NAMS 2002 Workshop - ICOM 2008

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were found to show significantly high permeance (1x10 -5 mol m -2 s -1 Pa -1 ) and high selectivity of H2/SF6 (> 1,000). [1] T. Tsuru, J. Sol-Gel Sci. Tech., in press. [2].T. Tsuru, T. Morita, T. Yoshioka, J. Membr. Sci., in press. [3] R. Igi, T. Yoshioka, Y. Ikuhara, Y. Iwamoto, T. Tsuru, J. Am. Cer. Soc., submitted.
Inorganic Membranes III – 2 Friday July 18, 10:15 AM-10:45 AM, O’ahu/Waialua Development of Novel CO2 Affinity-Enhanced Carbon Membranes: Characterization and CO2 Separation Performance T. Kai (Speaker), Research Institute of Innovative Technology for the Earth (RITE), Kyoto, Japan S. Kazama, Research Institute of Innovative Technology for the Earth (RITE), Kyoto, Japan - kazama@mvc.biglobe.ne.jp Y. Fujioka, Research Institute of Innovative Technology for the Earth (RITE), Kyoto, Japan The concentration of carbon dioxide (CO2), a greenhouse gas, has been increasing in the atmosphere. Several methods have been devised to reduce the amount of CO2 emissions into the atmosphere. Among them, the sequestration of CO2 underground or in the oceans is regarded as one of the promising means to mitigate carbon dioxide emissions. One problem with the sequestration is the cost of recovering CO2 from emissions. For example, chemical absorption, the best-known method of separating and recovering CO2 to date, accounts for more than seventy percent of the entire cost of carbon sequestration. One promising means to lower the cost of CO2 separation is the development of new, high- performance CO2 separation membranes that allow efficient CO2 recovery. It is well known that carbon membranes shows good CO2/N2 separation performance. To obtain higher separation performance using carbon membranes, it is very important to control CO2 affinity on the pore surface as well as pore size control. In this presentation, we will report on development of novel carbon membranes with enhanced CO2 affinity for CO2 separation to obtain higher CO2 separation performance by incorporating CO2 affinity materials in the pores of the carbon membranes. Polyimide was chosen as the precursor for carbon membranes. Tubular porous a-alumina membrane (pore diameter: 150nm (symmetric), Outer- diameter: 10mm, inner-diameter: 7mm)) was purchased from Noritake Co., Limited., Japan, and was used as the porous support. The precursor solution was coated on the outer surface of the alumina support by the dip-coating method. After drying, the precursor-coated membrane was carbonized under a N2 atmosphere at 600 degrees centigrade for 3 hours. Alkali metal carbonates (Na2CO3, K2CO3, Rb2CO3, Cs2CO3) and an amine (DL- 2,3-Diaminopropionic acid hydrochloride (DAPA)) were chosen as a CO2 affinity materials. Two preparation methods were examined; Method A (Blend CO2 affinity materials with precursor solution) and method B (Post-treatment, Dip- coating of carbon membranes). From EDX spectra of the surface of Cs2CO3- incorporated carbon membrane (method A), it was confirmed that the amount of incorporated Cs2CO3 increased
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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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Page 473 and 474: Electron Microscopy (TEM) analyses
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Page 487 and 488: Membrane Fouling IV - RO & Desalina
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Page 511 and 512: CO2/H2 selectivity at high temperat
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Page 539 and 540: Results Critical flux measurements
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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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