NAMS 2002 Workshop - ICOM 2008

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Facilitated Transport Membranes – 4 Friday July 18, 11:15 AM-11:45 AM, Wai’anae CO2 Capture: Reduction in Greenhouse Gas Levels D. Smith, Carbozyme, Inc., Monmouth Junction, New Jersey, USA R. Cowan, Carbozyme, Inc., Monmouth Junction, New Jersey, USA M. Trachtenberg (Speaker), Carbozyme, Inc., Monmouth Junction, New Jersey, USA - mct@cz-na.com Separation of flue gas carbon dioxide (CO2) from natural gas, petroleum or coal fired furnaces is the single most difficult and expensive step (>65% of total) in the capture-transport-geologic storage scenario proposed by national and international organizations focused on control of greenhouse gases. The object, as laid out by the DOE National Energy Technology Laboratory (NETL), is to extract 90% of the CO2 to yield 95% purity with an energy penalty of less than 20% for the stream derived from combustion of pulverized coal and to have the scalability to manage a gas flow of thousands of cubic meters (hundreds of thousands of cubic feet) each day. We have been developing an enzyme-based, contained liquid membrane (CLM), dual hollow fiber permeator for this purpose. The key next step is progressive scale up of this design and testing with actual flue gas under development facility conditions in anticipation of later, yet larger, pilot scale field trials. The design and operation of the permeator is critical to maximizing performance. However, a multiple hollow fiber design of the type we developed has not been demonstrated before nor has it been manufactured commercially. Key elements to successful design are: " Thermal regulation as the evaporation of large quantities of water will affect operating temperature. Control of this temperature by circulating the CLM will affect system selectivity and CO2 recovery. Lack of control of this temperature will result in condensation within the hollow fibers and/or membrane pores. " Uniformity of thermal management effects driving forces for system flow. " Permeate pressure control is necessary to minimize the energy burden imposed by the capture system. However this will effect CO2 recovery and have an effect on selectivity. Each of these issues has now been addressed. Process engineering studies and system simulations provide the basis for size selection. Modeling of the effect of pulverized coal fired flue gas components on the CLM has been carried out to determine the flue gas component acceptance values as well as the preferred gas flow rates, pressure and temperature. Modeling has been used to design post-capture treatment to provide a stream that satisfies pipeline acceptance values. Primary interest is on the micro components of PC
fired boiler flue gas, SOx and mercury. These components will have significant effects on the permeator function and there control before admission to the permeator is important. Acceptance criteria for them have been established. To date, using smaller, laboratory scale devices, we have studied both analog (ersatz) streams and flue gas derived from combusting methane or propane. The feed gas CO2 concentration ranged from 0.05- 40% in air, and 6%-13% derived from burning hydrocarbon fuels. Feed gas source or composition did not affect CO2 permeance. The solubility of each non-reactive gas in the solvent liquid alone determined the specific permeance and thus the selectivity. For coal (natural gas) feed streams will contain about 13.8% (3.5%) CO2; the retentate, returned to the stack, are expected to contain 1.6% (0.4%) CO2, while the dry compressed product is 94.9% (89%) CO2 for a given permeator design. We are in process of determining the actual operation values. The status will be discussed.
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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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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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Page 473 and 474: Electron Microscopy (TEM) analyses
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Page 539 and 540: Results Critical flux measurements
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Packaging and Barrier Materials - 1
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Historically, all the approaches de
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