NAMS 2002 Workshop - ICOM 2008

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Drinking and Wastewater Applications I – 6 Monday July 14, 12:15 PM-12:45 PM, Maui Oxygen and Carbon Dioxide Control by Membrane Contactors in Desalination A. Criscuoli (Speaker), Institute on Membrane Technology, ITM-CNR, Italy, a.criscuoli@itm.cnr.it M. Carnevale, Institute on Membrane Technology, ITM-CNR, Italy H. Mahmoudi, Sciences & Engineering Sciences Faculty,University of Chlef, Algeria S. Gaeta, GVS S.P.A., Italy F. Lentini, GVS S.P.A., Italy S. Reggiani, GVS S.P.A., Italy E. Drioli, Department of Chemical Engineering and Materials, University of Calabria, Italy In a desalination plant the content of oxygen and carbon dioxide has to be controlled because it is responsible of corrosion problems in pipelines and of the pH and the conductivity of the water. Moreover, the pH of the water can influence the precipitation and scaling phenomena, so an adequate control becomes essential for reducing fouling issues inside the plant. Chemical agents are often used for adjusting the pH while vacuum/stripping towers have traditionally been used to remove dissolved gasses. More recently, membrane contactors have been proposed as alternative systems for water deoxygenation (particularly for the semiconductor industry and boilers). The aim of this work is to apply membrane contactors for the oxygen removal, as well as the pH control in a desalination plant. Experimental tests have been carried out in a lab set-up with a flat membrane module of 40 cm 2 of membrane area, by feeding in a countercurrent mode the liquid stream and a gas stream (consisting of CO2 or N2). The liquid stream was recycled to the module while the gas stream was sent in continuous. Different parameters have been varied, such as the temperature, the streams flow rates, the liquid composition. In particular, the liquid streams sent to the system were distilled water and synthetic solutions, prepared for simulating the reverse osmosis permeate and brine and the nanofiltration permeate. In this way, the performance of the membrane contactor in different parts of a desalination plant has been studied in terms of oxygen removal and pH variations. Five different flat hydrophobic membranes of 0.2 mm were tested and compared: PVDF, PVDF-treated, acrylic-based, PTFE and PP membranes. Before tests, all membranes have been characterized by swelling, CAM and SEM analysis. The oxygen removals were higher at higher temperatures and higher liquid flow rates, varying slightly with the gas flow rates. Higher removals were achieved for the more concentrated streams, due to the ‘salting-out effect’. Both CO2 and N2 gas streams were able to strip, in a similar extent, the dissolved oxygen from the liquid solutions. However, the final pH of the water decreased after the tests with CO2, whereas increasing or remaining constant after using N2, depending on the solution treated. This result is of extreme interest, because, depending on the specific needs, it will be possible to couple the
oxygen removal to the desired pH. Concerning the performance of membranes, the highest oxygen removal from distilled water has been obtained with the PTFE membrane; however, during tests with saline solutions the removal decreased, probably due to a reduction of the open structure, as observed by SEM. Acknowledgements The authors acknowledge the financial support of the European Commission within the 6th Framework Program for the grant to the Membrane-Based Desalination: An Integrated Approach project (acronym MEDINA). Project no.: 036997.
Page 1 and 2: ICOM 2008 Oral Presentation Proceed
Page 3 and 4: Professor Yoram Cohen Professor Joh
Page 5 and 6: ICOM 2008 Staff: The University of
Page 7 and 8: ICOM 2008 Workshop Schedule: Saturd
Page 9 and 10: Monday, July 14 - Afternoon Session
Page 11 and 12: Tuesday, July 15 - Afternoon Sessio
Page 13 and 14: 8:15AM 8:35AM EMS Barrer Prize (Mau
Page 15 and 16: Friday, July 18 - Morning Sessions
Page 17 and 18: Oral Presentation Abstracts Morning
Page 19 and 20: Gas Separation I - 1 - Keynote Mond
Page 21 and 22: esulting permeability selectivity o
Page 23 and 24: chain packing. To ensure a well pha
Page 25 and 26: Gas Separation I - 5 Monday July 14
Page 27 and 28: satisfactory way the corresponding
Page 29 and 30: Drinking and Wastewater Application
Page 35 and 36: an adjusted water management in the
Page 37: prospect for new energy sources as
Page 41 and 42: (Cl - , SO4 2- , As(V)) and water t
Page 43 and 44: [1] R. Lima de Miranda, J. Kruse, K
Page 45 and 46: Polymeric Membranes I - 4 Monday Ju
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Page 49 and 50: Biomedical and Biotechnology I - 1
Page 53 and 54: Acknowledgments The Authors acknowl
Page 55 and 56: isolation of CD34+ cells was achiev
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Page 83 and 84: Conclusions Reverse electrodialysis
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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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Drinking and Wastewater Application
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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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Oral Presentation Abstracts Morning
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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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Oral Presentation Abstracts Morning
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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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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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