the RO stage. Furthermore, reaction with a compound added after the media filter can cause a precipitate to form. This ismost noticeable with antiscalants. Nearly all antiscalants are negatively charged and will react with cationic coagulants orflocculants present in the water. The membranes in several RO plants have been heavily fouled by a gel formed by reactionbetween cationic polyelectrolytes and antiscalants.Direct interference occurs when the compound itself affects the membrane resulting in a flux loss. The ionic strength of thewater may have an effect on the interference of the coagulant or flocculant with the membrane. If so, the result at brackishwater conditions could be different from that at seawater conditions. To minimize the risk of direct or indirect interference withthe RO membrane, anionic or nonionic flocculants are preferred rather than cationic flocculants. Overdosing must beavoided.2.5.5 Coagulation-FlocculationFor raw waters containing high concentrations of suspended matter resulting in a high SDI, the classic coagulationflocculationprocess is preferred. The hydroxide flocs are allowed to grow and settle in specifically designed reactionchambers. The hydroxide sludge is removed, and the supernatant water is further treated by media filtration.For the coagulation-flocculation process, either a solids-contact type clarifier (see also Section 2.3.6 Lime Softening) or acompact coagulation-flocculation reactor may be used. For details, please refer to the general water treatment textbooks /3, 4/.2.5.6 Microfiltration/UltrafiltrationMicrofiltration (MF) or ultrafiltration (UF) membrane removes virtually all suspended matter and, in the case of ultrafiltration,also dissolved organic compounds depending on their molecular mass and on the molecular mass cut-off of the membrane.Hence, an SDI
If the differential pressure across the filter increases rapidly, it is an indication of possible problems in the raw water supply orin the pretreatment process. The filter provides some degree of short-term protection for the membranes while correctiveaction is taking place.Replacing cartridge filters more often than every 1 to 3 months usually indicates a problem with the pretreatment. Thecartridge filter, however, is not meant to be a major component for the removal of high amounts of filterable solids. Thiswould not only be an inefficient use of rather expensive filters, but would probably lead to premature failure of the membranesystem due to the high probability that some of the unwanted material will break through. An alternative approach would beto use a second cartridge with larger pore size upstream.2.5.8 Other MethodsMethods to prevent colloidal fouling other than those described in the previous sections also exist.Lime softening has already been described as a method for silica removal (Section 2.3.6). Removal of iron and colloidalmatter are further benefits.Strong acid cation exchange resin softening not only removes hardness, but it also removes low concentrations of ironand aluminum that otherwise could foul the membrane. Softened water is also known to exhibit a lower fouling tendency thanunsoftened (hard) water because multivalent cations promote the adhesion of naturally occurring colloids, which are usuallynegatively charged. The iron removal efficiency depends on the Fe species present. Fe 2+ and Fe 3+ are removed very well bythe SAC resin and, if in excess of 0.05 ppm, have a tendency to foul the membrane and catalyze its degradation. Colloidal ororgano-Fe-complexes are usually not removed at all and will pass through into the product water. Insoluble iron-oxides are,depending on their size, filtered out depending on the flow rate and bed-depth used.When dealing with higher concentration of ferrous iron, one needs special care to avoid ferric iron fouling. It was reportedthat addition of SMBS was able to prevent membrane foulingAntifoulants: certain scaling inhibitors, also called antifoulants, can handle iron. This pretreatment process can be used forrelatively low concentrations of iron.2.5.9 Design and Operational ConsiderationsThe prevention of colloidal fouling is not only a matter of the proper pretreatment selection, but also of the system design andoperation. As an extreme example, surface water could be pretreated by coagulation-flocculation and ultrafiltration. The ROsystem could then operate with a high permeate flux, and almost no cleaning would be required. If the same water, however,is just filtered with cartridge filtration, then the RO system would need much more membrane area, and more frequentcleaning and maintenance would be required. A poor pretreatment process can be partially compensated for by adding moremembrane area and modifying the system (see Section 3, System Design), and by more frequent and/or harsh cleaning. Onthe other hand, improving the pretreatment system means lower membrane costs.To minimize the pretreatment effort and/or improve the feed water quality, the best available raw water quality should beused. The location of the intake of surface water, including seawater, is of paramount importance. Contamination of the rawwater with waste water effluent may cause serious problems in the RO plant. A deep well close to the shore or the river ispreferred. If an open intake is required, it should be located well away from the shore and some meters below the watersurface.New wells often release suspended matter in the first days of operation. Care must be taken that wells are properly rinsedout. Fouling by iron oxide is also a common problem. It can be avoided by selecting noncorrosive materials (see Section3.14, Materials of Construction, Corrosion Control).Page 55 of 180 ® Trademark of The Dow Chemical <strong>Company</strong> ("Dow") or an affiliated company of Dow Form No. 609-00071
- Page 1 and 2:
DowWater SolutionsFILMTEC Reverse O
- Page 3: 2.6 Biological Fouling Prevention .
- Page 7 and 8: 1. Basics of Reverse Osmosis and Na
- Page 9 and 10: Nanofiltration (NF)Nanofiltration r
- Page 11 and 12: How to Use Reverse Osmosis and Nano
- Page 13 and 14: 1.4 Membrane DescriptionThe FILMTEC
- Page 15 and 16: Membrane systems are typically desi
- Page 17 and 18: 1.8 Element CharacteristicsFILMTEC
- Page 19 and 20: 2. Water Chemistry and Pretreatment
- Page 21 and 22: SeawaterSeawater with TDS of 35,000
- Page 23 and 24: Table 2.5 Water analysis for RO/NFS
- Page 25 and 26: Table 2.7 Solubility products of sp
- Page 27 and 28: In this process, only Ca 2+ , Ba 2+
- Page 29 and 30: For the concentration ranges presen
- Page 31 and 32: The conditions for CaCO 3 scale con
- Page 33 and 34: Figure 2.3 Langelier saturation ind
- Page 35 and 36: These computations have been descri
- Page 37 and 38: Figure 2.5 “K” versus ionic str
- Page 39 and 40: Figure 2.6 Ksp for CaSO 4 versus io
- Page 41 and 42: 2.4.6 Calcium Fluoride Scale Preven
- Page 43 and 44: Figure 2.8 K sp for SrSO 4 versus i
- Page 45 and 46: 2.4.7 Silica Scale PreventionDissol
- Page 47 and 48: Table 2.10 Solubility of SiO 2 vers
- Page 49 and 50: 2.4.8 Calcium Phosphate Scale Preve
- Page 51 and 52: Table 2.9 Various fouling indicesIn
- Page 53: Frequent shutdowns and start-ups sh
- Page 57 and 58: 1. Intake (surface) or well, before
- Page 59 and 60: or combined residual chlorine (CRC)
- Page 61 and 62: 2.6.5 DBNPADBNPA (2,2, dibromo-3-ni
- Page 63 and 64: 2.6.11 Use of Fouling Resistant Mem
- Page 65 and 66: 2.11 Treatment of Feedwater Contain
- Page 67 and 68: 2.13 Summary of Pretreatment Option
- Page 69 and 70: 26. Handbook of Industrial Membrane
- Page 71 and 72: Table 3.1 System design information
- Page 73 and 74: 3.2 Batch vs. Continuous ProcessAn
- Page 75 and 76: 3.4 Single-Stage SystemIn a single-
- Page 77 and 78: The apparent salt passage of the sy
- Page 79 and 80: Instead of having a separate high-p
- Page 81 and 82: 3.9.1 Membrane System Design Guidel
- Page 83 and 84: In Table 3.6, the small commercial
- Page 85 and 86: Table 3.8 Number of stages of a sea
- Page 87 and 88: 3.11 System Performance Projection3
- Page 89 and 90: 3.11.2 Design Equations and Paramet
- Page 91 and 92: Table 3.10 Design equations for pro
- Page 93 and 94: 3.11.3 Comparing Actual Performance
- Page 95 and 96: The high-pressure concentrate is fe
- Page 97 and 98: If the product water from an RO sys
- Page 99 and 100: Besides the above recommendations,
- Page 101 and 102: 4. Loading of Pressure VesselsThis
- Page 103 and 104: The process of shimming is performe
- Page 105 and 106:
4.5.2 Summary of Large Element Inte
- Page 107 and 108:
5. System Operation5.1 Introduction
- Page 109 and 110:
5.2.3 Start-Up SequenceProper start
- Page 111 and 112:
5.2.4 Membrane Start-Up Performance
- Page 113 and 114:
5.5.3 SeawaterIn principle, the ope
- Page 115 and 116:
Table 5.1 Reverse osmosis operating
- Page 117 and 118:
A. Normalized Permeate FlowQS=ΔPsP
- Page 119 and 120:
For the operating conditions we hav
- Page 121 and 122:
4. During recirculation of cleaning
- Page 123 and 124:
2. The cleaning pump should be size
- Page 125 and 126:
6.7 Effect of pH on Foulant Removal
- Page 127 and 128:
Cleaning ProcedureThere are seven s
- Page 129 and 130:
If the organic fouling is the resul
- Page 131 and 132:
There are two factors that greatly
- Page 133 and 134:
7. Handling, Preservation and Stora
- Page 135 and 136:
7.4 Preservation of RO and NF Syste
- Page 137 and 138:
If the normalized actual performanc
- Page 139 and 140:
8.3.3 Localization of High Solute P
- Page 141 and 142:
Figure 8.2 Permeate probing apparat
- Page 143 and 144:
8.4.5 Performance TestThe standard
- Page 145 and 146:
8.5.1.1 Low Flow and Normal Solute
- Page 147 and 148:
. Metal Oxide FoulingMetal oxide fo
- Page 149 and 150:
. Organic FoulingThe adsorption of
- Page 151 and 152:
8.5.3 High Pressure DropHigh differ
- Page 153 and 154:
In case of fullfit or heat sanitiza
- Page 155 and 156:
Breakpoint chlorinationBreak tankBr
- Page 157 and 158:
FeedThe input solution to a treatme
- Page 159 and 160:
Milligram per litre (mg/L)Mixed-bed
- Page 161 and 162:
SBS Sodium bisulfite, NaHSO 3.Scale
- Page 163 and 164:
9.2 Specific Conductance of Sodium
- Page 165 and 166:
Figure 9.1 Conductivity of ionic so
- Page 167 and 168:
9.6 Temperature Correction FactorTa
- Page 169 and 170:
9.9 Osmotic Pressure of Sodium Chlo
- Page 171 and 172:
Details - TestEquipment andSpecific
- Page 173 and 174:
satisfactory for such a determinati
- Page 175 and 176:
case for almost all tested biocides
- Page 177 and 178:
9.12 Key Word IndexAbrasion - 150 B
- Page 179 and 180:
Positive displacement pump - 95 Shu