The MBR Book: Principles and Applications of Membrane

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Case studies 215 area of 15 840 m 2 . This plant operates under similar aeration conditions as that of Porlock and also operates with manual diffuser flushing with no diffuser air-scour. The most recent Kubota MBR plants installed for sewage treatment in the UK have an automated diffuser maintenance programme, whereby they are periodically flushed with water and air-scoured. It is generally recognised by the operator that these plants require careful maintenance to suppress clogging (or sludging), since the filling of the channels with sludge represents a very significant constraint to the viable operation of these plant. To this end, more conservative peak fluxes of 27 LMH appear to be appropriate, though mean operating fluxes are much lower, coupled with rigorously cleaned aerators to maintain the aeration rate, and thus air-scour, in the membrane flow channels. 5.2.1.3 Daldowie Sludge liquor and treatment The plant at Daldowie is a sludge liquor treatment plant owned and operated by Scottish Water. Sludge liquor is the aqueous fraction of sewage sludge which has undergone dewatering by processes such as belt pressing, rotary drum vacuum filtration and centrifugation following conditioning with coagulant and/or polymeric flocculant reagents. It may contain up to 25% of the TN load in the original sludge and contribute as little as 2% of the total influent flow. It is thus highly concentrated in ammonia (Table 5.3), as well as in dissolved organic matter. Composition and flow are extremely variable and dependent on the upstream sludge handling and treatment processes. Whilst the most economical option is to return the liquor to the head of works, this is not always possible either due to logistical limitations or due to the excessive load it would place on the existing sewage treatment process. Under such circumstances, a number of options for its treatment can be considered (Table 5.4). Of key importance in choosing the most suitable option are confidence in a robust solution, cost and environmental factors such as the impact of the wastes generated. Speed of start-up may also be of importance if the plant will only run seasonally. Plant design and operation As is often the case for this duty, the choice of technology at Daldowie was seen as being between a sequencing batch reactor (SBR) and an MBR. However, the large fluctuations in organic loading arising from periodical releases of poor-quality effluent from the centrifuges and the belt presses meant that operation of an SBR was seen as being more problematic than the MBR. This was Table 5.3 Sludge liquor properties Parameter Average concentration Range (mg/L) (mg/L) BOD 1221 162–3004 COD 941 470–1411 NH 4-N 750 162–1218 SS 1442 50–5000 Alkalinity 2200 1900–2500 pH 7.2 7–7.5
216 The MBR Book Table 5.4 Summary of treatment options (modified from Jeavons et al., 1998) Method Advantages Disadvantages Magnesium Ammonium Low capital costs High operating costs phosphate (struvite) TN removal Difficult to control precipitation Instantaneous start-up Centrafugation required High sludge production No large-scale experience Ammonia stripping TN removal Disposal of high ammonia liquid waste Limited experience of No large-scale experience in UK water similar technology industry Instantaneous start-up Nitrates returned to ASP Biological Tried and tested technology Start-up not instantaneous Simple to control No problem wastes Surplus sludge boosts nitrifier population in ASP (a) (b) Figure 5.5 The Daldowie sludge liquor treatment plant:(a) under construction and (b) operational. The photograph shows the plant with the membrane units and manifolding to the right principally due to the buffering capacity offered by the MBR, which can operate at an MLSS of 12–18 g/L rather than the 5 g/L of a conventional activated sludge process (ASP) or SBR. This means that the MBR is relatively tolerant to significant increases in organic and hydraulic loading, provided these do not exceed periods of 2–3 days. The sludge treatment facility incorporates 6 dryers and 12 centrifuges and was built to process most of the sludge produced by the city of Glasgow (�1.5 million people). As a result, the combined effluent liquors produced from this processing require a separate treatment facility as the liquors produced are very high in ammoniacal nitrogen, BOD and COD. The MBR plant was built to treat the liquors to a high enough standard to allow direct separate discharge to the river Clyde (Fig. 5.5), the discharge consent being 20:30:8 (BOD:SS:NH 3). It has been operating since December 2001, and the most recent report is from 2003 (Churchouse and Brindle, 2003). The main effluent streams are centrifuge centrate and dryer condensate, although other site liquors are also treated. The feedwater typically has a mean composition of
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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
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
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 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 242 and 243: Case studies 225 to be treated to a
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
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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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