NAMS 2002 Workshop - ICOM 2008

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Pervaporation and Vapor Permeation III – 4 Friday July 18, 4:00 PM-4:30 PM, Kaua’i Concentration of Bioethanol By Porous Hydrophobic Membranes T. Uragami (Speaker), Kansai University, Osaka, Japan - uragami@ipcku.kansai-u.ac.jp Porous poly(dimethylsiloxane) (PDMS) membranes were prepared by freeze drying aqueous emulsions of organopolysiloxane for the concentration of aqueous solutions of dilute ethanol which are produced from the fermentation of biomass. This paper introduces the preparation of porous PDMS membranes and the development of a new membrane separation technique for the concentration of bioethanol. Porous PDMS membranes were applied to a temperature- difference controlled evapomeation (TDEV) method developed as a new membrane separation technique that can be controlled temperatures of the feed solution and the membrane surroundings. When the temperature of the feed solution was kept constant but the temperature of membrane surroundings was lowered, the ethanol/water selectivity increased remarkably and the permeation rate decreased. The ethanol/water selectivity of a porous PDMS membrane in TDEV operation was almost equal to that of a dense PDMS membrane in TDEV, however, the permeation rate of the porous membrane was higher by three orders of magnitude. The permeation and separation mechanisms for aqueous ethanol solutions through porous PDMS membranes in TDEV were discussed as follows. When water and ethanol molecules, vaporized from the feed solution, come close to the membrane surroundings kept at lower temperature in TDEV, the water vapor aggregates much easier than the ethanol vapor, because the freezing point of water molecules is much higher than that of ethanol molecules, and the aggregated water molecules tend to be liquefied as the temperature of the membrane surroundings becomes lower. On the other hand, because the PDMS membrane has a relatively high affinity to the ethanol molecules, they are sorbed inside the pores in a porous PDMS membrane and this sorbed layer of the ethanol molecules is formed in an initial stage of the permeation. The vaporized ethanol molecule may be able to permeate across the membrane by surface diffusion on the sorbed layer of the ethanol molecules inside the pores. Both the aggregation of the water molecules and the surface diffusion of the ethanol molecules in the pores are responsible for the increase in the ethanol/water selectivity through a porous PDMS membrane in TDEV. The increase of the ethanol/water selectivity in TDEV can be attributed to both the degree of aggregation of the water molecules on the membrane surroundings and the thickness of the sorbed layer of the ethanol molecules inside the pores, which are significantly governed by the temperature of the membrane
surroundings. When the temperature of the membrane surroundings becomes lower, the degree of aggregation of the water molecules and the thickness of the sorbed layer of the ethanol molecules are increased. Therefore, an increase in the ethanol/water selectivity for aqueous ethanol solutions was observed with decreasing temperature of the membrane surroundings.
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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 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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Page 487 and 488: Membrane Fouling IV - RO & Desalina
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Page 501 and 502: Inorganic Membranes III - 1 - Keyno
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Page 531 and 532: that no absorbent was detected in t
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Page 539 and 540: Results Critical flux measurements
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Page 547 and 548: Ultra- and Microfiltration III - Me
Page 555 and 556: can be deduced from the imaginary p
Page 557 and 558: membranes. The analysis of the ligh
Page 559 and 560: Membrane Contactors - 2 Friday July
Page 561 and 562: absorption liquid in the pores of t
Page 567 and 568: Packaging and Barrier Materials - 1
Page 573 and 574: Historically, all the approaches de
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NAMS 2002 Workshop - ICOM 2008

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