NAMS 2002 Workshop - ICOM 2008

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Biomedical and Biotechnology II – 6 Wednesday July 16, 12:15 PM-12:45 PM, Honolulu/Kahuku Supported Liquid Membranes with Strip Dispersion for the Recovery of Cephalexin M. Vilt (Speaker), The Ohio State University, Columbus, Ohio, USA W. Ho, The Ohio State University, Columbus, Ohio, USA - ho@chbmeng.ohio-state.edu Cephalexin is an important and widely used semi- synthetic cephalosporin. Cephalosprorins along with penicillins are Beta-lactam antibiotics, which account for the majority of the antibiotic world market. Cephalexin is traditionally produced by a 10-step chemical synthesis. An enzymatic synthesis for Cephalexin has been developed, and offers several advantages over the classical route. The enzymatic synthesis reduces energy and solvent waste, but has been used in industrial production on a limited basis. The enzymatic reaction mixture contains Cephalexin, side products, and unconverted reactants, which are similar in structure, are difficult to separate. Liquid membranes, in particular supported liquid membranes (SLMs), are a promising solution to the separation. Reactive extraction with the quaternary ammonium compound Aliquat 336 has been demonstrated for Cephalexin and other semi-synthetic cephalosporins. SLMs are still not used industrially, as they still plagued with problem of long term instability. The SLM with strip dispersion has been a recent development to solve the issue of stability. SLM with strip dispersion can be described when an aqueous strip solution is dispersed in an organic membrane solution by a mixer, and passed on one side of a membrane support. When a microporous hydrophobic support is used, the organic phase of the dispersion becomes imbedded in the pores of the support, forming a stable SLM. Stability is maintained by having a constant supply of organic membrane solution to the pores. In this study, Cephalexin has been separated and concentrated from an aqueous solution using the SLM with strip dispersion. Experiments used a Liqui-Cel® hollow fiber module as a microporous support. The organic membrane solution of the SLM consisted of Aliquat 336, Isopar L (isoparaffinic hydrocarbon solvent), and 1- decanol. The aqueous strip solution was composed of potassium chloride and citrate buffer. The following key parameters were investigated: feed and strip dispersion flowrate, strip dispersion mixing rate, carrier concentration, counter ion concentration, pH, and volume of aqueous strip solution. High extraction and recovery rates were achieved when maintaining a proper pH in the aqueous strip solution combined with an excess of potassium chloride. An enrichment factor of up to 3.2 was observed in the aqueous strip solution while achieving over 99% extraction and 96.2% total recovery. In this case, the aqueous feed solution of
5500 ppm (15 mM) was lowered to 30 ppm when using an organic membrane solution containing 2.5% Aliquat 336. The resulting overall mass transfer coefficient was 1.6 x 10 -5 cm/sec. The mass flux of Cephalexin for this system was found to be independent of aqueous feed and strip dispersion flowrates, suggesting a major mass transfer resistance due to chemical reaction kinetics, which is supported by calculated individual mass transfer resistances. The pH of the aqueous strip phase was found to play a more significant role when trying to achieve higher enrichment ratios. It was observed that the highest stripping efficiency occurs when the pH of the aqueous strip phase is between the values of 5 and 6.
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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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Membrane Modeling II - Gas Separati
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Page 259 and 260: [10] Wang BG, Lv HL, Yang JC. Chem
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Page 317 and 318: models developed suggests that ther
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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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Membrane and Surface Modification I
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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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