WO2013181029A1 - Cross-flow filtration system including particulate settling zone - Google Patents
Cross-flow filtration system including particulate settling zone Download PDFInfo
- Publication number
- WO2013181029A1 WO2013181029A1 PCT/US2013/042130 US2013042130W WO2013181029A1 WO 2013181029 A1 WO2013181029 A1 WO 2013181029A1 US 2013042130 W US2013042130 W US 2013042130W WO 2013181029 A1 WO2013181029 A1 WO 2013181029A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fluid
- cross
- zone
- flow filtration
- flow
- Prior art date
Links
- 238000009295 crossflow filtration Methods 0.000 title claims abstract description 57
- 239000012530 fluid Substances 0.000 claims abstract description 185
- 239000012528 membrane Substances 0.000 claims abstract description 49
- 238000000034 method Methods 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 230000008569 process Effects 0.000 claims abstract description 37
- 238000004891 communication Methods 0.000 claims abstract description 33
- 239000000706 filtrate Substances 0.000 claims abstract description 33
- 230000037361 pathway Effects 0.000 claims abstract description 32
- 230000004888 barrier function Effects 0.000 claims description 31
- 238000004140 cleaning Methods 0.000 claims description 23
- 230000002093 peripheral effect Effects 0.000 claims description 19
- 238000000926 separation method Methods 0.000 abstract description 21
- 239000013618 particulate matter Substances 0.000 abstract description 7
- 239000002245 particle Substances 0.000 description 27
- 238000001914 filtration Methods 0.000 description 11
- 239000000463 material Substances 0.000 description 11
- 239000007787 solid Substances 0.000 description 11
- 239000000203 mixture Substances 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 230000004907 flux Effects 0.000 description 5
- 238000011144 upstream manufacturing Methods 0.000 description 5
- 230000000712 assembly Effects 0.000 description 3
- 238000000429 assembly Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000012798 spherical particle Substances 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000001133 acceleration Effects 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000011086 high cleaning Methods 0.000 description 1
- 230000003116 impacting effect Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000007560 sedimentation technique Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000011885 synergistic combination Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/88—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices
- B01D29/90—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for feeding
- B01D29/908—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for feeding provoking a tangential stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/0006—Settling tanks provided with means for cleaning and maintenance
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/0012—Settling tanks making use of filters, e.g. by floating layers of particulate material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/0018—Separation of suspended solid particles from liquids by sedimentation provided with a pump mounted in or on a settling tank
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/003—Sedimentation tanks provided with a plurality of compartments separated by a partition wall
- B01D21/0036—Horizontal partition walls
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/24—Feed or discharge mechanisms for settling tanks
- B01D21/2488—Feed or discharge mechanisms for settling tanks bringing about a partial recirculation of the liquid, e.g. for introducing chemical aids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/26—Separation of sediment aided by centrifugal force or centripetal force
- B01D21/267—Separation of sediment aided by centrifugal force or centripetal force by using a cyclone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/30—Control equipment
- B01D21/34—Controlling the feed distribution; Controlling the liquid level ; Control of process parameters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/11—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements
- B01D29/31—Self-supporting filtering elements
- B01D29/33—Self-supporting filtering elements arranged for inward flow filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/62—Regenerating the filter material in the filter
- B01D29/64—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element
- B01D29/6407—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element brushes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/62—Regenerating the filter material in the filter
- B01D29/64—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element
- B01D29/6407—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element brushes
- B01D29/6415—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element brushes with a rotary movement with respect to the filtering element
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/62—Regenerating the filter material in the filter
- B01D29/64—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element
- B01D29/6469—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element scrapers
- B01D29/6476—Regenerating the filter material in the filter by scrapers, brushes, nozzles, or the like, acting on the cake side of the filtering element scrapers with a rotary movement with respect to the filtering element
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/02—Construction of inlets by which the vortex flow is generated, e.g. tangential admission, the fluid flow being forced to follow a downward path by spirally wound bulkheads, or with slightly downwardly-directed tangential admission
- B04C5/04—Tangential inlets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/08—Vortex chamber constructions
- B04C5/081—Shapes or dimensions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/08—Vortex chamber constructions
- B04C5/103—Bodies or members, e.g. bulkheads, guides, in the vortex chamber
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/14—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/22—Apparatus in which the axial direction of the vortex is reversed with cleaning means
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/0039—Settling tanks provided with contact surfaces, e.g. baffles, particles
- B01D21/0042—Baffles or guide plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
- B04C2009/004—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks with internal filters, in the cyclone chamber or in the vortex finder
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Geometry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Filtration Of Liquid (AREA)
- Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
Abstract
Cross-flow filtration systems and corresponding methods for separation particulate matter from liquids. A representative system includes a cross-flow filtration zone (24) in fluid communication with a particulate settling zone (30) and further includes a fluid inlet (14) in fluid communication with one of the zones and a process fluid outlet (20) and in fluid communication with the other zone. A fluid treatment pathway (28) extends from the fluid inlet (14), through the cross-flow filtration and particulate settling zones (24, 30) to the process fluid outlet (20). A filter assembly (26) is located within the cross-flow filtration zone (24) and comprises a membrane surface (44) that isolates a filtrate chamber (46) from the fluid treatment pathway (28), and the filtrate chamber (46) is in fluid communication with a filtered fluid outlet (16). A recirculation pump (Z) in fluid communication with the process fluid outlet (20) and fluid inlet (14). A pressurizable recirculation loop (A) comprises the fluid treatment pathway (28) and recirculation pump (Z) and the recirculation pump (Z) is adapted for driving pressurized through the recirculation loop (A). A feed pump (Y) is adapted to introduce feed liquid into the system (10); and an effluent outlet (18) in fluid communication with the particulate settling zone (30). The feed pump (Y), effluent outlet (18) and filtered fluid outlet (16) reside outside of the recirculation loop (A).
Description
CROSS-FLOW FILTRATION SYSTEM INCLUDING
PARTICULATE SETTLING ZONE
TECHNICAL FIELD
The invention is generally directed to cross-flow filtration assemblies for separating particulate matter from liquids.
BACKGROUND
Various techniques have been utilized to separate suspended particles from liquids including coagulation, flocculation, sedimentation, filtration and cyclonic separation. For example, in a typical hydroclone embodiment, pressurized feed liquid is introduced into a conically shaped chamber under conditions that create a vortex within the chamber. Feed liquid is introduced near the top of a conical chamber and an effluent stream is discharged near the bottom. Centrifugal forces associated with the vortex urge denser particles towards the periphery of the chamber. As a result, liquid located near the center of the vortex has a lower concentration of particles than that at the periphery. This "cleaner" liquid can then be withdrawn from a central region of the hydroclone. Examples of hydroclones are described in: US3061098, US3529544, US 4414112, US5104520, US5407584 and US5478484. Separation efficiency can be improved by including a filter within the chamber such that a portion of the liquid moving to the center of the chamber passes through the filter. In such embodiments, cyclonic separation is combined with cross-flow filtration. Examples of such embodiments are described in: US7632416, US7896169, US2011/0120959 and US2012/0010063.
Size and separation efficiency are limiting factors for any given separation system. For example, while flocculation and sedimentation techniques are relatively energy efficient, they typically require settling ponds and long separation times. Hydroclones offer a smaller footprint, but have higher energy demand and are less effective at removing small particulate matter. Cross-flow filtration systems are small and produce high quality separations but are prone to fouling and are energy intensive. New systems are sought which offer an improved balance of attributes including overall size and separation efficiency. SUMMARY
The invention includes a cross-flow filtration system and corresponding methods for separating particulate matter from liquids. A representative system includes a cross-flow filtration zone in fluid communication with a particulate settling zone. The system further includes: a fluid inlet (14) in fluid communication with one of the zones and a process fluid outlet (20) in fluid communication with the other zone. A fluid treatment pathway (28) extends from the fluid inlet (14), through the cross-flow filtration and particulate settling zones (24, 30) to the process fluid outlet (20).
A filter assembly (26) is located within the cross-flow filtration zone (24) and comprises a membrane surface (44) that isolates a filtrate chamber (46) from the fluid treatment pathway (28), and the filtrate chamber (46) is in fluid communication with a filtered fluid outlet (16). A recirculation pump (Z) is in fluid communication with the process fluid outlet (20) and the fluid inlet (14). A pressurizable recirculation loop (A) comprises the fluid treatment pathway (28) and recirculation pump (Z), and the recirculation pump (Z) is adapted for driving pressurized through the recirculation loop (A). A feed pump (Y) is adapted to introduce feed liquid into the system (10); and an effluent outlet (18) is in fluid communication with the particulate settling zone (30). The feed pump (Y), effluent outlet (18), and filtered fluid outlet (16) reside outside of the recirculation loop (A).
The invention finds particular utility in the treatment of: pulp effluent generating by paper mills, process water generated by oil and gas recovery, and municipal and industrial waste water.
BRIEF DESCRIPTION OF THE DRAWINGS
Various aspects of the invention may be better understood by reference to the following description taken in conjunction with the accompanying drawings wherein like numerals have been used throughout the various views to designate like parts. The depictions are illustrative and are not intended to be to scale or otherwise limit the invention.
Figures 1A-F are schematic views of alternative embodiments of the invention.
Figure 2 is a cross-sectional view showing one embodiment of the invention.
Figure 3A is a partially cut-away perspective view of a representative filter assembly.
Figure 3B is a perspective view of the filter of Figure 3A including a cleaning assembly.
Figure 3C is a perspective view of the assembly of Figure 3B including an inlet flow shield.
Figures 4A and B are cross-sectional views showing additional embodiments of the invention.
Figures 5A and B are cross-sectional views showing yet additional embodiment of the invention
Figures 6A and B are perspective views of embodiments of vortex flow barriers.
Figure 7A, B and C are perspective views of various embodiments of effluent barriers.
Figure 8 is an exploded perspective view of an alternative embodiment of a tank including a vortex and effluent barrier.
DETAILED DESCRIPTION
The present invention includes cross-flow filtration systems for separating particulate matter from liquids and methods for using such systems. The term "system" refers to an interconnected assembly of components. In one embodiment, the invention combines cross-flow filtration and particle settling within a pressurized recirculation loop. Particle settling may include floatation or sedimentation based on particle density differences with water. In a preferred embodiment, the system further incorporates cyclonic separation.
Representative system (10) are schematically illustrated in Figures 1A-F including a pressurizable cross-flow filtration zone (24) in fluid communication with a particulate settling zone (30). As implied by the name, cross-flow filtration occurs in the cross-flow filtration zone (24), e.g. by way of passing feed fluid across a membrane surface. Similarly, particle settling occurs in the particulate settling zone (30). The zones (24, 30) are sequentially aligned along a fluid treatment pathway. In preferred embodiments, the particulate settling zone (30) is located downstream from the cross-flow filtration zone (24), as shown in Figures 1 A, C and F, (where "downstream" is defined by a zone operating at relatively lower pressure than the other). Alternatively, the cross-flow filtration zone (24) may be located downstream from the particulate settling zone (30) as shown in Figures IB, D and E. While shown as including two zones, additional separation zones may be included. The zones (24, 30) may reside in separate pressurizable modules or vessels, or be housed within a common pressurizable tank. In one embodiment described in connection with Figure 2, both zones (24, 30) reside within a common tank (12).
The system (10) further includes: a fluid inlet (14) in fluid communication with one of the zones (e.g. cross-flow filtration zone (24) in Figure 1 A and particulate settling zone (30) in Figure IB), and a process fluid outlet (20) in fluid communication with the other zone. An effluent outlet (18) is also in fluid communication with the particulate settling zone (30). A fluid treatment pathway extends from the fluid inlet (14), through the cross-flow filtration zone (30) and particulate settling zone (30) to the process fluid outlet (20). While not shown, the system (10) may include additional inlets and outlets.
The system includes a recirculation pump (Z) in fluid communication with the process fluid outlet (20) and fluid inlet (14). The recirculation pump (Z) along with the process fluid outlet (20), fluid inlet (14) and fluid treatment pathway (28) collectively define a pressurizable recirculation loop (A).
The system (10) also includes a feed pump (Y) adapted for introducing a pressurized liquid mixture (feed) to be treated into the recirculation loop (A). Figures 1A and IB show introducing a feed liquid mixture into the fluid inlet (14) through an adjacent junction point (15). Figures 1C through IF show alternative designs where the recirculation pump (Z) is located at various positions
within the loop (A) relative to the feed pump (Y), the cross-flow filtration zone (24), and particulate settling zone (30). While not shown, the system (10) may include additional pumps and corresponding valves for facilitating movement of liquids and solids. While in fluid communication with the recirculation loop (A), the feed pump (Y), effluent outlet (18) and filtered fluid outlet (16) reside outside of the recirculation loop (A) and only serve as one-way inlets and outlet with the loop (A). In a preferred embodiment, the recirculation pump (Z) is adapted to drive at least twice the volume of liquid through the recirculation loop (A) as introduced by the feed pump (Y). In another embodiment, the feed pump (Y) is adapted to provide a greater pressure increase than provided by the recirculation pump (Z).
The particulate settling zone (30) is adapted to facilitate the separation of solids from liquid as a feed mixture flows through the zone. In a preferred embodiment, solids are separated from liquid by gravitational and frictional drag forces occurring as fluid flows through the zone (30). Large and dense particulate matter settles out of the fluid flow and may exit the particulate settling zone (30) by way of the effluent outlet (18) while the remaining liquid mixture either exits as process fluid by way of the process fluid outlet (20) as illustrated in Figure 1 A, or flows downstream to the cross-flow filtration zone (24) as illustrated in Figure IB. In an alternative embodiment, less dense particulates may accumulate for removal in a raised region of the particulate settling zone (30), and both sedimentation and floatation separation methods may be used together.
As will be described with reference to Figures 2-5, a filter assembly is located within the cross-flow filtration zone (24) and includes a membrane surface adjacent the fluid treatment pathway that isolates the fluid treatment pathway from a filtrate chamber. The filtrate chamber is in fluid communication with a filtered fluid outlet (16). In operation, feed liquid enters the cross-flow filtration zone (24) and flows across (i.e. "cross-flow") the membrane surface. A portion of feed passes through the membrane and enters the filtrate chamber as "filtrate," which may then exit the system (10) by way of the filtered fluid outlet (16).
Figure 2 illustrates an embodiment of the invention wherein the cross-flow filtration zone (24) and particulate settling zone (30) are both housed within a common tank (12), and the membrane surface encloses the filtrate chamber. While not required, the illustrated tank (12) is adapted to operate as a hydroclone. For purposes of the present description, the term "hydroclone" refers to a filtration device that at least partially relies upon centrifugal forces generated by vortex fluid flow to separate constituents from a fluid mixture. As illustrated, the system (10) includes a tank (12) having a removable lid (13), a fluid inlet (14), a filtered fluid outlet (16), an effluent outlet (18), a process fluid outlet (20) and an inner peripheral wall (22) enclosing a chamber centered about an axis (X). While depicted as including a single chamber, additional chambers may also be included as described in connection with Figures 4-5. Similarly, additional fluid inlets and outlets may also be
included. While shown as having a cylindrical upper section and a frustro-conical base, the tank (12) may have other configurations including a cylindrical shape.
A filter assembly (26) is preferably centrally located within the chamber and is evenly spaced from the inner peripheral wall (22) of the tank (12). As best shown in Figure 3A, the assembly (26) may include a cylindrical outer membrane surface (44) symmetrically located about the axis (X) and enclosing a filtrate chamber (46) that is in fluid communication with the filtered fluid outlet (16). While shown as being shaped as a simple cylinder, other configurations may be used including stepped and conical shaped filters. The membrane surface (44) may be fabricated from a wide variety of materials including porous polymers, ceramics and metals. In one embodiment, the membrane is relatively thin, e.g. from 0.2 - 0.4 mm and is supported by an underlying rigid frame or porous support (not shown). A representative example is described in US2012/0010063. The pore size (e.g. 1 to 500 micron), shape (e.g. V-shape, cylindrical, slotted) and uniformity of the membrane surface (44) may vary depending upon application. In many preferred embodiments, the membrane surface (44) comprises a corrosion-resistant metal (e.g. electroformed nickel screen) including uniform sized pores having sizes from 5 to 200 microns, or even 10 to 100 microns. Representative examples of such materials are described: US7632416, US7896169, US2011/0120959, US 2011/0220586 and
US2012/0010063, the entire subject matter of which is incorporated herein by reference. For purposes of this description, the pore size is defined by the minimum distance across the pore, so that it restricts passage of materials larger than this dimension.
Returning to Figure 2, a fluid treatment pathway (28) extends from the fluid inlet (14) and defines a vortex region (25) between the inner peripheral wall (22) of the chamber and the membrane surface (44). In operation, pressurized feed fluid (e.g. preferably from 4 to 120 psi) enters the tank (12) via the fluid inlet (14) and follows along the fluid treatment pathway (28) which generates a vortex about the filter assembly (26). Centrifugal forces urge denser materials toward the inner peripheral wall (22) of the tank (12) while less dense liquid flows radially inward toward the filter assembly (26). A portion of this liquid flows through the membrane surface (44) into a filtrate chamber (46) and may subsequently exit the tank (12) as "filtrate" by way of the filtered fluid outlet (16). The remaining "non-filtrate" flows downward from the cross-flow filtration zone (24) to the particulate settling zone (30). Fluid flow slows and denser materials (e.g. particles) preferentially settle toward the lower center of the tank (12) and may then exit the tank by way of effluent outlet (18). The remaining liquid (hereinafter referred to as "process fluid") flows downward and may exit the tank (12) via process fluid outlet (20). As illustrated by the dashed circle (A) representing a recirculation loop, process fluid may be recycled back to the fluid inlet (14) for further treatment.
The system (10) may further include a cleaning assembly (50) for removing debris from the membrane surface (44) of the filter assembly (26). A representative embodiment is illustrated in
Figure 3B wherein the assembly (50) is concentrically located and rotatably engaged about the membrane surface (44) and includes one or more spokes (52) extending radially outward. A brush (54) extends downward from the end of the spoke (52) and engages (e.g. touches or comes very near to) the membrane surface (44). While shown as a brush (54), alternative cleaning means may be included including wipers, squeegees or scrappers. From 2 to 50 brushes, and preferably from 18 to 24 brushes are used in most embodiments. As represented by curved arrows, the cleaning assembly (50) rotates about filter assembly (26) such that the brush (54) sweeps the surface of the membrane substrate (54) and removes debris, e.g. by creating turbulence near the surface or by directly contacting the surface. One or more paddles (56) may be mounted at the end of at least one spoke (52) such that fluid flowing into the cross-flow filtration chamber (24) rotates the cleaning assembly (50) about the filter assembly (26). Spacing paddles (56) evenly about the filter assembly adds stability to the rotating movement of the cleaning assembly (50) and may help maintain vortex fluid flow in the cross-flow filtration chamber (24). While shown as extending radially outward from the membrane surface (44), the paddles may be slanted, (e.g. from -5° to -30° or 5° to 30° from the radial axis) to increase rotational velocity. Bearings may be used between the filter and cleaning assemblies (26, 50) to further facilitate rotation without impeding vortex fluid flow. In alternative embodiments not shown, the cleaning assembly (50) may be driven by alternative means, e.g. electronic motor, magnetic force, etc. In yet another embodiment, the filter assembly may move relative to a fixed cleaning assembly. In another yet embodiment not shown, the cleaning assembly may be concentrically located within and rotationally engaged with a surrounding membrane surface (44). In this case, the membrane surface (44) may also surround the fluid treatment pathway (28) and itself be located within the filtrate chamber (46).
The feed fluid inlet pressure and spacing between the outer periphery of the filter assembly (26) and the inner peripheral wall (22) of the tank (12) can be adapted to create and maintain a vortex fluid flow within the chamber (24). In order to further facilitate the creation and maintenance of vortex fluid flow, the fluid inlet (14) preferably directs incoming feed fluid on a tangential path about the vortex chamber, as indicated in Figure 2. Even following such a tangential path, pressurized feed fluid may directly impinge upon the membrane surface (44) of the filtration assembly (26) and lead to premature wear or fouling - particularly in connection with feed fluids having high solids content. To protect the membrane surface (44), an inlet flow shield (58) may be located between the fluid inlet (14) and the membrane surface (44), e.g. concentrically located about the filter assembly (26). A representative example is illustrated in Figure 3C. As shown, the shield (58) preferably comprises a non-porous cylindrical band of material, e.g. plastic, which blocks at least a portion of fluid flowing into the chamber (24) from the fluid inlet (14) from directly impinging upon (impacting) the membrane surface (44). The band may be formed from a continuous loop of material or by way of
independent arcs. In a preferred embodiment, the shield (58) has a height approximating the height of the membrane surface (44) such that the shield (58) and membrane surface (44) forms concentric cylinders. In a preferred embodiment, the shield may be removably mounted to the cleaning assembly (50). By way of a non-limiting example, the paddles (56) of the cleaning assembly (50) may include vertical slots (60) for receiving the shield (58).
As illustrated in Figures 4A,4B and 5 A, the system (10) may also include an optional conduit (31) including a process fluid inlet (33) located near the axis (X) (e.g. centrally located) within the particulate settling chamber (30) which is in fluid communication with the process fluid outlet (20). The process fluid inlet (33) may include a region wider than the conduit (31) at its inlet to facilitate particle collection and this wider region may be sloped. The hydroclone (10) may further include an optional baffle (35) located about (e.g. concentrically) the inlet (33). The baffle (35) limits the amount of solids entering the inlet (33) by blocking a direct pathway. By blocking a direct or near linear fluid pathway from the vortex chamber (24), solids tend to settle out of the more dynamic fluid flow entering the inlet (33). In the embodiment of Fig 4A, the axis (X) is vertically aligned and the fluid inlet (33) faces vertically upward near the center of the particulate settling chamber (30). In this configuration, the fluid treatment pathway (28) follows a serpentine path from the cross-flow filtration chamber (24) to the fluid outlet (20). Importantly, the path reverses course, initially flowing generally downward and then upward, and finally downward within the conduit (31). Particles within the bulk flowing along this pathway tend to be drawn downward to the effluent outlet (18) and are unable to reverse flow direction due to gravitational forces. Figure 4B illustrates an alternative arrangement wherein the inlet (33) faces downward and a baffle is located concentric about the inlet (33) extending upward. The use of an optional baffle (35) enhances the separation. While the baffle (35) is shown as having a cylindrical or conical structure, other structures which block a direct pathway may also be used.
Both Figures 4A and 4B illustrate that more than one effluent opening (38, 38') and corresponding effluent outlets (18, 18') may be present for collection and concentration of substantially different particulate matter. In these figures, the openings (38, 38') are oppositely oriented. The position and orientation of openings (38, 38') within the particulate settling chamber (30) may be selected to separate solids differing in average density (e.g. by at least 0.05 g/cc or even 0.1 g/cc) or particulates differing in average size (by at least 50% in diameter). Material from either or both of different effluent outlets (18, 18') may be subject to additional differing post-treatment steps.
In Figure 4B the settling zone (30) is located above the cross flow filtration zone (24) within a common tank (12). In this embodiment, the lower effluent opening (38) protrudes within the filtrate
chamber (46) and both the effluent opening and filtrate chamber are surrounded by the cylindrical membrane surface (44).
In Figures 4 A and 4B, the length of the membrane cylinder exceeds it diameter and twice its diameter, respectively. This aspect ratio has implications for both cross flow and the vortex, as it is difficult to maintain the same rotational flow over a longer cylinder length. To support operation with high cross flow in this geometry, several options may be used. The fluid inlet (14) may be configured to provide feed liquid down the length of the membrane cylinder at a variable rate. More brushes may be present on the downstream section of a rotating cleaning assembly (50), to help maintain rotational flow. Brushes may be angled to increase cross flow velocity parallel to the axis (X). The inner periphery of the filtration chamber (24) may be angled or incorporate volume-filling inserts (43), as illustrated in Figure 4B, to increase velocity with reduced fluid flow in the downstream section. Due to pressure drop along the fluid treatment pathway (28), the long aspect ratio of the membrane cylinder also has negative implications for flux. To counter unevenness in filtrate flux between the upstream and downstream sections of the membrane surface (44), the filtrate chamber may be divided into isolated sections having separate filtered fluid outlets (16) or having flow resistances therebetween, wherein the pressure of an upstream filtrate section exceeds that of a downstream filtrate section by at least 1 psi and/or the flow resistance between an upstream filtrate section and a downstream filtrate section exceeds at least 50% of the flow resistance across the membrane (e.g. from the fluid pathway 28 to filtrate chamber (46)). Also to reduce flux differences between upstream and downstream membrane sections of the cylinder, the properties of the membrane surface may be different in these regions, preferably using a membrane surface (44) with smaller pores on the upstream section.
Figure 5A illustrates an embodiment similar to that shown in Figure 2 but additionally includes a vortex flow barrier (34) located between the cross-flow filtration and particulate settling zones (24, 30). The barrier (34) effectively creates "chambers" out of the zones (24, 30). The flow barrier (34) limits fluid flow between the chambers (24, 30) by directing a majority of fluid flow between the cross-flow filtration chamber (24) and particulate settling chamber (30) to locations adjacent to the inner peripheral wall (22) of the tank (12). The vortex flow barrier (34) is preferably designed to maintain vortex fluid flow in the cross-flow filtration chamber (24) while allowing a reduced fluid velocity within the particulate settling chamber (30). Preferably, the vortex flow barrier (34) at least partially disrupts vortex fluid flow (28) as fluid flows from the cross-flow filtration chamber (24) into the particulate settling chamber (30). In a preferred embodiment, the vortex flow barrier (34) includes an outer periphery (40) extending to locations adjacent to (e.g. within 50 mm, 25 mm or even 10 mm) or in contact with the inner peripheral wall (22) of the tank (12) and may optionally include a plurality of apertures (42) located near the periphery (40) and extending
therethrough. The size and shape of apertures (42) is not particularly limited, e.g. scalloped-shaped, slots, elliptical, etc. A few representative examples are illustrated in Figures 6A-B. In yet other non- illustrated embodiment, the vortex flow barrier (34) may include an outer periphery that includes no apertures and extends to locations adjacent to (e.g. within 50 mm, 25 mm or even 10 mm) the inner peripheral wall (22) of the tank (12). The vortex flow barrier (34) is designed to control the flow of fluid through the chambers of the tank (12) with a majority (e.g. preferably at least 50%, 75%, and in some embodiments at least 90%) of volumetric flow being preferentially directed to locations near (e.g. within at least 50 mm, 25 mm or even 10 mm) the inner peripheral wall (22) of the tank (12). With that said, a minority (e.g. less than 50% and more preferably less than 75% and still more preferably less than 90%) of the fluid flow may occur at alternative locations including the center location. While the illustrated embodiments have a plate or disc configuration, the vortex flow barrier may assume other configurations including one having an angled or curved surface, e.g. cone- or bowl-shaped.
Figure 5B illustrates an embodiment similar to that shown in Figure 5A but additionally includes an effluent barrier (36) (best shown in Figure 7) located below the particulate settling chamber (30) that is adapted to direct fluid flow from the particulate settling chamber (30) to the process fluid outlet (20). The effluent barrier (36) includes an outer periphery (40') extending to locations adjacent to or in contact with the inner peripheral wall (22) of the tank (12) and may further include a plurality of apertures (42') located near the periphery (40') and extending therethrough. In a preferred embodiment, the apertures (42) of the vortex flow barrier (34) are vertically off-set from the apertures (42') of the effluent barrier (36). The effluent barrier (36) also includes a centrally located effluent opening (38) in fluid communication with the effluent outlet (18) by which effluent may exit the tank (12).
While in one embodiment the effluent barrier (36) includes scalloped-shaped apertures (42'), (see Figure 8), alternatively shaped apertures including radial slots, angled slots and triangular openings located about the outer periphery (40') (see Figure 7). Similarly, alternatively shaped apertures (42) may be used with respect to the vortex flow barrier (34). The shape and size of the aperture (42, 42') may be designed to control the flow of fluid downward through the chambers (24, 30, 32) of the tank (12), with flow being preferentially directed to the inner peripheral wall (22) of the tank (12). With that said, a minority (e.g. less than 50% and more preferably less than 75% and still more preferably less than 90%) of the downward flow (i.e. non-effluent fluid with respect to the effluent barrier (36)) may occur at alternative locations including the center location of one or both barriers (42, 36). In yet other non-illustrated embodiment, one or both of the vortex flow barrier (34) and effluent barrier (36) may include outer peripheries that do not contact the inner peripheral wall (22) of the tank (12) and include no apertures. Experiments and simulations have shown that
offsetting apertures (42) between the vortex flow barrier (34) and effluent barrier (36) can create regions (41) that transition to an average positive upward component of velocity for fluids in the bulk, and this offsetting of apertures increases separation efficiency.
The embodiments illustrated in Figures 4 and 5 each include a filter assembly (26) centrally located within the cross-flow filtration chamber (24) and enclosing a filtrate chamber (46). The filtrate chamber (46) is in fluid communication with the filtered fluid outlet (16). The particulate settling chamber (30) is located below (except in Fig 4B) and is in fluid communication with the cross-flow filtration chamber (24). The particulate settling chamber (30) is adapted for receiving unfiltered fluid from the cross-flow filtration chamber (24). In the embodiment of Figure 5B, a process fluid chamber (32) is in turn located below and is in fluid communication with the particulate settling chamber (30). The process fluid chamber (32) is adapted for receiving a process fluid from the particulate settling chamber (30) and is in fluid communication with the process fluid outlet (20) by which process fluid may exit the tank (12).
In operation, pressurized feed fluid (e.g. preferably from 4 to 120 psi) enters the tank (12) via the fluid inlet (14) and follows along the fluid treatment pathway (28) which generates a vortex about the filter assembly (26). Centrifugal forces urge denser materials toward the inner peripheral wall (22) of the tank (12) while less dense liquid flows radially inward toward the filter assembly (26). A portion of this liquid flows through the filter assembly (26) into a filtrate chamber (46) and may subsequently exit the tank (12) as "filtrate" by way of the filtered fluid outlet (16). The remaining "non-filtrate" flows downward from the cross-flow filtration chamber (24) to the particulate settling chamber (30).
In some embodiments, a vortex flow barrier (34) is present and directs the majority (e.g. preferably at least 75% and in some embodiments at least 90%) of such downward flow to locations along or adjacent to an inner peripheral wall (22) of the tank (12). This arrangement is believed to help maintain vortex flow within the cross-flow filtration chamber (24) while disrupting the vortex flow as fluid enters the particulate settling chamber (30). Fluid flow slows in the particulate settling chamber (30) and denser materials (e.g. particles) preferentially settle toward the center of the effluent barrier (34) and enter into the effluent opening (38) and may then exit the tank by way of the effluent outlet (18). In the embodiment of Figure 5B, the remaining liquid (hereinafter referred to as "process fluid") in the particulate settling chamber (30) flows downward into the process fluid chamber (32). The effluent barrier (36) directs a majority (e.g. preferably at least 75% and in some embodiments at least 90%) of fluid flow between the particulate settling and process fluid chambers (30, 32) to locations along or adjacent to an inner peripheral wall (22) of the tank (12), i.e. through apertures (42').
In a preferred embodiment, the fluid treatment pathway (28) in the particulate settling
chamber (30) includes a region (41) passed through by most particles, where bulk fluid initially moving towards the effluent outlet (18) is caused to decelerate and move away from the effluent outlet (18). For instance, transition to an upward component of bulk flow can promote separation and settling of particles under gravity. In Figures 4A, 4B, and 5 A, upward or downward acceleration may be created at such regions (41).
The system (10) may also include a valve (37) for selectively removing effluent from the particulate settling chamber (30). Preferably, a valve (37) is suitable to alternate between a closed position that restricts flow from the effluent outlet (18) and creates a quiescent region within the particulate settling chamber (30) and an open position that purges effluent from the quiescent region through the effluent outlet (18). The quiescent region is preferably located adjacent to the effluent outlet (18) and has an average flow velocity less than 1% of the bulk flow velocity at the process fluid inlet (33) of the particle settling chamber (30). Preferably, the quiescent region encompasses a cubic region of at least 2x2x2 cm3, to limit particles leaving. It is also preferably that the quiescent region encompasses at least 25% of the particulate settling zone volume.
The valve (37) is preferably automated to open based on a measurement (e.g. measured concentrations in the particulate settling zone (30) or recirculation loop (A)), or based upon a periodical timing. The valve (37) is preferably in the closed position most of the time, and this may be more than 90% or 95% or even 99% of the time. Time intervals during which the valve is closed preferably exceed 1 min, 5 min, or even 15 min. Longer times between openings allow for higher accumulation of solids within the quiescent zone. The solids level discharged from the particulate settling zone through the effluent outlet may exceed 10%, 25%, or even 50% by weight. This may be at least 100 times the concentration of the liquid supplied by the feed pump (Y).
The valve (37) preferably opens after time intervals shorter than the average residence time for a 200 micron sphere (density 1.09 g/cc) in the quiescent zone. The system is preferably operated such that the average residence time for a 200 micron spherical particle (density 1.09 g/cc) in the quiescent region adjacent the effluent outlet (18) exceeds 1 minute, or even 5 minutes, when the valve is closed. Preferably, a 200 micron sphere has at least two times, or even five times, the probability of being capture in the quiescent zone for more than 5 minutes during a pass through the settling chamber (30), as compared to similar sphere (1.09 g/cc) having diameter equal to the average membrane pore size. For purposes of these measurements, spherical particles having a wide range of sizes and densities may be available from Cosphereic (Santa Barbara, CA).
Use of a cleaning assembly (50) that continuously engages with the membrane surface (44) is particularly advantaged in combination when the filter assembly (26) and particulate settling chamber (30) are in series within a recirculation loop. Experiments have demonstrated that removal of particles in the particulate settling zone (30) was strongly dependent on particle size. Removal
efficiency can low be for particles of 50 microns. During filtration, particles may be agglomerated and/or compacted and then removed by the cleaning assembly, increasing their removal rate in the particulate settling chamber (30). By providing a rotating cleaning assembly (50) that continuously dislodges particles, the size of particles may be sufficiently increased while still maintaining a high flux rate. This is particularly important for high recovery operations, such as those involving liquid mixtures with solids greater than 0.2, 0.5, or 1% by mass.
Due to the continuous cleaning, high recirculation, removal and concentration of particles by the particulate settling zone, and relatively low recoveries in both the filtration and particulate settling zones, the system can operate well with high solids. In operation, the system is preferably operated with an average volumetric recovery of at least 85%, 90%, 95%, or even 99% (i.e. the fraction of liquid that leaves the system through the membrane as filtrate).
When a system includes both a filtration zone and a particulate settling zone in series, the use of both a feed pump (Y) and recirculation pump (Z) is also advantaged. As each pass through the settling chamber has relatively low recovery of particles, several passes through the two zones are needed on average to remove each particle. Within the filtration zone, an applied pressure at the filtration zone inlet must exceed the transmembrane pressure, and uniform flux along the fluid treatment path is more readily attained when systems are designed for a higher transmembrane pressure. Since pressure drops associated with each operating zone and pass are cumulative, a system designed around a single pump can have substantial efficiency losses through re-pressurization of each pass. By contrast, if a feed pump (Y) is used to provide a pressurized liquid to a pressurized recirculation loop driven by a second pump (Z), the energy losses on successive passes associated with re -pressurizing to a transmembrane pressure and any filtrate back-pressure are avoided. The recirculation pump needs only to supply energy to drive fluid through the recirculation loop, and, in some embodiments, create relative motion between the membrane surface (44) and cleaning assembly (50). Using separate pumps to provide pressure and volume requirements is particularly advantaged when the recirculation pump (Z) drives a volume of liquid through the recirculation loop that is at least twice, more preferably at three times, the volume of feed liquid introduced by the feed pump (Y) to the recirculation loop. Because of the further synergies provided by multiple passes through the continuous cleaning assembly and a particulate settling zone, the dual pump arrangement is additionally advantaged.
In another embodiment, the system may include a plurality of particulate settling zones (30) and/or filtration zones (24) ganged together in parallel to a common recirculation pump (Z). The recirculation pump (Z) may simultaneously drive flow through two or more parallel filter assemblies (26) within the recirculation loop. Similarly, the recirculation pump may drive flow through two or more settling chambers (30) within the recirculation loop (A). Preferably, the recirculation pump (Z)
drives flow through parallel tanks (12) comprising both a filter assembly (26) and a settling chamber (30). The pressurized recirculation loop (A) may be fed by a common feed pump (Y).
The invention is particularly advantaged because particles may be removed through a plurality of passes through the system. The filtration zone is preferably operated with recoveries less than 50%, 25%, or even 10%, allowing both a high cross flow velocity and high cleaning rates.
(Although cleaning is continuously performed, short times exist between discrete engagements of the rotatable cleaning assembly with any given location on the membrane.) Particles within a given pass through the settling chamber also have a relatively low probability of removal. For example, the probability that a 200 micron plastic sphere (density 1.09) may be removed in a given pass may be less than 30%, or even less than 10%.
As previously described, pressure losses from successive passes are minimized by use of the recirculation pump. The is particularly important, because the pressure drop across the membrane (from fluid treatment pathway to the filtrate region) can then be a small fraction of the pressure provided by the feed pump, less than 50%, 25%, or even 10%. In a preferred embodiment, at least 50%, more preferably 80%, of the pressure provided by the feed pump is used to drive a downstream operation (e.g. microfiltration, ultrafiltration, nanofiltration, or reverse osmosis). The pressure drop between locations on the fluid treatment pathway (28) at opposite ends cross-flow filtration zone (24)is also preferably small, e.g. less than 20%, 10%, or 1% of pressure supplied by the feed pump
00·
The subject separations systems provide superior separation efficiencies as compared with previous designs. These efficiencies allow the systems to be used in a broader range of applications; particularly in embodiments where process fluid is recycled and optionally blended with make-up feed fluid. In certain preferred embodiments, feed fluid is subjected to a synergistic combination of multiple separation processes within a single device. Specifically, feed fluid is subject to cyclonic separation based at least partially upon density with denser material (e.g. particles, liquids) being urged toward the inner periphery of the tank. Fluid passing through the filter assembly is additionally subjected to cross-flow filtration. The subject inlet feed shield prevents the membrane used in cross- flow filtration from being subject to excessive wear or fouling attributed to the feed pressures and feed content associated with cyclonic separations. The entire subject matter of each of the US patents mentioned herein references are fully incorporated by reference.
Claims
1. A cross-flow filtration system (10) comprising:
a cross-flow filtration zone (24) in fluid communication with a particulate settling zone (30); a fluid inlet (14) in fluid communication with one of said zones and a process fluid outlet (20) and in fluid communication with the other zone;
a fluid treatment pathway (28) extending from the fluid inlet (14), through the cross-flow filtration and particulate settling zones (24, 30) and to the process fluid outlet (20);
a filter assembly (26) located within the cross-flow filtration zone (24) and comprising a membrane surface (44) that isolates a filtrate chamber (46) from the fluid treatment pathway (28), wherein the filtrate chamber (46) is in fluid communication with a filtered fluid outlet (16);
a cleaning assembly (50) movably engaged with the membrane surface (44);
a recirculation pump (Z) in fluid communication with the process fluid outlet (20) and fluid inlet (14);
a pressurizable recirculation loop (A) comprising the fluid treatment pathway (28) and recirculation pump (Z), wherein the recirculation pump (Z) is adapted for driving pressurized through the recirculation loop (A);
a feed pump (Y) adapted to introduce feed liquid into the system (10); and
an effluent outlet (18) in fluid communication with the particulate settling zone (30);
wherein the feed pump (Y), effluent outlet (18) and filtered fluid outlet (16) reside outside of the recirculation loop (A).
2. The system (10) of claim 1 wherein the recirculation pump (Z) is adapted to drive at least twice the volume of liquid through the recirculation loop (A) as introduced by the feed pump (Y) and wherein the feed pump (Y) is adapted to provide a greater pressure increase than provided by the recirculation pump (Z).
3. The system (10) of claim 1 further comprising a valve (37) movable between a closed position that restricts flow of effluent from the particulate settling zone (30) and an open position that permits effluent to exit the system (10) by way of the effluent outlet (18) particulate settling zone (30).
4. The system (10) of claim 1 wherein cross-flow filtration zone (24) and particulate settling zone (30) are serially arranged along the fluid treatment pathway (28) with the particulate settling zone (30) being located downstream from the cross-flow filtration zone (24).
5. The system (10) of claim 4 further comprising a tank (12) including an inner peripheral wall (22) surrounding the cross-flow filtration and particulate settling zones (24, 30), wherein:
the cross-flow filtration and particulate settling zones (24, 30) are sequentially aligned along an axis (X);
the membrane surface (44) is symmetrically located about the axis (X);
the cleaning assembly (50) is concentrically located about and rotatably engaged with the membrane surface (44); and
the fluid treatment pathway (28) extends from the fluid inlet (14) and between the inner peripheral wall (22) of the cross-flow filtration zone (24) and the membrane surface (44) and further extends into the particulate settling zone (30) to exit the tank (12) through the process fluid outlet (20); and
an effluent pathway (29) extends from the particulate settling zone (30) and exits the tank (12) through the effluent outlet (18).
6. The system (10) of claim 5 wherein the fluid treatment pathway (28) includes a vortex region (25) located between the inner peripheral wall (22) of the tank (12) and the membrane surface (44) that is adapted for receiving incoming liquid and generating a vortex fluid flow about the filter assembly (26).
7. The system (10) of claim 6 further comprising a flow barrier (34) located between the cross- flow filtration and particulate settling zones (24, 30) and defining a respective cross-flow filtration chamber (24) and particulate settling chamber (30).
8. The system (10) of claim 7 wherein the flow barrier (34) directs a majority of fluid flow between the cross-flow filtration chamber (24) and particulate settling chamber (30) to locations adjacent to the inner peripheral wall (22) of the tank (12).
9. The system (10) of claim 7 wherein the flow barrier (34) disrupts vortex fluid flow from the cross-flow filtration chamber (24) and the particulate settling chamber (30).
10. The system (10) of claim 5 further comprising comprises a conduit (31) including a process fluid inlet (33) located near the axis (X) of the particulate settling chamber (30) that is fluid communication with the process fluid outlet (18).
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201380028972.5A CN104334246B (en) | 2012-06-01 | 2013-05-22 | Cross-flow filtration system including particle decanting zone |
US14/391,128 US9101859B2 (en) | 2012-06-01 | 2013-05-22 | Cross-flow filtration system including particulate settling zone |
CA2872329A CA2872329A1 (en) | 2012-06-01 | 2013-05-22 | Cross-flow filtration system including particulate settling zone |
EP13727744.8A EP2825276A1 (en) | 2012-06-01 | 2013-05-22 | Cross-flow filtration system including particulate settling zone |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US201261654418P | 2012-06-01 | 2012-06-01 | |
US61/654,418 | 2012-06-01 | ||
US201261655654P | 2012-06-05 | 2012-06-05 | |
US61/655,654 | 2012-06-05 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2013181029A1 true WO2013181029A1 (en) | 2013-12-05 |
Family
ID=48577913
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2013/042130 WO2013181029A1 (en) | 2012-06-01 | 2013-05-22 | Cross-flow filtration system including particulate settling zone |
Country Status (5)
Country | Link |
---|---|
US (1) | US9101859B2 (en) |
EP (1) | EP2825276A1 (en) |
CN (1) | CN104334246B (en) |
CA (1) | CA2872329A1 (en) |
WO (1) | WO2013181029A1 (en) |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014066036A3 (en) * | 2012-10-26 | 2014-10-02 | Dow Global Technologies Llc | Hydroclone |
US8960450B2 (en) | 2010-12-08 | 2015-02-24 | Dow Global Technologies Llc | Apparatus and method for implementing hydroclone based fluid filtration systems with extensible isolated filter stages |
US9050610B2 (en) | 2012-05-17 | 2015-06-09 | Dow Global Technologies Llc | Hydroclone with inlet flow shield |
US9101859B2 (en) | 2012-06-01 | 2015-08-11 | Dow Global Technologies Llc | Cross-flow filtration system including particulate settling zone |
US9186604B1 (en) | 2012-05-31 | 2015-11-17 | Dow Global Technologies Llc | Hydroclone with vortex flow barrier |
WO2016099822A1 (en) | 2014-12-18 | 2016-06-23 | Dow Global Technologies Llc | Cylindrical filter screen with tensioning mechanism |
US9527091B2 (en) | 2013-12-05 | 2016-12-27 | Dow Global Technologies Llc | Hydroclone with improved cleaning assembly |
GB2582042A (en) * | 2019-10-08 | 2020-09-09 | Inheriting Earth Ltd | Microplastic Separator |
GB2588376A (en) * | 2019-10-08 | 2021-04-28 | Inheriting Earth Ltd | Filter pressure consumption regeneration apparatus and method |
GB2600921A (en) * | 2020-11-04 | 2022-05-18 | Xeros Ltd | Filter unit, textile treatment apparatus and method |
GB2619323A (en) * | 2022-05-31 | 2023-12-06 | Xeros Ltd | A microparticle filter, a textile treatment apparatus, use thereof and a method of filtering microparticles |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102012015064B4 (en) * | 2012-07-31 | 2018-08-02 | Joh. Heinr. Bornemann Gmbh | Method for operating a multi-phase pump and device thereto |
GB2534159B (en) * | 2015-01-14 | 2017-08-30 | Clyde Process Ltd | Apparatus for drying conveyed material |
CN106475236A (en) * | 2016-11-29 | 2017-03-08 | 成都聚智工业设计有限公司 | A kind of sewage disposal centrifuge |
EP3658889B1 (en) * | 2017-07-25 | 2022-07-13 | Koninklijke Philips N.V. | Particle sensor and particle sensing method |
CN107376500A (en) * | 2017-08-15 | 2017-11-24 | 四川奥恒环保科技有限公司 | A kind of sewage water filtration sedimenting system |
BR112020021267A2 (en) * | 2018-04-18 | 2021-01-26 | Sudhin Biopharma | particle sedimentation devices |
US10926197B2 (en) * | 2018-06-22 | 2021-02-23 | Hamilton Sunstrand Corporation | Multifunctional phase separation apparatus |
CN110342608B (en) * | 2019-05-27 | 2022-03-08 | 安徽理工大学 | Cyclone grading type composite concentration sedimentation device |
CA3172276A1 (en) | 2020-03-19 | 2021-09-23 | Dhinakar S. Kompala | Particle settling devices |
CN113399131B (en) * | 2021-05-28 | 2022-05-24 | 江西理工大学 | Vortex symmetric feeding hydrocyclone |
CN114166466B (en) * | 2021-12-03 | 2022-11-25 | 上海交通大学 | Particle recovery device, hydraulic lifting test system and particle recovery method |
CN116059732B (en) * | 2023-04-06 | 2023-06-23 | 广东桑醇酒业有限公司 | Step-by-step filtering device based on cross-flow collection and application of step-by-step filtering device in fruit wine brewing |
Citations (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3061098A (en) | 1960-07-18 | 1962-10-30 | Beloit Iron Works | Centrifugal classifier and stock cleaner |
US3529544A (en) | 1966-10-07 | 1970-09-22 | Shigeru Inoue | Method of screen printing a label on a disk record blank |
US4414112A (en) | 1982-01-29 | 1983-11-08 | Recovery Technology Associates | Oil/water separator |
US5104520A (en) | 1990-06-25 | 1992-04-14 | The United States Of America As Represented By The United States Department Of Energy | Apparatus and method for separating constituents |
US5407584A (en) | 1990-09-28 | 1995-04-18 | Broussard, Sr.; Paul C. | Water clarification method |
DE4420760C1 (en) * | 1993-07-01 | 1995-05-11 | Gerd Wurster | Process and plant for reprocessing or concentration of used surfactant-containing iron phosphatising baths |
US5466384A (en) * | 1992-11-05 | 1995-11-14 | Institut Francais Du Petrole | Device and process for carrying out phase separation by filtration and centrifugation |
US5478484A (en) | 1991-07-25 | 1995-12-26 | Serck Baker Limited | Apparatus and method including a hydrocyclone separator in combination with a tubular filter |
US6613231B1 (en) * | 1997-11-26 | 2003-09-02 | Profiltra | Apparatus, system and method for separating liquids |
DE102005027509A1 (en) * | 2005-06-15 | 2006-12-28 | Werner Lauth | Filer to separate solid particles in suspension from fluid has filter elements located at boundary between two vortex systems |
US20070039900A1 (en) * | 2005-08-18 | 2007-02-22 | Clean Filtration Technologies, Inc. | Hydroclone based fluid filtration system |
US20110220586A1 (en) | 2010-03-12 | 2011-09-15 | Levitt David J | Fluid filtration and particle concentration device and methods |
WO2011160087A1 (en) * | 2010-06-17 | 2011-12-22 | Clean Filtration Technologies, Inc. | Cleaning assembly for use in fluid filtration systems |
Family Cites Families (72)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3285422A (en) | 1966-11-15 | Sand trap | ||
US431448A (en) | 1890-07-01 | Filter | ||
US2706045A (en) | 1955-04-12 | Liquid separation | ||
US1107485A (en) | 1909-09-01 | 1914-08-18 | Sf Bowser & Co Inc | Separator. |
US1919653A (en) | 1931-11-27 | 1933-07-25 | Raymond A Hill | Hydraulic sand extractor |
US2788087A (en) | 1955-04-07 | 1957-04-09 | Research Corp | Gas cleaning apparatus |
US2917173A (en) | 1957-08-21 | 1959-12-15 | Rakowsky Victor | Centrifugal method and apparatus for separating solids |
US3219186A (en) | 1962-10-30 | 1965-11-23 | Victor Rakowsky | Whirlpool apparatus |
US3529724A (en) | 1969-09-10 | 1970-09-22 | Univ Oklahoma State | Hydrocyclone filter |
US3822533A (en) | 1972-03-04 | 1974-07-09 | Nederlandse Gasunie Nv | Device for removing impurities from gases |
US3893914A (en) | 1973-04-05 | 1975-07-08 | Roy A Bobo | Cyclone centrifuge apparatus |
US3947364A (en) | 1974-06-13 | 1976-03-30 | Laval Claude C | Apparatus for removing particles from fluid |
CA1038353A (en) | 1976-08-31 | 1978-09-12 | Canarco Inc. | Centrifugal separator |
SE410276B (en) | 1976-10-20 | 1979-10-08 | Sala International Ab | DYNAMIC SUSPENSION ENRICHMENT EQUIPMENT |
US4146468A (en) | 1977-05-24 | 1979-03-27 | Wilson George E | Apparatus and method of classifying solids and liquids |
US4120783A (en) | 1977-07-05 | 1978-10-17 | Baummer George P | Apparatus and process for ordinary and submarine mineral beneficiation |
GB2007118B (en) | 1977-08-02 | 1982-02-24 | British Petroleum Co | Cyclone |
US4219409A (en) | 1977-12-14 | 1980-08-26 | Liller Delbert I | Inlet line deflector and equalizer means for a classifying cyclone used for washing and method of washing using deflectors and equalizers |
US4178258A (en) | 1978-05-18 | 1979-12-11 | Edwin Cooper, Inc. | Lubricating oil composition |
AU536655B2 (en) | 1979-04-11 | 1984-05-17 | British Petroleum Company Limited, The | m |
US4298465A (en) | 1979-06-07 | 1981-11-03 | Racor Industries, Inc. | Fuel filter and water separator apparatus |
GB2158741B (en) | 1984-05-14 | 1988-08-17 | Hydro Int Ltd | Separation of components of a fluid mixture |
US4575406A (en) | 1984-07-23 | 1986-03-11 | Polaroid Corporation | Microporous filter |
DE3437037A1 (en) | 1984-10-09 | 1986-04-10 | Krupp Polysius Ag, 4720 Beckum | CYCLONE ARRANGEMENT |
US4608169A (en) | 1985-07-15 | 1986-08-26 | Arvanitakis Kostas S | Filter brush |
US4651540A (en) | 1986-03-21 | 1987-03-24 | Tecumseh Products Company | Suction accumulator including an entrance baffle |
US4698156A (en) | 1986-04-03 | 1987-10-06 | Microspun Technologies Inc. | Rotating filter apparatus for separating fine particles of solids from a liquid |
FR2623419B1 (en) | 1987-11-25 | 1990-03-23 | Combustion Eng Europ | SELF-CLEANING FILTER APPARATUS |
EP0380817B1 (en) | 1989-02-03 | 1993-01-13 | Gerardus Louis Beusen | A method and a device for treating or mixing components in gas or liquid streams |
US5188238A (en) | 1989-06-21 | 1993-02-23 | Hydro International Limited | Separator for separating solids components of liquid mixtures and method of using the same |
GB2241904B (en) | 1990-03-16 | 1993-12-01 | Hydro Int Ltd | Separator |
NZ239581A (en) | 1990-09-13 | 1993-03-26 | Mitsubishi Heavy Ind Ltd | Gas-liquid separator with tangential inflow nozzle to cylindrical body with central discharge pipe |
US5227061A (en) | 1992-01-13 | 1993-07-13 | Bedsole Robert D | Fuel/contaminant separator |
EP0566792A1 (en) | 1992-04-24 | 1993-10-27 | Hydro International Limited | Separator |
NO176507C (en) | 1992-12-01 | 1995-04-19 | Sinvent Sintef Gruppen | Rotor for classifier |
US5277705A (en) | 1992-12-30 | 1994-01-11 | Iowa State University Research Foundation, Inc. | Powder collection apparatus/method |
US6117340A (en) | 1995-05-01 | 2000-09-12 | Carstens; Christopher | Pool vacuum prefiltering method, utilizing centrifugal force |
GB2309182A (en) | 1996-01-19 | 1997-07-23 | Grant Budge | Dry solids/solids separation process |
US5879545A (en) | 1997-05-05 | 1999-03-09 | Antoun; Gregory S. | Cyclonic filter assembly |
US5972215A (en) | 1997-09-03 | 1999-10-26 | Kammel; Refaat A. | Continuous particle separation and removal cleaning system |
GB9817071D0 (en) | 1997-11-04 | 1998-10-07 | Bhr Group Ltd | Cyclone separator |
US6210457B1 (en) | 1998-04-08 | 2001-04-03 | Lee Valley Tools Ltd. | Transparent lid for auxiliary dust removal receptacle |
US6238579B1 (en) | 1998-05-12 | 2001-05-29 | Mba Polymers, Inc. | Device for separating solid particles in a fluid stream |
US6110242A (en) | 1998-10-13 | 2000-08-29 | Blower Application Company, Inc. | Apparatus for separating solids from a gas |
US6896720B1 (en) | 1999-02-18 | 2005-05-24 | Adrian Christopher Arnold | Cleaning apparatus |
US6251296B1 (en) | 1999-07-27 | 2001-06-26 | G.B.D. Corp. | Apparatus and method for separating particles from a cyclonic fluid flow |
GB0005898D0 (en) | 2000-03-10 | 2000-05-03 | Templeton Stephen J | Method and apparatus for introducing a moving liquid into a larger mass of moving liquid |
AU2001287020A1 (en) | 2000-09-01 | 2002-03-13 | Shell International Research Maatschappij B.V. | Cyclone entrance nozzle |
US6511599B2 (en) | 2000-12-18 | 2003-01-28 | Nelson Industries, Inc. | Multi-element cylindrical filter with equalized flow |
EP1295647A1 (en) | 2001-09-24 | 2003-03-26 | The Technology Partnership Public Limited Company | Nozzles in perforate membranes and their manufacture |
US7166230B2 (en) | 2002-01-09 | 2007-01-23 | Halvor Nilsen | Apparatus and method for separating and filtering particles and organisms from flowing liquids |
US6739456B2 (en) | 2002-06-03 | 2004-05-25 | University Of Florida Research Foundation, Inc. | Apparatus and methods for separating particles |
DE60200483T2 (en) | 2002-07-24 | 2005-05-25 | Cattani S.P.A. | Cyclone separator for variable flow rates |
AU2003900226A0 (en) | 2003-01-21 | 2003-02-06 | Sarah Elizabeth Chenery Lobban | A filter system |
US7025890B2 (en) | 2003-04-24 | 2006-04-11 | Griswold Controls | Dual stage centrifugal liquid-solids separator |
US7727386B2 (en) | 2003-11-21 | 2010-06-01 | Dibella Alberto | Voraxial filtration system with self-cleaning auxiliary filtration apparatus |
US7351269B2 (en) | 2003-12-22 | 2008-04-01 | Lau Kwok Yau | Self cleaning filter and vacuum incorporating same |
WO2006011921A2 (en) | 2004-03-10 | 2006-02-02 | Gordon Construction, Inc. | Method and system for filtering sediment-bearing fluids |
GB2423264A (en) | 2005-02-17 | 2006-08-23 | Lorne Entwistle | A sludge separator |
NL1030081C2 (en) | 2005-09-30 | 2007-04-02 | Stork Veco Bv | Sieve material from metal and method for its manufacture. |
JP4831480B2 (en) * | 2006-06-21 | 2011-12-07 | 三浦工業株式会社 | Membrane filtration system |
JP5340915B2 (en) | 2007-03-22 | 2013-11-13 | 武郎 吉田 | Filter |
US7785479B1 (en) | 2007-05-01 | 2010-08-31 | Michael Hays Hosford | Apparatus and method of separating |
DE102007063243A1 (en) | 2007-12-31 | 2009-07-02 | Mahle International Gmbh | filtering device |
KR101462945B1 (en) | 2008-01-02 | 2014-11-20 | 삼성전자주식회사 | Dust separating apparatus for vaccum clear |
US8048307B2 (en) | 2008-08-14 | 2011-11-01 | Brent Lee | Dynamic filtration device using centrifugal force |
US7998251B2 (en) | 2008-10-03 | 2011-08-16 | B/E Aerospace, Inc. | Vortex waste separator apparatus |
US8389807B2 (en) | 2009-12-30 | 2013-03-05 | Pioneer Hi-Bred International, Inc. | Method for increasing efficiency of germplasm screening in plant transformation |
US8960450B2 (en) | 2010-12-08 | 2015-02-24 | Dow Global Technologies Llc | Apparatus and method for implementing hydroclone based fluid filtration systems with extensible isolated filter stages |
CN103347580B (en) | 2011-05-06 | 2015-05-20 | 陶氏环球技术有限责任公司 | Multi-chambered hydroclone |
WO2013181028A1 (en) | 2012-05-31 | 2013-12-05 | Dow Global Technologies Llc | Hydroclone with vortex flow barrier |
US9101859B2 (en) | 2012-06-01 | 2015-08-11 | Dow Global Technologies Llc | Cross-flow filtration system including particulate settling zone |
-
2013
- 2013-05-22 US US14/391,128 patent/US9101859B2/en active Active
- 2013-05-22 EP EP13727744.8A patent/EP2825276A1/en not_active Withdrawn
- 2013-05-22 WO PCT/US2013/042130 patent/WO2013181029A1/en active Application Filing
- 2013-05-22 CN CN201380028972.5A patent/CN104334246B/en active Active
- 2013-05-22 CA CA2872329A patent/CA2872329A1/en not_active Abandoned
Patent Citations (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3061098A (en) | 1960-07-18 | 1962-10-30 | Beloit Iron Works | Centrifugal classifier and stock cleaner |
US3529544A (en) | 1966-10-07 | 1970-09-22 | Shigeru Inoue | Method of screen printing a label on a disk record blank |
US4414112A (en) | 1982-01-29 | 1983-11-08 | Recovery Technology Associates | Oil/water separator |
US5104520A (en) | 1990-06-25 | 1992-04-14 | The United States Of America As Represented By The United States Department Of Energy | Apparatus and method for separating constituents |
US5407584A (en) | 1990-09-28 | 1995-04-18 | Broussard, Sr.; Paul C. | Water clarification method |
US5478484A (en) | 1991-07-25 | 1995-12-26 | Serck Baker Limited | Apparatus and method including a hydrocyclone separator in combination with a tubular filter |
US5466384A (en) * | 1992-11-05 | 1995-11-14 | Institut Francais Du Petrole | Device and process for carrying out phase separation by filtration and centrifugation |
DE4420760C1 (en) * | 1993-07-01 | 1995-05-11 | Gerd Wurster | Process and plant for reprocessing or concentration of used surfactant-containing iron phosphatising baths |
US6613231B1 (en) * | 1997-11-26 | 2003-09-02 | Profiltra | Apparatus, system and method for separating liquids |
DE102005027509A1 (en) * | 2005-06-15 | 2006-12-28 | Werner Lauth | Filer to separate solid particles in suspension from fluid has filter elements located at boundary between two vortex systems |
US20070039900A1 (en) * | 2005-08-18 | 2007-02-22 | Clean Filtration Technologies, Inc. | Hydroclone based fluid filtration system |
US7632416B2 (en) | 2005-08-18 | 2009-12-15 | Clean Filtration Technologies, Inc. | Hydroclone based fluid filtration system |
US7896169B2 (en) | 2005-08-18 | 2011-03-01 | Clean Filtration Technologies, Inc. | Hydroclone based fluid filtration system |
US20110120959A1 (en) | 2005-08-18 | 2011-05-26 | Clean Filtration Technologies, Inc. | Hydroclone based fluid filtration system |
US20110220586A1 (en) | 2010-03-12 | 2011-09-15 | Levitt David J | Fluid filtration and particle concentration device and methods |
WO2011160087A1 (en) * | 2010-06-17 | 2011-12-22 | Clean Filtration Technologies, Inc. | Cleaning assembly for use in fluid filtration systems |
US20120010063A1 (en) | 2010-06-17 | 2012-01-12 | Clean Filtration Technologies, Inc. | Cleaning assembly for use in fluid filtration systems |
Cited By (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8960450B2 (en) | 2010-12-08 | 2015-02-24 | Dow Global Technologies Llc | Apparatus and method for implementing hydroclone based fluid filtration systems with extensible isolated filter stages |
US9050610B2 (en) | 2012-05-17 | 2015-06-09 | Dow Global Technologies Llc | Hydroclone with inlet flow shield |
US9186604B1 (en) | 2012-05-31 | 2015-11-17 | Dow Global Technologies Llc | Hydroclone with vortex flow barrier |
US9101859B2 (en) | 2012-06-01 | 2015-08-11 | Dow Global Technologies Llc | Cross-flow filtration system including particulate settling zone |
US9192946B2 (en) | 2012-10-26 | 2015-11-24 | Dow Global Technologies Llc | Hydroclone |
WO2014066036A3 (en) * | 2012-10-26 | 2014-10-02 | Dow Global Technologies Llc | Hydroclone |
US9527091B2 (en) | 2013-12-05 | 2016-12-27 | Dow Global Technologies Llc | Hydroclone with improved cleaning assembly |
WO2016099822A1 (en) | 2014-12-18 | 2016-06-23 | Dow Global Technologies Llc | Cylindrical filter screen with tensioning mechanism |
GB2582042A (en) * | 2019-10-08 | 2020-09-09 | Inheriting Earth Ltd | Microplastic Separator |
GB2582042B (en) * | 2019-10-08 | 2021-03-03 | Inheriting Earth Ltd | Microplastic separator |
GB2588376A (en) * | 2019-10-08 | 2021-04-28 | Inheriting Earth Ltd | Filter pressure consumption regeneration apparatus and method |
GB2588376B (en) * | 2019-10-08 | 2022-03-23 | Inheriting Earth Ltd | Filter pressure consumption regeneration apparatus and method |
GB2600921A (en) * | 2020-11-04 | 2022-05-18 | Xeros Ltd | Filter unit, textile treatment apparatus and method |
GB2600921B (en) * | 2020-11-04 | 2023-09-13 | Xeros Ltd | Filter unit, textile treatment apparatus and method |
GB2619323A (en) * | 2022-05-31 | 2023-12-06 | Xeros Ltd | A microparticle filter, a textile treatment apparatus, use thereof and a method of filtering microparticles |
Also Published As
Publication number | Publication date |
---|---|
EP2825276A1 (en) | 2015-01-21 |
CN104334246A (en) | 2015-02-04 |
US9101859B2 (en) | 2015-08-11 |
CA2872329A1 (en) | 2013-12-05 |
US20150083651A1 (en) | 2015-03-26 |
CN104334246B (en) | 2017-03-15 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US9101859B2 (en) | Cross-flow filtration system including particulate settling zone | |
US9186604B1 (en) | Hydroclone with vortex flow barrier | |
CA2828922C (en) | Multi-chambered hydroclone | |
US9192946B2 (en) | Hydroclone | |
US9050610B2 (en) | Hydroclone with inlet flow shield | |
JP2015520672A5 (en) | ||
US9782698B2 (en) | Liquid refinement | |
US11167293B2 (en) | Cyclone separator | |
RU2226419C1 (en) | Centrifugal type device for purification of liquid from dispersible impurities |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 13727744 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 14391128 Country of ref document: US |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2013727744 Country of ref document: EP |
|
ENP | Entry into the national phase |
Ref document number: 2872329 Country of ref document: CA |
|
NENP | Non-entry into the national phase |
Ref country code: DE |