Membrane Based Triethylene Glycol Separation and Recovery from ...

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Table 2.9 Detail Explanation of Different Membrane Processes Membrane Pressure driven membrane processes Microfiltration Ultrafiltration Nanofiltration Reverse Osmosis Piezodialysis symmetric porous Asymmetric porous Thickness ≈ 10-150 µm ≈ 150µm 16 Composite Sub layer ≈ 150 µm Top layer
Clean Membrane Fouled Membrane Figure 2.6 Membrane fouling The selectivity of membrane toward diluted mixture is generally expressed by percentage of rejection (R), demonstrated as follows; C p % R 1100 C f Where Cp = solute concentration in permeate Cf = solute concentration in feed 2.4.5 Factors affecting membrane filtration 2.4.5.1 Hydrophobicity/hydrophilicity of membrane 17 Equation.2.2 Hydrophobicity/hydrophilicity of membrane is described for its ability to allow water passing through. It is investigated by measurement of contact angle of water droplet on membrane surface. Greater than 90˚ of contact angel indicates that the membrane has low affinity to water (hydrophobicity) leading to low permeate flux as compared to hydrophilic one. Moreover, hydrophobicity of membrane also affects removal of organic compound. 2.4.5.2 pH pH of solution relates to presenting charge of membrane and a compound beside it involves proton dissociation of functional group, attached on membrane surface or composed in compounds. Thus, it directly affects electrostatic forces between compound and membrane surface. Zeta potential is defined as power of charges showing on membrane surface. The negatively charged membrane has been reported to highly reject negatively charged organic compound through electrostatic repulsion (Bellona et al., 2004). However, the electrostatic repulsion was reported to decrease with feed containing some contaminants such as salts (Na + , Mg 2+ , etc.). It resulted because the positive ions
Page 1 and 2: Membrane Based Triethylene Glycol S
Page 3 and 4: Abstract Triethylene glycol (TEG) i
Page 5 and 6: 5 4.1 Phase I: High Pressure Membra
Page 7 and 8: List of Figure Figure Title Page 2.
Page 9 and 10: 1.1 Background of the Study Chapter
Page 11 and 12: Phase II: membrane of pervaporation
Page 13 and 14: 2.1.2 Uses of TEG (Triethylene glyc
Page 15 and 16: or mildly irritating. Moreover, for
Page 17 and 18: 2.2 Gas Separation Plants (GSPs) 2.
Page 19 and 20: Table 2.7 Sources of TEG Wastewater
Page 21 and 22: mineral, pharmaceutical, electronic
Page 23: Reverse osmosis (RO) The pore size
Page 27 and 28: Table 2.10 Comparison of Rejection
Page 29 and 30: Table 2.12 Overview of Chosen Membr
Page 31 and 32: Hollow fiber module This module is
Page 33 and 34: 2.4.7.6 Applications Generally, the
Page 35 and 36: Chapter 3 Methodology This study co
Page 37 and 38: Figure 3.2 Flow diagram of membrane
Page 39 and 40: The compound rejection (%) by membr
Page 41 and 42: Figure 3.5 Flow diagram of pervapor
Page 43 and 44: Table 3.5 List of UF Membranes and
Page 45 and 46: Analysis result 1. Preparation of C
Page 47 and 48: 4.1.2 Permeate flux The result of p
Page 49 and 50: study. Fast flux reduction resulted
Page 51 and 52: Conversely, higher removal of TEG i
Page 53 and 54: From Figure 4.5 and 4.6, it is obvi
Page 55 and 56: 4.3.2 Efficiency of TEG wastewater
Page 57 and 58: Table 4.4 Wastewater Characteristic
Page 59 and 60: Permeate Flux (L/m 2 .h.bar) 1 0.8
Page 61 and 62: Rejection (%) of TEG Rejection (%)
Page 63 and 64: to protect membrane from fouling by
Page 65 and 66: Phase III: Design Pre-Treatment Pro
Page 67 and 68: References Alberta Environment. Soi
Page 69 and 70: Orecki, A., Tomaszewska, M. and Kar
Page 71 and 72: Appendix A Experimental setup 63
Page 73 and 74: 61.8 mm Knob 3/8 in 180 mm A A Conc
Page 75 and 76:
Table B-1 Permeate Flux with Synthe
Page 77 and 78:
Table B-7 Normalized Flux at The En
Page 79 and 80:
Cold Trap Zeolite membrane module F
Page 81 and 82:
Table D-1 Permeate Fluxes at The En
Page 83 and 84:
Appendix E Experimental Details for
Page 85 and 86:
Appendix F Photos of the experiment
Page 87:
NF-TS80 with 0.1% real wastewater a
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