NAMS 2002 Workshop - ICOM 2008

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EMS Barrer Prize – 7 Thursday July 17, 9:30 AM-9:30 AM, Maui On the Origin of the Overlimiting Current in Electrodialysis M. Wessling (Speaker), University of Twente, Netherlands - m.wessling@utwente.nl The origin of the current flow above the limiting current density has been a puzzle ever since its discovery. Loss in membrane selectivity, gravitational convection, and in particular enhanced water splitting have been used as arguments to explain the occurrence of the overlimiting current. Yet another explaination is the emergence of electro-convection. This presentation reflects on these theories, but will present for the first time explicit experimental proof of the existance of electro-convection.
Ultra- and Microfiltration II - Processes – 1 – Keynote Thursday July 17, 8:15 AM-9:00 AM, Moloka’i Membrane Applications in the Pulp and Paper Industry: New Developments and Case Studies F. Lipnizki (Presenting), Alfa Laval Product Centre Membranes, Soborg, Denmark - frank.lipnizki@alfalaval.com T. Persson, Lund University, Lund, Sweden A.-S. Jönsson, Lund University, Lund, Sweden Every year, 100,000 tons of dissolved hemicelluloses are discharge unused with wastewater from thermomechanical pulp mills around the world. Isolation of these hemicelluloses from the wastewater would not only reduce the treatment costs for the pulp mills but would also provide an excellent raw material for high value applications such as oxygen barriers in food packaging. The isolation of the hemicelluloses can be combined with polishing of the wastewater by using different filtration processes. The initial step in this combination is either a drum filter or a microfiltration treatment to remove solid residues from the wastewater followed by ultrafiltration to concentrate the hemicelluloses. The permeate from the ultrafiltration can then be further polished by reverse osmosis before recycling. The focus of this paper is on the optimisation of the ultrafiltration step concentrating on the membrane selection and its impact on the process economics. The membrane selection includes the newly developed commercial UFX5 pHt membrane (Alfa Laval, Denmark) based on hydrophilised polyethersulfone. The feed studied in this paper is process water from the thermomechanical pulp mill Stora Enso Kvarnsveden (Sweden). The temperature of this process stream is 75°C. To reduce the need for cooling and preserve the energy, temperature tolerance is an important membrane selection parameter. Further, since the process water contains resin and lignin, which tend to foul membranes, the hydrophilicity of the membrane is another important selection parameter. Based on this, five membranes with molecular weight cut- offs (MWCOs) between 1 - 10 kD were pre-selected: (1) a hydrophilised fluoro polymer membrane ETNA10PP, MWCO: 10 kD, (2) a hydrophilised fluoro polymer membrane ETNA01PP, MWCO: 1 kD, (3) a hydrophilised polyethersulfone membrane UFX5 pHt, MWCO: 5 kD (all Alfa Laval, Denmark), (4) a regenerated cellulose membrane UC005, MWCO: 5 kD, and (5) a polyethersulfone membrane UP005, MWCO: 5 kD (all Microdyn-Nadir, Germany). The ETNA10PP, ETNA01PP, and UC005 are limited to a temperature of 60/55°C and to a pH range of 1 to 11, whereas the UP005 and UFX5pHt can be operated up to 75°C and in a pH range from 1 to 14/13. In the initial study, a small flat test module was used to study the pure water fluxes and the fouling behaviour of the membranes related to octanoic acid, a fouling substance which represents a significant number of small hydrophobic substances. Based on this,
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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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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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Page 297 and 298: 5. Erdodi, G.; Kennedy, J. P.; Prog
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Page 347: therapy options have been modelled
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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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