US20050126980A1 - Cross-flow filtration unit - Google Patents

Cross-flow filtration unit Download PDF

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Publication number
US20050126980A1
US20050126980A1 US10/168,806 US16880602A US2005126980A1 US 20050126980 A1 US20050126980 A1 US 20050126980A1 US 16880602 A US16880602 A US 16880602A US 2005126980 A1 US2005126980 A1 US 2005126980A1
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US
United States
Prior art keywords
permeate
ply
membrane
flow
filtration
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US10/168,806
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English (en)
Inventor
Ina Pahl
Hans-Weddo Schmidt
Ulrich Grummert
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sartorius Stedim Biotech GmbH
Original Assignee
Sartorius AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sartorius AG filed Critical Sartorius AG
Assigned to SARTORIUS AG reassignment SARTORIUS AG ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GRUMMERT, ULRICH, SCHMIDT, HANS-WEDDO, PAHL, INA
Publication of US20050126980A1 publication Critical patent/US20050126980A1/en
Priority to US11/602,884 priority Critical patent/US7520988B2/en
Assigned to SARTORIUS BIOTECH GMBH reassignment SARTORIUS BIOTECH GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SARTORIUS AG
Assigned to SARTORIUS STEDIM BIOTECH GMBH reassignment SARTORIUS STEDIM BIOTECH GMBH CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). Assignors: SARTORIUS BIOTECH GMBH
Abandoned legal-status Critical Current

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Classifications

    • 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
    • B01D63/082—Flat membrane modules comprising a stack of flat membranes
    • B01D63/084—Flat membrane modules comprising a stack of flat membranes at least one flow duct intersecting the membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/12—Composite membranes; Ultra-thin membranes
    • B01D69/1218—Layers having the same chemical composition, but different properties, e.g. pore size, molecular weight or porosity
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/44—Cartridge types
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • a liquid feed flows tangentially over the surface of a filter material and is thereby split into a concentrate (retentate) stream and a filtrate (permeate) stream.
  • microporous membranes are used which fall into the ultrafiltration and microfiltration classifications.
  • Ultrafiltration membranes have average pores sizes that are capable of retaining macromolecules having a molecular weight between 500 and 1,000,000 Daltons, known in the filtration art as having a molecular weight cutoff (MWCO) of 500 to 1,000,000 Daltons.
  • MWCO molecular weight cutoff
  • Microfiltration membranes exhibit average pore sizes of between 0.01 and 10 microns. See generally Chapter 4.3.3 in Gasper, Handbook of Industrial Solids/Fluids Filtration (1990).
  • Retentate flowing over the surface of the separation membrane is typically recycled to flow over the membrane's surface repeatedly.
  • the permeate which penetrates the membrane generally perpendicular to its surface is removed from the back side of the membrane.
  • the target substances can be in either the permeate and/or the retentate.
  • Cross-flow filtration units are often used in the form of filter cassettes, as described, for example in U.S. Pat. No. 4,715,955 and in DE PS 34 41 249.
  • Cassettes are comprised of a multiplicity of adjacent filter arrays, each array generally consisting of flat custom-cut sections of retentate spacers which form feed flow channels, a first single membrane layer, a spacer for the formation of a filtrate collection opening, and a second single membrane layer.
  • Each feed flow channel is in fluid communication with a liquid feed inlet and with a retentate outlet, and each permeate channel is in fluid communication with a permeate outlet.
  • UK Patent Application 2,236,693 discloses a similar cross-flow filter, but with either self-supporting porous filter plates or porous polymeric membranes supported by and bonded to a porous ceramic layer having larger pores.
  • the retentate substance As the feed flows over the membrane surface, the retentate substance, because of its size, is blocked from passage through the pores of the membrane and is rinsed away from the membrane surface, so that it will not plug the membrane pores, thus preventing its permeation through the membrane. In spite of this, for various reasons, build-up of non-filtered residue is formed on the surface of the feed side of the membrane, which generally impairs the filtering capacity, the yield of targeted substances and the service life of the cross-flow filtration unit.
  • a primary object of the invention is to provide an improved cross-flow filtration unit, which is characterized by an improved filtration capacity, a longer service life and a high product yield.
  • the present invention provides an improved cross-flow filtration unit that separates
  • the essence of the invention comprises sizing the pores in the two layers of a two-ply microporous membrane such that the pores of the layer facing the feed channel of the cross-flow filtration unit are on average 1.3 to 5 times the pores of the layer facing the permeate channel.
  • fluids can be filtered which include liquids, emulsions, suspensions, potable fluids such as beer, beer flavorants, wine, juice, water, milk and whey; laboratory grade water; wastewater; fluids in the fields of pharmaceuticals, medicine, cosmetics, chemistry, biotechnology, gene technology, environmental protection and in laboratory work.
  • the inventive cross-flow filtration units can be employed for recovery of valuable material, for separation of substances such as macromolecules and biomolecules, for depyrogenation and sterilization of solutions, for the separation of corrosive substances from fluids, for the filtration and concentration of biological solutions, for the separation of microorganisms such as bacteria, yeasts, virus and cell components and for the desalination of protein solutions and other biological media.
  • FIG. 1 is a schematic cross-sectional view of the operative parts of an exemplary cross-flow filtration unit of the present invention.
  • the present invention comprises an improvement in cross-flow filtration unit that enhances its efficiency and extends its service life and provides greater yield of target substances.
  • FIG. 1 there is depicted in schematic form the operative parts of a cross-flow filtration unit of the invention, consisting of a series of liquid feed inlets 10 , feed flow channels 12 , permeate flow channels 20 , permeate outlets 22 , retentate outlets 30 and two-ply microporous polymeric membranes 40 , each membrane consisting of a front side layer or ply 41 facing feed flow channel 12 , and a back side layer or ply 42 facing permeate flow channel 20 , with the two plys 41 and 42 being joined together by small spacers 43 in their peripheries.
  • the two plys 41 and 42 physically lie one on top of the other, but are not bonded together in the area 44 between them.
  • the feed and permeate collection channels are advantageously held open by spacers (not shown in FIG. 1 ) which are conventional.
  • the flow of fluid through the filtration unit is as depicted by the arrows in FIG. 1 , with the liquid feed initially entering the unit through feed inlet 10 , flowing through feed flow channel 12 , where the stream is split into a retentate-containing fluid flowing out through retentate outlet 30 and a permeate-containing fluid that permeates membrane 40 substantially perpendicularly from its front side 41 to its back side 42 into permeate flow channel 20 and permeate flow outlet 22 .
  • the pore sizes of the membrane layers differ by a factor of less than 1.3, then, from a commercial operation standpoint, either insignificant or no effects on filtration efficiency are observed.
  • the pore sizes in the membrane layers differ by a factor of greater than 5, then blinding of the membrane layer with the greater average pore size occurs very quickly, especially in the case of particulate-laden feed liquids, causing a halt to filtration.
  • the cross-flow filtration unit is constructed as a filter cassette, the membrane layers of which consist of microfiltration membranes.
  • a filter cassette in which the membrane layers facing the permeate collection channels have an average pore diameter in the range of 0.1 to 1.2 ⁇ m.
  • the filtration unit has a single two-ply membrane, a single feed inlet and channel, a single retentate outlet and a single permeate channel and outlet wherein the two layers of the microporous membrane are oriented as noted above, and the average pore sizes of the two layers comply with the above-noted restriction.
  • a cross-flow filtration unit having the pores of the two-ply membranes sized as noted above is used to filter a yeast cell suspension (pichia) with a cell concentration of 6 ⁇ 10 6 yeast cells (retentate content) per mL, which contains a targeted protein having a molecular weight of 70,000 Daltons (permeate content) in a concentration of 127 mL.
  • the filtration takes place in a cross-flow mode with recycle of the retentate.
  • the filtration unit is operated at a constant transmembrane pressure of 0.64 bar (the transmembrane pressure is equal to [input pressure+outlet pressure]/2 minus permeate pressure). The pressure was at 0.9 bar at the feed inlet, 0.4 bar at the retentate outlet and 0.1 bar at the permeate outlet.
  • the cell suspension feed was held constant for both the Example and the Comparative Example.
  • a cross-flow filtration unit fabricated in the form of a filter cassette was employed with two-ply membranes exposed to the liquid feed and having a total membrane surface area of 0.4 m 2 , and which had 13 feed flow channels and 12 permeate flow channels.
  • the membrane layers facing the permeate flow channels were of cellulose acetate with an average pore size of 0.2 ⁇ m and the membrane layers facing the feed flow channels were also of cellulose acetate, but having an average pore size of 0.45 ⁇ m, larger by a factor of 2.25.
  • a volume of 7.3 L of the cell suspension was concentrated to a final volume of 1 L.
  • the average permeate flow rate was 0.875 L/min ⁇ m 2 . Filtration was conducted for 18 minutes.
  • the concentration of the target protein in the permeate and the retentate was 107 and 238 mg/L, respectively.
  • the yield of targeted protein was 72%.
  • both plys of the two-ply membrane had an average pore size of 0.2 ⁇ m, so that the ratio of pore sizes was less than 1.3, i.e., 1; the average permeate flow rate was 0.29 L/min ⁇ m 2 ; filtration was conducted for 54 minutes; the concentration of the target protein in the permeate and in the retentate was 86 and 387 g/L, respectively; and the yield was 58%, or 14% less than with the inventive filtration device.
  • the average pore size of the ply facing the feed flow channel was 1.2 ⁇ m, while that of the ply facing the permeate channel was 0.2 ⁇ m, so that the ratio of pore sizes was greater than 5, i.e., 6; the average permeate flow rate was 0.49 L/min ⁇ m 2 ; filtration was conducted for 37 minutes; the concentration of the target protein in the permeate and in the retentate was 89 and 365 g/L, respectively; and the yield was 61%, or 11% less than with the inventive filtration device.
  • a cross-flow filtration cassette of conventional design (Sartocon® from Sartorius AG of Goettingen, Germany) was employed having a membrane surface exposed to the same feed of 0.7 m 2 , which had 17 feed flow channels and 16 permeate flow channels.
  • the membrane layers facing the permeate flow channels consisted of a single-ply cellulose acetate membrane with an average pore size of 0.2 ⁇ m.
  • a volume of 12.7 L of the cell suspension were concentrated to a final volume of 1 L.
  • the average permeate flow was 0.328 L/min ⁇ m 2 .
  • the filtration was terminated after 51 minutes.
  • the concentration of targeted protein in the permeate and retentate was found to be 81.3 and 621 mg/L, respectively.
  • the yield of targeted protein in the filtrate was thus 59%, or 13% less than with the inventive filtration device.
  • the permeate flow was increased by a factor of 2.7.
  • a further advantage apparent from use of the inventive cross-flow filtration unit was that a single filtration simultaneously encompassed both pre-filtration and final filtration; by way of contrast, in conventional practice two filtration steps must be carried out to achieve pre- and final filtration.
  • use of the cross-flow filtration unit of the invention clearly results in a reduction of the costs of filtration.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
US10/168,806 2000-01-05 2000-12-21 Cross-flow filtration unit Abandoned US20050126980A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US11/602,884 US7520988B2 (en) 2000-01-05 2006-11-20 Cross-flow filter cassette

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE100001963 2000-01-05
DE10000196A DE10000196B4 (de) 2000-01-05 2000-01-05 Verbesserte Crossflow-Filtrationseinheit
PCT/EP2000/013073 WO2001049401A1 (de) 2000-01-05 2000-12-21 Crossflow-filtrationseinheit

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US11/602,884 Continuation-In-Part US7520988B2 (en) 2000-01-05 2006-11-20 Cross-flow filter cassette

Publications (1)

Publication Number Publication Date
US20050126980A1 true US20050126980A1 (en) 2005-06-16

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US10/168,806 Abandoned US20050126980A1 (en) 2000-01-05 2000-12-21 Cross-flow filtration unit
US11/602,884 Expired - Lifetime US7520988B2 (en) 2000-01-05 2006-11-20 Cross-flow filter cassette

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Country Status (6)

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US (2) US20050126980A1 (de)
EP (1) EP1268044A1 (de)
JP (1) JP2003519005A (de)
CN (1) CN1420801A (de)
DE (1) DE10000196B4 (de)
WO (1) WO2001049401A1 (de)

Cited By (2)

* Cited by examiner, † Cited by third party
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US20050255227A1 (en) * 2004-05-14 2005-11-17 Kamalesh Sirkar Highly selective membrane systems and methods for protein ultrafiltration
US20100304953A1 (en) * 2009-05-21 2010-12-02 Battelle Memorial Institute Zeolite Membranes for Separation of Mixtures Containing Water, Alcohols, or Organics

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DE102006026081B4 (de) * 2006-06-03 2014-11-27 Sartorius Stedim Biotech Gmbh Verfahren zur Herstellung von trinkfertigem Branntwein
JP4899681B2 (ja) * 2006-07-18 2012-03-21 富士ゼロックス株式会社 マイクロ流路デバイス
JP5151204B2 (ja) * 2007-03-27 2013-02-27 富士ゼロックス株式会社 マイクロ流路デバイス及びマイクロ流路デバイスの製造方法
JP5119848B2 (ja) * 2007-10-12 2013-01-16 富士ゼロックス株式会社 マイクロリアクタ装置
JP2010115624A (ja) * 2008-11-14 2010-05-27 Fuji Xerox Co Ltd マイクロ流路デバイス、分離装置、並びに、分離方法
JP5003702B2 (ja) 2009-03-16 2012-08-15 富士ゼロックス株式会社 マイクロ流体素子及びマイクロ流体制御方法
BRPI1005181A2 (pt) * 2009-08-13 2019-07-02 Geosynfuels Llc processo para a produção de produtos de alto valor de biomassa
CA2770439A1 (en) 2009-08-13 2011-02-17 Geosynfuels, Llc Apparatus and process for fermentation of biomass hydrolysate
US8480978B2 (en) * 2010-08-12 2013-07-09 University Of Southern California Microfluidic fluid separator and related methods
US9475709B2 (en) 2010-08-25 2016-10-25 Lockheed Martin Corporation Perforated graphene deionization or desalination
US20120208255A1 (en) * 2011-02-14 2012-08-16 Geosynfuels, Llc Apparatus and process for production of an encapsulated cell product
AU2012372141B2 (en) * 2011-12-23 2015-01-15 Intelligent Packaging Pty Limited Wine packaged in aluminium containers
US9463421B2 (en) 2012-03-29 2016-10-11 Lockheed Martin Corporation Planar filtration and selective isolation and recovery device
US10005038B2 (en) 2014-09-02 2018-06-26 Lockheed Martin Corporation Hemodialysis and hemofiltration membranes based upon a two-dimensional membrane material and methods employing same
US10980919B2 (en) 2016-04-14 2021-04-20 Lockheed Martin Corporation Methods for in vivo and in vitro use of graphene and other two-dimensional materials
US9834809B2 (en) 2014-02-28 2017-12-05 Lockheed Martin Corporation Syringe for obtaining nano-sized materials for selective assays and related methods of use
US10653824B2 (en) 2012-05-25 2020-05-19 Lockheed Martin Corporation Two-dimensional materials and uses thereof
US9744617B2 (en) 2014-01-31 2017-08-29 Lockheed Martin Corporation Methods for perforating multi-layer graphene through ion bombardment
US10376845B2 (en) 2016-04-14 2019-08-13 Lockheed Martin Corporation Membranes with tunable selectivity
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EP3099645A4 (de) 2014-01-31 2017-09-27 Lockheed Martin Corporation Verfahren zur formung von verbundstrukturen mit einem zweidimensionalen material unter verwendung einer porösen, nichtbeschädigenden trägerschicht
CA2938273A1 (en) 2014-01-31 2015-08-06 Peter V. Bedworth Perforating two-dimensional materials using broad ion field
JP2017512129A (ja) 2014-03-12 2017-05-18 ロッキード・マーチン・コーポレーション 有孔グラフェンから形成された分離膜
US20150268150A1 (en) * 2014-03-24 2015-09-24 Lockheed Martin Corporation Large area membrane evaluation apparatuses and methods for use thereof
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JP2019519756A (ja) 2016-04-14 2019-07-11 ロッキード・マーチン・コーポレーション 欠陥形成または欠陥修復をその場で監視して制御する方法
WO2017180137A1 (en) 2016-04-14 2017-10-19 Lockheed Martin Corporation Method for treating graphene sheets for large-scale transfer using free-float method
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RU2687921C1 (ru) * 2018-05-03 2019-05-16 Закрытое Акционерное Общество "Владисарт" Фильтрующий элемент для разделения и концентрирования жидких сред
RU2687906C1 (ru) * 2018-05-03 2019-05-16 Закрытое Акционерное Общество "Владисарт" Фильтрующий элемент для разделения и концентрирования жидких сред
MX2021010891A (es) * 2019-03-11 2021-12-10 Genzyme Corp Filtracion tangencial de virus.
CN110551617B (zh) * 2019-09-03 2022-11-01 中国科学院北京基因组研究所 用于体液细菌与细胞分离的芯片、制作方法及其使用方法

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US5256294A (en) * 1990-09-17 1993-10-26 Genentech, Inc. Tangential flow filtration process and apparatus
US6099730A (en) * 1997-11-14 2000-08-08 Massachusetts Institute Of Technology Apparatus for treating whole blood comprising concentric cylinders defining an annulus therebetween

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050255227A1 (en) * 2004-05-14 2005-11-17 Kamalesh Sirkar Highly selective membrane systems and methods for protein ultrafiltration
US7497950B2 (en) * 2004-05-14 2009-03-03 New Jersey Institute Of Technology Highly selective membrane systems and methods for protein ultrafiltration
US20100304953A1 (en) * 2009-05-21 2010-12-02 Battelle Memorial Institute Zeolite Membranes for Separation of Mixtures Containing Water, Alcohols, or Organics

Also Published As

Publication number Publication date
US7520988B2 (en) 2009-04-21
US20070062856A1 (en) 2007-03-22
JP2003519005A (ja) 2003-06-17
DE10000196B4 (de) 2013-10-10
WO2001049401A1 (de) 2001-07-12
CN1420801A (zh) 2003-05-28
EP1268044A1 (de) 2003-01-02
DE10000196A1 (de) 2001-07-12

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