The MBR Book: Principles and Applications of Membrane

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Table 5.6 Design criteria, Running Springs Parameters Units Current Future in December 2003 demonstrated that a stable net flux of around 54 LMH (32 GFD, Fig. 5.9) was achieved following the addition of 400 mg/L of the polymer. Performance with respect to purification and system hydraulics is given in Tables 5.5 and 5.6, respectively, with the latter including a summary of the process design. 5.2.2 Brightwater Engineering Case studies 221 Maximum month average daily flow MLD 2.3 3.8 Peak day flow MLD 4.6 7.6 Minimum day average process temperature °C 15 15 Maximum day average process temperature °C 20 20 Annual average flux LMH 25 a 25 Peak hour average flux LMH 50 50 Membrane cassette type – EK300 EK200 Number of cartridges per cassette – 150 100 Surface area per cassette m 2 120 120 Number of cassettes installed per train – 8 16 Number of MBRs (membrane tanks) – 2 2 Coarse bubble aeration rate (20°C), per cartridge l/min 7.5 7.5 Typical cleaning cycle time days 180 180 Typical cleaning reagent – hypo hypo Typical cleaning reagent strength b mg/L 8000 8000 Typical Cleaning (soak) time/protocol h 2 2 a Assuming an operating temperature of 15°C. b An existing sodium hypochlorite system is used that generates a 0.8% solution that is stronger than the 0.5% solution recommended by the system supplier. 5.2.2.1 Coill Dubh, Ireland Background Coill Dubh is a small village about a 1 h drive west of Dublin. The existing works consisted of basic concrete primary/septic tanks followed by peat filter beds. Effluent was directly discharged from these peat beds to a small local river. The works was in a poor condition and, on completion of the MBR scheme, was demolished. The new works (Fig. 5.10) was provided by a developer as part of his planning consent for a housing estate close to the site. This works was to treat the sewage from this new estate plus the existing village. At the tender and design stage in 2001–2003, little information was available on the influent, other than it was to be mainly domestic in nature, contain storm flows, have a maximum flow to treatment of 50 m 3 /h and contain loads of 2000 p.e. (population equivalent). The treated effluent consent was: BOD 10 mg/L, SS 10 mg/L, NH 3 5 mg/L and total phosphorus 1 mg/L. Though this standard could arguably be achieved with a conventional treatment process, the small footprint and relatively shallow tanks afforded by the MBR process led to this technology being selected; the new works was to be built on a peat bog with a very high water
222 The MBR Book Figure 5.10 The Coill Dubh site. The four MBR tanks are adjacent to the lifting davits table, making deep excavations difficult and expensive. The simplicity of the MEMBRIGHT ® design made this option competitive and attractive. No piloting was undertaken as this influent was considered “normal” domestic sewerage based on an inland catchment with an observable existing treatment process. The contract was led by the house developer MDY Construction. MDY also supplied the civil element to the contract based on supplied designs. The process, mechanical and electrical design element of the contract was delivered by Bord na Mona Environmental and supplied by Brightwater Engineering. M&E installation was supplied by BnM subcontractors, while process commissioning, verification and pre-handover operational support was supplied by Brightwater. The plant was commissioned in June 2004. Design The works (Fig. 5.11) consists of an inlet flume, followed by an overflow sump from where flows in excess of 50 m 3 /h are diverted to a storm tank with 2 h retention at flows between 50 and 100 m 3 /h. Excess flows from the storm tank discharge from it direct to the stream. Storm water is pumped back to the inlet sump once works inlet flows have reduced. Flows to treatment are dosed with ferric for phosphorous control and pumped to a 6mm free-standing wedgewire rotary screen. Flows drop from the screen into a stilling zone located in a settling tank that also acts as the works sludge and scum storage. From the stilling zone, flows pass under a fat-retaining submerged weir and onto a 3 mm drum screen. Flows are then diverted via a common manifold to four membrane tanks, each containing six modules. Each module provides a total effective surface area of 92 m 2 from 50 panels. Aeration is supplied to the modules only by duty/duty blowers. Treated effluent/permeate gravitates by siphoning from each reactor to a common collection sump via flow measurement on each reactor. Permeate
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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)
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 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 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
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
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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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The MBR Book: Principles and Applications of Membrane

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