The MBR Book: Principles and Applications of Membrane

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Table 3.4 Comparative pilot plant trials hand it is widely recognised that analogues can never satisfactorily represent real sewage, particularly so in the case of such crucially important parameters as fouling propensity, and can be extremely expensive to produce. For pilot trials of MBR technologies of a reasonable scale (i.e. based on a small number of full-scale membrane modules), conducting trials based on real feedwaters is always preferred. A number of such trials have been carried out since around the turn of the millennium which permit a useful technology comparison (Table 3.4), albeit with certain caveats. The studies identified in Table 3.2 all employ at least one full-scale membrane module per bioreactor and at least three different technologies. Not all of these studies have been published, however. 3.2.2 Beverwijk wastewater treatment plant, the Netherlands Design 135 Technology Reference tested Adham et al. van der Tao et al. Honolulu Lawrence Trento Eawag (2005) Roest et al. (2005) et al. (2002) (2005) Zenon � � � � � � Kubota � � � � � � Mitsubishi � � � � � Rayon Norit X-Flow – � – Huber (�) � Memcor � � � Toray � An extensive comparative pilot trial was carried out at Beverwijk–Zaanstreek wastewater treatment works between 2000 and 2004, with a substantial body of work published in 2002 (van der Roest et al., 2002). The work represents one of the earliest large-scale comparative pilot trials and was conducted by DHV in collaboration with the Dutch Foundation of Applied Water Research (STOWA). The ultimate goal of the work was the construction of a number of full-scale plants of 60–240 megalitres per day (MLD) capacity in the Netherlands, scheduled for installation between 2003 and 2006. Results from trials on four MBR systems of 24–120 m 3 /day capacity were published in the 2002 report. The four technologies originally tested were Kubota, Norit X-Flow, Mitsubishi Rayon and Zenon. Subsequent reports by this group (Lawrence et al., 2005; Schyns et al., 2003) have not contained the same level of technical detail regarding operation and maintenance. The reported trials (van der Roest et al., 2002) were conducted in four phases: I. Primary clarification with ferric dosing prior to screening II. Primary clarification with simultaneous ferric dosing (i.e. downstream of screening) III. Raw wastewater with simultaneous precipitation IV. Raw wastewater with bio-P removal.
136 The MBR Book Table 3.5 Feedwater quality Parameter (mg/L) Raw sewage Advanced primary treated sewage COD 548–621 297–422 TKN 57–61 39–67 Total phosphate-P 9.3–12.1 7.1–8.3 Table 3.6 Design information Kubota Mitsubishi Rayon Zenon Norit X-Flow Flow (m3 /day) Peak 190–240 154–230 30–43 Normal (design) 48–72 32–48 44–74 9 Screening 2.0 mm basket 0.75 mm 0.75 mm static 0.5 mm filter, SD; parabolic half drum rotating Tank sizes (m 2.5–1 mm rotary drum filter, DD sieve with brush drum 3 ) Denitrification 12.0 15.6 12.0 3.6 Nitrification – 7.8 7.7 2.1 Membrane 18.8 10.8 3.9 �0.1 (ALSS) Recycle ratio Membrane �8 �12 �8 �5 Type 510 SUR 234 ZW500, a or c F-4385 Configuration 150 panels Triple deck 4 modules 8 modules, per deck, SD/DD 2 � 4 Total membrane area (m 240 315 184 240 2 ) SD � single deck; DD � double deck, ALSS-airlift sidestream: no membrane tank. All MBRs were configured with a denitrification zone, with an anaerobic tank added for Phase IV. The Kubota system was initially fitted with a single deck; a double deck was fitted mid-way through Phase II. Data presented in the following tables refer only to the first three phases. Water quality data (Table 3.5) relates to the range of mean values (i.e. not the total range of values recorded) reported for the four technologies tested. The process design and pre-treatment (i.e. screening) were all as specified by the supplier. A noticeable impact on alpha factor was recorded independent of the membrane type, with the value decreasing from 0.78–0.79 for the conventional ASP in operation at the works to 0.43–0.54 across all the MBR technologies. Design (Table 3.6) and operation and maintenance (Table 3.7) data are reported below. Comparison of process performance is somewhat difficult from the reported data, since the process operating conditions were changed frequently throughout the trials. Variation in hydraulic retention time (HRT) meant that the organic loading rate varied significantly between the different technologies tested, from 0.043 to 0.059 kg biological oxygen demand (BOD)/m 3 for the Mitsubishi Rayon module to
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The MBR Book
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The MBR Book: Principles and Applic
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Contents Preface ix Contributors xi
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Contents vii 4.2.5 The Industrial T
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Preface What’s In and What’s No
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Term Meaning Common units MLD Megal
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Contributors A number of individual
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Contributor(s) Association/Organisa
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Introduction With acknowledgements
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such as the filtration market, tech
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D R IVE R S R EST R AI N TS Bathing
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Introduction 7 Much of the legislat
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of non-point source pollution contr
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exploitation index (WEI), the value
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1 500 000 1 250 000 1 000 000 750 0
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Alternative immersed FS and HF memb
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1.6 Conclusions Whilst the most sig
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Introduction 19 USEPA (2006b) www.e
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Fundamentals With acknowledgements
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they can be put, which then provide
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3µm (a) (b) membrane is chemically
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Table 2.2 Membrane configurations C
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2.1.4 Membrane process operation 2.
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only pseudo-steady-state (or stabil
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P max P dP/dt backwash cycle t b Ba
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Fundamentals 35 2.1.4.6 Critical fl
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neo-exponential increase at fluxes
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Screened raw sewage biologically ar
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Table 2.4 Microbial metabolism type
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which affords the operator complete
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Cumulative %ile undersize 1 0.8 0.6
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occurs from the surrounding air to
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(Madoni et al., 1993). The inter-re
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Viscosity (mPa s) 100 10 1 Viscosit
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on discharged P levels have been im
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Membrane process mode Diffusion Ext
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energy demand in kWh/m 3 permeate p
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Table 2.5 System facets of denitrif
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Fundamentals 61 Moreover, the poten
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iomass. There are also issues with
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Table 2.6 Effect of pore size on MB
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Fundamentals 67 fouling to be influ
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Fundamentals 69 fouling (i.e. membr
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2.3.6 Feed and biomass characterist
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Fouling relative distribution (%) 1
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has been proposed by Cho and co-wor
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Fundamentals 77 in the influent. Ab
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MLSS sample Centrifugation 5 min 50
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Table 2.11 Concentration of SMP com
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Fundamentals 83 correlation of MBR
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Page 104 and 105: Fundamentals 87 air cannot be used
Page 106 and 107: Table 2.12 Dynamic effects Determin
Page 108 and 109: Fundamentals 91 Table 2.13 Sub-crit
Page 110 and 111: Fundamentals 93 sludge (Cho and Fan
Page 112 and 113: Fundamentals 95 2.3.9.2 Employing a
Page 114 and 115: Fundamentals 97 Whilst ultrasonic c
Page 116 and 117: and immersed hybrid PAC-MBR (Kim an
Page 118 and 119: Lastly, the vast majority of all st
Page 120 and 121: Fundamentals 103 Brookes, A., Judd,
Page 122 and 123: Fundamentals 105 Côté, P., Buisso
Page 124 and 125: Fundamentals 107 Fuchs, W., Schatzm
Page 126 and 127: Fundamentals 109 Howell, J.A., Chua
Page 128 and 129: Fundamentals 111 Krauth, K. and Sta
Page 130 and 131: Fundamentals 113 Liu, R., Huang, X.
Page 132 and 133: Fundamentals 115 Nielson, P.H. and
Page 134 and 135: Fundamentals 117 Sato, T. and Ishii
Page 136 and 137: Fundamentals 119 Van Lier, J.B. (19
Page 138 and 139: Fundamentals 121 Zhang, Y., Bu, D.,
Page 140 and 141: Design With acknowledgements to: Ch
Page 142 and 143: Other contributions to pumping ener
Page 144 and 145: where J c is the cleaning flux. Fro
Page 146 and 147: Table 3.1 Main features of aeration
Page 148 and 149: Table 3.2 Biological operating para
Page 150 and 151: Table 3.3 Physical operating parame
Page 154 and 155: Table 3.7 O&M data Design 137 Kubot
Page 156 and 157: Table 3.8 Feedwater quality, PLWTP
Page 158 and 159: Table 3.11 Cleaning protocols for t
Page 160 and 161: Figure 3.1 The planned location of
Page 162 and 163: Table 3.14 O&M data, Pietramurata W
Page 164 and 165: Design 147 Table 3.17 Design inform
Page 166 and 167: Maintenance CIP was conducted throu
Page 168 and 169: Permeability, LMH/bar 800 700 600 5
Page 170 and 171: Table 3.22 Summary of pilot plant p
Page 172 and 173: Table 3.25 Feedwater specification
Page 174 and 175: Table 3.34 Aeration design Paramete
Page 176 and 177: In short, the design calculation de
Page 178 and 179: complications arise when estimating
Page 180 and 181: Chapter 4 Commercial Technologies W
Page 182 and 183: 4.1 Introduction Available and deve
Page 184 and 185: Commercial technologies 167 suction
Page 186 and 187: synonymous with R V Equation (3.13)
Page 188 and 189: (a) (b) Figure 4.8 The Huber VRM ®
Page 190 and 191: and is very robust. However, the la
Page 192 and 193: Commercial technologies 175 (a) (b)
Page 194 and 195: (a) (b) (c) Commercial technologies
Page 196 and 197: Other equipment 1.11% Process air b
Page 198 and 199: Thus far, almost all of the install
Page 200 and 201: Figure 4.22 A rack of Memcor B10R m
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Tensile elongation retention (%) 10
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Figure 4.28 Pilot plant at Mooka Co
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at 10 000-12 000 mg/L. The membrane
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4m 4m 1m Commercial technologies 19
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Figure 4.36 Ejector aerator Commerc
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Denitrification Nitrification Waste
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modules, with pore sizes ranging fr
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(a) (b) Figure 4.46 (a) Han-S Envir
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aerobic counterpart. This may be pa
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of the particularly large-diameter
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(c) air channelling, the risk of wh
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Case Studies With acknowledgements
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5.1 Introduction Membrane Bioreacto
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Case studies 211 Table 5.1 Comparis
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Case studies 213 0.6 m 3 per unit.
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Case studies 215 area of 15 840 m 2
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Aeration tank 1 FBDA FBDA 32 x J200
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Case studies 219 In this UNR config
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Table 5.6 Design criteria, Running
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Works inlet Inlet works Storm tank
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Case studies 225 to be treated to a
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Case studies 227 membranes, assembl
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Figure 5.16 A Naston package plant
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Air Influent DN N M Figure 5.18 The
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Table 5.9 Toray membrane-based MBR
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Figure 5.23 Aeration tank and cover
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Figure 5.24 The original plant at B
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Main permeate header Permeate pump
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Case studies 241 flow. Sludge waste
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Table 5.15 Water quality data, Unif
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TMP (Kpa) 80 70 60 50 40 30 20 10 0
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10 LMH; the plant operated at fluxe
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Table 5.17 Feed and treated water q
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Table 5.18 Water quality, Sobelgra
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Figure 5.37 Airlift municipal WWTP,
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Case studies 255 has been 20 g/L, b
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Case studies 257 The company had in
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Filtrate (ml) 25 20 15 10 5 IIndust
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Inflow Buffer tank Filtration Denit
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Figure 5.45 The VHP MBR (a) (b) Cas
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Figure 5.47 The Eden Project MBR Ba
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Table 5.25 Basis for process design
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5.4.7 Other Orelis plant Case studi
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two membrane module configurations.
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Appendix A Blower Power Consumption
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or or (A.4) where � is the ratio
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Appendix B MBR Biotreatment Base Pa
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Y 0.61 g VSS/g COD Fan et al. (1996
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Appendix C Hollow Fibre Module Para
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L being the internal module length
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Appendix D Membrane Products
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Table D.3 Membrane module details o
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Table D.4 (continued) Supplier Asah
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Table D.5 Membrane module details o
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Appendix E Major Recent MBR and Was
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Conference title meet Dates Locatio
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Event Last held Location Website Fo
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Appendix F Selected Professional an
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Japan Water Works Association (JWWA
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Nomenclature � Separation (m) �
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Nomenclature 305 Rsup Hydraulic res
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Abbreviations The following lists k
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PES Polyethylsulphone PP Polypropyl
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Glossary of Terms A number of key t
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Floc Aggregated solid (biomass) par
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Glossary of terms 315 Relaxation Ce
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Index A � factor 47, 49-50 and vi
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investment 9 for membrane replaceme
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I Iberia 2 immersed biomass-rejecti
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Nordkanal wastewater treatment work
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SUR unit 180 surface porosity 30 Su
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