The MBR Book: Principles and Applications of Membrane

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Table 2.4 Microbial metabolism types in wastewater biotreatment Component Process Electron acceptor Type Fundamentals 41 Organic-carbon aerobic biodegradation O 2 Aerobic Ammonia Nitrification O 2 Aerobic Nitrate Denitrification NO 3 � Facultative Sulphate Sulphate reduction SO 4 2� Anaerobic Organic-carbon Methanogensis CO 2 Anaerobic group of bacteria have been shown to be �-subclass Proteobacteria (Manz et al., 1994; Sofia et al., 2004;); all currently characterised ammonia oxidisers belong to this group. Although these bacteria remained dominant in an MBR, a higher proportion of other bacteria (52–62%) were recorded in these studies suggesting that the long SRT shifted the microbial population away from Proteobacteria-� (Luxmy et al., 2000; Sofia et al., 2004). Nitrosomonas and Nitrosospira are the autotrophic ammoniaoxidising bacteria found in activated sludge, and Nitrobacter and Nitrospira the nitrite-oxidising bacteria, and it is thus between these groups that the nitrification process is carried out (Wagner et al., 1996, 1998). Sofia et al. (2004) found the predominant nitrifiers were Nitrosospira and Nitrospira, whilst Witzig et al. (2002) showed no Nitrosomonas or Nitrobacter or Nitrosospira to be found in membranefiltered sludge. This implies that the ammonia-oxidising bacteria are system-specific and that Nitrospira are responsible for the reduction of nitrite. Nitrifying autotrophs are known to be slow-growing bacteria. The long SRTs available in an MBR system are thus accepted as being highly advantageous for nitrification. Micro-organisms can be classified according to the redox conditions in which they prevail (Table 2.4), and hence the process type, and their energy requirements. Heterotrophs use organic carbon as an energy source and for synthesis of more cellular material, and are responsible for BOD removal and denitrification. Autotrophs use inorganic reactions to derive energy, for example, oxidation of iron (II) to iron (III) or hydrogen to water, and obtain assimilable material from an inorganic source (such as carbon from carbon dioxide) to carry out such processes as nitrification, sulphate reduction and anaerobic methane formation. Autotrophs are generally less efficient at energy gathering than heterotrophs and therefore grow more slowly. Microbial growth relies on appropriate conditions of total dissolved solids (TDS) concentration, pH and temperature. Most micro-organisms can only function in relatively dilute solutions, around neutral pH and at ambient temperature, though some can grow under extreme conditions: Thiobacillus growth is optimum at pH 1.5–2.0. Some MBRs are based on growth of specific cultures, such as for nitrification (Section 2.2.4.4), or recalcitrant organics biodegradation in extractive MBRs (Section 2.3.2). Classification of micro-organisms according to the temperature at which they are most active provides the terms psychrophilic, mesophilic and thermophilic for optimum growth temperatures of 15, 35 and 55°C, respectively. While most aerobic biological processes are operated at ambient temperatures, the micro-organisms usually have mesophilic temperature optima, such that pumping operations in sMBRs can provide additional benefit in raising the reactor temperature to both increase biotreatment efficacy and reduce liquid viscosity (Van Dijk and Roncken, 1997). Few examples exist
42 The MBR Book of MBRs operating under thermophilic conditions, though this mode appears to offer some promise for treatment of heavy COD loads and/or recalcitrant organic matter (Section 5.4.4). 2.2.4 Process design and operation fundamentals Monod kinetics can be used to design biological systems for a limiting substrate (S kg/m 3 ), usually organic carbon provided as BOD or COD. Using known biokinetic constants (Appendix B) the system kinetics and system mass balance can be used to define the rate of substrate degradation, biomass growth and sludge production. A full description of Monod kinetics for process design can be found in Metcalf and Eddy (2003). 2.2.4.1 Substrate degradation The rate biokinetics determine the loading rate (the rate at which organic matter is introduced into the reactor, kg BOD/m 3 ), as determined by Monod kinetics. Accordingly, the rate of reaction is first order with respect to a limiting substrate up to a maximum specific growth rate, after which growth is unaffected by any increase in substrate concentration: mmS m � K � S (2.2) where � is the growth rate (/h), and � m is the maximum specific growth rate (/h), S is the limiting substrate concentration (g/m 3 ) and K s is the saturation coefficient (g/m 3 ). It follows that there is a maximum specific substrate utilisation rate which is defined as: k s � Y mm (2.3) Where Y is the biomass yield (i.e. the mass of cells formed per mass of substrate consumed) (g Volatile suspended solids (VSS)/g BOD). Y can be controlled by manipulating environmental factors such as temperature and pH, but such changes are detrimental to biodegradation in the reactor (Eckenfelder and Grau, 1998). Substituting terms defined by Monod kinetics into a mass balance expression for the system and rearranging produces an expression in terms of effluent dissolved substrate S e in g/m 3 : ( ) ( ) Ks 1� keux S � u Yk �k�1 x e (2.4) where � x is the SRT or sludge age (/day) and k e term is the death rate constant. SRT is an important design parameter used for suspended growth systems. One of the advantages of an MBR system is that all of the solids are retained by the membrane
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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
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 42 and 43: 3µm (a) (b) membrane is chemically
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 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
Page 92 and 93: has been proposed by Cho and co-wor
Page 94 and 95: Fundamentals 77 in the influent. Ab
Page 96 and 97: MLSS sample Centrifugation 5 min 50
Page 98 and 99: Table 2.11 Concentration of SMP com
Page 100 and 101: Fundamentals 83 correlation of MBR
Page 102 and 103: (Cui et al., 2003) by inducing liqu
Page 104 and 105: Fundamentals 87 air cannot be used
Page 106 and 107: 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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