The MBR Book: Principles and Applications of Membrane

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Case studies 241 flow. Sludge wasted from the tank is dewatered by centrifuge to around 25 wt%. There is also a simultaneous precipitation for phosphorous removal. Plant operation The plant is operated at an SRT of 25 days, which maintains the mixed liquor at between 10 and 15 g/L. The membranes are operated at a net flux of 25 LMH and a mean permeability of 150–200 LMH/bar. Intermittent coarse bubble aeration is provided at 34 000 m 3 /h on a 10 s on/10 s off basis, giving a SAD m of 0.40 Nm 3 /h per m 2 and a SAD p of 17 m 3 air per m 3 . Physical cleaning comprises a backflush every 7 min for 60 s at 1.5 times the operating flux. A maintenance chemical clean is conducted every two weeks by draining the membrane tank and backflushing for 1 h alternately with different cleaning agents, including 500 mg/L hypochlorite. Cleaning is conducted on individual tanks, that is 12.5% of the installed capacity. The number of membranes on-line is adjusted according to the flow, but this is controlled in such a way as to ensure that no membrane train is off-line for more than a total of 70 min. The total specific power demand for all operations is 0.9 kWh/m 3 , which compares to an average of 0.5 kWh/m 3 for all conventional sewage treatment plants operated by the Erftverband. The plant, which incurred a total capital cost of €25 m, has been successfully operating for 23 months without major incidents. 5.3.1.4 Unifine Richardson Foods effluent treatment plant Background The plant at Unifine Richardson Foods in St Mary’s, Ontario (Figs 5.28 and 5.29) is an industrial pretreatment facility that discharges to a municipal wastewater treatment works and must meet 300 mg/L BOD and 350 mg/L TSS. Any organic load in excess of this is levied an additional surcharge by the municipality. Reliance on the municipality to receive and treat any high-strength waste leaves the industrial client in a vulnerable position should the works not be able to receive the industrial wastewater in the future. Richardson Foods moved to its new production facility in 1999 and needed a new wastewater pretreatment facility to replace the existing SBR, which was over 20 years old. The latter was labour-intensive, generated nuisance odours and was subject to upsets due to the proliferation of filamentous bacteria. Richardson Foods hired CH2MHill to select bidders for a new wastewater pretreatment system and, as a result of the selection process, Zenon Environmental Inc. was selected to design, build and install the system on a complete turn-key basis. The total contract value was $1 102 000, and installation and commissioning were completed in November 2000. Plant design and operation Unifine Richardson Foods Ltd. manufactures condiments for the food service industry. The plant makes over 200 products, including drink syrups, sundae toppings, sauces, mayonnaise and salad dressings. The wastewater strength and composition is highly variable and changes with product changes, tank flushes, etc. The mean influent COD and BOD concentrations are 7400 and 5500 mg/L, respectively, and the average daily flow is 0.15 MLD. There is a significant concentration of oil and grease in the wastewater. Wastewater from the
242 The MBR Book Equalization tank (Aerated) Transfer pump Figure 5.28 The Unifine Richardson Foods effluent treatment plant Dissolved air floatation Feed pump Bioreactor (Aerated) Recirculation pump Aeration blower ZW-500c membranes Waste sludge disposal Vacuum pump Air separator Process pump Figure 5.29 Schematic of Unifine Richardson Foods Backpulse tank Backpulse to membranes Permeate to sewer (Blended with waste sludge stream) industrial plant is pumped into an aerated equalisation tank, which is of bolted carbon steel construction, and is then pumped continuously into a dissolved air flotation (DAF) process for FOG and solids removal. The DAF float is stored and tankered to a rendering facility. The DAF effluent is pumped to the bioreactor tank, also of bolted carbon steel construction. A coarse bubble diffuser grid distributes air into the bioreactor from positive displacement blowers. Caustic soda and phosphorous can be added to the biological process by chemical metering stations. Mixed liquor from the bioreactor
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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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Commercial technologies 175 (a) (b)
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(a) (b) (c) Commercial technologies
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Other equipment 1.11% Process air b
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Thus far, almost all of the install
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Figure 4.22 A rack of Memcor B10R m
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Tensile elongation retention (%) 10
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Figure 4.28 Pilot plant at Mooka Co
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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
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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 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 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
Page 292 and 293: or or (A.4) where � is the ratio
Page 294 and 295: Appendix B MBR Biotreatment Base Pa
Page 296 and 297: Y 0.61 g VSS/g COD Fan et al. (1996
Page 298 and 299: Appendix C Hollow Fibre Module Para
Page 300 and 301: L being the internal module length
Page 302 and 303: Appendix D Membrane Products
Page 304 and 305: Table D.3 Membrane module details o
Page 306 and 307: 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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