NAMS 2002 Workshop - ICOM 2008

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An interesting surface property of the nanofiber membranes is its higher water contact angle as compared to conventional polymeric films made of the same materials. A PVDF nanofiber membrane has an average static contact angle of 145°. In comparison the contact angle of a PVDF film is only about 60-90°. We believe that the surface roughness of the nanofibers and trapped air pockets, given the high porosity of the nanofiber membrane contribute to this increased hydrophobicity. This hydrophobic characteristic of the nanofiber membrane is particularly important in some liquid filtration applications e.g. membrane distillation. Nanofiber membranes when produced may not have suitable mechanical strength to be used in liquid filtration processes. We have conducted extensive studies on the effect of heat treatment on the nanofiber properties. Tensile strength tests were conducted on two nanofibrous membranes, with one undergoing further heat treatment at 150°C for 3 hours. The heat treated membrane exhibited much higher mechanical strength with an ultimate tensile strength of 8.5 MPa for the heat treated membrane as compared to 0.4 MPa for the non-heat treated membrane. The mechanical strengthening of the heat treated nanofiber membranes, suggests that the structure of the nanofiber membranes changes after heat treatment. Differential scanning calorimetric profiles for the heat treated membranes indicate two peaks unlike the single peak found for non-heat treated PVDF nanofiber membranes. This signaled the presence of a more ordered fiber structure as a result of heat treatment. It was further found that when the heat applied is below the melting point (Tm) of the polymeric material used, it results in the overlapping nanofibers fusing together. The produced PVDF nanofiber membranes have a pore size distribution of between 4-10.6 µm. This is too large to be compared with commercial microfiltration and ultrafiltration membranes. To reduce the pore size of the nanofiber membranes but still maintain the nanofiber architecture, plasmainduced graft copolymerization of poly(metharcylic acid) on the PVDF nanofiber membrane was carried out. The pore size distribution of the grafted PVDF nanofiber membrane was then found to be similar to a commercial hydrophilic MF membrane of pore size 0.45 µm (HVLP, Millipore). The surface contact angles of both the grafted nanofiber membrane and the commercial hydrophilic membrane were the same at approximately 60°. This allowed a fairer comparison between the membranes. Both membranes were tested for filtration flux using distilled water and the nanofiber membrane had a higher flux compared with the commercial membrane at all pressures tested. The grafted nanofiber membrane had on average fluxes that were 1.6-2.0 times that of the commercial membrane. The higher flux of the nanofiber membrane indicates its potential to be used as a new next generation membrane material for water filtration.
Polymeric Membranes II – 5 Wednesday July 16, 11:45 AM-12:15 PM, Moloka’i Perfluoropolymer Membranes for Gasoline Vapor Emissions Reduction J. Bowser (Speaker), Compact Membrane Systems, Inc., Wilmington, Delaware, USA - jbowser@compactmembrane.com S. Majumdar, Compact Membrane Systems, Inc., Wilmington, Delaware, USA The California Air Resources Board (CARB) has required that the 13,000 gasoline stations in California install vapor processing equipment to become compliant with new air quality regulations. The only technology currently certified by CARB for installation in 90% of these stations is an air/vapor separation process based on amorphous perfluoropolymer membranes. This paper discusses why this class of membrane is ideal for abatement of gasoline vapor emissions and similar applications requiring the separation of volatile organic compounds from atmospheric gasses. Design of the vapor processor for optimal use of the membrane's characteristics will also be discussed.
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ICOM 2008 Oral Presentation Proceed
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Professor Yoram Cohen Professor Joh
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ICOM 2008 Staff: The University of
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ICOM 2008 Workshop Schedule: Saturd
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Monday, July 14 - Afternoon Session
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Tuesday, July 15 - Afternoon Sessio
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8:15AM 8:35AM EMS Barrer Prize (Mau
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Friday, July 18 - Morning Sessions
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Oral Presentation Abstracts Morning
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Gas Separation I - 1 - Keynote Mond
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esulting permeability selectivity o
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chain packing. To ensure a well pha
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Gas Separation I - 5 Monday July 14
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satisfactory way the corresponding
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Drinking and Wastewater Application
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an adjusted water management in the
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prospect for new energy sources as
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oxygen removal to the desired pH. C
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(Cl - , SO4 2- , As(V)) and water t
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[1] R. Lima de Miranda, J. Kruse, K
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Polymeric Membranes I - 4 Monday Ju
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Polymeric Membranes I - 5 Monday Ju
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Biomedical and Biotechnology I - 1
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Acknowledgments The Authors acknowl
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isolation of CD34+ cells was achiev
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membranes were then challenged with
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in crossflow mode operation were in
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hydroxide. For Mg/Ca = 0, the fouli
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improvement of filterability also t
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scale where fouling rates are commo
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observed in two subsequence phenome
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Membrane Modeling I - Fundamental A
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Membrane Modeling I - Fundamental A
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of the impact of the operating para
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Oral Presentation Abstracts Afterno
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Hybrid and Novel Processes I - 2 Mo
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Arora, M.B., J.A. Hestekin, S.W. Sn
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Conclusions Reverse electrodialysis
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energy recovery. This is a remarkab
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eaction with mediator due to the co
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Nanofiltration and Reverse Osmosis
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4.3x10 -6 to 7.4x10 -6 cm 2 /s. Bas
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The development of these membranes
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permeability, defined as water perm
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supports including charged (PSF/SPE
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[4] L. M. Robeson, Journal of Membr
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y conventional polymers and provide
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[3] P.M. Budd, K.J. Msayib, C.E. Ta
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Nanostructured Membranes I - 5 Mond
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Fuel Cells I - 1 Monday July 14, 2:
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investigated at first. As a result,
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Desalination I - 2 Monday July 14,
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Composite Polymeric Membrane Format
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NAMS Alan S. Michaels Award - 1a Tu
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NAMS Alan S. Michaels Award - 2 Tue
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opportunities for improving membran
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NAMS Alan S. Michaels Award - 4b Tu
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[4] K. Vanherck et al. Accepted for
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accumulation had a strong effect on
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and, if so, to develop correlations
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non-porous and porous membranes are
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[2] Palmeri, J., Sandeaux, R. Sande
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fouling. Information obtained from
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This work performed under the auspi
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etween Ru(bi-pyridine)3 2+ and meth
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[1] M. Barboiu, C. Luca, C. Guizard
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Nanostructured Membranes II - 5 Tue
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Nanostructured Membranes II - 6 Tue
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than 10 nm. XRD data suggest that t
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Pervaporation and Vapor Permeation
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ethanol/butanol (non solvent) combi
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forward osmosis, the RO process is
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Osmotically Driven Membrane Process
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References: [1] Stupp, S. I.; Lebon
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temperatures might bring about the
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References [1] S. Benita, Microenca
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solvent, were investigated (where a
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ease of manipulation as this allows
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Horizontal shrinkage does not have
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Absorption of water was determined
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Gas Separation II - 1 - Keynote Tue
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Gas Separation II - 2 Tuesday July
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concentration. These results are co
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Gas Separation II - 5 Tuesday July
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will be shown that homogeneous film
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which can adsorb on the surface of
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were collected, the viable bacteria
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pressure, and permporosimetry with
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Inorganic Membranes I - 3 Tuesday J
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Membrane Fouling - UF & Water Treat
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Membrane Fouling - UF & Water Treat
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Page 251 and 252: Membrane Modeling II - Gas Separati
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Page 329 and 330: Gas Separation IV - 2 Thursday July
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EMS Barrer Prize - 5 Thursday July
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therapy options have been modelled
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Ultra- and Microfiltration II - Pro
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in the vicinity of the rising bubbl
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of feed water ionic strength) on re
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technology that has gained growing
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Optimize polymeric membranes for sa
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Inorganic Membranes II - 2 Thursday
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confirms that the carbon dioxide pe
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permeability, stability issues comp
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Fuel Cells II - 2 Thursday July 17,
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5. Conclusion In this work, the evo
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Oral Presentation Abstracts Afterno
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an essentially pure H2 product is c
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In the presentation, we will presen
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was observed, indicative of the sim
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References Arora, M.B., J.A. Hestek
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performance of fibers is analyzed a
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Membrane Fouling III - RO & Biofoul
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[4] H. Noureddini, Book of Abstract
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component (PX, OX) separation via p
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Generally these results were in goo
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introduction of methyl groups into
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separation quality (10 µS/cm) and
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Desalination II - 3 Thursday July 1
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drop are linearly related (although
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antiscalant oxidation has been limi
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Membrane and Surface Modification I
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oth 15±5 kDa, which suggests that
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Atomic Force Microscopy (AFM), and
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y single gas permeation experiments
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PDMS toplayers were only partially
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noting that cross-linking agents co
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such extended parameter space in th
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Hybrid Membranes - 6 Thursday July
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Plenary Lecture III Friday July 18.
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Gas Separation V - 1 - Keynote Frid
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References: [1] H. Lin, E. Van Wagn
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elative contributions of Fickian di
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Gas Separation V - 4 Friday July 18
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Gas Separation V - 6 Friday July 18
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Electron Microscopy (TEM) analyses
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- Hybrid RO train: A hybrid RO trai
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concentration as well as on the sod
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scaling deposits in the DCMD device
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Silica colloidal solution with diff
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Membrane Fouling IV - RO & Desalina
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Polyacrylonitrile (PAN) UF membrane
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the polymer dope was PEI (12 wt%),
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Inorganic Membranes III - 1 - Keyno
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Inorganic Membranes III - 2 Friday
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CO2/H2 selectivity at high temperat
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ammonia complexes in aqueous soluti
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possible to have a membrane capable
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fired boiler flue gas, SOx and merc
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EPR/Ago/p-benzoquinone composite sh
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elated to the presence of free elec
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surroundings. When the temperature
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that no absorbent was detected in t
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days of filtration from 120 to 7-10
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was performed to restore membrane f
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with the SRT of 65 days, no correla
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Results Critical flux measurements
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MLSS is not directly proportional t
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Fuel Cells III - 2 Friday July 18,
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Fuel Cells III - 4 Friday July 18,
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Ultra- and Microfiltration III - Me
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can be deduced from the imaginary p
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membranes. The analysis of the ligh
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Membrane Contactors - 2 Friday July
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absorption liquid in the pores of t
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Packaging and Barrier Materials - 1
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Historically, all the approaches de
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