NAMS 2002 Workshop - ICOM 2008

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Hybrid and Novel Processes I – 4 Monday July 14, 4:00 PM-4:30 PM, Kaua’i Power Generation by Reverse Electrodialysis P. Dlugolecki (Speaker), University of Twente, Wetsus, The Netherlands, piotr.dlugolecki@wetsus.nl K. Nymeijer, University of Twente, The Netherlands S. Metz, University of Twente, Wetsus, The Netherlands M. Wessling, University of Twente, The Netherlands Introduction Membrane technology provides an opportunity to gain sustainable energy from salinity gradients via reverse electrodialysis [1-4] . RED can be applied where two solutions of different salinity gradient mix, e.g. where river water flows into the sea. Ion-exchange membrane properties (resistance, selectivity, ion exchange capacity, structure and thickness) affect the performance of the RED process. Up to now it is not known which membranes properties are important for the RED process. Therefore, we determined the membrane properties of several commercial membranes and compared them for their RED performance with a theoretical model [4] . Theory In RED, a concentrated salt solution and a fresh water are brought into contact through an alternating series of anion exchange membranes (AEM) and cation exchange membranes (CEM). Anions migrate through the AEM towards the anode and cations move through the CEM towards the cathode. The difference in chemical potential between both solutions is the driving force for this process. Electrons migrate from anode to cathode through an external electrical circuit in order to maintain electro-neutrality in the cathode and anode compartment. This electron migration can be used to generate electrical power. The theoretical value of the chemical potential for an aqueous monovalent electrolyte can be calculated using the Nerst equation. Results and discussion The theoretical membrane model for reverse electrodialysis was used to predict the theoretical power density obtainable using experimental membrane characterization data. Results show that large increases in power density can be obtained by decreasing the membrane resistance and the thickness of the river water compartment. Improvement of membrane properties has only a significant effect if such small membrane spacing is applied. When the membrane spacing is 150µm the membrane resistance becomes a dominant factor to generate energy. When 600µm spacer was applied the membrane selectivity seems to play an equal role with the membrane resistance. However, with this stack configuration membrane performance has less influence on obtained power density. According to membrane model is feasible to reach the power density up to 5 W/m 2 with commercial available membranes. Tailor-made membranes can improve this performance even further more.
Conclusions Reverse electrodialysis is a non-polluting, sustainable technology to generate direct electricity from the mixing of fresh and salt water. The ion exchange membranes are the key elements in RED. Based on the results, the best benchmarked commercially available anion exchange membranes reach a power density of more than 5 W/m 2 whereas the best cation exchange membranes show a theoretical power density of more than 4 W/m 2 . According to the membrane model calculations power densities higher than 6 W/m 2 could be obtained by using thin spacers and tailor made membranes with low membrane resistance and high permselectivity especially designed for reverse electrodialysis. This makes RED a potentially attractive and alternative for sustainable energy production. Reference 1. R.E. Pattle, Production of Electric Power by mixing Fresh and Salt Water in the Hydroelectric Pile, Nature, 174 (1954) 660. 2. J.W. Post, J. Veerman, H.V.M. Hamelers, G.J.W. Euverink, S.J. Metz, K. Nymeijer, C.J.N. Buisman, Salinity-gradient power: Evaluation of pressure- retarded osmosis and reverse electrodialysis, Journal of Membrane Science, 288 (2007) 218. 3. J. Veerman, J.W. Post, M. Saakes, S.J. Metz, G.J. Harmsen, Reducing power losses caused by ionic shortcut currents in reverse electrodialysis stacks by a validated model, Journal of Membrane Science, 310 (<strong>2008</strong>) 418-430. 4. P. Dlugolecki, K. Nymeijer, S. Metz, M. Wessling, Current status of ion exchange membranes for power generation from salinity gradients, Journal of Membrane Science, (<strong>2008</strong>) Submitted. 5. J.N. Weinstein, F.B.J.W. Leitz, Electric power from differences in salinity: the dialytic battery, Science, 191 (1976) 557.
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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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Page 49 and 50: Biomedical and Biotechnology I - 1
Page 53 and 54: Acknowledgments The Authors acknowl
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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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Nanofiltration and Reverse Osmosis
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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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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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