The MBR Book: Principles and Applications of Membrane

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Case studies 225 to be treated to a 10/10 (BOD/TSS) standard or better. The flow rate to be treated was a maximum of 0.012 MLD. Given the very low flow and relatively tight discharge consent, an MBR plant was offered as the most attractive process option based on the comparatively low capital and whole life costs of the MBR over that of conventional activated sludge treatment with tertiary treatment polishing. Colloide Engineering Systems was commissioned to provide the plant by the developer on a design and build contract. The plant was installed and commissioned in August 2004. The reactor comprises a pre-existing elliptically shaped concrete tank divided into two sections, each of 2 m 3 volume (Fig. 5.13a). The first compartment is used as an inlet section for settlement of gross solids; settlement comprises the only pretreatment used at this site. The wastewater is allowed to flow to the second chamber via an interconnecting pipe fitted near the top of the tank. The tank is installed below ground, with its top at ground level. The membrane assembly comprises two 10 m 2 Sub Snake modules, providing a total membrane area of 20 m 2 . The modules are mounted in a PVC frame which also holds a tubular fine bubble air diffuser, positioned directly below each membrane module. This complete membrane assembly is immersed in the second chamber of the tank. A float switch is also mounted in this chamber to control the water levels. A control kiosk is positioned above ground adjacent to the wastewater treatment tank with a duct running between the tank and the kiosk. The kiosk houses a 0.2 kW air blower delivering air to the diffusers, the permeate suction pump discharging treated water and all process control equipment. The system is operated at a TMP of 0.4 bar (4 m head), which provides a flux of 20–30 LMH. A filtration cycle of 6 min on/2 min relaxation is employed, with a cleaning cycle time estimated as being 6–12 months, using 200 ppm sodium hypochlorite. No coarse bubble aeration is used, fine bubble aeration being provided at a rate of 10 m 3 /h to the total membrane assembly, yielding a SAD p of 20 m 3 air per m 3 . The plant has generally operated very well. The hydraulics of the system have never been an issue with this plant, and the membranes remove practically all Control panel Power supply Effluent in Air blower Treated effluent out Treated effluent pump (a) (b) Figure 5.13 The Fisherman Cottages MBR: (a) schematic and (b) in situ. The membranes are in the second of the two underground concrete tanks in the picture, only the kiosk housing the control equipment is mounted above ground
226 The MBR Book suspended solids. The reactor biomass took some time to develop and acclimatise due to a combination of the plant not being properly seeded and disinfectant chemicals being discharged into the plant. However, the plant has been operating to the design specification over a year. 5.2.4 Huber Technology 5.2.4.1 Knautnaundorf The water and wastewater company in Leipzig (KWL) is responsible for the operation of 30 sewage treatment plants in and around Leipzig. Many of these plants were found to be no longer able to meet the tighter effluent quality standards imposed by the government and so required upgrading. Prior to upgrading, the sewage treatment plant at Knautnaundorf was equipped with a balancing tank, two primary tanks and four small activated sludge plants for biological clarification of the wastewater. Oxygen supply to the plant had been controlled using simple timers, with no feedback control based on DO levels in the mixed liquor. The quality of the treated water, which is discharged into the Weiße Elster river, was therefore poor. After a tendering process, the vaccum rotating time (VRM) ® system was selected to provide water meeting the new effluent standards, which specify microbiological parameters. The new treatment plant (Fig. 5.14), was designed for a maximum flow rate of 18 m 3 /h and a daily flow of 0.113 MLD. It contains a stack of trapezoidal plate Figure 5.14 Municipal WWTP at Knautnaundorf
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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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(Cui et al., 2003) by inducing liqu
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Fundamentals 87 air cannot be used
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Table 2.12 Dynamic effects Determin
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Fundamentals 91 Table 2.13 Sub-crit
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Fundamentals 93 sludge (Cho and Fan
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Fundamentals 95 2.3.9.2 Employing a
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Fundamentals 97 Whilst ultrasonic c
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and immersed hybrid PAC-MBR (Kim an
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Lastly, the vast majority of all st
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Fundamentals 103 Brookes, A., Judd,
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Fundamentals 105 Côté, P., Buisso
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Fundamentals 107 Fuchs, W., Schatzm
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Fundamentals 109 Howell, J.A., Chua
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Fundamentals 111 Krauth, K. and Sta
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Fundamentals 113 Liu, R., Huang, X.
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Fundamentals 115 Nielson, P.H. and
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Fundamentals 117 Sato, T. and Ishii
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Fundamentals 119 Van Lier, J.B. (19
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Fundamentals 121 Zhang, Y., Bu, D.,
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Design With acknowledgements to: Ch
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Other contributions to pumping ener
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where J c is the cleaning flux. Fro
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Table 3.1 Main features of aeration
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Table 3.2 Biological operating para
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Table 3.3 Physical operating parame
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Table 3.4 Comparative pilot plant t
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Table 3.7 O&M data Design 137 Kubot
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Table 3.8 Feedwater quality, PLWTP
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Table 3.11 Cleaning protocols for t
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Figure 3.1 The planned location of
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Table 3.14 O&M data, Pietramurata W
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Design 147 Table 3.17 Design inform
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Maintenance CIP was conducted throu
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Permeability, LMH/bar 800 700 600 5
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Table 3.22 Summary of pilot plant p
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Table 3.25 Feedwater specification
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Table 3.34 Aeration design Paramete
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In short, the design calculation de
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complications arise when estimating
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Chapter 4 Commercial Technologies W
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4.1 Introduction Available and deve
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Commercial technologies 167 suction
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synonymous with R V Equation (3.13)
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(a) (b) Figure 4.8 The Huber VRM ®
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and is very robust. However, the la
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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
Page 202 and 203: Tensile elongation retention (%) 10
Page 204 and 205: Figure 4.28 Pilot plant at Mooka Co
Page 206 and 207: at 10 000-12 000 mg/L. The membrane
Page 208 and 209: 4m 4m 1m Commercial technologies 19
Page 210 and 211: Figure 4.36 Ejector aerator Commerc
Page 212 and 213: Denitrification Nitrification Waste
Page 214 and 215: modules, with pore sizes ranging fr
Page 216 and 217: (a) (b) Figure 4.46 (a) Han-S Envir
Page 218 and 219: aerobic counterpart. This may be pa
Page 220 and 221: of the particularly large-diameter
Page 222 and 223: (c) air channelling, the risk of wh
Page 224 and 225: Case Studies With acknowledgements
Page 226 and 227: 5.1 Introduction Membrane Bioreacto
Page 228 and 229: Case studies 211 Table 5.1 Comparis
Page 230 and 231: Case studies 213 0.6 m 3 per unit.
Page 232 and 233: Case studies 215 area of 15 840 m 2
Page 234 and 235: Aeration tank 1 FBDA FBDA 32 x J200
Page 236 and 237: Case studies 219 In this UNR config
Page 238 and 239: Table 5.6 Design criteria, Running
Page 240 and 241: Works inlet Inlet works Storm tank
Page 244 and 245: Case studies 227 membranes, assembl
Page 246 and 247: Figure 5.16 A Naston package plant
Page 248 and 249: Air Influent DN N M Figure 5.18 The
Page 250 and 251: Table 5.9 Toray membrane-based MBR
Page 252 and 253: Figure 5.23 Aeration tank and cover
Page 254 and 255: Figure 5.24 The original plant at B
Page 256 and 257: Main permeate header Permeate pump
Page 258 and 259: Case studies 241 flow. Sludge waste
Page 260 and 261: Table 5.15 Water quality data, Unif
Page 262 and 263: TMP (Kpa) 80 70 60 50 40 30 20 10 0
Page 264 and 265: 10 LMH; the plant operated at fluxe
Page 266 and 267: Table 5.17 Feed and treated water q
Page 268 and 269: Table 5.18 Water quality, Sobelgra
Page 270 and 271: Figure 5.37 Airlift municipal WWTP,
Page 272 and 273: Case studies 255 has been 20 g/L, b
Page 274 and 275: Case studies 257 The company had in
Page 276 and 277: Filtrate (ml) 25 20 15 10 5 IIndust
Page 278 and 279: Inflow Buffer tank Filtration Denit
Page 280 and 281: Figure 5.45 The VHP MBR (a) (b) Cas
Page 282 and 283: Figure 5.47 The Eden Project MBR Ba
Page 284 and 285: Table 5.25 Basis for process design
Page 286 and 287: 5.4.7 Other Orelis plant Case studi
Page 288 and 289: two membrane module configurations.
Page 290 and 291: 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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