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Membrane Processes for Reclamation of Municipal Wastewater 443 obtained. The results obtained from the pilot trial study showed that 2.5 mg/L Al was an appropriate dosing concentration in this particular application. Hagmeyer et al. (23) worked on drinking water treatment of reservoir water using a UF process with alum dosage and concluded that the optimal alum dosing concentration was depending on the feed water quality. On the other hand, within an NaOCl CEB interval, biofouling of the UF membrane was formed due to the substances of microbial origin that clung to the membrane surface and could not be removed through the backwash. It was increased with time. The biofouling could be eliminated after the NaOCl CEB at pH 11.5. Immediately after that, H2SO4 CEB at pH 2 was followed to remove the scaling. Finally, the membrane flux was recovered again. 3.3.3. Normalized Flux as a Function of Time Normalized flux (corrected to 20 C) of the UF membranes as a function of time throughout the study under different concentrations of alum dosage is shown in Fig. 10.5. Corresponding to TMP, a low TMP resulted in a high normalized flux since the water flow rate was fixed, and vice versa. A stable TMP also provided a stable flux. Figure 10.5a indicated that the normalized flux dropped from 250–300 L/m 2 h at 0.1 MPa to 200–250 L/m 2 h at 0.1 MPa as alum concentration was reduced from 4.8 to 1.3 mg/L, which could be explained as follows. Since the flocculation capacity of alum reduced with a decrease in alum concentration, the size of flocculated particles decreased for the fixed flocculation duration. Subsequently, small colloidal might easily enter the surface pores of the UF membrane, and they were more difficult to be removed through the normal backwash than the large flocs. As a consequence, the membrane resistance was enhanced and high membrane fouling was resulted. Figure 10.5b illustrated that the normalized flux had been stable when alum concentration was 2.5 mg/L since 29 April, and it was between 200 and 250 L/m 2 h at 0.1 Map from 9 May–6 June. The results showed that the optimum alum concentration was 2.5 mg/L for maintaining a stable flux of the UF membranes. 3.3.4. Overall Process Consideration It is a proper combination of the dead-end flow operation of hollow fiber membranes with alum dosage for treating the secondary treated effluent because the flocs formed are much larger than the membrane pores and can be easily removed with a normal backwash, which benefits flux recovery. Alum dosing concentration was found critical for achieving stable plant operation in dead-end flow. The containerized pilot plant is equipped with an advanced programmable logic controller (PLC) control system and is able to operate automatically with well-designed programs. The successful pilot trial runs have demonstrated that the employment of a UF membrane process in dead-end operation mode is capable of recovering 90.1% of the secondary treated sewage effluent and the reclaimed water met target quality as RO feed for NEWater production. Based on the results of the pilot trials under the operating conditions of feed flow 5.0 m 3 /h and backwash interval 25 min during the stable operation of the plant, an economic evaluation in terms of consumption of chemical and power is summarized in Table 10.5. It can be seen that for 1 m 3 of product water, the cost on chemical consumption is S$0.02 or
444 J. Qin and K.A. Kekre Fig. 10.5. Normalized flux as a function of time (13). (a) Concentration of alum dosage: 4.8, 1.3 and 0.6 mg/L (b) Concentration of alum dosage: 2.5 mg/L 1.3 cents (US) and the total power consumption is 0.194 kW-h/m 3 which is quite low compared to previous studies (24–26). The total cost, including chemical and energy consumption for producing 1 m 3 of product water, is around S$0.05 or 2.7 cents (US). The results of the economic evaluation indicate that the UF membrane process is attractive for the reclamation of the secondary treated sewage effluent. It should be noted that the inclusion of this would have further improved the economics when the chemicals are purchased as a bulk amount, and the pump efficiency is enhanced for a full-scale plant.
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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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172 N.K. Shammas and L.K. Wang chec
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178 N.K. Shammas and L.K. Wang 4. C
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182 N.K. Shammas and L.K. Wang Sens
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186 N.K. Shammas and L.K. Wang Maxi
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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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282 J. Paul Chen et al. solutions a
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284 J. Paul Chen et al. Salt cheese
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286 J. Paul Chen et al. Table 7.2 L
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288 J. Paul Chen et al. Table 7.3 L
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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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298 J. Paul Chen et al. into a smal
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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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330 J. Paul Chen et al. 55. Basu OD
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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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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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674 K. Mohanty and R. Ghosh 3.2. Tw
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680 K. Mohanty and R. Ghosh Cabassu
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682 K. Mohanty and R. Ghosh 4.3. Ga
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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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