The MBR Book: Principles and Applications of Membrane

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3µm (a) (b) membrane is chemically cleaned (Section 2.1.4.3), and should ideally offer some resistance to fouling. Whilst, in principal, any polymer can be used to form a membrane, only a limited number of materials are suitable for the duty of membrane separation, the most common being: ● polyvinylidene difluoride (PVDF) ● polyethylsulphone (PES) ● polyethylene (PE) ● polypropylene (PP) Fundamentals 25 Figure 2.3 Anisotropic UF membranes: (a) polymeric (thickness of “skin” indicated) and (b) ceramic (by kind permission of Ionics (a) and Pall (b)) Rejection rate (%) 120 100 0 0 0.05 0.1 0.15 0.2 0.25 All the above polymers can be formed, through specific manufacturing techniques, into membrane materials having desirable physical properties, and they each have reasonable chemical resistance. However, they are also hydrophobic, which makes the susceptible to fouling by hydrophobic matter in the bioreactor liquors they are filtering. This normally necessitates surface modification of the base material to produce a hydrophilic surface using such techniques as chemical oxidation, organic 80 60 40 20 Diameter of uniform latex (µm) Figure 2.4 Surface of membrane and pore-size distribution with respect to rejection of homodispersed latex (by kind permission of Asahi-Kasei)
26 The MBR Book chemical reaction, plasma treatment or grafting. It is this element that, if at all, most distinguishes one membrane material product from another formed from the same base polymer. This modification process, the manufacturing method used to form the membrane from the polymer, most often PVDF for many MBR membranes, and the method for fabricating the membrane module (Section 2.1.4) from the membrane are all regarded as proprietary information by most suppliers. 2.1.3 Membrane configurations The configuration of the membrane, that is, its geometry and the way it is mounted and oriented in relation to the flow of water, is crucial in determining the overall process performance. Other practical considerations concern the way in which the membrane elements, that is the individual discrete membrane units themselves, are housed in “shells” to produce modules, the complete vessels through which the water flows. Ideally, the membrane should be configured so as to have: (a) a high membrane area to module bulk volume ratio, (b) a high degree of turbulence for mass transfer promotion on the feed side, (c) a low energy expenditure per unit product water volume, (d) a low cost per unit membrane area, (e) a design that facilitates cleaning, (f) a design that permits modularisation. All membrane module designs, by definition, permit modularisation (f), and this presents one of the attractive features of membrane processes per se. This also means that membrane processes provide little economy of scale with respect to membrane costs, since these are directly proportional to the membrane area which relates directly to the flow. However, some of the remaining listed characteristics are mutually exclusive. For example, promoting turbulence (b) results in an increase in the energy expenditure (c). Direct mechanical cleaning of the membrane (e) is only possible on comparatively low area:volume units (a). Such module designs increase the total cost per unit membrane area (d), but are inevitable given that cleaning is of fundamental importance in MBR processes where the solids and foulant loading on the membrane from the bioreactor liquor is very high. Finally, it is not possible to produce a high-membrane area to module bulk volume ratio without producing a unit having narrow retentate flow channels, which will then adversely affect turbulence promotion and ease of cleaning. There are six principal configurations currently employed in membrane processes, which all have various practical benefits and limitations (Table 2.2). The configurations are based on either a planar or cylindrical geometry and comprise: 1. plate-and-frame/flat sheet (FS) 2. hollow fibre (HF) 3. (multi)tubular (MT) 4. capillary tube (CT) 5. pleated filter cartridge (FC) 6. spiral-wound (SW) Of the above configurations, only the first three (Fig. 2.5, Table 2.2) are suited to MBR technologies, principally for the reasons outlined previously: the modules must
Page 2 and 3: The MBR Book
Page 4 and 5: The MBR Book: Principles and Applic
Page 6 and 7: Contents Preface ix Contributors xi
Page 8 and 9: Contents vii 4.2.5 The Industrial T
Page 10 and 11: Preface What’s In and What’s No
Page 12 and 13: Term Meaning Common units MLD Megal
Page 14 and 15: Contributors A number of individual
Page 16 and 17: Contributor(s) Association/Organisa
Page 18 and 19: Introduction With acknowledgements
Page 20 and 21: such as the filtration market, tech
Page 22 and 23: D R IVE R S R EST R AI N TS Bathing
Page 24 and 25: Introduction 7 Much of the legislat
Page 26 and 27: of non-point source pollution contr
Page 28 and 29: exploitation index (WEI), the value
Page 30 and 31: 1 500 000 1 250 000 1 000 000 750 0
Page 32 and 33: Alternative immersed FS and HF memb
Page 34 and 35: 1.6 Conclusions Whilst the most sig
Page 36 and 37: Introduction 19 USEPA (2006b) www.e
Page 38 and 39: Fundamentals With acknowledgements
Page 40 and 41: they can be put, which then provide
Page 44 and 45: Table 2.2 Membrane configurations C
Page 46 and 47: 2.1.4 Membrane process operation 2.
Page 48 and 49: only pseudo-steady-state (or stabil
Page 50 and 51: P max P dP/dt backwash cycle t b Ba
Page 52 and 53: Fundamentals 35 2.1.4.6 Critical fl
Page 54 and 55: neo-exponential increase at fluxes
Page 56 and 57: Screened raw sewage biologically ar
Page 58 and 59: Table 2.4 Microbial metabolism type
Page 60 and 61: which affords the operator complete
Page 62 and 63: Cumulative %ile undersize 1 0.8 0.6
Page 64 and 65: occurs from the surrounding air to
Page 66 and 67: (Madoni et al., 1993). The inter-re
Page 68 and 69: Viscosity (mPa s) 100 10 1 Viscosit
Page 70 and 71: on discharged P levels have been im
Page 72 and 73: Membrane process mode Diffusion Ext
Page 74 and 75: energy demand in kWh/m 3 permeate p
Page 76 and 77: Table 2.5 System facets of denitrif
Page 78 and 79: Fundamentals 61 Moreover, the poten
Page 80 and 81: iomass. There are also issues with
Page 82 and 83: Table 2.6 Effect of pore size on MB
Page 84 and 85: Fundamentals 67 fouling to be influ
Page 86 and 87: Fundamentals 69 fouling (i.e. membr
Page 88 and 89: 2.3.6 Feed and biomass characterist
Page 90 and 91: 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
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aerobic counterpart. This may be pa
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of the particularly large-diameter
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(c) air channelling, the risk of wh
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Case Studies With acknowledgements
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5.1 Introduction Membrane Bioreacto
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Case studies 211 Table 5.1 Comparis
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Case studies 213 0.6 m 3 per unit.
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Case studies 215 area of 15 840 m 2
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Aeration tank 1 FBDA FBDA 32 x J200
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Case studies 219 In this UNR config
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Table 5.6 Design criteria, Running
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Works inlet Inlet works Storm tank
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Case studies 225 to be treated to a
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Case studies 227 membranes, assembl
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Figure 5.16 A Naston package plant
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Air Influent DN N M Figure 5.18 The
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Table 5.9 Toray membrane-based MBR
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Figure 5.23 Aeration tank and cover
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Figure 5.24 The original plant at B
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Main permeate header Permeate pump
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Case studies 241 flow. Sludge waste
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Table 5.15 Water quality data, Unif
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TMP (Kpa) 80 70 60 50 40 30 20 10 0
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10 LMH; the plant operated at fluxe
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Table 5.17 Feed and treated water q
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Table 5.18 Water quality, Sobelgra
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Figure 5.37 Airlift municipal WWTP,
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Case studies 255 has been 20 g/L, b
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Case studies 257 The company had in
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Filtrate (ml) 25 20 15 10 5 IIndust
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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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The MBR Book: Principles and Applications of Membrane

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