NAMS 2002 Workshop - ICOM 2008

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Nanofiltration and Reverse Osmosis II - Imaging and Characterization – 7 Tuesday July 15, 12:00 PM-12:30 PM, Maui Characterization of the Polyamide Active Layer in NF/RO Membranes Using Gold Nanoparticles F. Pacheco (Speaker), Stanford University, Stanford, CA, USA, fpacheco@stanford.edu M. Reinhard, Stanford University, Stanford, CA, USA J. Leckie, Stanford University, Stanford, CA, USA The goal of this project was to investigate the deposition of nanoparticles during filtration to better understand how transport and rejection mechanisms occur within the active layer of a RO membrane. The active layer in state of the art RO membranes consists of cross-linked networks of fully aromatic polyamide, with an average thickness of approximately 200 nm and a very heterogeneous structure that confers the membrane a relatively rough surface, also described in the field as the peak-and-valley structure. Because of the thinness of this layer, characterization at the microscale is extremely difficult and as result knowledge of the transport and separation mechanisms is incomplete. Experiments were performed with gold nanoparticles in a dead-end filtration system without stirring at a pressure of 4.8 bar (70 psi). The membrane investigated was a commercial low pressure RO membrane with a fully aromatic polyamide layer featuring the characteristic peak- and-valley rough structure. The ability to separate the polyamide layer from the underlying polysulfone support was used to develop a novel TEM based technique that allowed us to image the spatial distribution of the gold nanoparticles with respect to the projected surface area of the polyamide layer. The resulting images show that the particles did not accumulate uniformly over the surface of the membrane, but instead formed distinct clusters around the areas where the polyamide layer was the thickest, i.e. the areas near the peaks. TEM images of polyamide cross sections, as well as SEM images of the membrane surface, confirmed that the particles accumulated preferentially on the peaks rather than in the valleys of the polyamide structure. Although the deposited nanoparticles only covered about 30% of the projected surface area of the membrane, water flux was significantly reduced. These results suggest that there are areas within the polyamide layer that have higher permeability to water and that are the most sensitive to fouling. The effects of particle size and concentration, pH and ionic strength were investigated. The use of nanoparticles in combination with advanced microscopic imaging techniques can be used to examine which sections of the polyamide layer in NF and RO membranes are actively involved in the transport and rejection mechanisms, as well as those that are highly sensitive to the initial stages of
fouling. Information obtained from these experiments can also be useful to better understand how membranes will perform with feeds containing other kinds of nanoparticles.
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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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Page 115 and 116: investigated at first. As a result,
Page 117 and 118: Desalination I - 2 Monday July 14,
Page 127 and 128: Composite Polymeric Membrane Format
Page 135 and 136: NAMS Alan S. Michaels Award - 1a Tu
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Page 139 and 140: opportunities for improving membran
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Page 151 and 152: [4] K. Vanherck et al. Accepted for
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Page 169 and 170: Nanostructured Membranes II - 5 Tue
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Page 173 and 174: than 10 nm. XRD data suggest that t
Page 175 and 176: Pervaporation and Vapor Permeation
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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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Pervaporation and Vapor Permeation
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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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