The MBR Book: Principles and Applications of Membrane

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Figure 5.23 Aeration tank and covers, Perthes en Gatinais plant Table 5.10 Discharge consents, Perthes en Gatinais plant Parameter Units Value COD mg/L 40 BOD mg/L 5 TSS mg/L 5 TN mg/L 10 Total P mg/L 2.5 Total coliforms Log removal 5 Table 5.11 Characteristics of plant and effluent, Perthes en Gatinais plant Parameter Units Value Population equivalent p.e. 4500 Dry weather daily flow rate m 3 /day 900 Rain weather flow m 3 /day 1440 Peak hourly flow m 3 /h 140 Maximum flow rate at inlet Biosep m 3 /h 85 COD load kg/day 675 TSS load kg/day 315 TN-load kg/day 67.5 Total P-load kg/day 18 Temperature range °C 10–20 Case studies 235
236 The MBR Book Table 5.12 Membrane characteristics and maintenance, Perthes en Gatinais plant Parameter Value TMP range 0.2–0.5 bar Backwash frequency and duration Every 10 min for 45 s CIP Once a week with hypochlorite External chemical cleaning Hypochlorite/acid soak 1–4 times a year Coarse bubble aeration is applied at a rate of 1 m 3 /h per m 2 membrane area. The permeability is routinely between 70 and 120 LMH/bar over the range of TMP indicated in Table 5.12. Regular flushing, around once every 10 min, together with the CIP procedures outlined (Table 5.12), enable the required steady-state flux rates to be maintained. External recovery cleaning with sodium hypoclorite is conducted by taking the membrane out of the aeration tank and transferring it to an adjacent cleaning tank where both cleaning chemical reagents (acid and sodium hypochlorite) and cleaning durations can be employed more flexibly. Cassettes in the aeration tank can be backflushed separately, and the backflushing process demands around 25% of the product permeate. Full nutrient removal is achieved by the plant. Phosphate removal is achieved by dosing ferric chloride into the effluent, the phosphate being removed with the excess sludge. The resulting excess sludge production, including the solids created by chemical dosing, is around 0.5 kg TSS/kg COD. The dewatering unit consists of a sludge thickener combined with a belt press. The total sludge production is �270 kg/day. To achieve a satisfactory thickness of 16% after the belt press, a polymer dose of 6 kg/ton DS is required. After dewatering, the solids content of the sludge product is increased and the sludge is further stabilised with lime at a rate of 0.52 kg CaO/kg. The end product (Fig. 5.22) has a DS concentration 25 wt% and is distributed to local farmers and disposed to land. 5.3.1.2 Brescia sewage treatment works Background At the existing conventional plant at Brescia, the Verziano WWTP had three trains, each consisting of primary clarification, biological oxidation, secondary clarification and final chlorination (Fig. 5.24). Pretreatment of the incoming untreated wastewater prior to the three trains was undertaken by coarse and fine screening and with sand for oil and grease removal. Trains A and C were identical in design capacity, treating 24 MLD each, while Train B had an original capacity of 12 MLD. Shortly after assuming operations at the Verziano WWTP in July 1995, the water company ASM Brescia undertook a series of evaluations and identified problems relating to additional discharges. The most significant problem was plant capacity, which was about two-thirds of that required. In response, several important projects were undertaken over the subsequent 5-year period (1995–2000) to remedy these issues. The principal remedial step was the upgrading of Train B, the oldest of the three trains, from 12 MLD to 38 MLD annual average flow capacity by converting the
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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
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 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 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.
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
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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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