WO2006130815A2 - Crossflow membrane filtration module - Google Patents
Crossflow membrane filtration module Download PDFInfo
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- WO2006130815A2 WO2006130815A2 PCT/US2006/021418 US2006021418W WO2006130815A2 WO 2006130815 A2 WO2006130815 A2 WO 2006130815A2 US 2006021418 W US2006021418 W US 2006021418W WO 2006130815 A2 WO2006130815 A2 WO 2006130815A2
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- WO
- WIPO (PCT)
- Prior art keywords
- membrane filtration
- filtration module
- module
- set forth
- flow channel
- Prior art date
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- 238000005374 membrane filtration Methods 0.000 title claims abstract description 49
- 239000012530 fluid Substances 0.000 claims abstract description 14
- 238000009295 crossflow filtration Methods 0.000 claims abstract description 4
- 239000012466 permeate Substances 0.000 claims description 27
- 239000012528 membrane Substances 0.000 claims description 26
- 238000007906 compression Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 7
- 239000011521 glass Substances 0.000 claims description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 239000005350 fused silica glass Substances 0.000 claims description 4
- 239000004417 polycarbonate Substances 0.000 claims description 4
- 229920000515 polycarbonate Polymers 0.000 claims description 4
- 125000006850 spacer group Chemical group 0.000 claims description 4
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 3
- 238000013461 design Methods 0.000 abstract description 7
- 238000004088 simulation Methods 0.000 abstract description 5
- 239000002245 particle Substances 0.000 description 6
- 238000001914 filtration Methods 0.000 description 4
- 238000003384 imaging method Methods 0.000 description 3
- 238000002595 magnetic resonance imaging Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
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- 230000004907 flux Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000917 particle-image velocimetry Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 238000013341 scale-up Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 239000004677 Nylon Substances 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 239000004695 Polyether sulfone Substances 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 238000010364 biochemical engineering Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000004624 confocal microscopy Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
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- 235000013365 dairy product Nutrition 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- FKLFBQCQQYDUAM-UHFFFAOYSA-N fenpiclonil Chemical compound ClC1=CC=CC(C=2C(=CNC=2)C#N)=C1Cl FKLFBQCQQYDUAM-UHFFFAOYSA-N 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
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- 230000014759 maintenance of location Effects 0.000 description 1
- 238000013507 mapping Methods 0.000 description 1
- 238000009285 membrane fouling Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000011859 microparticle Substances 0.000 description 1
- 238000000386 microscopy Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920006393 polyether sulfone Polymers 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000004627 regenerated cellulose Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
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- 239000002904 solvent Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/18—Apparatus therefor
-
- 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
- B01D61/08—Apparatus therefor
-
- 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
- B01D61/10—Accessories; Auxiliary operations
-
- 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
- B01D61/12—Controlling or regulating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/20—Accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/22—Controlling or regulating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/08—Flat membrane modules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/08—Flat membrane modules
- B01D63/081—Manufacturing thereof
-
- 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
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/10—Cross-flow filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/10—Use of feed
Abstract
The present invention provides a membrane filtration module with an inlet and outlet design that provides a more uniform fluid flow than conventional modules. The new membrane filtration module was designed and optimized based on computational fluid dynamics (CFD) simulations. The membrane filtration module contains a flow channel with width w and inlet and outlet ports that are collinear with the flow channel. The inlet and outlet ports each have a fanned section, with one end of the fanned section equal to width w. In addition, the inlet and outlet ports each have an inclined section that is in fluid connection with the flow channel. This inclined section is preferably at about a 45 degree angle relative to the flow channel. The new membrane filtration module is well suited for cross-flow filtration.
Description
CROSSFLOW MEMBRANE FILTRATION MODULE
FIELD OF THE INVENTION
The present invention relates generally to membrane filtration. More particularly, the present invention relates to a crossflow filtration module with improved hydrodynamic characteristics.
BACKGROUND Crossflow membrane filtration is a separation process frequently encountered in chemical engineering, bioprocess engineering, environmental engineering and related fields for the retention of solids, segregation of different sized particles, water purification, concentration of bacterial cells, proteins etc. Prior to scale up, membranes are tested in laboratory scale membrane modules for experimentation with various membrane types and in the investigation of operating conditions on filtration performance. Another common use of small modules is in the running of laboratory scale reactors.
The conventional laboratory membrane module contains 3 main components: two thick cover plates, a permeate plate and gaskets for sealing. The permeate plate, with membranes placed on its two faces, is positioned between the two cover plates. Each face of the permeate plate has a series of narrow grooves aligned laterally, allowing the permeate to be drained and collected. The membranes are secured in place by the surrounding gaskets, which are compressed by the cover plates, thus activating a seal. The thickness of the gasket after compression defines the depth of the flow channel.
Conventional membrane filtration modules have inlets and outlets that are orthogonally positioned with respect to the main flow direction. Thus, the incoming fluid has to maneuver through two 90° turns before reaching the flow channel. This unfavorable inlet condition results in a large entrance length that far exceeds the longitudinal dimension of the device, creating a flow field that is non-unidirectional and highly heterogeneous. There are many consequences of this hydrodynamic heterogeneity. For instance, different positions on the membrane will have different local permeabilities and fouling rates and therefore, the reported average permeate flux will have to be interpreted with this in mind. It also means experimental results will be partly dependent on the filter module used. Complication also arises when performing selective sampling for further analysis as the sampling area could have been subjected to quite a different flow condition than assumed.
In the filtration of concentrated particulates such as activated sludge, hydrodynamic heterogeneity becomes an even more critical problem. Regions experiencing low velocities, which are more susceptible to particle deposition, rapidly form a cake layer, fouling the membrane or even clogging the flow channel, forming dead zones. The useful membrane area is thus reduced. This phenomenon is common and has been recognized as a significant imperfection in module design. Accordingly, there is a need in the art to develop membrane filtration modules with inlet and outlet designs that promote a more hydrodynamically homogeneous fluid flow.
The present invention provides a membrane filtration module with an inlet and outlet design that provides a more uniform fluid flow than conventional modules. The new membrane filtration module was designed and optimized based on computational fluid dynamics (CFD) simulations. The membrane filtration module contains a flow channel with width w and inlet and outlet ports that are collinear with the flow channel. The inlet and outlet ports each have a fanned section, with one end of the fanned section equal to width w. In addition, the inlet and outlet ports each have an inclined section that is in fluid connection with the flow channel. This inclined section is preferably at about a 45 degree angle relative to the flow channel. The new membrane filtration module is well suited for cross-flow filtration.
According to the present invention, the flow channel and inlet and outlet ports are made from a cover plate and a permeate plate. The cover plate is preferably symmetric about the transverse axis, such that the inlet and outlet ports can be interchanged. Also preferably, the cover plate is fabricated from three attached sections. In a preferred embodiment, the cover plate contains a view port, which may be made of any optically clear material, including but not limited to glass and fused silica. The permeate plate preferably has longitudinal or transverse grooves, depending on the application. These grooves are preferably adjacent to the exit of the inclined section of the port. Preferably, the membrane filtration module also includes spacers to prevent over-compression of the module.
fabricated from acrylic or polycarbonate. The dimensions of the module are preferably about 158 mm x 60 mm x 37 mm, but may have any dimensions that retain this ratio (i.e. about 4.3:1.6:1 length: width: height). The membrane filtration module also preferably accommodates a membrane with a length in the range of about 86 to about 94 mm and a width in the range of about 27 to about 34 mm. Additionally, the membrane filtration module can preferably support a flow rate of between about 0-20 liters per minute (LPM) and will maintain structural integrity at a pressure up to about 400 kPa.
BRIEF DESCRIPTION OF THE FIGURES
The present invention together with its objectives and advantages will be understood by reading the following description in conjunction with the drawings, in which: FIG. 1 shows a cover plate according to the present invention.
FIG. 2 shows a permeate plate according to the present invention. FIG. 3 shows a membrane filtration module according to the present invention.
FIG. 4 shows fabrication of a cover plate according to the present invention.
FIG. 5 shows a simulated flow domain (A) and a simulated longitudinal velocity field (B) according to the present invention.
DETAILED DESCRIPTION OF THE INVENTION
Structure of Membrane Filtration Modules
The present invention provides a membrane filtration module including a cover plate and a permeate plate. FIG. 1 shows a cross-sectional (A) and a top (B) view of an example of a cover plate 100 according to the present invention. The cover plate has an inlet port 110
as shown, such that inlet port 110 and outlet port 120 are interchangeable. Inlet port 110 and outlet port 120 each contain a section to receive a tubing adapter (112 and 122, respectively), a fanned section (114 and 124, respectively), and an inclined section (116 and 126, respectively) that ends in an opening (118 and 128, respectively) to a flow channel (not shown). The tubing may be connected to cover plate 100 by any means, including but not limited to via hose barbed adapters or compression fittings.
Inlet port 110 and outlet port 120 are sized such that they are large enough to ensure a low inflow/outflow velocity relative to the crossflow velocity. This is necessary to prevent a momentum jet-like behavior from affecting the channel flow field. In addition, the end of the fanned section (114 and 124) that connects to the inclined section (116 and 126) is fanned to a width that corresponds to the width of the main flow. This further reduces the velocity of the inflow prior to entering the inclined section. The inclined section (116 and 126) is preferably at about a 45 degree angle relative to the flow channel formed from attaching the cover plate 100 to the permeate plate. Directing fluid to the membrane surface at this angle minimizes flow separations.
The cover plate 100 may also contain a depression 130 in the top of the plate. The cover plate 100 also has holes 150 for attaching cover plate 100 to the permeate plate.
FIG. 2 shows a cross-sectional (A) and a top (B) view of an example of a permeate plate 200 according to the present invention, where dashed lines indicate features below the surface of permeate plate 200. The permeate plate 200 preferably has a depression 210, as
grooves 220 for permeate drainage aligned in the longitudinal direction, as shown, to reduce perturbations in the flow. Alternatively, grooves 220 may be aligned laterally to induce turbulence, useful for long term operation of the module and in cases for which a consistent flow field is not critical. Grooves 220 drain into channel 230, which ends in section 232, designed to receive a tubing adapter. The tubing may be connected to permeate plate 200 by any means, including but not limited to via hose barbed adapters or compression fittings. Permeate plate 200 also contains holes 250 for attaching permeate plate 200 to the cover plate. Holes 250 contain a section 252 for receiving the body of a screw, and a section 254 for receiving a head of a screw. (For simplicity, only one hole 250 is shown in the cross-sectional view). Section 254 ensures that the screw head is flush with the bottom of permeate plate 200.
FIG. 3 shows a cross-sectional view of an example of a membrane filtration module 300 according to the present invention. Module 300 includes cover plate 100 and permeate plate 200, which are secured, preferably by a nut and bolt action, through holes 150 and 250, pictured in FIG. 1 and FIG. 2. (Holes 150 and 250 are out of the plane of the section shown in FIG. 3). Sealing of the membrane filtration module 300 is activated by compression of a sheet gasket 310 surrounding flow channel 320. Preferably, spacers 330 are situated between cover plate 100 and permeate plate 200 to prevent over compression of module 300. The actual depth of flow channel 320 can be precisely estimated by measuring the thickness of module 300 before and after compression. The depth of flow channel 320 can be altered by using gaskets/spacers of different thickness. This is especially valuable in experiments where vertical mass transport is important.
Solid arrows 340 illustrate the direction of flow through module 300. Fluid flows into module 300 through inlet 110, into flow channel 320 and then out of module 300 through outlet 120. The design of the different parts of the flow path ensures a smooth flow transition across the membrane module, resulting in a low longitudinal pressure gradient. This implies a smaller variation in the localized transmembrane pressure (TMP) across the membrane. In addition, the low pressure gradient simplifies scale up. Permeate that flows through a membrane (not shown) situated in depression 210 drains through grooves 220 into channel 230, and out of module 300 through section 232.
Membrane filtration modules according to the present invention may be any size, but preferably have dimensions of about 158 mm x 60 mm x 37 mm. Modules preferably can accommodate a membrane with a length in the range of about 86 to about 94 mm and a width in the range of about 27 to about 34 mm. Any type of membrane can be used according to the present invention, including but not limited to polysulfone, polyethersulfone, polyvinylidene fluoride, regenerated cellulose, nylon and polycarbonate. In addition, different membranes can be used at different times due to the ease of disassembling the module. Modules may be scaled up or down from the above dimensions, where the ratios of the described dimensions are preferably maintained. A vertically stacked system using membrane filtration modules according to the present invention may be constructed if higher permeate flux is desired. Any fluid may be filtered using a module according to the present invention. Examples include activated sludge, dairy products, yeast suspensions and contaminated water. Membrane filtration modules
of acrylic or polycarbonate.
Membrane filtration modules according to the present invention preferably support a flow rate of between about 0-20 LPM before the membrane will collapse. In addition, modules preferably maintain structural integrity at a pressure of up to about 400 kPa. The entire module can be placed flat on a horizontal surface, minimizing the possibility of vibrations affecting the flow or membrane attached foulants.
Membrane filtration modules according to the present invention also preferably include an optically clear view port at the center to allow the entrance of a microscopic objective lens for a close-up view of the flow channel or the membrane surface. The view port contains a window that is preferably made of glass, more preferably fused silica. Proper engineering and designing of this view port enables the thickness of the port to be reduced to a dimension suitable for imaging yet retain sufficient structural integrity to withstand up to 400 kPa of working pressure. The sizing of the window thickness is determined based on:
Membrane filtration modules according to the present invention can function in a non- filteration mode for studying particle deposition and adsorption on surfaces. The permeate plate can be flipped such that the membrane is in contact with the flat surface without grooves thereby preventing permeation and the creation of transmembrane pressure. Moreover, porous membranes can be substituted with non-porous membranes or films with specific surface properties. In addition, membrane separation by reverse osmosis can be performed with this invention by constructing the body with stainless steel. This is to confer structural strength in order to withstand the high pressures involved.
Although filtration modules according to the present invention are intended for use in carefully controlled experimental work on membrane filtration, they are equally suitable for general low volume filtration applications and as a flow through device for research work on particle attachment onto surfaces. The particles can be colloids, bacteria cells, nanosized particles, larger particulates etc. The attachment surfaces can have a variety of properties such as porosity, charge, roughness, hydrophilicity/hydrophobicity, chemical reactivity and so on limited only by the availability of the materials.
The permeate plate is manufactured using standard techniques and will not be described here. The cover plate is preferably fabricated from three sections as shown in FIG. 4. First a block 400 of the material of choice is drilled on the bottom at an angle to create inclined channels 410. Next, the top of block 400 is milled to give fanned sections 420 of the inlet/outlet ports. The milled block is then attached to sections 430 and 440, which form the top of the cover plate. Sections 430 and 440 may be angled, as shown, or have squared edges. Alternatively, sections 430 and 440 may be combined into one section. Sections 430 and 440 may be attached to milled block 440 using solvent welding. Once the three sections have been attached, they are drilled on both sides to make the tubing adapter receiving ends 450 of the inlet/outlet ports. If it is desired for the flow channel to be larger, the bottom of block 400 may be milled at this point.
EXAMPLE Design of a membrane filtration module
The design of the interior geometry of the module was initiated based on computational fluid dynamics (CFD). Only geometries that produced hydrodynamically satisfactory results were further evaluated in terms of viability and simplicity in fabrication. Structural integrity and a pressure rating commensurate with MF/UF were also given due consideration.
Several other factors were taken into account. These included an option for the placement of a glass view port that allows in situ microscopic examination of the membrane surface as well as MRI compatibility.
The interior geometry was modeled and meshed using GAMBIT 2.1 (Fluent Inc.) while the computation was performed with FLUENT 6.1 (Fluent Inc.). The simulated domain was an exact replica of the final product down to the details such as curvatures created by the machining process. Such details are necessary due to the small length scale of the flow. Only half the channel was simulated, taking advantage of the symmetry of the module.
The domain was subdivided into a number of connected sections so that hexahedral mapping and the coopering scheme could be applied as much as possible. Tetrahedrals were packed in the remaining volumes. In this way, the number of skewed elements can be minimized. Attention was paid on meshing the region at and close to the inclined channel as that directly influences the entrance length. The unstructured grid had an initial size of over 240,000 elements.
As the inlet is connected to a tubing through an adapter, the actual inlet condition should be based on separate simulations of the chosen connector. Due to the multitude of possibilities, a laminar pipe flow profile was applied at the inlet as an approximation.
To assess the computed results in a meaningful manner and to enable comparison with theoretical solutions, all simulations were performed under a baseline condition. That is, a Newtonian fluid with a kinematic viscosity of 7 x 10"6 m2/s flowing through a 1.5 mm channel with impermeable walls. The viscosity was chosen to be comparable to that of
such viscosity.
Several simulations were performed in the laminar regime at Reynolds Number (Re) ranging from 107 to 857, where Re was calculated based on the channel depth and average crossflow velocity. The segregated solver was used together with the SIMPLEC (Semi- Implicit Method for Pressure-Linked Equation Consistent) algorithm for pressure-velocity coupling, a standard pressure interpolation scheme and the QUICK (Quadratic Upwind) scheme for momentum discretization. During the computational runs, the grid was adapted to resolve finer details. Convergence was assessed based on the area-weighted longitudinal velocity and static pressure at the half depth of the main flow channel. This was in addition to monitoring the drop in residuals of the velocity components. Each run was terminated only when a grid converged solution was obtained.
FIG. 5 A illustrates a simulated flow domain resulting from running the above algorithms. The geometry of this flow domain is an exact replica of a prototype membrane filtration module. FIG. 5B illustrates the longitudinal velocity field at the plane of symmetry and half depth of the crossflow channel. The scale in FIG. 5B is in m/s. The average crossflow velocity is 1 m/s. The velocity field demonstrates that a relatively uniform velocity can be obtained using the model membrane filtration module.
As one of ordinary skill in the art will appreciate, various changes, substitutions, and alterations could be made or otherwise implemented without departing from the principles
the following claims and their legal equivalents.
Claims
1. A membrane filtration module, comprising:
a) a flow channel with width w; and
b) an inlet port and an outlet port, wherein said inlet port and said outlet port are
collinear with said flow channel and wherein said inlet port and said outlet
port each comprise:
i) a fanned section, wherein one end of said fanned section is equal to
width w;
ii) an inclined section in fluid connection with said flow channel.
2. The membrane filtration module as set forth in claim 1, wherein said module is
designed for cross-flow filtration.
3. The membrane filtration module as set forth in claim 1, further comprising a
cover plate.
4. The membrane filtration module as set forth in claim 3, wherein said
cover plate comprises a view port.
5. The membrane filtration module as set forth in claim 4, wherein
said view port comprises glass.
6. The membrane filtration module as set forth in claim 5,
wherein said glass is fused silica.
7. The membrane filtration module as set forth in claim 3, wherein said
cover plate is symmetric about the transverse axis.
8. The membrane filtration module as set forth in claim 3, wherein said
cover plate comprises three attached sections. permeate plate.
10. The membrane filtration module as set forth in claim 9, wherein said permeate plate comprises longitudinal or transverse grooves.
11. The membrane filtration module as set forth in claim 9, wherein said groves are adjacent to the exit of said inclined section of said inlet port.
12. The membrane filtration module as set forth in claim 1, wherein said module comprises acrylic or polycarbonate.
13. The membrane filtration module as set forth in claim 1, wherein said module has dimensions of about 158 x 60 x 37 mm.
14. The membrane filtration module as set forth in claim 1, wherein said module has dimensions with a ratio of about 4.3 (length): 1.6 (width): 1 (height).
15. The membrane filtration module as set forth in claim 1, wherein said module supports a flow rate of between about 0 — 20 LPM.
16. The membrane filtration module as set forth in claim 1, wherein said module maintains structural integrity at a pressure up to about 400 kPa.
17. The membrane filtration module as set forth in claim 1, further comprising spacers to prevent over compression of said module.
18. The membrane filtration module as set forth in claim 1, wherein said inclined section is at an angle of about 45° relative to said flow channel. accommodates a membrane with a length in the range of about 86 to about 94 mm and a width in the range of about 27 to about 34 mm.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US68719805P | 2005-06-02 | 2005-06-02 | |
| US60/687,198 | 2005-06-02 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2006130815A2 true WO2006130815A2 (en) | 2006-12-07 |
| WO2006130815A3 WO2006130815A3 (en) | 2007-02-22 |
Family
ID=37482334
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/US2006/021418 WO2006130815A2 (en) | 2005-06-02 | 2006-06-02 | Crossflow membrane filtration module |
Country Status (1)
| Country | Link |
|---|---|
| WO (1) | WO2006130815A2 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007087578A2 (en) * | 2006-01-24 | 2007-08-02 | The Regents Of The University Of California | Method and system for monitoring reverse osmosis membranes |
| WO2015148548A3 (en) * | 2014-03-24 | 2015-12-10 | Lockheed Martin Corporation | Large area membrane evaluation apparatuses and methods for use thereof |
| WO2017171638A1 (en) * | 2016-03-28 | 2017-10-05 | Nanyang Technological University | Cross-flow membrane filtration with inclined filtration channel |
| WO2019058865A1 (en) * | 2017-09-25 | 2019-03-28 | 株式会社村田製作所 | Filtration device |
| US10864483B2 (en) | 2018-11-16 | 2020-12-15 | Integrated Protein Technologies, Snc. | Molecular weight filtration system and apparatus |
| US10960357B2 (en) | 2018-04-23 | 2021-03-30 | Noria Water Technologies, Inc. | Method and apparatus for real-time direct membrane monitoring |
| EP4014961A1 (en) * | 2020-12-17 | 2022-06-22 | Helixpharma S.r.l. | Process for the depyrogenation of a snail secretion and related production plant |
| US11786847B2 (en) | 2017-09-19 | 2023-10-17 | Murata Manufacturing Co., Ltd. | Filtration device and filtration method |
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|---|---|---|---|---|
| WO2007087578A2 (en) * | 2006-01-24 | 2007-08-02 | The Regents Of The University Of California | Method and system for monitoring reverse osmosis membranes |
| WO2007087578A3 (en) * | 2006-01-24 | 2007-10-18 | Univ California | Method and system for monitoring reverse osmosis membranes |
| US7910004B2 (en) | 2006-01-24 | 2011-03-22 | The Regents Of The University Of California | Method and system for monitoring reverse osmosis membranes |
| WO2015148548A3 (en) * | 2014-03-24 | 2015-12-10 | Lockheed Martin Corporation | Large area membrane evaluation apparatuses and methods for use thereof |
| WO2017171638A1 (en) * | 2016-03-28 | 2017-10-05 | Nanyang Technological University | Cross-flow membrane filtration with inclined filtration channel |
| US11786847B2 (en) | 2017-09-19 | 2023-10-17 | Murata Manufacturing Co., Ltd. | Filtration device and filtration method |
| CN111107920A (en) * | 2017-09-25 | 2020-05-05 | 株式会社村田制作所 | Filter device |
| JPWO2019058865A1 (en) * | 2017-09-25 | 2020-07-30 | 株式会社村田製作所 | Filtration device |
| US11529579B2 (en) | 2017-09-25 | 2022-12-20 | Murata Manufacturing Co., Ltd. | Filtration device |
| WO2019058865A1 (en) * | 2017-09-25 | 2019-03-28 | 株式会社村田製作所 | Filtration device |
| US10960357B2 (en) | 2018-04-23 | 2021-03-30 | Noria Water Technologies, Inc. | Method and apparatus for real-time direct membrane monitoring |
| US11826708B2 (en) | 2018-04-23 | 2023-11-28 | Noria Water Technologies, Inc. | Method and apparatus for real-time direct membrane monitoring |
| US10864483B2 (en) | 2018-11-16 | 2020-12-15 | Integrated Protein Technologies, Snc. | Molecular weight filtration system and apparatus |
| EP3881051A4 (en) * | 2018-11-16 | 2022-10-26 | Integrated Protein Technologies, Inc. | Molecular weight filtration system and apparatus |
| EP4014961A1 (en) * | 2020-12-17 | 2022-06-22 | Helixpharma S.r.l. | Process for the depyrogenation of a snail secretion and related production plant |
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| WO2006130815A3 (en) | 2007-02-22 |
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