The MBR Book: Principles and Applications of Membrane

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Case studies 213 0.6 m 3 per unit. Each tank contains six membrane units with 150 panels per unit, giving a total membrane panel area of 2880 m 2 provided by 3600 membrane panels at 0.8 m 2 membrane area per panel. Pretreatment comprises a 3 mm perforated screen, this having replaced the original 2 mm wedgewire screen during the first year of operation. At a peak flow of 1.9 megalitres per day (MLD), the plant operates at a flux of 27 litres per m 2 per hour (LMH) and generally operates at a transmembrane pressure (TMP) between 0.02 and 0.11 bar under gravity-feed conditions (governed by the tank depth and pipework losses) and can sustain a flux of �20 LMH. This means that the permeability is normally between 200 and 500 LMH per bar, but can rise higher when the fouling and clogging propensity is low. The membrane module is aerated at a rate of 0.75 Nm 3 /h per m 2 membrane area (SAD m) the standard coarse bubble aeration rate for the Kubota system, which means that each m 3 of permeate product demands around 32 Nm 3 air (SAD p � 32). The membrane is relaxed for 30–60 min daily as a result of low overnight flows, and cleaning in place with 0.5 wt% hypochlorite is undertaken every 8–9 months. Diffusers are flushed manually without air scour. The plant operates at solids retention times (SRTs) of 30–60 days, producing 0.38–0.5 kg sludge per kg of BOD, 3–6.5 m 3 /day of 2% dry solids (DS) sludge. The recommended mixed liquor suspended solids (MLSS) concentration range is 12–18 g/L, but it has been operated as high as 30 g/L and is regularly over 20 g/L. The plant is of a simple and robust, possibly conservative, design and construction and has generally proved very reliable. Membrane replacement due to actual membrane failure for this plant during the first 8 years of operation has been minimal. Indeed, a consideration of all UK and US membrane plants based on this technology reveals membrane replacement per annum to be very low (Table 5.2) – generally �1% and always �3%. Permeate water quality has always been well within consent, and the plant produces very low odour levels (�2mgm �3 H 2S). Porlock was originally costed on the basis of a membrane life of 7 years, a milestone that has already been passed. Periodic fouling events have been encountered at this plant, and some of these have been linked with seawater intrusion. Shock loads of salinity Table 5.2 Total number of membrane failures by age of original panel Within No installed panels Panel failures % p.a. Cumulative (%) of age in year Year 1 (i.e. 0–1) 141 061 192 0.14 0.14 Year 2 (i.e. 1–2) 115 985 598 0.52 0.65 Year 3 (i.e. 2–3) 89 714 690 0.77 1.42 Year 4 (i.e. 3–4) 74 606 1 388 1.86 3.28 Year 5 (i.e. 4–5) 36 247 33 0.09 3.37 Year 6 (i.e. 5–6) 32 772 95 0.29 3.66 Year 7 (i.e. 6–7) 14 938 20 0.13 3.80 Year 8 (i.e. 7–8) 4 200 0* 0 3.80 Year 9/10 (i.e. 8–10) 386 Note: Data as at June 2005, 45 operational plants (including all 40 UK and Ireland, both municipal and industrial). Data excludes �300 panels repaired by client following accidental damage. *No failures reported in this year as at June 2005. Kennedy and Churchouse (2005).
214 The MBR Book are known to cause increases in soluble COD levels in the mixed liquor, and this has been shown to increase fouling propensity (Section 2.3.7.3) (Reid, 2006). 5.2.1.2 Other Wessex Water regional Kubota plant Subsequent Wessex Water MBR plant at Swanage (12.7 MLD) and the small plant at South Wraxall (0.26 MLD) were designed based on slightly higher peak fluxes than that of Porlock: 33 LMH rather than 27 and operates at a lower MLSS (8–12 g/L). Other plants in the region, specifically Westbury (4.8 MLD) and Longbridge (1.6 MLD), have similar design fluxes to that of Porlock. Westbury has a significant industrial effluent input, and chemical phosphorous removal has been successfully retrofitted at this plant. The plant at Swanage is of some significance, it being the largest MBR installation in the UK at the time of installation, though Daldowie (Section 5.1.3) is significantly larger in membrane area (25 600 panels) and larger in average flow but similar on design full flow at 12.9 MLD. The Swanage plant is also one of the least visible largescale sewage treatment works. The plant has been completely landscaped into the Dorset coastline (Fig. 5.4), a considerable feat of civil engineering incurring a correspondingly considerable cost. The plant has six aeration tanks of 3.3 � 22.5 � 5m dimension with average liquid depth 3.5 m, giving a volume of 250 m 3 . It contains a total of 132 units (22 per tank) with 150 panels per unit providing a total membrane (a) (b) Figure 5.4 View of Swanage sewage treatment works:(a) from the sea and (b) from the air
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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
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
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 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 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
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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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