lower side of
apparatus 3901,lower spring 4005 column oscillates simultaneously with themodule 3405, while at the upper side ofapparatus 3901upper spring 4005 column remains steadier so that the connecting end ofconduit 4003 remains motionless in its sealingseat 4019. This is due to the return spring pressure acting upon the upper retainer which keeps the upper male connecting end securely in its sealing seat. - In accordance with yet another aspect of this invention,
FIGS. 19 and 20 illustrate a high shear and high amplitude internal membrane separation apparatus and methods. This invention relates to permeate continuity in water treatment processes. More particularly, the purpose of this aspect of the invention is to achieve high shear in such processes to increase permeate continuity while treating high load of colloidal and slimy matter (polysaccharide, etc.) in treatment station feed water. -
Apparatus 4101 illustrated inFIG. 19 offers high shear operation for internally vibrating membrane separation systems of the types heretofore disclosed. This high shear option is provided by means of a high vibration amplitude in the range of 1/32″ to ⅜″. However, such high amplitude vibration could damagemembrane element 3405. Thus, in accord with this invention, an all-surroundingmembrane support tube 4103 with upper and lower connectingend pieces tube 4103 by split tongue andgroove rings 4109 are provided, thus convertingmembrane element 3405 intomembrane cartridge 4111 havingelement 3405 therein.Membrane cartridge 4111 provides a backlash free, non-load bearing and non-force transmitting, hardened operating environment formembrane element 3405. -
End pieces Upper end piece 4105 has twoconduits 4113 for crossflow feed influent and 4115 for produced permeate effluent.Lower end piece 4107 has multiple inclined conduits 4117 (at least four conduits for smaller membranes) all merging into largeretentate effluent conduit 4119 ofventuri nozzle 4121.Nozzle 4121 has an outside cone angle of about 21° to support venturi function and enhance rapid transfer of the pulsating, make up feed flow at elevated operating frequencies. High pressure vibrating pulsatingfeed input 4123 through lower flange andinjector body assembly 4124 is positioned to operate againstsurface 4125 oflower end piece 4107 to vibratecartridge 4111. - Overall, a
containment housing 4127 is welded to transfer flange assemblies 4129 (upper) andouter flange 4130 ofassembly 4124, the lower flange assembly bolted together by bolt and nut sets 4131 through lowerinner flange 4132 andouter flange 4130 ofassembly 4124. Upper flange assembly is bolted together with bolt andnut sets 4133 havingrecoil springs 4135 thereover for recoil adjustment.Safety guard 4137 is mounted at the top ofapparatus 4101 and includes a window for on-site amplitude inspection. - The structural integrity of the
membrane element 3405 needs to be strong enough to sustain its own vibratory mass acceleration forces within its hardened enclosure. To provide maximum structural membrane element strength, the preferred spirally-wound membrane element design for all high frequency membrane separation applications in high shear mode includes fiberglassed outside for holdingelement 3405 together. However, amplitudes greater than ⅜″ are not recommended for the spirally-wound membrane elements under any circumstances since adhesive membrane joints fatigue prematurely at higher operating frequencies (60 Hz). -
Apparatus 4101 allows operation of vibratory membrane implementations at higher shear at moderate frequency (20 to 60 Hz).Membrane cartridge 4111 is relatively light and vibrates internally at an adjustable up to a relatively high frequency within housing 4127 (rather than vibrating the entire heavy membrane module as is common in conventional vibratory membrane separation processes). - A primary application for this high shear option for high frequency membrane separation systems is the effluent treatment of dewatered electrocoagulation sludge. This is an important treatment step whenever a required electrocoagulation process generates sludge and the produced sludge requires dewatering prior to disposal. Any other application where an elevated shear energy requirement for treatment of a specific feed water is diagnosed would benefit from use of
apparatus 4101. - A secondary application for this high shear option exists where electrocoagulation pre-treatment is abandoned in favor of standard nanofiltration treatment. This will produce a concentrate having colloidal loading too high for standard low shear high frequency membrane separation processes. Yet another application occasioned in any circumstance where limited disposal options are present in extreme high flow yield (high concentration factor) treatment setting.
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End pieces flow distribution plug 4139 havingsplash dome 4141 blocks direct throughflow and guides the feed flow into ring roomflow distribution channel 4143 defined atend piece 4105.Splash dome plug 4139 rests on a shoulder in the lower section offeed conduit 4113 and is secured in its upper position by stainlesssteel retainer ring 4142. A flared fluid transfer opening fromring room 4143 faces towards the anti-telescoping device at the lead end ofmembrane element 3405. - Step bore 4145 in
end piece 4105 seals (at o-ring 4147) the upper end ofpermeate collection tube 4149. The outside ofupper end piece 4105 includes groove structures, the first to receive upper reciprocatinggroove ring seal 4151 to seal the upper portion ofmembrane cartridge 4111. A second high andshallow groove 4153 receives the overlapping split tongue ring 4109 (connectable at its other end ingroove 4155 oftube 4103. The split tongue ring halves can be held together by dual spring rings or other suitable means. O-ring 4157 sealupper end piece 4105 andsupport tube 4103. - To take up axial slack and minimize movement of
membrane element 3405 within its all-surrounding enclosure, shims can be added to flow distribution andscreen plate 4159 sandwiched betweenupper end piece 4105 and the anti-telescoping device at the lead end ofmembrane element 3405. (and where applicable, at the permeate collection tube). Membrane element backlash is thus virtually eliminated. -
Plate 4159 provides the necessary pressure drop for proper crossflow feed distribution around the feed ring room. In conjunction with anti channelingflow distribution plug 4139,plate 4159 minimizes localized feed channeling, thus utilizing more efficiently the available membrane area for diffusive fluid transfer.Plate 4159 also acts as a crossflow pump discharge filter screen to catch any particles and foreign objects. -
Support tube 4103 can be made from a thin-walled metal alloy a heavier walled, suitable plastic material in order to reduce the vibratory mass.Support tube 4103 is grooved at it bottom end (at 4155) to provide a connection sites for tongue andgroove ring 4109 thereat.U-cup seal gasket 4161 is placed around the outside (in a concentrate seal holder 4162) of the lead end of themembrane element 3405. This gasket sealsmembrane element 3405 toexternal support tube 4103 and prevents the crossflow feed influent from bypassing the membrane element. - Downstream,
membrane element 3405 is equipped with an anti-telescoping device that is connected tolower end piece 4107 by means of the extended lower end of itspermeate collection tube 4162.Tube 4162 is sealed at o-ring 4163 atlower end piece 4107.Lower end piece 4107 itself is rigidly coupled and sealed to supporttube 4103 in the same manner asupper end piece 4105. The top face oflower end piece 4107 is equipped with a tapered,shallow ring groove 4165.Groove 4165 collects and distributes concentrate/retentate fluid through multiple inclinedfluid transfer conduits 4117 which are distributed aroundgroove 4165. -
Protruding venturi nozzle 4121, is fitted ininlet chamber 4166 which is defined byinjector body 4167 ofassembly 4124 protruding intolower end piece 4107 leaving asmall ring room 4169adjacent surface 4145 ofend piece 4107 for the distribution of the high pressure, pulsating make up feed flow.Venturi nozzle 4121 has an effective sealing length equivalent to the maximum operating amplitude. -
End piece 4107 has a dual purposeconcentric guide shroud 4171 providing a close fit concentricity between the axially vibratinglower end piece 4107 andnon-vibrating injector body 4167.Shroud 4171 defines a reasonable operating clearance betweenend piece 4107 andexternal housing 4127 to ensure proper operation ofreciprocating seal 4172sealing housing 4127 and vibratingmembrane cartridge 4111 from potential fluid loss.Shroud 4171 also providesimpact surface 4173 contacting amplitude regulatingimpact ring 4175.Ring 4175 is preferably made from polyether-based urethane (60 on the Shore A scale), providing shock deadening.Ring 4175 is configured and positioned for highly resilient operation providing quick recovery in high-frequency vibration applications (rebound values from 50 to 70%). Vibration amplitude ranges can be regulated by ring height selection. An increase in ring height increases the volume of thedistribution ring room 4169 while reducing the effective height of the cylindrical shaped section ofnozzle 4121. - In operation, the unchanged volume of the displacement stroke of high pressure piston pump (2907 or 2911, for example, in
FIG. 7 ) first fills the volume ofring room 4169 with feed liquid before it starts to initiate an axial, upward movement ofmembrane cartridge 4111. Once the cartridge travel upwards and exceeds the reduced height of the outer diameter ofnozzle 4121, a fluid transfer passage around nozzle 4121 (fromring room 4169 to chamber 4166) opens and passes the liquid which then flows by the 21° cone-shaped end ofnozzle 4121 oflower end piece 4107. Consequently, the feed flow through this transfer passage is entrained and carried along by the venturi effect of the concentrate/retentate discharge and is subject to the priming suction of the crossflow recirculation pump (2909 or 2913, for example, inFIG. 7 ). -
Injector body 4167 is also preferably a unitary structure, machined, for example, from either suitable metallic alloys or plastic material.Injector body 4167 haslarge conduit 4177 andsmaller conduit 4179,conduit 4177 for transfer of concentrated retentate and the pulsating, make up feed influent to crossflow recirculation pump as discussed hereinabove.Conduit 4179 is the input for the vibration inducing feed.Injector body 4167 is sealed atouter housing 4127 with o-ring 4181.Camber 4166 tapers down atconduit 4177 to funnel the flow into recirculationsuction connector pipe 4183 maintained through innerlower flange 4132. -
Injector body 4167 is positioned and kept in place insideexternal housing 4127 byflange 4132. The weldment offlange 4130 andhousing 4127 could be replaced by an integral structure such as a pipe spool. An upper impact and buffering ring 4185 (made from a polyurethane material) is located betweenupper end piece 4105 and upperinner flange 4186 of flange assembly 4129 (the weldment offlange 4187 ofassembly 4129 tohousing 4127 could also be replaced by an integral structure such as a pipe spool). - While not preferred, a potentially useful alternative draw off arrangement for
apparatus 4101 as illustrated inFIG. 20 could be utilized. This arrangement providessecondary retentate conduit 4201 inconduit 4183 and throughinjector body 4167 andchamber 4166 defined bylower end piece 4107 so that itsinlet 4203 resides aboveventuri nozzle 4121 inconduit 4119. In this way draw off received throughcartridge 4111 can be at least partially segregated from mixed retentate and feed received during operations fromring room 4169. - As may be appreciated from the foregoing apparatus and methods are provided for mechanical (motorized or hydrodynamic) axial vibration in membrane separation treatment of effluents wherein use of readily available, membrane elements and/or modules is accommodated. The apparatus can be mounted so that membrane modules are maintained in a vertical flow gravity assisted position, and adjustable crossflow operation may be utilized.
Claims (20)
1. A method for axial vibration in membrane separation treatment of effluents comprising the steps of:
locating a membrane element in a support structure;
feeding effluent for treatment into said support structure;
initiating axial vibration of said membrane element in said support structure without securement of said membrane element to a source of vibration; and
withdrawing treated effluent from said support structure.
2. The method of claim 1 further comprising the step of selectively providing a crossflow in said support structure.
3. The method of claim 1 wherein the step of axially vibrating said element further comprises hydrodynamically vibrating said membrane element.
4. The method of claim 1 further comprising the step of locating said membrane element in a protective tube and axially locating said tube in said support structure, and wherein the step of axially vibrating said element further comprises hydrodynamically vibrating said tube in said support structure.
5. The method of claim 1 further comprising sealing components of said membrane element and said support structure.
6. The method of claim 1 wherein the step of axially vibrating said element further comprises vibrating said membrane element by means of a pump and spring installation.
7. The method of claim 1 wherein the step of axially vibrating said element comprises the step of vibrating said support structure.
8. The method of claim 1 wherein the step of axially vibrating said membrane element occurs linearly in a vertical plane.
9. A method for axial vibration in membrane separation treatment of effluents comprising the steps of:
locating a membrane element having an axial dimension in a membrane support structure without any direct attachment of said membrane element to said support structure or other structure outside said support structure; and
vibrating said membrane element in said support structure in said axial dimension one of hydrodynamically, electromagnetically and mechanically.
10. The method of claim 9 further comprising the step of crossflow pumping of effluent at said membrane element.
11. The apparatus of claim 9 wherein the step of vibrating said membrane element includes the steps locating a spring arrangement in said membrane support structure and pulsing fluid in said support structure thereby, in combination with said spring arrangement, oscillating said membrane element in said support structure.
12. The method of claim 9 wherein said support structure includes a tube for receiving said membrane element, said tube and element together defining a membrane cartridge, and further comprising the steps of axially mounting plural said cartridges at a frame structure and vibrating said frame structure.
13. The method of claim 12 wherein the step of vibrating said membrane element includes vibrating said frame structure linearly using at least a first motor.
14. A method for axial vibration in membrane separation treatment of effluents comprising the steps of:
positioning a membrane module in a containment housing configured for free axial movement of the membrane module therein;
adjustably limiting extent of axial movement of said membrane module in said containment housing; and
hydrodynamically activating axial vibration of said membrane module in said containment housing as limited.
15. The method of claim 15 further comprising locating said membrane module at a piston structure and vibrating said piston structure in said containment housing.
16. The method of claim 15 further comprising locating a spring at said containment housing to assist axial vibration.
17. The method of claim 14 wherein the step of hydrodynamically activating axial vibration includes pulsing fluid through a fluid port at one end of said containment housing to move said membrane module therein in a first axial direction.
18. The method of claim 17 wherein the step of hydrodynamically activating axial vibration includes utilizing a mechanism at an opposite end of said containment housing to move said membrane module therein in a second axial direction.
19. The method of claim 17 wherein the step of pulsing fluid includes pulsing fluid to be treatment in said containment housing.
20. The method of claim 14 further comprising the steps of feeding effluent for treatment into said containment housing at one end and withdrawing treated effluent from said containment housing at an opposite end.
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US13/987,738 US20130341271A1 (en) | 2007-08-01 | 2013-08-27 | Mechanical axial vibration in membrane separation treatment of effluents |
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US12/452,786 Expired - Fee Related US8623209B2 (en) | 2007-08-01 | 2008-07-31 | Fluid head height and foam/gas level control in electrocoagulation apparatus |
US12/452,775 Expired - Fee Related US8257592B2 (en) | 2007-08-01 | 2008-07-31 | Biological wastewater treatment apparatus and methods using moving belt contractor |
US12/452,776 Expired - Fee Related US8435391B2 (en) | 2007-08-01 | 2008-07-31 | Electrocoagulation apparatus with in-place electrode cleaning |
US12/452,787 Expired - Fee Related US8858791B2 (en) | 2007-08-01 | 2008-07-31 | Electrocoagulation apparatus with integrated sludge control chamber and feed controller assembly |
US12/452,779 Expired - Fee Related US8758604B2 (en) | 2007-08-01 | 2008-07-31 | Integrated vacuum evacuation of waste foam/gas from an electrocoagulation unit during effluent treatment |
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US12/452,780 Expired - Fee Related US8741153B2 (en) | 2007-08-01 | 2008-07-31 | Non-sacrificial electrodes and/or coils for immersed wastewater treatment apparatus and methods |
US12/452,778 Expired - Fee Related US8524082B2 (en) | 2007-08-01 | 2008-07-31 | Mechanical axial vibration in membrane separation treatment of effluents |
US12/452,773 Expired - Fee Related US8663464B2 (en) | 2007-08-01 | 2008-07-31 | Apparatus and methods for enhanced electrocoagulation processing using membrane aeration |
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US12/452,786 Expired - Fee Related US8623209B2 (en) | 2007-08-01 | 2008-07-31 | Fluid head height and foam/gas level control in electrocoagulation apparatus |
US12/452,775 Expired - Fee Related US8257592B2 (en) | 2007-08-01 | 2008-07-31 | Biological wastewater treatment apparatus and methods using moving belt contractor |
US12/452,776 Expired - Fee Related US8435391B2 (en) | 2007-08-01 | 2008-07-31 | Electrocoagulation apparatus with in-place electrode cleaning |
US12/452,787 Expired - Fee Related US8858791B2 (en) | 2007-08-01 | 2008-07-31 | Electrocoagulation apparatus with integrated sludge control chamber and feed controller assembly |
US12/452,779 Expired - Fee Related US8758604B2 (en) | 2007-08-01 | 2008-07-31 | Integrated vacuum evacuation of waste foam/gas from an electrocoagulation unit during effluent treatment |
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US13/999,466 Expired - Fee Related US9108160B2 (en) | 2007-08-01 | 2014-03-03 | Methods for enhanced electrocoagulation processing using membrane aeration |
US14/120,724 Abandoned US20140366730A1 (en) | 2007-08-01 | 2014-06-20 | Methods for vacuum evacuation of waste foam/gas from an electrocoagulation unit during effluent treatment |
US14/544,599 Abandoned US20150225262A1 (en) | 2007-08-01 | 2015-01-26 | Electrocoagulation apparatus having integrated clarifier and sludge control |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR101782631B1 (en) | 2017-07-20 | 2017-09-27 | 더죤환경기술(주) | Water Treatment System containing Dissolved AirFloatation System and Membrane |
CN113975860A (en) * | 2021-12-23 | 2022-01-28 | 常州铭赛机器人科技股份有限公司 | Glue vibration defoaming device |
Families Citing this family (120)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7758742B2 (en) * | 1998-02-27 | 2010-07-20 | Scott Wade Powell | Method and apparatus for separation of water from petroleum products in an electrocoagulation process |
DE10323774A1 (en) * | 2003-05-26 | 2004-12-16 | Khd Humboldt Wedag Ag | Process and plant for the thermal drying of a wet ground cement raw meal |
US7669349B1 (en) * | 2004-03-04 | 2010-03-02 | TD*X Associates LP | Method separating volatile components from feed material |
US9994767B2 (en) | 2005-10-14 | 2018-06-12 | Aquero Company, Llc | Amino acid, carbohydrate and acrylamide polymers useful as flocculants in agricultural and industrial settings |
US7353621B2 (en) * | 2006-02-22 | 2008-04-08 | M-I L.L.C. | Cleaning apparatus for vertical separator |
US20090032446A1 (en) * | 2007-08-01 | 2009-02-05 | Triwatech, L.L.C. | Mobile station and methods for diagnosing and modeling site specific effluent treatment facility requirements |
US8790517B2 (en) * | 2007-08-01 | 2014-07-29 | Rockwater Resource, LLC | Mobile station and methods for diagnosing and modeling site specific full-scale effluent treatment facility requirements |
US20150034558A1 (en) * | 2007-08-01 | 2015-02-05 | Triwatech, Llc | Three phase elctrocoagulation effluent treatment apparatus and methods |
CA2698049C (en) * | 2007-08-27 | 2014-10-28 | Larry D. Sanderson | System and method for purifying an aqueous stream |
US8529770B2 (en) * | 2007-09-27 | 2013-09-10 | Water Of Life, Llc. | Self-contained UV-C purification system |
US8541623B2 (en) * | 2011-01-04 | 2013-09-24 | Linde Aktiengesellschaft | Oxidation method and reactor |
US8465295B2 (en) * | 2008-02-06 | 2013-06-18 | The Mitre Corporation | Fluid percussion system and method for modeling penetrating brain injury |
DE102008029923B4 (en) * | 2008-06-24 | 2016-06-30 | Holger Blum | Process and device for water treatment |
CA2731608C (en) | 2008-07-23 | 2016-10-18 | Aquero Company, Llc | Flotation and separation of flocculated oils and solids from waste waters |
US7781744B2 (en) * | 2008-08-21 | 2010-08-24 | Comecer S.P.A. | Procedure for the preparation of radioisotopes |
US7981301B2 (en) * | 2008-11-21 | 2011-07-19 | Scott W. Powell | Method and apparatus for treatment of contaminated liquid |
CA2686836C (en) * | 2008-12-01 | 2017-04-11 | International Water-Guard Industries, Inc. | Water distribution system with dual use water treatment unit |
US8906237B2 (en) * | 2009-06-09 | 2014-12-09 | Curt Johnson | Water treatment and reuse system |
US8772004B2 (en) * | 2009-06-25 | 2014-07-08 | Old Dominion University Research Foundation | System and method for high-voltage pulse assisted aggregation of algae |
US8506685B2 (en) | 2009-08-17 | 2013-08-13 | Celgard Llc | High pressure liquid degassing membrane contactors and methods of manufacturing and use |
US8409442B2 (en) | 2009-08-20 | 2013-04-02 | Ng Innovations, Inc. | Water separation method and apparatus |
US20110155666A1 (en) * | 2009-12-30 | 2011-06-30 | Chevron U.S.A. Inc. | Method and system using hybrid forward osmosis-nanofiltration (h-fonf) employing polyvalent ions in a draw solution for treating produced water |
US20140110262A1 (en) * | 2010-01-22 | 2014-04-24 | Rockwater Resource, LLC | Fluid head height and foam/gas level control in electrocoagulation apparatus |
WO2011103286A2 (en) | 2010-02-17 | 2011-08-25 | University Of South Florida | Solids retention time uncoupling by selective wasting of sludge |
CA2698880A1 (en) * | 2010-04-01 | 2011-10-01 | Sean Frisky | Method and apparatus for electrocoagulation |
US8430996B2 (en) * | 2010-05-26 | 2013-04-30 | Kaspar Electroplating Corporation | Electrocoagulation reactor having segmented intermediate uncharged plates |
US8647516B2 (en) * | 2010-09-03 | 2014-02-11 | Johnny Leon LOVE | Filtration method with self-cleaning filter assembly |
AR080632A1 (en) * | 2010-12-10 | 2012-04-25 | Ecoglobalh2O Srl | COMPACT INTEGRAL MODULE FOR THE TREATMENT OF LIQUID AND / OR CLOACAL INDUSTRIAL WASTE AND PROVISION THAT USES IT |
USH2271H1 (en) * | 2010-12-13 | 2012-07-03 | James Thomas Sears | Production and application of an aircraft spreadable, cyanobacterial based biological soil crust inoculant for soil fertilization, soil stablization and atmospheric CO2 drawdown and sequestration |
US8940169B2 (en) * | 2011-03-10 | 2015-01-27 | General Electric Company | Spiral wound membrane element and treatment of SAGD produced water or other high temperature alkaline fluids |
WO2012145787A1 (en) * | 2011-04-21 | 2012-11-01 | Aviva Pure Holdings Pty Ltd | Apparatus and method for reducing fouling and scaling in a fluid treatment system |
US9758395B2 (en) | 2011-04-28 | 2017-09-12 | Aquero Company, Llc | Lysine-based polymer coagulants for use in clarification of process waters |
US20120298526A1 (en) * | 2011-05-27 | 2012-11-29 | Atlantis Life Systems Incorporated | Method and apparatus for electrochemical treatment of contaminated water or wastewater |
US9011681B2 (en) | 2011-08-26 | 2015-04-21 | Wasserwerk, Inc. | Self-contained irrigation polishing system |
US8974672B2 (en) | 2011-08-26 | 2015-03-10 | Wasserwerk, Inc. | Self-contained irrigation polishing system |
US9771710B2 (en) | 2011-08-26 | 2017-09-26 | Wasserwerk, Inc. | System and method for treating contaminated water |
US20130075334A1 (en) * | 2011-09-22 | 2013-03-28 | Prakhar Prakash | Apparatus and Process For Treatment of Water |
CN102381813B (en) * | 2011-10-09 | 2012-12-19 | 东莞市威迪膜科技有限公司 | System and method for processing rubbish percolate |
CN102372340B (en) * | 2011-10-09 | 2013-01-16 | 东莞市威迪膜科技有限公司 | System and method for treating organic wastewater of circuit board |
US20130146530A1 (en) * | 2011-12-08 | 2013-06-13 | General Electric Company | Membrane, water treatment system, and method of making |
US20130186822A1 (en) * | 2012-01-20 | 2013-07-25 | Hydration Systems, Llc | Low energy forward osmosis membrane water processing system |
WO2013119718A1 (en) * | 2012-02-07 | 2013-08-15 | Jones Coyte | Treating waste streams with organic content |
WO2013126346A1 (en) * | 2012-02-20 | 2013-08-29 | Ccr Technologies, Ltd. | Process for removing salts from a processing liquid |
CA2873872A1 (en) * | 2012-05-18 | 2013-11-21 | H20 Reclamation Technologies Llc | Water reclamation apparatus and method of operation |
US8673154B2 (en) | 2012-07-12 | 2014-03-18 | Heliae Development, Llc | Tunable electrical field for aggregating microorganisms |
US8668827B2 (en) | 2012-07-12 | 2014-03-11 | Heliae Development, Llc | Rectangular channel electro-acoustic aggregation device |
US8709250B2 (en) | 2012-07-12 | 2014-04-29 | Heliae Development, Llc | Tubular electro-acoustic aggregation device |
US8709258B2 (en) | 2012-07-12 | 2014-04-29 | Heliae Development, Llc | Patterned electrical pulse microorganism aggregation |
US8702991B2 (en) | 2012-07-12 | 2014-04-22 | Heliae Development, Llc | Electrical microorganism aggregation methods |
WO2014018452A1 (en) * | 2012-07-24 | 2014-01-30 | Aquero Company, Llc | Process for reducing soluble organic content in recovered water |
WO2014052520A1 (en) * | 2012-09-26 | 2014-04-03 | Wasserwerk, Inc. | Self-contained irrigation polishing system |
US9884295B2 (en) | 2012-10-08 | 2018-02-06 | Doosan Heavy Industries & Construction Co., Ltd. | Membrane bioreactor system using reciprocating membrane |
US20140151300A1 (en) * | 2012-12-05 | 2014-06-05 | Water & Power Technologies, Inc. | Water treatment process for high salinity produced water |
US9234468B2 (en) | 2012-12-21 | 2016-01-12 | Caterpillar Inc. | Fuel system |
US9446974B2 (en) * | 2013-02-06 | 2016-09-20 | Energysolutions, Inc. | Fluid treatment methods and systems |
US10745299B2 (en) | 2013-02-22 | 2020-08-18 | NiBru Traka, Inc. | Struvite formation by precipitation of ammonia in electrocoagulation process |
US10358361B2 (en) | 2013-02-22 | 2019-07-23 | Loren L. Losh | System and method for remediation of wastewater including aerobic and electrocoagulation treatment |
US11851347B2 (en) | 2013-03-13 | 2023-12-26 | Wasserwerk, Inc. | System and method for treating contaminated water |
US20150083652A1 (en) | 2013-09-23 | 2015-03-26 | Wayne R. HAWKS | System and method for treating contaminated water |
US20140262735A1 (en) * | 2013-03-13 | 2014-09-18 | Wasserwerk, Inc. | System and method for treating contaminated water |
US10724314B1 (en) | 2013-03-15 | 2020-07-28 | Rio Resources Llc | Method and apparatus for collection, treatment, and recycling of oilfield drilling fluids and wastewater |
RU2547482C2 (en) * | 2013-05-23 | 2015-04-10 | Закрытое Акционерное Общество "Аквафор Продакшн" (Зао "Аквафор Продакшн") | Water treatment system with hydraulic control |
CN103265128B (en) * | 2013-06-12 | 2014-04-23 | 张意立 | Internal thread flange nickel-base coupling insulation sea water desalting device |
CN103319035B (en) * | 2013-06-17 | 2016-11-23 | 李榕生 | The high throughput photocatalytic waste water degradation reactor of prevention light source placing chamber gushing water |
CN105683093B (en) | 2013-08-05 | 2019-07-09 | 格雷迪安特公司 | Water treatment system and correlation technique |
WO2015042584A1 (en) | 2013-09-23 | 2015-03-26 | Gradiant Corporation | Desalination systems and associated methods |
US20160279576A1 (en) * | 2013-11-08 | 2016-09-29 | Nanyang Technological University | A membrane filtration module |
WO2015127366A2 (en) * | 2014-02-21 | 2015-08-27 | Flsmidth A/S | Filter press for high performance liquid/solid separations and methods thereof |
US20150246830A1 (en) * | 2014-03-03 | 2015-09-03 | Jason D. Lalli | Electrocoagulation System Using Three Phase AC Power |
US10995995B2 (en) | 2014-06-10 | 2021-05-04 | Vmac Global Technology Inc. | Methods and apparatus for simultaneously cooling and separating a mixture of hot gas and liquid |
US9221694B1 (en) | 2014-10-22 | 2015-12-29 | Gradiant Corporation | Selective scaling in desalination water treatment systems and associated methods |
US20170334801A1 (en) * | 2014-10-27 | 2017-11-23 | Dirt 2 Soil Llc | A system for enhancing plant growth |
US20160123097A1 (en) * | 2014-10-29 | 2016-05-05 | Jerry W. Noles, Jr. | Method of Treating Flowback Fluid from a Well |
US10308526B2 (en) | 2015-02-11 | 2019-06-04 | Gradiant Corporation | Methods and systems for producing treated brines for desalination |
US10167218B2 (en) | 2015-02-11 | 2019-01-01 | Gradiant Corporation | Production of ultra-high-density brines |
WO2016183666A1 (en) * | 2015-05-19 | 2016-11-24 | Formarum Inc. | Water treatment system and method |
US10202695B2 (en) * | 2015-05-21 | 2019-02-12 | Palo Alto Research Center Incorporated | Photoelectrolysis system and method |
AU2016298326B2 (en) | 2015-07-29 | 2022-08-04 | Gradiant Corporation | Osmotic desalination methods and associated systems |
WO2017030932A1 (en) | 2015-08-14 | 2017-02-23 | Gradiant Corporation | Selective retention of multivalent ions |
WO2017030937A1 (en) | 2015-08-14 | 2017-02-23 | Gradiant Corporation | Production of multivalent ion-rich process streams using multi-stage osmotic separation |
US9833741B2 (en) * | 2015-08-24 | 2017-12-05 | Doosan Heavy Industries & Constructions Co., Ltd. | Submerged membrane filtration system using reciprocating membrane |
GB201516253D0 (en) * | 2015-09-14 | 2015-10-28 | Univ Montfort | Rotating contactor reactor |
PL3407998T3 (en) | 2016-01-27 | 2021-12-13 | Koch-Glitsch, Lp | Inlet vane device with inner beam for rigidity and vessel containing the device |
US10689264B2 (en) | 2016-02-22 | 2020-06-23 | Gradiant Corporation | Hybrid desalination systems and associated methods |
US10150059B2 (en) | 2016-02-25 | 2018-12-11 | Mountain Water Concepts | Small portable system for electrocoagulative fluid purification |
GB201605068D0 (en) * | 2016-03-24 | 2016-05-11 | Applied Biomimetic As | Electricity generation process |
GB201605070D0 (en) * | 2016-03-24 | 2016-05-11 | Applied Biomimetic As | Power generation process |
DE102016109822A1 (en) * | 2016-05-27 | 2017-11-30 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. | Electrolytic reactor |
US10465511B2 (en) | 2016-06-29 | 2019-11-05 | KCAS Drilling, LLC | Apparatus and methods for automated drilling fluid analysis system |
US9932257B2 (en) | 2016-07-29 | 2018-04-03 | Chevron U.S.A. Inc. | Systems and methods for producing regenerant brine and desalinated water from high temperature produced water |
US10941058B2 (en) | 2016-09-23 | 2021-03-09 | Jason D Lalli | Electrocoagulation system and method using plasma discharge |
IL251168B (en) * | 2017-03-14 | 2019-08-29 | Efraty Avi | Integrated reverse osmosis and membrane cleaning systems for fouling prevention |
EP3630337A4 (en) * | 2017-05-24 | 2021-03-10 | Openwater.in Pvt. Ltd. | A high throughput fluid treatment system |
GB201711240D0 (en) | 2017-07-12 | 2017-08-23 | Saltkraft Aps | Power generation process |
GB201711238D0 (en) | 2017-07-12 | 2017-08-23 | Saltkraft Aps | Power generation process |
US10837116B2 (en) | 2017-11-27 | 2020-11-17 | Fraunhofer-Gesellschaft Zur Foerderung Der Angewandten Forschung E.V. | Electrolytic reactor |
CN107954586A (en) * | 2017-12-02 | 2018-04-24 | 中节能(沧州)环保能源有限公司 | Water cycle utilization device and method are rinsed in desliming |
CN108191055B (en) * | 2018-01-30 | 2020-08-25 | 哈尔滨工业大学 | Split anaerobic ceramic membrane bioreactor capable of effectively relieving membrane pollution |
FI128091B (en) * | 2018-04-22 | 2019-09-13 | Timo Korpela | Combiflotation for purification and disinfection of waste water |
CN108394979B (en) * | 2018-05-13 | 2021-06-11 | 江苏天频植保科技有限公司 | Rotatory disturbance formula sewage treatment is with flocculation agitated vessel |
CN108947112B (en) * | 2018-07-09 | 2021-05-04 | 江苏自强环保科技有限公司 | Environment-friendly equipment using dynamic membrane method |
CN108947111A (en) * | 2018-07-09 | 2018-12-07 | 江苏自强环保科技有限公司 | It is a kind of for carrying out the automatic control system of sewage treatment |
CA3109230A1 (en) | 2018-08-22 | 2020-02-27 | Gradiant Corporation | Liquid solution concentration system comprising isolated subsystem and related methods |
CN110615528A (en) * | 2018-09-25 | 2019-12-27 | 青海洁神环境能源产业有限公司 | Three-dimensional rotary type net contact body device, biological rotating disc pool and sewage treatment equipment |
CN109928491B (en) * | 2019-03-11 | 2024-01-16 | 长江大学 | Biological rotating disc device and system |
WO2021005398A1 (en) * | 2019-07-08 | 2021-01-14 | Noubahar Salman | Water purification sink |
US11596912B2 (en) | 2019-07-23 | 2023-03-07 | University Of Kentucky Research Foundation | Single stage clarifier and mixing assembly |
US11207614B2 (en) | 2019-07-23 | 2021-12-28 | University Of Kentucky Research Foundation | Single stage clarifier and mixing assembly |
CN110723763B (en) * | 2019-10-21 | 2021-11-30 | 江苏河海给排水成套设备有限公司 | Sponge municipal sewage is collected and is used sewage treatment ware |
CN110818197B (en) * | 2019-11-26 | 2021-12-24 | 张家界贵友环保材料科技有限公司 | Sewage treatment method and device for improving sewage treatment efficiency and sewage treatment controller |
CN110980891B (en) * | 2019-12-17 | 2021-08-03 | 昆明理工大学 | Tower type electric flocculation water treatment device |
US11001518B1 (en) | 2020-02-12 | 2021-05-11 | Rio Resources Llc | Methods for treatment and purification of oil and gas produced water |
CN111320328A (en) * | 2020-03-13 | 2020-06-23 | 李海洋 | Sewage treatment process |
RU2751938C1 (en) * | 2020-04-29 | 2021-07-21 | Общество с ограниченной ответственностью "Научно-производственная фирма "ЭНАВЭЛ" | Device for electrostatic cleaning and regeneration of dielectric liquids |
CN111606428A (en) * | 2020-05-09 | 2020-09-01 | 殷富新 | Efficient sewage treatment system and method combining aeration purification and bioremediation |
CN111689564A (en) * | 2020-07-23 | 2020-09-22 | 方永辉 | Collect whirlwind separation and honeycomb filter sediment in water treatment facilities of an organic whole |
WO2022108891A1 (en) | 2020-11-17 | 2022-05-27 | Gradiant Corporaton | Osmotic methods and systems involving energy recovery |
CN113023992B (en) * | 2021-03-17 | 2023-05-05 | 河南绿迪净化工程有限公司 | Cyclone separation water treatment device |
US20230135497A1 (en) | 2021-11-01 | 2023-05-04 | Indian Oil Corporation Limited | Method for refinery wastewater treatment, a system and uses thereof |
CN115432851B (en) * | 2022-08-23 | 2023-06-23 | 长兴瑷晟环保装备有限公司 | High-efficient coagulation hydrodynamic cavitation all-in-one |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5190667A (en) * | 1991-06-19 | 1993-03-02 | University Of Florida | Separation of gases and solutes by augmented diffusion in counterflow |
US20050023219A1 (en) * | 2003-07-30 | 2005-02-03 | Phase Inc. | Filtration system with enhanced cleaning and dynamic fluid separation |
Family Cites Families (161)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1118614A (en) * | 1914-05-27 | 1914-11-24 | Allen Charles R | Slime-separator. |
US2336430A (en) | 1941-02-15 | 1943-12-07 | Western Electric Co | Separating apparatus |
US2635753A (en) * | 1948-06-01 | 1953-04-21 | Lyle G Mclean | Air stratifier |
US3006435A (en) | 1958-01-29 | 1961-10-31 | Union Carbide Corp | Liquid entrainment separator |
US3057786A (en) * | 1959-04-27 | 1962-10-09 | Phillips Petroleum Co | Foam eliminating feed distributor |
US3141000A (en) * | 1959-07-14 | 1964-07-14 | Petrolite Corp | Apparatus for creating uniform streams in flow passages |
US3455821A (en) * | 1964-02-01 | 1969-07-15 | Ahlstroem Oy | Apparatus for treating slurries or gases with screen or filter surfaces under pressure |
GB1178601A (en) * | 1967-01-05 | 1970-01-21 | Nat Res Dev | Biological Treatment of Waste Water containing Organic Matter |
US3535236A (en) * | 1967-05-11 | 1970-10-20 | Henry J Travis | Floating cover |
US3524213A (en) * | 1968-06-17 | 1970-08-18 | Mayer Spivack | Vacuum head |
GB1324358A (en) | 1970-10-23 | 1973-07-25 | Ames Crosta Mills & Co Ltd | Apparatus for the biological treatment of waste water by the biosorption process |
GB1333061A (en) | 1971-01-07 | 1973-10-10 | Ames Crosta Mills & Co Ltd | Biological treatment of waste water containing organic matter |
US3769207A (en) * | 1971-06-14 | 1973-10-30 | E Baer | Process of separation of emulsified or dispersed matter from water |
US3936364A (en) * | 1973-02-20 | 1976-02-03 | Middle Sidney A | Apparatus and method for treatment of water oligodynamically |
DE2409343B2 (en) * | 1974-02-27 | 1979-06-28 | Akzo Gmbh, 5600 Wuppertal | Process for removing the vaporous reaction products in the production of polyesters, in particular polyethylene terephthalate |
DE2640803C2 (en) * | 1975-09-18 | 1982-03-11 | Thune-Eureka A/S, Tranby | Lamella separator for sedimentation |
US4137062A (en) * | 1976-12-20 | 1979-01-30 | Great Circle Associates | Filtration with a compostable filter medium |
CA1091593A (en) * | 1977-10-05 | 1980-12-16 | Eli I. Robinsky | Gravitational separator having membrane baffles therein |
US4177147A (en) * | 1978-03-20 | 1979-12-04 | Roberts Filter Manufacturing Company | Biological treating systems |
ZA783467B (en) * | 1978-06-16 | 1979-09-26 | Fraser & Chalmers Equip Ltd | Feed distributors |
DK146800C (en) * | 1979-06-26 | 1984-07-02 | Frandsen Aksel S | CONTACT FILTER FOR USE IN A PLANT FOR BIOLOGICAL WASTE CLEANING |
SU929581A2 (en) * | 1979-06-27 | 1982-05-23 | Харьковский Ордена Ленина И Ордена Октябрьской Революции Моторостроительный Завод "Серп И Молот" | Apparatus for electrochemically purifying contaminated liquid |
CH651815A5 (en) * | 1980-06-25 | 1985-10-15 | Kh Polt I Im V I Lenina | Apparatus for electrochemical cleaning of effluent |
DE3029842C2 (en) * | 1980-08-08 | 1984-05-30 | Char'kovskij motorostroitel'nyj zavod "Serp i Molot", Char'kov | Process and apparatus for electrochemical waste water purification |
CH646404A5 (en) * | 1980-09-05 | 1984-11-30 | Kh Motorostroitel Z Serp Molot | Plant for electrochemical purification of waste water |
US4414091A (en) * | 1980-12-30 | 1983-11-08 | Axenko Alexandr A | Apparatus for electrochemical purification of contaminated liquids |
CH650417A5 (en) * | 1981-01-12 | 1985-07-31 | Kh Polt I Im V I Lenina | Plant for electrochemical cleaning of waste water |
US4383920A (en) * | 1981-05-29 | 1983-05-17 | Ecolochem, Inc. | Mobile fluid purification system |
US4416761A (en) * | 1982-07-27 | 1983-11-22 | The United States Of America As Represented By The Department Of Health And Human Services | Multi slab gel casting electrophoresis apparatus |
US4500329A (en) | 1983-04-25 | 1985-02-19 | United States Of America As Represented By Secretary Of The Interior | Self-actuating vacuum gas/liquid separator |
US4530763A (en) * | 1983-07-11 | 1985-07-23 | Clyde Robert A | Method for treating waste fluid with bacteria |
DE8328904U1 (en) * | 1983-10-06 | 1986-08-21 | Hidrotronic Watercleaning Systems, Ltd., Zug | Device for purifying water |
DE3568006D1 (en) * | 1984-05-24 | 1989-03-09 | Terumo Corp | Hollow fiber membrane type oxygenator and method for manufacturing same |
GB8413751D0 (en) * | 1984-05-30 | 1984-07-04 | Ontario Research Foundation | Biological contact gas scrubber |
US4504393A (en) * | 1984-06-08 | 1985-03-12 | Chevron Research Company | Method and apparatus for controlling a rotating biological contactor |
JPS6113148A (en) * | 1984-06-29 | 1986-01-21 | Hitachi Ltd | Continuous-type electrophoretic apparatus for nucleic acid drop |
US4728403A (en) * | 1984-08-11 | 1988-03-01 | Edgar Renzler | Process for the regeneration of cleaning and degreasing baths and device for application of the process |
DE3513602A1 (en) * | 1985-04-16 | 1985-11-14 | Grabowski Tropfkörper-Technik GmbH, 6352 Ober-Mörlen | HOLLOW BODY FOR BIOLOGICAL WASTE WATER TREATMENT |
US4600694A (en) * | 1985-05-24 | 1986-07-15 | Clyde Robert A | Apparatus for harvesting cells |
US4710292A (en) * | 1986-08-18 | 1987-12-01 | Atara Corporation | Digester tank with foam control cover |
US4872959A (en) * | 1987-07-17 | 1989-10-10 | Cleanup & Recovery Corp. (Cure) | Electrolytic treatment of liquids |
US4931225A (en) | 1987-12-30 | 1990-06-05 | Union Carbide Industrial Gases Technology Corporation | Method and apparatus for dispersing a gas into a liquid |
US4861352A (en) | 1987-12-30 | 1989-08-29 | Union Carbide Corporation | Method of separating a gas and/or particulate matter from a liquid |
US5004531A (en) * | 1988-01-26 | 1991-04-02 | Tiernan Joan E | Treatment of concentrated industrial wastewaters originating from oil shale and the like by electrolysis polyurethane foam interaction |
US4999116A (en) * | 1988-06-10 | 1991-03-12 | Southern Water Treatment Company, Inc. | Waste water treatment method |
US5000219A (en) * | 1988-06-30 | 1991-03-19 | Systems Specialties | Fluid flow control regulator |
US4826596A (en) * | 1988-07-07 | 1989-05-02 | Gene Hirs | Drum filter having a media supply roll and reroll drum |
GB8817793D0 (en) * | 1988-07-26 | 1988-09-01 | British Petroleum Co Plc | Mixing apparatus |
US4889624A (en) * | 1989-01-06 | 1989-12-26 | The Graver Company | Lamella gravity separator |
US4897356A (en) * | 1989-03-03 | 1990-01-30 | Solids Dewatering Systems, Inc. | Rotating coiled tube biological contactor |
JP2533942B2 (en) * | 1989-03-13 | 1996-09-11 | 株式会社日立製作所 | Knowledge extraction method and process operation support system |
US4919825A (en) * | 1989-03-20 | 1990-04-24 | Hallco Fabricators, Inc. | Filter apparatus and method for separating contaminants from liquids |
US4897359A (en) * | 1989-03-27 | 1990-01-30 | Bio-Response, Inc. | Apparatus for oxygenating culture medium |
US5034164A (en) * | 1989-10-02 | 1991-07-23 | Semmens Michael J | Bubbleless gas transfer device and process |
US5238574A (en) * | 1990-06-25 | 1993-08-24 | Kawasaki Jukogyo Kabushiki Kaisha | Method and apparatus having reverse osmosis membrane for concentrating solution |
DE69220526T2 (en) * | 1991-03-18 | 1998-02-05 | Asahi Chemical Ind | Bipolar filter press type electrolysis cell |
DE4117056C2 (en) | 1991-05-23 | 1994-01-27 | Textec Textil Eng & Consult | Rotating disc for rotating disc reactors |
FR2678260B1 (en) * | 1991-06-26 | 1994-02-18 | Otv Sa | SURFACE WATER TREATMENT CHAIN WITH SECURITY BARRIER, SECURITY BARRIER, AND APPLICATIONS THEREOF. |
US5271814A (en) * | 1992-03-19 | 1993-12-21 | David M. A. Metzler | Thin film electrocoagulation for removal for contaminants from liquid media |
SE505028C2 (en) * | 1992-05-13 | 1997-06-16 | Electrolux Ab | Method and apparatus for purifying water |
US5277176A (en) * | 1992-06-29 | 1994-01-11 | Habashi Nader M | Extracorporeal lung assistance apparatus and process |
US5578213A (en) * | 1992-07-28 | 1996-11-26 | Pall Corporation | Fluid treatment process |
US5244579A (en) * | 1992-10-09 | 1993-09-14 | Zenon Environmental Inc. | Transportable reverse osmosis water purification unit |
RU2060956C1 (en) * | 1992-10-14 | 1996-05-27 | Владимир Дмитриевич Назаров | Sewage purification from weighted substances method |
US5256570A (en) * | 1992-10-20 | 1993-10-26 | Clyde Robert A | Bioreactor configured for various permeable cell supports and culture media |
TW223613B (en) * | 1992-11-05 | 1994-05-11 | Shinmaywa Ind Ltd | |
US5403475A (en) * | 1993-01-22 | 1995-04-04 | Allen; Judith L. | Liquid decontamination method |
US5514278A (en) * | 1993-04-12 | 1996-05-07 | Khudenko; Boris M. | Counterflow microbiological processes |
GB9313854D0 (en) * | 1993-07-05 | 1993-08-18 | Diversey Eng Europ | Element |
FR2713220B1 (en) * | 1993-11-30 | 1996-03-08 | Omnium Traitement Valorisa | Installation of water purification with submerged filter membranes. |
GB2284906B (en) | 1993-12-16 | 1998-01-07 | B W T | Production of water and wastewater treatment plant |
US6110375A (en) * | 1994-01-11 | 2000-08-29 | Millipore Corporation | Process for purifying water |
US5443719A (en) * | 1994-02-23 | 1995-08-22 | Aqua-Ion Systems, Inc. | System and reactor for mixing coagulating agents into a contaminated water flow, and for removing contaminants therefrom |
GB9404709D0 (en) * | 1994-03-11 | 1994-04-27 | Multilyte Ltd | Binding assay |
US5547584A (en) * | 1994-03-17 | 1996-08-20 | Electronic Drilling Control, Inc. | Transportable, self-contained water purification system and method |
US5611907A (en) * | 1994-04-18 | 1997-03-18 | Global Water Industries, Inc. | Electrolytic treatment device and method for using same |
AU2251495A (en) * | 1994-05-02 | 1995-11-29 | Master Flo Technology Inc. | Reverse osmosis filtration system |
US5507934A (en) * | 1994-11-01 | 1996-04-16 | Visible Genetics Inc. | Apparatus for preparing gels for use in electrophoretic separations and similar applications |
US5558775A (en) * | 1994-11-01 | 1996-09-24 | Joseph Busch, Jr. | Process for the treatment of hazardous waste water |
FR2731420B1 (en) * | 1995-03-10 | 1997-06-13 | Mercier Dominique | METHOD AND DEVICE FOR TREATING WATER WITH A VIEW TO SOFTENING ELECTROCHEMICALLY |
US20020014449A1 (en) * | 1995-06-08 | 2002-02-07 | Luis Rios | Separation systems and methods |
EP0848642A1 (en) * | 1995-06-30 | 1998-06-24 | Pall Corporation | Separation systems and methods |
US5674433A (en) * | 1995-08-24 | 1997-10-07 | Regents Of The University Of Minnesota | High efficiency microbubble aeration |
US5756874A (en) * | 1995-10-10 | 1998-05-26 | Eosystems, Inc. | Electrochemical cell for processing organic wastes |
US5632892A (en) * | 1995-10-19 | 1997-05-27 | Mechanical Equipment Company, Inc. | Portable reverse osmosis water purification plant |
RU2094384C1 (en) * | 1995-11-15 | 1997-10-27 | Малое научно-производственное государственное предприятие "Технолог" | Electrochemical method of purification of protein-carrying liquid media and gear for its implementation |
US5741426A (en) * | 1995-12-05 | 1998-04-21 | Mccabe; Derald L. | Method for treatment of contaminated water |
US5601421A (en) * | 1996-02-26 | 1997-02-11 | Lee; W. Ken | Valveless double acting positive displacement fluid transfer device |
US5711051A (en) * | 1996-04-01 | 1998-01-27 | Professional Chemicals Corporation | Hard surface cleaning appliance |
GB9607160D0 (en) * | 1996-04-04 | 1996-06-12 | Wickins Jeremy | Waste water treatment apparatus |
US5846413A (en) * | 1996-04-26 | 1998-12-08 | Lenox Institute Of Water Technology, Inc. | Three zone dissolved air flotation clarifier with improved efficiency |
US5741416A (en) * | 1996-10-15 | 1998-04-21 | Tempest Environmental Systems, Inc. | Water purification system having plural pairs of filters and an ozone contact chamber |
CA2269605A1 (en) * | 1996-10-23 | 1998-04-30 | Louis H. Knieper | Electrochemical treatment of effluent water |
US6136186A (en) | 1997-01-31 | 2000-10-24 | Lynntech, Inc. | Photocatalytic oxidation of organics using a porous titanium dioxide membrane and an efficient oxidant |
JPH10225167A (en) * | 1997-02-06 | 1998-08-21 | Zexel Corp | Drive controller for brushless motor |
JP2001511282A (en) * | 1997-02-07 | 2001-08-07 | ジー. ブラウン,ピーター | System and method for simulation and modeling of a biopharmaceutical batch process manufacturing facility |
US6120688A (en) * | 1997-02-25 | 2000-09-19 | Zenon Environmental, Inc. | Portable reverse osmosis unit for producing drinking water |
DE19724005C1 (en) * | 1997-06-08 | 1999-07-29 | Hans Dr Ing Ritter | Electrode arrangement and anode scraping device for electro-flocculation |
CH692479A5 (en) * | 1997-07-08 | 2002-07-15 | Bucher Guyer Ag | Cross-flow filtration system and method for operating such a plant. |
US5972216A (en) * | 1997-10-24 | 1999-10-26 | Terra Group, Inc. | Portable multi-functional modular water filtration unit |
US5928493A (en) * | 1997-11-24 | 1999-07-27 | Kaspar Electroplating Corporation | Process and apparatus for electrocoagulative treatment of industrial waste water |
US6044903A (en) * | 1998-02-20 | 2000-04-04 | Frigid Units, Inc. | Water conditioning assembly |
KR100395731B1 (en) * | 1998-02-27 | 2003-08-25 | 스코트 웨이드 포웰 | Method and apparatus for electrocoagulation of liquids |
US7758742B2 (en) * | 1998-02-27 | 2010-07-20 | Scott Wade Powell | Method and apparatus for separation of water from petroleum products in an electrocoagulation process |
US7211185B2 (en) * | 1998-02-27 | 2007-05-01 | Scott Wade Powell | Method and apparatus for electrocoagulation of liquids |
US8048279B2 (en) * | 1998-02-27 | 2011-11-01 | Scott Wade Powell | Method and apparatus for electrocoagulation of liquids |
WO1999048588A1 (en) * | 1998-03-20 | 1999-09-30 | Mazzei Angelo L | Stripping of contaminants from water |
US6228255B1 (en) * | 1998-07-24 | 2001-05-08 | Dialysis Systems, Inc. | Portable water treatment facility |
JP4203777B2 (en) * | 1998-08-25 | 2009-01-07 | 株式会社オメガ | Waste water treatment method and treatment apparatus |
US6689271B2 (en) * | 1998-11-23 | 2004-02-10 | Kaspar Wire Works, Inc. | Process and apparatus for electrocoagulative treatment of industrial waste water |
US20040079650A1 (en) * | 1998-11-23 | 2004-04-29 | Morkovsky Paul E. | Electrocoagulation reactor |
US6241861B1 (en) * | 1998-12-11 | 2001-06-05 | Robert Herbst | Waste water treatment tank using an electrochemical treatment process |
US6256833B1 (en) * | 1999-01-20 | 2001-07-10 | Bissell Homecare, Inc. | Upright vacuum cleaner with handle-mounted lamp assembly and height adjustment |
AU4978200A (en) * | 1999-04-29 | 2000-11-17 | F. William Gilmore | Electrocoagulation chamber and method |
CA2272596A1 (en) * | 1999-05-21 | 2000-11-21 | Lawrence A. Lambert | Waste water treatment method and apparatus |
US6245236B1 (en) * | 1999-05-26 | 2001-06-12 | Cercona Of America Inc. | Reciprocating biological filter |
US6613202B2 (en) * | 1999-06-28 | 2003-09-02 | Current Water Technology, Inc. | Tank batch electrochemical water treatment process |
US6464884B1 (en) * | 1999-08-26 | 2002-10-15 | The Regents Of The University Of California | Portable water treatment unit |
US6408227B1 (en) * | 1999-09-29 | 2002-06-18 | The University Of Iowa Research Foundation | System and method for controlling effluents in treatment systems |
GB2361772B (en) * | 2000-04-29 | 2004-05-19 | Malvern Instr Ltd | Mobility and effects arising from surface charge |
US6719894B2 (en) * | 2000-08-11 | 2004-04-13 | Ira B. Vinson | Process for electrocoagulating waste fluids |
US6503125B1 (en) * | 2000-09-05 | 2003-01-07 | Raymond J. Harrington | Dust shroud for abrading machine |
US20020033363A1 (en) * | 2000-09-19 | 2002-03-21 | Resouse Biology Research Institute Co., Ltd. | Containerized polluted-water treatment apparatus |
US6572774B2 (en) * | 2001-02-16 | 2003-06-03 | Wastewater Technology, Inc. | Waste treatment method and apparatus with integral clarifier |
US20040060862A1 (en) * | 2001-03-14 | 2004-04-01 | Savage E. Stuart | Process for direct filtration of wastewater |
US6740245B2 (en) * | 2001-03-26 | 2004-05-25 | Enerox Technology Llc | Non-chemical water treatment method and apparatus employing ionized air purification technologies |
US6805806B2 (en) * | 2001-06-12 | 2004-10-19 | Hydrotreat, Inc. | Method and apparatus for treatment of wastewater employing membrane bioreactors |
US6582592B2 (en) * | 2001-06-12 | 2003-06-24 | Hydrotreat, Inc. | Apparatus for removing dissolved metals from wastewater by electrocoagulation |
US6607668B2 (en) * | 2001-08-17 | 2003-08-19 | Technology Ventures, Inc. | Water purifier |
WO2003032452A1 (en) * | 2001-10-12 | 2003-04-17 | Gilmore F William | Electrocoagulation reaction chamber and method |
AT412416B (en) * | 2001-10-23 | 2005-02-25 | Zackl Wilhelm | VALVE-FREE PUMP |
TWI245744B (en) * | 2001-12-21 | 2005-12-21 | Ind Tech Res Inst | System and method for removing deep sub-micron particles from water |
US6746593B2 (en) * | 2002-01-18 | 2004-06-08 | Robert J. Herbst | High volume electrolytic water treatment system and process for treating wastewater |
US6960301B2 (en) * | 2002-03-15 | 2005-11-01 | New Earth Systems, Inc. | Leachate and wastewater remediation system |
AU2002952743A0 (en) * | 2002-11-19 | 2002-12-05 | Waterpower Systems Pty Ltd | Electrocoagulation system |
US6797943B2 (en) * | 2002-05-07 | 2004-09-28 | Siemens Ag | Method and apparatus for ion mobility spectrometry |
US6852219B2 (en) * | 2002-07-22 | 2005-02-08 | John M. Hammond | Fluid separation and delivery apparatus and method |
US20040026335A1 (en) * | 2002-08-12 | 2004-02-12 | Fields William M. | Multi-stage photo-catalytic oxidation fluid treatment system |
US7087176B2 (en) * | 2002-11-11 | 2006-08-08 | Ira B. Vinson | High pressure process and apparatus for the electrocoagulative treatment of aqueous and viscous fluids |
US20040104153A1 (en) * | 2002-11-29 | 2004-06-03 | Chung-Hsiang Yang | Portable water purifier |
AU2003287814A1 (en) * | 2002-11-29 | 2004-06-23 | Les Technologies Elcotech Inc. | Apparatus and method for wastewater treatment by means of electroflotation and/or electrocoagulation |
US6972077B2 (en) * | 2003-05-28 | 2005-12-06 | Tipton Gary A | Cells and electrodes for electrocoagulation treatment of wastewater |
WO2005011848A1 (en) * | 2003-07-30 | 2005-02-10 | Phase Inc. | Filtration system and dynamic fluid separation method |
US7063789B2 (en) * | 2003-08-13 | 2006-06-20 | Koch Membrane Systems, Inc. | Filtration element and method of constructing a filtration assembly |
US20070199868A1 (en) * | 2003-09-23 | 2007-08-30 | Aquenox Pty Ltd. | Wastewater Purification Method |
US7156986B2 (en) * | 2003-11-26 | 2007-01-02 | Warrow Theodore U | Self-cleansing media for rotating biological contactors |
US6949191B1 (en) * | 2004-04-29 | 2005-09-27 | Jrj Holdings, Llc | Packaged wastewater treatment unit |
US7258800B1 (en) * | 2004-08-26 | 2007-08-21 | Herbst Robert J | Electrocoagulation waste water batch tank treatment system |
US7297278B2 (en) * | 2004-10-20 | 2007-11-20 | Baker Hughes Incorporated | Methods for removing metals from water |
US20070017874A1 (en) * | 2005-07-19 | 2007-01-25 | Renaud Craig P | Effluent treatment method and apparatus |
AU2006298434B2 (en) * | 2005-10-06 | 2011-09-01 | Weissman, Jeremy | Method and system for treating organically contaminated waste water |
US7727394B2 (en) * | 2005-10-28 | 2010-06-01 | Dual Vortex Microfiltration, Llc | System and method of fluid filtration utilizing cross-flow currents |
US7563939B2 (en) * | 2005-12-14 | 2009-07-21 | Mark Slater Denton | Method for treating radioactive waste water |
US7544287B2 (en) * | 2006-05-24 | 2009-06-09 | Seprotech Systems Incorporated | Reciprocating biological contactor and method of use |
US7410588B2 (en) * | 2006-09-22 | 2008-08-12 | John Klemic | Aqueous waste processing method |
US7998225B2 (en) * | 2007-02-22 | 2011-08-16 | Powell Scott W | Methods of purifying biodiesel fuels |
US20090107915A1 (en) * | 2007-03-12 | 2009-04-30 | Its Engineered Systems, Inc. | Treatment process and system for wastewater, process waters, and produced waters applications |
US20090008267A1 (en) * | 2007-07-05 | 2009-01-08 | Giovanni Del Signore | Process and method for the removal of arsenic from water |
US20090032446A1 (en) * | 2007-08-01 | 2009-02-05 | Triwatech, L.L.C. | Mobile station and methods for diagnosing and modeling site specific effluent treatment facility requirements |
US8337706B2 (en) * | 2007-10-14 | 2012-12-25 | 1612017 Alberta Ltd. | Solids removal system and method |
US8491762B2 (en) * | 2010-11-10 | 2013-07-23 | Pioneer H2O Technologies, Inc. | Water purification apparatus and process for purifying water |
-
2007
- 2007-08-01 US US11/888,512 patent/US20090032446A1/en not_active Abandoned
-
2008
- 2008-07-31 US US12/452,777 patent/US8858790B2/en not_active Expired - Fee Related
- 2008-07-31 WO PCT/US2008/009271 patent/WO2009017801A1/en active Application Filing
- 2008-07-31 US US12/452,785 patent/US20100126926A1/en not_active Abandoned
- 2008-07-31 US US12/452,780 patent/US8741153B2/en not_active Expired - Fee Related
- 2008-07-31 CA CA2694170A patent/CA2694170C/en not_active Expired - Fee Related
- 2008-07-31 US US12/452,778 patent/US8524082B2/en not_active Expired - Fee Related
- 2008-07-31 WO PCT/US2008/009254 patent/WO2009017787A1/en active Application Filing
- 2008-07-31 WO PCT/US2008/009269 patent/WO2009017799A1/en active Application Filing
- 2008-07-31 CA CA2694178A patent/CA2694178A1/en not_active Abandoned
- 2008-07-31 AU AU2008282787A patent/AU2008282787B2/en not_active Ceased
- 2008-07-31 WO PCT/US2008/009229 patent/WO2009017773A1/en active Application Filing
- 2008-07-31 EP EP08794898A patent/EP2173671A4/en not_active Withdrawn
- 2008-07-31 US US12/452,773 patent/US8663464B2/en not_active Expired - Fee Related
- 2008-07-31 WO PCT/US2008/009249 patent/WO2009017785A1/en active Application Filing
- 2008-07-31 WO PCT/US2008/009257 patent/WO2009017790A1/en active Application Filing
- 2008-07-31 US US12/452,774 patent/US20100116737A1/en not_active Abandoned
- 2008-07-31 WO PCT/US2008/009255 patent/WO2009017788A1/en active Application Filing
- 2008-07-31 WO PCT/US2008/009258 patent/WO2009017791A1/en active Application Filing
- 2008-07-31 AU AU2008282848A patent/AU2008282848B2/en not_active Ceased
- 2008-07-31 US US12/452,786 patent/US8623209B2/en not_active Expired - Fee Related
- 2008-07-31 CA CA2694156A patent/CA2694156A1/en not_active Abandoned
- 2008-07-31 US US12/452,775 patent/US8257592B2/en not_active Expired - Fee Related
- 2008-07-31 AU AU2008282785A patent/AU2008282785B2/en not_active Ceased
- 2008-07-31 WO PCT/US2008/009209 patent/WO2009017759A1/en active Application Filing
- 2008-07-31 WO PCT/US2008/009256 patent/WO2009017789A1/en active Application Filing
- 2008-07-31 CA CA2694171A patent/CA2694171C/en not_active Expired - Fee Related
- 2008-07-31 WO PCT/US2008/009250 patent/WO2009017786A1/en active Application Filing
- 2008-07-31 AU AU2008282786A patent/AU2008282786B2/en not_active Ceased
- 2008-07-31 US US12/452,776 patent/US8435391B2/en not_active Expired - Fee Related
- 2008-07-31 US US12/452,787 patent/US8858791B2/en not_active Expired - Fee Related
- 2008-07-31 WO PCT/US2008/009259 patent/WO2009017792A1/en active Application Filing
- 2008-07-31 US US12/452,779 patent/US8758604B2/en not_active Expired - Fee Related
-
2013
- 2013-08-27 US US13/987,738 patent/US20130341271A1/en not_active Abandoned
- 2013-09-11 US US13/987,874 patent/US8940166B2/en not_active Expired - Fee Related
-
2014
- 2014-03-03 US US13/999,466 patent/US9108160B2/en not_active Expired - Fee Related
- 2014-06-20 US US14/120,724 patent/US20140366730A1/en not_active Abandoned
-
2015
- 2015-01-26 US US14/544,599 patent/US20150225262A1/en not_active Abandoned
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5190667A (en) * | 1991-06-19 | 1993-03-02 | University Of Florida | Separation of gases and solutes by augmented diffusion in counterflow |
US20050023219A1 (en) * | 2003-07-30 | 2005-02-03 | Phase Inc. | Filtration system with enhanced cleaning and dynamic fluid separation |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR101782631B1 (en) | 2017-07-20 | 2017-09-27 | 더죤환경기술(주) | Water Treatment System containing Dissolved AirFloatation System and Membrane |
CN113975860A (en) * | 2021-12-23 | 2022-01-28 | 常州铭赛机器人科技股份有限公司 | Glue vibration defoaming device |
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