NAMS 2002 Workshop - ICOM 2008

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y high concentrations of COD, heavy metals, oil and surfactants. Furthermore, the widespread application of biocides during various production processes resulted in unfavorable COD/BOD ratios between 7 and 10. Thus, a biological treatment was impossible and the investigated concepts were based on pressure driven membrane processes in crossflow mode. In a comprehensive lab-scale study a coagulation agent and a membrane screening was conducted. Furthermore optimal process conditions in terms of permeate quality and filtration performance and the effect of various influencing factors (e.g. temperature, pH) were determined. To prove these lab-scale findings and to evaluate the filtration performance and operational reliability a set of different pilot plants was installed and operated over a period of 6 months: -An ultrafiltration plant with polymeric membranes (total membrane area: 15 m²) treating the collected wastewater from the paint shop -An ultrafiltration plant with ceramic membranes (total membrane area: 7 m²) treating the collected wastewater from the mechanical production areas -A nanofiltration plant treating the process water of the phosphating department within the pre-treatment of the paint shop -A reverse osmosis plant for the advanced treatment of the nanofiltration permeate -An ultrafiltration plant treating the process water of the degreasing step within the paint shop pre-treatment -An ultrafiltration plant treating the rinsing bath water of the degreasing step within the paint shop pre-treatment Results The results revealed a better performance of the ceramic ultrafiltration plant in comparison to the polymeric ultrafiltration plant characterized by lower total filtration resistances and comparable retention properties. Due to the high fouling potential of the wastewater submerged hollow fibre membranes (PURON®, Koch Membrane Systems, Germany) were irreversibly blocked after the production of 2.2 m³ permeate per m² membrane area. Porous ultrafiltration membranes in combination with pre-coagulation are able to reduce the heavy metal content to a level below the environmental legislation. The molar mass distribution of the wastewater showed the largest fraction (> 90%) with a molar mass lower than 1,500 Da. This finding was proved by the incomplete COD retention of the crossflow- ultrafiltration. Therefore advanced treatment processes (powdered activated carbon, nanofiltration) to decrease the organic content as a prerequisite for the recirculation into the process were investigated and the results will be presented. The production integrated nanofiltration within the phosphating department provided a sufficient removal of heavy metals. The organic content (TOC) was identified as remarkable parameter affecting the filtration performance adversely. Overall a broad set of data was generated and allows the presentation of a quantitative comparison of different membrane-based treatment technologies for
an adjusted water management in the automotive industry with respect to permeate quality, process performance and economical feasibility.
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 31 and 32: Drinking and Wastewater Application
Page 33: Drinking and Wastewater Application
Page 37 and 38: prospect for new energy sources as
Page 39 and 40: oxygen removal to the desired pH. C
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
Page 47 and 48: Polymeric Membranes I - 5 Monday Ju
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
Page 59 and 60: membranes were then challenged with
Page 61 and 62: in crossflow mode operation were in
Page 63 and 64: hydroxide. For Mg/Ca = 0, the fouli
Page 65 and 66: improvement of filterability also t
Page 67 and 68: scale where fouling rates are commo
Page 69 and 70: observed in two subsequence phenome
Page 71 and 72: Membrane Modeling I - Fundamental A
Page 73 and 74: Membrane Modeling I - Fundamental A
Page 75 and 76: of the impact of the operating para
Page 77 and 78: Oral Presentation Abstracts Afterno
Page 79 and 80: Hybrid and Novel Processes I - 2 Mo
Page 81 and 82: Arora, M.B., J.A. Hestekin, S.W. Sn
Page 83 and 84: 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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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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