NAMS 2002 Workshop - ICOM 2008

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Pervaporation and Vapor Permeation II – 4 Thursday July 17, 4:00 PM-4:30 PM, Moloka’i Study of the Effect of Framework Substitution on the Pervaporation of Xylene Isomers through MFI-type Zeolite Membranes J. O'Brien-Abraham (Speaker), Arizona State University, Tempe, Arizona, USA J. Lin, Arizona State University, Tempe, Arizona, USA - jerry.lin@asu.edu Changing conventional xylene separation techniques such as extractive or azeotrophic distillation to continuous membrane processes has been the focus of much research in recent years. Specifically, the use of pervaporation to efficiently separate p-xylene (PX) from its isomers o-xylene and m-xylene (OX, MX) has gained significant attention. The success of such technology will rely on the ability of the membrane to provide significant flux and selectivity as well as good thermal and chemical stability under desired operating conditions. Molecular sieving inorganic membranes such as MFI-type zeolite show promise for this application. MFI-type zeolite membranes possess a microporous structure consisting of sinusoidal, elliptical channels (0.51 x 0.54 nm) interconnected with straight, circular channels (0.54 x 0.56 nm). Apertures of these sizes suggest that the membranes should be able to separate xylene isomers based solely on size selectivity given that PX is the only isomer small enough to enter the zeolite pores. However, for pervaporation applications saturated feed-side coverages cause high adsorption loadings of the MFI crystals. Under these conditions, the zeolite framework molecules shift to accommodate an entropically favorable packing of the PX molecules which leads to overall distortion of the MFI pores. This distortion allows for OX to be able to enter the pore structure causing competitive adsorption between the isomers. Ultimately, these PX-framework and PX-OX interactions reduce the ability of the membrane to separate the isomers via size selectivity. Our findings show that membrane performance is highly dependent on the relative concentration of isomers in the feed; the higher the PX concentration the lower the selectivity observed. Although high selectivity (~18) was observed at low PX concentration in the feed, it was not stable over time. The focus of this work is to use membranes with isomorphously substituted framework atoms in order to induce differences in both adsorption properties and membrane microstructure. Specifically, the metal ion Boron (B) was substituted into the MFI framework for Si. Boron was chosen because of its smaller size (relative to Si) which causes a reduction in the unit cell volume; it is speculated that this may induce some structural rigidity preventing the above mentioned affect of framework distortion at high PX loadings. Additionally, because B is a trivalent atom its presence in the microstructure will introduce acid sites that can affect the membrane adsorption properties. B-ZSM5 membranes were synthesized utilizing templated seeded growth methods and characterized via xray diffraction (XRD) and scanning electron microscopy (SEM). Single and multi-
component (PX, OX) separation via pervaporation was performed at room temperature under a variety of feed compositions on both silicalite and B-ZSM5 membranes to evaluate to effectiveness of the substituted B in reducing the affects of framework flexibility and competitive adsorption at high loadings of PX.
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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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Page 375 and 376: Drinking and Wastewater Application
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Page 397 and 398: 5. Conclusion In this work, the evo
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Page 473 and 474: Electron Microscopy (TEM) analyses
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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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