NAMS 2002 Workshop - ICOM 2008

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crosslinking agents, citric acid, oxalic acid and maleic acid, and different temperatures: 60, 80, 100 and 150°C. The characterization of the crosslinked PVA was performed by DSC, TGA and FTIR analysis, as well as water swelling degree. Ultrafiltration poly(ether sulfone) hollow fibers with cut-off of 50 kDa were used as porous support for a selective layer of PVA. The composite fibers were characterized by SEM and by permeation of sodium sulfate solution in a lab setup. The transport properties in combination with morphological analysis allow establishing criteria for selection of the best conditions to prepare PVA composite membranes for RO and NF processes. The results with these composite membranes showed salts rejection were around 95%. To evaluate the chlorine resistance, PVA films were analyzed by FTIR after immersion in chlorine solution. Results indicate that it is a promising method to produce chlorine resistant membranes.
Composite Polymeric Membrane Formation – 5 Monday July 14, 4:30 PM-5:00 PM, Waialua Experimental Verification of Effect of Support on Membrane Performance R. Takagi (Speaker), Shukugawa Gakuin College, Nishinomiya, Japan, takagi@shukugawac.ac.jp A. Pihlajamäki, Lappeenranta University of Technology, Lappeenranta, Finland T. Shintani, Nitto Denko Corporation, Osaka, Japan M. Nyström, Lappeenranta University of Technology, Lappeenranta, Finland Generally, a membrane is a composite, made by forming a skin layer on a support. The ion permeability coefficient of the support is generally different from that of the skin layer. Thus, the characteristic properties of the support also affect membrane performance. The effect of the support on the membrane performance has been theoretically studied. It is already reported that the variation of membrane charge, pore radius, porosity and thickness of the support affect the ion flux and, then, affect the rejection of the membrane. It is very important to know the effect of the support on the membrane performance to design a new membrane. Unfortunately, it is very difficult to verify the effect of the support experimentally. It will be possible to verify the effect of the support experimentally, if the characteristic properties of the skin layer and the support are known separately. It is possible to characterize the support as a separate membrane experimentally. However, it is very difficult to experimentally characterize the skin layer as a separate membrane, since the skin layer is very thin and it is almost impossible to obtain the skin layer as a separate membrane. In this paper, a potential way to experimentally verify the effect of the support is discussed. The composite membrane will be asymmetric with respect to membrane charge, since the porosity and the pore radius of the support are different from those of the skin layer. It is theoretically reported that the membrane potential of the asymmetric membrane with respect to membrane charge varies by changing the membrane setting from (bulk solution 1|skin layer | support | bulk solution 2) to (bulk solution 1| support | skin layer | bulk solution 2). The membrane potential is an electric potential difference generated between the bulk solutions when the membrane separates two bulk solutions with different concentration of electrolyte or different kind of electrolyte. Then, if the skin layer and the support are homogeneously charged and the membrane potential of the composite membrane varies by changing the membrane setting, it shows that the membrane is asymmetric with respect to membrane charge. It means that the effect of the support is not negligibly small and that the support affects the membrane performance.
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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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Page 83 and 84: Conclusions Reverse electrodialysis
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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 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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[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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Nanofiltration and Reverse Osmosis
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Nanofiltration and Reverse Osmosis
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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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