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IntroductionThe combination of membrane filtration technology with biological processes forwastewater treatment is the origin of membrane bioreactors (MBR) and also tertiarymembrane filtration (TMF), which are the two major applications for low-pressuremembranes within wastewater treatment (Gallagher et al., 2008).The ability to attach a physical process of filtration in conjunction with a biologicalwastewater treatment allows combining the individual advantages of each one of thetechniques, giving also a synergy between the two technologies, resulting in clearimprovements in the overall treatment process. First, biological treatment can remove notonly most of the organic matter but nutrients working in the proper configuration. Moreover,filtration process allows to obtain a permeate of excellent quality, with negligible amountsof suspended solids and organic matter, and the absence of microorganisms, viruses andfecal coliforms. In general, the permeate obtained not only meets the current dischargelimits, it encourages reuse applications such as irrigation, heating or cooling water or forcleaning purposes. Moreover, the use of membrane technology (MF or UF) has beenshown to be the ideal pre-treatment for RO in water reclamation and even seawaterdesalination (Côté et al., 2005).1.2. Membrane configuration and characteristicsMembrane geometry and the way it is mounted and oriented in relation to the flow ofwater, is crucial in determining the overall process performance. There are mainly threeconfigurations that are currently used to manufacture membranes for MBR or TMFapplications (figure 1.2). These configurations are based on both flat and cylindricalgeometries and include hollow fiber, flat sheet, and tubular. It is very common to havemultiple membrane elements to form a multi-tubular module (MT), a flat sheet module (FS)or a hollow fiber module (HF).The production of permeate in HF or FS membranes occurs from outside to inside byaspiration (being the shell-side in contact with the mixed liquor), while in tubularmembranes the filtration takes place from inside to outside by introducing the mixed liquoralong the lumen of the membrane, (being the shell-side in contact with the permeate)(figure 1.3).31
Chapter 1ABCAgua residualAgua residualAgua residualEfluenteEfluenteRecirculaciónde lodosRecirculaciónde lodosRecirculaciónde lodosReactor delodos activosClarificadorReactor delodos activosClarificador Reactor delodos activosExcesode lodoExcesoMezcla aire fresco/ contaminadode lodoExcesoMezcla aire fresco/ contaminadode lodoFigure 1.2. Pictures of Flat sheet (A), hollow fiber (B) and tubular (C) membranes.Mezcla aire fresco/ contaminadoa b cFigure 1.3. Schematics showing flow through membrane configured as: flat sheet (a),hollow fiber (b) and tubular (c).The main considerations that have to be taken into account with respect a membranemodule are (Judd, 2011): a high membrane area to module bulk volume ratio, a high degree of turbulence for mass transfer promotion on the feed side, a low energy expenditure per unit product water volume, a low cost per unit of membrane area, a design that facilitates cleaning and modularization.Membranes can be also classified attending to the material they are constructed within organic polymeric membranes, ceramic membranes and metal membranes, althoughthe use of metal membranes in MBR is rare due to their high cost.32
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TEP (mgXG·L -1 )Chapter 22.4.4.4.
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Chapter 2Ripley, L.E., Boyle, W.C.,
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Chapter 33.1. IntroductionIn recent
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Chapter 3same in both modules; tap
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Chapter 3phases were varied (table
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Chapter 3to time was higher than 10
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COD removal (%)Chapter 3120100Perio
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DTN and N-NH 4+ (mg·L-1 )DTN and N
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Chapter 3operated with high MLTSS c
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TMP (kPa)TMP (kPa)TMP (kPa)TMP (kPa
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SMP carbohydrates (mg·L -1 )Chapte
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Volume (%)Chapter 3Therefore, the c
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Chapter 3identical to that of the c
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Chapter 3Massé, A. Spérandio, M.,
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Chapter 44.1. IntroductionThe appli
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Chapter 4support were added in this
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Chapter 4This cleaning was performe
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COD (mg·L -1 )COD removal (%)OLR (
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Chapter 4the recirculation ratio be
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(mg·L -1 )Chapter 4and ammonium) n
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Chapter 4recirculation from the MBR
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Chapter 4days 57 (period I) and 316
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Chapter 4excellent COD removal perf
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Chapter 4Rosenberger, S., Evenblij,
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Chapter 55.1. IntroductionAnaerobic
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Chapter 55.3. Material and methods5
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Chapter 5represented an increment o
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Chapter 5operating with similar mem
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Chapter 5behaviour might be related
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Fouling Rate (Pa·min -1 )Fouling R
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Concentration (mg·L -1 )DOC (mg·L
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Chapter 5in table 5.3 showed that h
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Chapter 5Ho, J., Sung, S. 2010. Met
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Chapter 6Denitrification with disso
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Denitrification with dissolved meth
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(mg·L -1 )Denitrification with dis
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DTN effluent (mg·L -1 )CH 4 desorb
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Chapter 7Membrane fouling in an AnM
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Membrane fouling in an AnMBR treati
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OLR and ORR(kgCOD ·m -3·d -1 )pHO
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TEP removed (mg·L -1 )OA removed (
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R col (m -1 )SRF (m·kg -1 )Membran
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BPC, cBPC and TEP concentration(mg
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Cake and Colloidal Resistance (m -1
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Conclusionessentido, el uso de una
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Conclusionesensuciamiento de la mem
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Conclusiónspresenza de soporte de
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Conclusións6. Aplicabilidade e per
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ConclusionsMoreover, biomass concen
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Conclusionstechnology and interesti
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List of symbolsHFHRTHyVABHollow Fib
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List of symbolsFR/J Normalized Foul
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List of publicationsBrand, C., Sán
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List of publicationsConference on E
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