LALI 13-Membranes - Membrane Processes •A membrane is a...

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Unformatted text preview: Membrane Processes •A membrane is a selective barrier that permits the separation of certain species in a fluid by combination of sieving and diffusion mechanisms •Membranes can separate particles and molecules and over a wide particle size range and molecular weights Membrane Processes Four common types of membranes: Reverse Osmosis Nanofiltration Ultrafiltration Microfiltration The R.O. membrane is semi-permeable with thin layer of annealed material supported on a more porous sub-structure. The thin skin is about 0.25 micron thick and has pore size in the 5 – 10 Angstrom range. The porous substructure is primarily to support the thin skin. The pore size of the skin limits transport to certain size molecules. Dissolved ions such as Na and Cl are about the same size as water molecules. However, the charged ions seem to be repelled by the active portion of the membrane and water is attracted to it. So adsorbed water will block the passage and exclude ions. Under pressure attached water will be transferred through the pores. Nanofiltration is a complementary process to reverse osmosis, where divalent cations and anions are preferentially rejected over the monovalent cations and anions. Some organics with MW > 100 -500 are removed There is an osmotic pressure developed but it is less than that of the R.O. process. Microfiltration and Ultrafiltration are essentially membrane processes that rely on pure straining through porosity in the membranes. Pressure required is lower than R.O. and due entirely to frictional headloss Hollow fiber: Spiral wound Ceramic Membrane Elements Spiral UF system Pressure requirements are based on osmotic pressure for R.O., osmotic pressure and fluid mechanical frictional headloss (straining) for nanofiltration, and purely fluid mechanical frictional headloss (straining) for ultra- and microfiltration. If clean water and water with some concentration of solute are separated by a semi-permeable membrane (permeable to only water) water will be transported across the membrane until increases hydrostatic pressure on the solute side will force the process to stop. The osmotic pressure head (at equilibrium) can be calculated from thermodynamics. The chemical potential (Gibbs free energy per mole) of the solvent and the solute(s) in any phase can be described as: µi =µi0(T,p) + RTlnXi Where µi0(T,p) is the “standard state” free energy of a pure solvent or solute at T and p (usually 250C and 1 atm). Xi = mole fraction of solvent or solute. At equilibrium for the solute and pure solvent system, respectively: 0(T,p) µ(T,p +π,X) =µ µ0(T,p +π) + RTlnX =µ0(T,p) Because: dG = −SdT + Vdp 0(T,p +π) −µ0(T,p) = µ p+π ∫ p V0 dp p+π ∫ p V 0 dp + RTlnX = 0 V0π+ RTlnX = 0 After some algebraic manipulation: n2 π= R ⋅T = R ⋅T ⋅C Vtotal π= osmotic pressure Water flux through the membrane is the most important design and operational parameter. Next most important is solute exclusion. Some solute will diffuse (by molecular diffusion) through the membrane because there will be a significant gradient of the solute across the membrane. Water Flux: Fw = K(∆p −∆π) Solute transport is complicated by the type of ions being transported. Transport is generally modeled by : Fs = B (C1 − C2) Fs = salt flux (g/cm2 –sec) Applications of Micro- and Ultrafiltration: •Conventional water treatment (replace all processes except disinfection). •Pretreat water for R.O and nanofiltration. •Iron/Manganese removal (after oxidation). •Removal of DBP precursors. Applications for R.O. and nanofiltration: •R.O. application mostly desalination. •Nanofiltration first developed to remove hardness. •Nanofiltration can be used to remove DBP precursors Operating pressure ranges: R.O./NF: 80 – 600 psig MF/UF: 5 – 60 psig Fouling of membranes due to accumulation of solute/particulates at the membrane interface has to be addressed for economic reasons. The membranes are too expensive to be replaced for reasons of fouling. Fouling issue Traditional membrane technology is generally affected by fouling. This long-term loss in throughput capacity is due primarily to the formation of a boundary layer that builds up naturally on the membrane surface during the filtration process. In addition to cutting down on the flux performance of the membrane, this boundary or gel layer acts as a secondary membrane reducing the native design selectivity of the membrane in use. This inability to handle the buildup of solids has also limited the use of membranes to low-solids feed streams. Fouling There are various ways to reduce this fouling such as: • Periodic pulsing of feed • Periodic pulsing filtrate (backwashing) • Increasing shear at by rotating membrane •Vibrating membrane (VSEP technology , next slide) Vibrating shear to prevent fouling VSEP Technology A common method to clean the membrane system is to just reverse the flow pattern: Membrane Processes are becoming popular because they are considered “Green” technology - no chemicals are used in the process. Electrodialysis: In the ED process a semi-permeable barrier allows passage of either positively charged ions (cations) or negatively charged ions (anions) while excluding passage of ions of the opposite charge. These semi-permeable barriers are commonly known as ion-exchange, ion-selective or electrodialysis membranes. Current required in amps: F ⋅ Q ( Cin − Cout ) I= n ⋅ξ amp ⋅ sec F = Faraday = 96,485 equivalent Cin,out = concentration in equiv/m 3 ξ = current efficiency (typically 0.8 to 0.9) n = number of cells Voltage required is determined by: E=IxR R = resistance across unit (all cells + feed and product water), ohms. Generally in range of 10 – 50 ohms. I, in amps, as determined in previous calculation. Electrode reactions: Small amounts of hydrogen gas are generated at the cathode: 2e + 2H 2 O → H 2 (g) + 2OH At the anode small amounts of oxygen gas are generated: − − H 2 O → 2H + 1/ 2O 2 (g) (also possible 2Cl → Cl2 (g) + 2e ) − + ...
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This note was uploaded on 01/07/2011 for the course CHEM 6153 taught by Professor - during the Spring '10 term at University of Florida.

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