The MBR Book: Principles and Applications of Membrane

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Table 5.18 Water quality, Sobelgra plant Parameter Feed concentration Load Effluent concentration (mg/L) (mg/L) (kg/day) (mg/L) COD 1880–2100 4000 100–200 BOD 700–930 2000 2–5 TSS 330–460 800 0 TN 35–50 100 1–2 TP 13–15 30 �1 Figure 5.36 Koch membrane systems PURON ® modules at Sobelgra Case studies 251 Belgium. This meant that the capacity of the existing conventional WWTP had to be doubled and, due to lack of space on the factory site, conventional technology could not be used. The MBR plant (Fig. 5.36) was piloted in the Spring of 2003 and installed by the Belgian turnkey constructor ENPROTECH with the Belgian Engineering company SEE:WATER supplying and assembling the MF system. The MBR was retrofitted into the existing aeration tank, which was divided into two parts to provide an aeration tank and a separate membrane tank. The tank of the former clarifier has been converted to an additional bioreactor, such that, in the new process, 25% of the total treatment volume is occupied by the membranes. The membrane tank is equipped with 16 500 m 2 PURON ® membrane modules, providing a total membrane area of 8000 m 2 .
252 The MBR Book The plant consists of a screening at 0.25 mm prior to biotreatment using two tanks in series. The sludge is then transferred to two membrane compartments, with a third chamber being available for future extensions of the plant. The membrane compartments are fed from the bottom so that the sludge flows upwards through the membrane modules. Permeate is extracted from the membrane modules under a slight vacuum. The activated sludge is concentrated during this process and is led back into the biology tanks by means of spillways. 5.3.5 Asahi Kasei The Asahi Kasei Microza HF membrane module was installed at a 0.6 MLD food effluent treatment plant in Japan in August 2004 and subsequently expanded to 0.9 MLD in early 2005. The respective mean BOD, COD and TSS values of the feed are 1080, 630 and 377 mg/L, respectively, and all are removed by at least 99.5% by the process. Originally, 16 racks of 100 m 2 modules (i.e. a total membrane area of 1600 m 2 ), each containing four elements (Fig. 4.27a), were inserted in the tank to achieve the total flow capacity required, the modules being retrofitted into an existing MBR membrane tank plant. The plant is operated at �8 g/L MLSS. A stable TMP of around 0.2 bar was maintained over the first 3 months of operation at a flux close to 16 LMH at an aeration rate of 384 m 3 /h, equating to a SAD m of 0.24 m 3 /h per m 2 and a SAD p of 15 m 3 air per m 3 . 5.4 Sidestream membrane plants 5.4.1 Norit X-Flow airlift process The earliest example of the use of an airlift sidestream membrane bioreactor (sMBR) for municipal wastewater is probably that of the pilot plant at Vienna (Fig. 5.37), installed in 1999. This plant has a capacity of 0.24 MLD and the feed strength is 300–700 mg/L COD. The plant provides an effluent of �30 mg/L COD at all times. The plant comprises pretreatment using a coarse grid followed by a sand and FOG trap. A submersible pump, which also provides a degree of comminution, pumps the raw effluent into a sedimentation tank with an HRT of 30–60 min. The supernatant is then fed through a 0.8 mm screen and into the bioreactor, into which ferric coagulant is dosed directly. Membrane separation is achieved by four vertically-mounted 38PR-type MT modules fitted with 5.2 mm F4385 membranes. The modules are operated at a TMP of 0.05–0.15 bar with a combined pumped air and liquid crossflow rate of �1 m/s. This achieves a flux of 40 LMH for dry weather flow, rising to 55 LMH at full capacity when the TMP is at its highest value of 0.3 bar. The permeability is generally maintained between 300 and 400 LMH/bar, only falling below this range when fluxes of �50 LMH are sustained for several days. Membrane cleaning is achieved by chemical soaking every 15–30 days using a combined chemical clean of hypochlorite and citric acid (Fig 5.37).
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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
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4m 4m 1m Commercial technologies 19
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Figure 4.36 Ejector aerator Commerc
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Denitrification Nitrification Waste
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modules, with pore sizes ranging fr
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(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 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 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
Page 308 and 309: Table D.5 Membrane module details o
Page 310 and 311: Appendix E Major Recent MBR and Was
Page 312 and 313: Conference title meet Dates Locatio
Page 314 and 315: Event Last held Location Website Fo
Page 316 and 317: 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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