NAMS 2002 Workshop - ICOM 2008

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petrochemical industries. In view of the expected growth of the SRNF market and the relatively limited number of commercial membranes, a clear need still exists to develop robust membranes to solve separation problems in existing industrial processes and open new application areas. Polar aprotic solvents (NMP, DMF, DMSO) are frequently applied in pharmaceutical and chemical processes. Chemical cross-linking with diamines allows preparing chemically stable asymmetric polyimide (PI)- based SRNF membranes that have been successfully applied in polar aprotic solvents and THF[4]. Objectives -Characterize skin layer thicknesses, densities, differences in porosity and porosity evolution between skin layers and sublayers of of polyimide (PI)based membranes prepared by phase inversion with PA(L)S. -Correlate the information obtained through PA(L) S with performance data in laboratory-made and commercial PI membranes (Starmem") and other characterization techniques to study the influence of synthesis parameters (polymer concentration, evaporation time) and post- treatment conditions (chemical crosslinking) on the performance of asymmetric PI (P84) based membranes in filtrations of Rose Bengal (RB, 1017 Da) in 2-propanol (IPA), DMF and THF. Results and discussion As expected, an increase of the initial polymer concentration in the casting solution, containing P84 in a NMP/THF mixture improves RB retention but decreases the permeability. It can be related, to the formation of a denser skin layer, also observed from PAS profiles and confirmed by SEM. Increasing the evaporation time prior immersion in the coagulation bath drops IPA and THF permeabilities but no significant changes in the RB retention were observed. The longest evaporation times have no effect in performance and no differences were observed in PAS profiles. For membranes chemically crosslinked, a 90% flux drop was noticed as compared to uncross-linked ones together with better retentions. Solvent fluxes followed the order THFDMFHIPA. The chemical cross-linking involves the transformation of imide bonds to amide bonds, reducing the interstitial space among chains and thus the free volume, which results in a decrease in the top layer thickness, as confirmed by PAS. Conclusions laboratory-prepared P84-based SRNF membranes showed higher fluxes compared to the commercial ones. From the analysis of profiles of the energy of annihilation, differences in porosities between top and support layers in membranes and different evolution from the skin layer to the mesoporous regions can be estimated and be related to the performance results from filtration experiments. References [1] K. Boussu at al. ChemPhysChem 2007, 8, 370. [2] H. Chen et al. Macromolecules 2007, 40, 7542. [3] P. Vandezande et al. Chem. Soc. Rev. <strong>2008</strong>, 37, 365.
[4] K. Vanherck et al. Accepted for publication in J. Membr. Sci.
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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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Page 115 and 116: investigated at first. As a result,
Page 117 and 118: Desalination I - 2 Monday July 14,
Page 127 and 128: Composite Polymeric Membrane Format
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Page 139 and 140: opportunities for improving membran
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Page 147 and 148: Nanofiltration and Reverse Osmosis
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Page 159 and 160: [2] Palmeri, J., Sandeaux, R. Sande
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Page 167 and 168: [1] M. Barboiu, C. Luca, C. Guizard
Page 169 and 170: Nanostructured Membranes II - 5 Tue
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Page 173 and 174: than 10 nm. XRD data suggest that t
Page 175 and 176: Pervaporation and Vapor Permeation
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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 Modeling II - Gas Separati
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[10] Wang BG, Lv HL, Yang JC. Chem
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Membrane and Surface Modification I
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Gas Separation III - 1 - Keynote We
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Gas Separation III - 2 Wednesday Ju
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separation was next blended with di
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Polymeric Membranes II - 1 - Keynot
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Polymeric Membranes II - 3 Wednesda
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5. Erdodi, G.; Kennedy, J. P.; Prog
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observed for different locations in
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Biomedical and Biotechnology II - 3
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applied in the first two fields wil
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distribution of SBMA units within t
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5500 ppm (15 mM) was lowered to 30
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increasing the effective size of th
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etween 0 and 1), the automatic feed
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Membrane Modeling III - Process Sim
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Membrane Modeling III - Process Sim
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models developed suggests that ther
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start level has a huge impact on th
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Ultra- and Microfiltration I - Tran
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all three binary protein UF systems
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Synthetic solutions of ±-lactalbum
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Gas Separation IV - 2 Thursday July
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6. T. C. Merkel, Z. He, I. Pinnau,
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EMS Barrer Prize - 1b Thursday July
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EMS Barrer Prize - 3 Thursday July
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EMS Barrer Prize - 4b 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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Pervaporation and Vapor Permeation
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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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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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