The MBR Book: Principles and Applications of Membrane

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Inflow Buffer tank Filtration Denitrification Nitrification Ultrafiltration Solids velocity is 2 m/s. This velocity provides fluxes between 50 and 60 LMH at a specific energy demand of 2–3 kW/m 3 . Following excessive rainfall, it is sometimes necessary to operate at higher fluxes (up to 90 LMH), which can be achieved by increasing the liquid pumping rate to achieve a CFV of up to 4 m/s. At this flow rate, the specific energy demand increases to 5–6 kW/m 3 . During summer months of low rainfall and so reduced volumetric demand on the MBR, the circulation pump can be either switched off or operated at low flow, in which case the energy demand decreases. The MLSS is generally between 12 and 15 g/L. 5.4.3.4 Performance comparison Given the availability of the data (Robinson, 2005), it is instructive to compare: ● the hydraulic performance characteristics of the pumped and airlift mode sMBRs; ● treatment of leachate vs. dairy effluent feedwaters. This comparison yields an indication of the relative fouling propensities of the respective mixed liquors generated by the two matrices. Data for the airlift and pumped configurations (Table 5.24) indicate that the latter operate at almost twice the flux of the airlift type (107 LMH daily average for Bilbao, cf. 57 for Freiburg) but at the expense of a 66% higher specific energy demand (5 vs. 3 kWh/m 3 permeate). The projected membrane life for the airlift configuration is also higher, such that the overall specific operating cost for this mode of operation is 32% lower than that of the pumped sMBR. The filterability of the Bilbao leachate sludge is also much higher than that of Freiburg. Compared with the three food effluent MBRs for which data are provided, the landfill leachate plant operates at a higher cost, associated mainly with a higher energy demand (due to the higher crossflow required to maintain the flux) and a shorter membrane life (brought about by the low filterability/high fouling propensity of the leachate biomass). 5.4.4 Thermophylic MBR effluent treatment, Triqua, the Netherlands Air Figure 5.44 The treatment scheme at Freiburg Activated carbon Case studies 261 Sludge Effluent Veiligheidspapierfabriek (VHP) Ugchelen B.V., based near Apeldoorn in the Netherlands, is a subsidiary of the international banknote paper manufacturer Arjo Wiggins.
262 The MBR Book Table 5.24 Data for various Wehrle leachate and food effluent treatment plant Customer/site: Units Freiburg Bilbao Kellogg Dairy Crest Dairy Gold Application: Leachate Leachate Food Dairy Dairy Airlift Pumped Pumped Pumped Pumped Flow rate MLD 0.12 1.8 1.8 1.2 2.0 Membrane area m 2 88 700 864 486 648 Flux (year average) LMH 54 102 71 98 125 Flux (day average) LMH 57 107 87 103 129 Membrane price total € 19 360 189 000 198 400 111 600 163 200 Membrane life years 6 4 4.50 5.00 6.00 Membrane replacement €/a 3227 47 250 44 089 22 320 27 200 cost Specific energy demand b kWh/m 3 3 5 3.75 3.18 2.14 Specific energy cost €/kWh 0.06 0.06 0.06 0.06 0.06 Total energy cost €/a 7490 187 245 121 564 79 347 91 264 Total operating cost c €/a 10 716 234 495 165 653 101 667 118 464 Total specific operating €/m 3 0.26 0.38 0.31 0.24 0.17 cost aMembrane � Biology � Civils bUF stage cSum of energy and membrane replacement Robinson (2005). Banknote paper is made from cotton combers bleached with sodium hydroxide and hydrogen peroxide. The project concerned the use of an MBR, originally developed for landfill leachate treatment, operating under thermophilic conditions for removing colloidal and high molecular weight dissolved material to allow the reuse of wastewater from the bleaching plant. The process, based on 8 mm diameter MT polyvinyllidene difluoride (PVDF) membranes, has been piloted on a variety of highstrength recalcitrant industrial effluents. A trial was originally conducted between June and October 1999 for the clarification of wastewater from the bleaching plant. Wastewater from the bleaching process has a mean COD of 4500 mg/L, a pH of �12 and a temperature of 75–85°C. The quality of the effluent from these trials, which has a COD of around 400 mg/L, was sufficient to allow it to be reused in the bleaching vessels and led to the decision to install a full-scale plant (Fig. 5.45) with a capacity of 0.24 MLD in November 2000. The system comprises a buffer tank followed by a dual-chamber DAF process for the removal of cotton flocks and fibres. In the second chamber, waste carbon dioxide from the boiler house is introduced to lower the pH of the solution from �12 to 8–9, an ingenious use of waste gas which reduces CO 2 emissions. The pH-adjusted clarified effluent is then transferred to the MBR aeration tank, 250 m 3 in volume and thus providing an HRT of �24 h. The MBR operates at between 55°C and 60°C and an MLSS of 20 g/L. Three sidestream MT membrane units are employed (Fig. 5.46), each comprising 6 � 3 m-long modules in series with each module having a membrane area of 4 m 2 and hence providing a total area of 72 m 2 . The membrane units operate at a mean flux of �120 LMH, an average TMP of 4 bar, and a mean crossflow velocity of �4.5 m/s. The permeate COD concentration is 400–500 mg/L, and it is reheated by passing it through a heat exchanger with the influent before being reused
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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
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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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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 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 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
Page 318 and 319: Japan Water Works Association (JWWA
Page 320 and 321: Nomenclature � Separation (m) �
Page 322 and 323: Nomenclature 305 Rsup Hydraulic res
Page 324 and 325: Abbreviations The following lists k
Page 326 and 327: 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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