The MBR Book: Principles and Applications of Membrane

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Works inlet Inlet works Storm tank Ferric dosing 6 and 2 mm screens Storm water 4 No. MBR tanks Case studies 223 Permeate pumping chamber Permeate to river Figure 5.11 Schematic of Coill Dubh wastewater treatment works is then, on level, pumped to outfall, or can be recycled back to the inlet of the works via a divert valve, conducted to assist in commissioning. Excess sludge is removed manually from each reactor via a single progressive cavity pump and discharged into the inlet sludge storage tank. Fat, scum and grit are also collected in this tank, and the accumulated waste periodically removed from site. Also supplied on-site are a control/mess building, ferric storage and a standby generator. A remote monitoring system provides Brightwater with site feedback. Operation and maintenance The MBR operates at a maximum TMP of 300 mbar and a gross flux of 27 LMH (hence �90 LMH/bar permeability) with relaxation for 5 min every hour. Aeration is supplied by an aeration lateral system located at the base of each plate providing coarse-bubble aeration for both membrane scour and process aeration at a rate of up to 118 Nm 3 /h per module, or a SAD m of 1.28 Nm 3 /(m 2 h). No additional fine bubble aeration system is required for the combined sewer loads supplied to Coill Dubh. Although chemical cleaning is suggested at 12-monthly intervals, none has been applied over the first 18 months of operation; the performance of the membranes is maintained with the air scour rate supplied. Cleaning is to be conducted ex situ by sluicing, followed by a 4–12 h soak in either hypochlorite or citric acid, depending on the assessed fouling. Flushing of the aeration system can be conducted at the same time. The design sludge age is 21 days, though this often increases to �30days such that the design MLSS concentration of 12 g/L increases to �15 g/L. The HRT is �11 h at full flow. The process at Coill Dubh was built as a low-tech approach to membrane technology and has performed better than anticipated despite periods of operational stress. The permeability remains acceptable at flux rates between 22 and 27 LMH and the permeate water contaminant levels have consistently been below most of the parameter limits of detection (i.e. �5 mg/L BOD, �5 mg/L SS, �0.5 mg/L N-NH � 4 and �0.05 mg/L TP). While the effluent quality exceeds that required for discharge, the simplicity of the system and the robustness of the membranes have made this plant very simple to operate, despite fat and rag levels far in excess of those anticipated. The continued operation without the requirement for chemical cleaning
224 The MBR Book makes the system even more attractive. A preventative inspection/clean is currently being discussed with the client, who is now Cork County Council. 5.2.2.2 Other Brightwater plant Another of Brightwater’s MBR plants (450 p.e. or 0.276 MLD flow design capacity), operated by Bord na Mona on behalf of the local council, is located at Halfway WWTW near Cork in Ireland (Fig. 5.12). This plant is fitted with a 3 mm screw wedgewire screen and has an anoxic reactor (�45 min HRT) for TN removal (the consented concentration being 5 mg/L TN) and ferric dosing for phosphorous removal. The plant is fitted with six membrane modules in a single aeration reactor, providing a total area of 552 m 2 . All process aeration is supplied by the scour air system described for Coill Dubh. Mixed liquors are recycled from the aeration reactor to the baffled and mixed anoxic reactor to enable nitrate removal. Screened and ferricdosed influent is also fed into the anoxic reactor at this point. 5.2.3 Colloide Engineering Systems 5.2.3.1 Fisherman cottages, Lough Erne, Northern Ireland At this site a small wastewater treatment plant was required for a group of cottages on the side of Lough Erne, Co. Fermanagh in Northern Ireland. The wastewater had Figure 5.12 The plant at Halfway. The screen is located mid/top picture, with the inlet pump chamber behind it. The anoxic tank is below the screen, and MBR is the covered tank with the swan-neck air feed lines. The sludge tank is located behind the MBR and to the right of the anoxic tank. The permeate pump chamber is behind the sludge tank
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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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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 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
Page 288 and 289: 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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