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Membrane Processes for Reclamation of Municipal Wastewater 449 Table 10.9 Normalized flux and salt rejection of the RO membrane (14) Parameter Test 1 Test 2 Test 3 Test 4 Flux rate (gallon/ft 2 day) 26 20 15 10 Operating pressure (psi) 136–141 117–136 75–83 52–62 Normalized flux (L/m 2 h MPa at 25 C) 43.6–36.6 34.3–25.9 40.9–33.4 42.4–34.0 Rejection (%) 98.4–98.6 98.1–97.8 96.9–97.5 96.1–96.5 Figure 10.7 and Table 10.9 show that the normalized flux of the RO membrane dropped obviously by 3.2% per day from 43.6 to 36.6 L/m 2 h MPa at 25 C within 5 days from 12 to 16 May when the RO unit was operated at the flux rate of 26 gallon/ft 2 day. Then, it was operated at 10 gallon/ft 2 day for 2 weeks from 20 May to 3 June; the normalized flux dropped slightly by 0.3% per day from 39.1 to 37.7 L/m 2 h. And then, the flux rate was increased to 15 gallon/ ft 2 day during 3–18 June, the normalized flux dropped slightly by 0.3% per day from 37.2 to 35.5 L/m 2 h. After that, the flux rate was further increased to 20 gallon/ft 2 day; the normalized flux declined significantly 12.2% per day from 34.3 to 25.9 L/m 2 h within 2 days, 18–20 June. Then, the first CIP was conducted. When RO unit was operated again at 15 gallon/ft 2 day during 24 June–14 July, the normalized flux declined by 1% per day from 40.9 to 33.4 L/m 2 h over 3 weeks. CIP was done for the second time. Finally, RO unit was operated at 10 gallon/ft 2 day during 15 July–20 August, and the normalized flux declined by 0.6% per day from 42.4 to 34.0 L/m 2 h over 5 weeks. The average normalized flux was 38 L/m 2 h MPa at 25 C. Both of the normalized flux decline rates for the first operating flux rate of 10 and 15 gallon/ft 2 day were 0.3% per day, whereas they increased to 0.6 and 1% per day for the second 10 and 15 gallon/ft 2 day, respectively. The increases in the normalized flux decline rates could be attributed to the facts that they were calculated based on the respective initial normalized fluxes after the system operation was stable for the first run but immediately after a CIP was conducted for the second run. However, the normalized flux decline rates of 0.3–0.6% per day at 10 gallon/ft 2 day and of 0.3–1% per day at 15 gallon/ft 2 day were much lower than those of 3.2–12.2% per day at higher operation flux rates of 20–26 gallon/ft 2 day. The above results indicate that the optimal operation flux rate of the RO membrane ranged from 10 to 15 gallon/ft 2 day for this application. Figure 10.6 also shows that the normalized flux recovery after the first CIP and second CIP comparing to the initial flux was 94 and 97%, respectively. Table 10.9 also indicates that salt rejections of the RO membrane ranged of 96–97% at 10 gallon/ft 2 day, 97–98% at 15 gallon/ft 2 day, and over 98% at 20 gallon/ft 2 day. Higher flux rate was the RO membrane operated at, higher rejection was obtained. It appeared that salt rejection increased with time by 0.8% of the maximum at the beginning of each test at a fixed operation flux rate and then fluctuated within 0.5%. Table 10.10 shows the permeate quality of the RO membrane during the study and the target quality as NEWater (20). It can be seen that the quality of the RO permeate meets the target quality as NEWater in terms of the parameters measured except pH which could be easily raised by adding NaOH.
450 J. Qin and K.A. Kekre Table 10.10 Comparison of the RO permeate quality and the target quality (14) Parameter RO permeate quality Target quality pH 5.7–6.1 7–8.5 Conductivity (mS/cm) 18.4–46.4
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Membrane and Desalination Technolog
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Editors Dr. Lawrence K. Wang Zorex
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vi Preface Our treatment of polluti
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Contents Preface . ................
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Contents xi 3.4. Considering Existi
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Contents xiii 7. Membrane Separatio
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Contents xv 6. Design for Large Com
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Contents xvii 13. Desalination of S
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Contributors JIRAPAT ANANPATTARACHA
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CONTENTS 1 Membrane Technology: Pas
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Membrane Technology: Past, Present
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48 J. Ren and R. Wang Key Words Pol
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50 J. Ren and R. Wang Nonporous den
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52 J. Ren and R. Wang pervaporation
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54 J. Ren and R. Wang HO HO OH O OH
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56 J. Ren and R. Wang Fig. 2.7 Chem
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58 J. Ren and R. Wang N O O 3.10. P
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60 J. Ren and R. Wang inversion, th
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62 J. Ren and R. Wang where Dm i an
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64 J. Ren and R. Wang as nucleation
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66 J. Ren and R. Wang and no polyme
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68 J. Ren and R. Wang where b ¼ v1
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70 J. Ren and R. Wang S gelation ti
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72 J. Ren and R. Wang structure wil
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74 J. Ren and R. Wang Viscous finge
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76 J. Ren and R. Wang nonsolvent so
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78 J. Ren and R. Wang Thickness of
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80 J. Ren and R. Wang 5.1.1. Rheolo
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82 J. Ren and R. Wang the spinneret
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84 J. Ren and R. Wang Dynamic visco
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86 J. Ren and R. Wang where A is th
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88 J. Ren and R. Wang In the spinni
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90 J. Ren and R. Wang stress, espec
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92 J. Ren and R. Wang solution at t
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94 J. Ren and R. Wang TIPS ¼ Therm
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96 J. Ren and R. Wang 5. Kesting RE
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98 J. Ren and R. Wang 51. Matsuyama
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100 J. Ren and R. Wang 92. Ren J, C
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102 L. Song and K.Guan Tay Key Word
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104 L. Song and K.Guan Tay Flux A A
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106 L. Song and K.Guan Tay increase
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108 L. Song and K.Guan Tay Table 3.
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110 L. Song and K.Guan Tay • A fe
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112 L. Song and K.Guan Tay Feed wat
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114 L. Song and K.Guan Tay Fouling
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116 L. Song and K.Guan Tay Fouling
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118 L. Song and K.Guan Tay The symb
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120 L. Song and K.Guan Tay Table 3.
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122 L. Song and K.Guan Tay Permeate
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124 L. Song and K.Guan Tay Average
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128 L. Song and K.Guan Tay generati
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132 L. Song and K.Guan Tay flux. Un
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134 L. Song and K.Guan Tay 14. Kaak
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136 N.K. Shammas and L.K. Wang remo
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138 N.K. Shammas and L.K. Wang The
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140 N.K. Shammas and L.K. Wang excu
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142 N.K. Shammas and L.K. Wang dire
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144 N.K. Shammas and L.K. Wang broa
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146 N.K. Shammas and L.K. Wang remo
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148 N.K. Shammas and L.K. Wang 4. T
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150 N.K. Shammas and L.K. Wang 8. S
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152 N.K. Shammas and L.K. Wang 4.5.
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154 N.K. Shammas and L.K. Wang Tabl
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156 N.K. Shammas and L.K. Wang phys
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158 N.K. Shammas and L.K. Wang mono
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164 N.K. Shammas and L.K. Wang Fig.
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170 N.K. Shammas and L.K. Wang CSTR
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188 N.K. Shammas and L.K. Wang 2. 2
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196 N.K. Shammas and L.K. Wang PFR
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198 N.K. Shammas and L.K. Wang 16.
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5 Treatment of Industrial Effluents
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Treatment of Industrial Effluents,
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CONTENTS 6 Treatment of Food Indust
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Treatment of Food Industry Foods an
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272 J. Paul Chen et al. formation a
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274 J. Paul Chen et al. the rejecte
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276 J. Paul Chen et al. The MF memb
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278 J. Paul Chen et al. Most UF mem
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280 J. Paul Chen et al. The applica
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284 J. Paul Chen et al. Salt cheese
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290 J. Paul Chen et al. Fig. 7.7. V
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292 J. Paul Chen et al. Considering
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294 J. Paul Chen et al. Approximati
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296 J. Paul Chen et al. 5.2. The Po
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300 J. Paul Chen et al. 6.2.3. Tubu
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302 J. Paul Chen et al. Fig. 7.13.
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304 J. Paul Chen et al. a Feed b Me
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306 J. Paul Chen et al. l Product c
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308 J. Paul Chen et al. Feed Permea
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310 J. Paul Chen et al. From Table
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312 J. Paul Chen et al. To calculat
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314 J. Paul Chen et al. biofilm for
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316 J. Paul Chen et al. magnesium,
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318 J. Paul Chen et al. reduction o
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320 J. Paul Chen et al. Table 7.6 C
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322 J. Paul Chen et al. many factor
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324 J. Paul Chen et al. 9.2. Gas Se
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326 J. Paul Chen et al. c w2 ¼ Con
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332 J. Paul Chen et al. 99. Teodosi
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334 N.K. Shammas and L.K. Wang 1. I
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342 N.K. Shammas and L.K. Wang impo
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348 N.K. Shammas and L.K. Wang 5-20
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CONTENTS 9 Adsorption Desalination:
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Adsorption Desalination: A Novel Me
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Adsorption Desalination: A Novel Me
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518 P. Kajitvichyanukul et al. 8. A
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12 Desalination of Seawater by Ther
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Desalination of Seawater by Thermal
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CONTENTS 13 Desalination of Seawate
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Desalination of Seawater by Reverse
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670 K. Mohanty and R. Ghosh 1. INTR
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672 K. Mohanty and R. Ghosh municip
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680 K. Mohanty and R. Ghosh Cabassu
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684 K. Mohanty and R. Ghosh Membran
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688 K. Mohanty and R. Ghosh MBRs ca
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690 K. Mohanty and R. Ghosh two pro
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692 K. Mohanty and R. Ghosh can be
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694 K. Mohanty and R. Ghosh 27. Bel
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696 K. Mohanty and R. Ghosh 70. Fut
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Acceptance testing, 384-385 ACF. Se
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Index 701 Challenge test solution d
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Index 703 Disinfection by-products
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Index 705 Hemodialysis, 2, 6, 281 H
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Index 707 Membrane bioreactor-rever
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Index 709 Microfiltration-reverse o
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Index 711 Physical cleaning, 322-32
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Index 713 Reynolds number, 676, 679
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Index 715 Thermal concentration, 25
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