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Cake and Colloidal Resistance (m -1 )SRF (m·kg -1 )Membrane fouling in an AnMBR treating industrial wastewater at high total solids concentrationslayer. Moreover, their size can clog membrane pores, particularly in the case ofmicrofiltration membranes.1.6E+147E+161.4E+141.2E+141E+148E+136E+134E+132E+1306E+165E+164E+163E+162E+161E+1600 50 100 150 200Time (d)Figure 7.9. Evolution of specific R Cake resistance R to colloidal filtration (•) and SRF resistances of cake ()and colloidal fractions (▲). Dashed line represents the day when PAC addition in thereactor took place.The resistance of the colloidal fraction in the mixed liquor was always around 40% ofthe cake resistance. Therefore, according to the results obtained in batch experiments(figure 7.7), a certain improvement on membrane performance might be expected whenPAC was added to the AnMBR mixed liquor. Choo and Lee (1996) suggested that theaddition of an adsorbent or a coagulant could enhance permeate flux by agglomerating thefine colloids, present in the mixed liquor, forming larger particles that have a lowertendency to foul membranes. Although this effect was observed during batch experiments,it did not occur when the PAC was added to the AnMBR, and colloidal fraction resistancewas not positively affected. The main hypothesis of such behavior was related with thepresence of a compact sticky layer over the membrane surface observed when themembrane module was replaced on day 76. The module was submerged in water and thepermeability before and after removing the cake by rinsing with tap water (no chemicalcleaning) was evaluated. It was observed that the permeability before removing the cakewas around the 10% of the permeability after doing it (350 L·m -2·h -1·bar -1 ). Considering that189
Chapter 7measured permeability of the new membrane module was 500 L·m -2·h -1·bar -1 , it can beassumed that the main membrane fouling mechanism was cake layer formation. This cakelayer acted like a shield, protecting the membrane from internal pore blocking. Therefore,the high MLTS concentration led to the formation of a dense sticky cake layer that cloggedthe membrane, and the SGD m applied, which was lower than the recommended value ofthe full scale module, did not help to alleviate its effect.Sludge properties, including biopolymer concentration, are the core parameters ingoverning sludge cake formation and membrane fouling in submerged AnMBR systems(Lin et al., 2009). The characteristics of the mixed liquor in an AnMBR are expected to varysignificantly based on the type of wastewater being treated (Kataoka et al., 1992). Inaddition, inorganic fouling should not be underestimated when treating complexwastewaters such as industrial herbal extraction wastewater since Inorganic species caninteract with biopolymers in the reactor and enhance the mechanical stability of the foulinglayer (Lin et al., 2009). The high COD concentration in the effluent led to increase MLTSconcentration in order to achieve higher removal capacities. However, COD removal wasonly slightly improved due to the poor anaerobic biodegradability of the wastewater butmembrane performance was seriously limited.The existence of a threshold value (30 g·L -1 ) above which the MLTS concentrationhas a negative influence on membrane filtration has been reported (Yamamoto et al. 1994;Lubbecke et al., 1995; Hong et al., 2002). In accordance with this studies, Robles et al.(2013) recently established a MLTS critical value between 28 and 31.5 g·L -1 for an AnMBRtreating municipal wastewater. Operation above this critical value would lead to lowerfluxes and shorter membrane lifespan. Therefore, the MLTS concentrations, between 38and 61 g·L -1 , achieved during the operation led to the severe fouling of the membrane andthe futility of PAC addition.In order to achieve higher membrane fluxes it would be recommended to diminishMLTS concentration below 25 g·L -1 . In this scenario, PAC addition might influence sludgefilterability and enhance membrane performance.Nevertheless, with the proposed treatment, COD values were much higher that theallowed threshold value for direct or indirect discharge. Therefore an aerobic treatmentstep has to be established. A combination of another high strength anaerobic system suchas an upflow anaerobic sludge blanket reactor (UASB) with an aerobic MBR would achievehigher COD removals, allowing to apply higher membrane fluxes as reported in Chapter 5(Sánchez et al., 2013).190
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UNIVERSIDAD DE SANTIAGO DE COMPOSTE
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padres Macario y Marisa, les agrade
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2.1.2. Nitrogen compounds 662.1.2.1
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Chapter 4: Combining UASB and MBR f
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Objetivos y resumenEsta tesis se en
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Objetivos y resumenpermeabilidad de
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Objetivos y resumenuno de los pará
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Objetivos y resumenel sistema propu
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Objetivos y resumenconcentraciones
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Obxectivos e resumoauga tratada. O
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Obxectivos e resumoNo Capítulo 3,
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Obxectivos e resumog·L -1 , valore
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Obxectivos e resumoparámetros clav
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Objectives and summaryThis thesis i
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Objectives and summaryOn the basis
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Objectives and summaryfrom the MBR
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Objectives and summaryconsidering t
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Chapter 1IntroductionSummaryIn this
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IntroductionThe combination of memb
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IntroductionThe membranes should ha
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Introductionof water. Energy saving
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number of plants (cum. values)Intro
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IntroductionSubmerged MBR system in
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Introductionchanges of the foulant
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Introductionof 2% NaOH and 0.5% cit
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IntroductionFigure 1.8. Posible rel
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IntroductionSide-stream MBRs involv
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Introductionutilizes the advantages
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Introductionmeans of settlers, of s
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IntroductionUASB, achieving total n
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IntroductionEvenblij, H., van der G
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IntroductionMtinch, E.V., Ban, K.,
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IntroductionYang, S., Yang, F., Fu,
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Chapter 22.1. Liquid phaseIn this s
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Chapter 2where:M fas: molarity of F
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Acetic Acid (mg·L -1 )Chapter 2VFA
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N-NO 2-(mg·L -1 )Chapter 22.1.2.2.
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N-NO 3-(mg·L -1 )Chapter 2interfer
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P-PO 43-(mg·L -1 )Chapter 2Interfe
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Chapter 2alkalinity (IA), which is
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Chapter 22.2.3. Sludge volumetric i
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Chapter 2eq. 2.10eq. 2.11eq. 2.12Th
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Carbohydrate (mg·L -1 )Chapter 2In
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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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Page 153 and 154: Fouling Rate (Pa·min -1 )Fouling R
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Page 159 and 160: Chapter 5Ho, J., Sung, S. 2010. Met
Page 162 and 163: Chapter 6Denitrification with disso
Page 164 and 165: Denitrification with dissolved meth
Page 174 and 175: (mg·L -1 )Denitrification with dis
Page 176 and 177: DTN effluent (mg·L -1 )CH 4 desorb
Page 186 and 187: Chapter 7Membrane fouling in an AnM
Page 188 and 189: Membrane fouling in an AnMBR treati
Page 194 and 195: OLR and ORR(kgCOD ·m -3·d -1 )pHO
Page 196 and 197: TEP removed (mg·L -1 )OA removed (
Page 198 and 199: R col (m -1 )SRF (m·kg -1 )Membran
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Page 211 and 212: Conclusionessentido, el uso de una
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Page 217 and 218: Conclusións6. Aplicabilidade e per
Page 219 and 220: ConclusionsMoreover, biomass concen
Page 221 and 222: Conclusionstechnology and interesti
Page 223 and 224: List of symbolsHFHRTHyVABHollow Fib
Page 225 and 226: List of symbolsFR/J Normalized Foul
Page 227 and 228: List of publicationsBrand, C., Sán
Page 229: List of publicationsConference on E
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