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Thermodynamics of Separation Operations

Thermodynamics of Separation Operations. Chapter2. Purpose and Requirements: Know the importance and mechanism of separation Learn to select feasible separation process. Key and Difficult Points: Key Points Phase Equilibria: Fugacities and activity Coefficients

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Thermodynamics of Separation Operations

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  1. Thermodynamicsof Separation Operations Chapter2

  2. Purpose and Requirements: • Know the importance and mechanism of separation • Learn to select feasible separation process Key and Difficult Points: Key Points • Phase Equilibria: Fugacities and activity Coefficients • Graphical Correlations of Thermodynamic Properties • Calculation of K-value Difficult Points • Nonidea Thermodynamic Property Modes • Activity Coefficient Models for the Liquid Phase

  3. Outline • 2.1 ENERGY, ENTROPY, AND AVAILABILITY -BALANCES • 2.2 PHASE EQUILIBRIA • 2.3 IDEAL GAS, IDEAL LIQUID SOLUTION MODEL • 2.4 GRAPHICAL CORRELATIONS OF THERMODYNAMIC PROPERTIES • 2.5 NONIDEAL THERMODYNAMIC PROPERTY MODELS • 2.6 Activity Coefficient Models for the Liquid Phase

  4. 2.1ENERGY, ENTROPY, AND AVAILABILITY -BALANCES • Gas Mixture (Solutes or Absorbate) • Liquid (Solvent or Absorbent) • Separate Gas Mixtures • Remove Impurities, Contaminants, Pollutants, or Catalyst Poisons from a Gas(H2S/Natural Gas) • Recover Valuable Chemicals

  5. 2.2 PHASE EQUILIBRIA • A = L/KV Component A = L/KV K-value Water 1.7 0.031 Acetone 1.38 2.0 Oxygen 0.00006 45,000 Nitrogen 0.00003 90,000 Argon 0.00008 35,000 • Larger the value of A，Fewer the number of stages required • 1.25 to 2.0 ，1.4 being a frequently recommended value

  6. 2.3 IDEAL GAS, IDEAL LIQUID SOLUTION MODEL • Stripping • Distillation • Stripping Factor(S解吸因子) • S = 1/ A= KV/L High temperature Low pressure is desirable Optimum stripping factor ：1.4.

  7. 6.1 EQUIPMENT trayed tower packed column bubble column spray tower centrifugal contactor Figure 6.2 Industrial Equipment for Absorption and Stripping

  8. Trayed Tower(Plate Clolumns板式塔) Figure 6.3 Details of a contacting tray in a trayed tower

  9. (a) perforation (b) valve cap (c) bubble cap (d) Tray with valve caps Figure 6.4 Three types of tray openings for passage of vapor up into liquid

  10. Froth Liquid carries no vapor bubbles to the tray below Vapor carries no liquid droplets to the tray above No weeping of liquid through the openings of the tray Equilibrium between the exiting vapor and liquid phases is approached on each tray. (a) Spray(b) Froth(c) Emulsion(d) Bubble(e)Cellular Foam Figure 6.5 Possible vapor-liquid flow regimes for a contacting tray

  11. Packed Columns Figure 6.6 Details of internals used in a packed column

  12. More surface area for mass transfer • Higher flow capacity • Lower pressure drop Packing Materails (a) Random Packing Materials (b) Structured Packing Materials • Expensive • Far less pressure drop • Higher efficiency and capacity Figure 6.7 Typical materials used in a packed column

  13. SUMMARY 1.Separation processes are often energy-intensive. Energy requirements are determined by applying the first law of thermodynamics. Estimates of minimum energy needs can be made by applying the second law of thermodynamics with an entropy balance or an availability balance. 2. Phase equilibrium is expressed in terms of vapor-liquid and liquid-liquid AT-values, which are formulated in terms of fugacity and activity coefficients. 3. For separation systems involving an ideal gas mixture and an ideal liquid solution, all necessary thermodynamic properties can be estimated from just the ideal gas law, a vapor heat capacity equation, a vapor pressure equation, and an equation for the liquid density as a function of temperature.

  14. 4. Graphical correlations of pure-component thermodynamic properties are widely avail­able and useful for making rapid, manual calculations at near-ambient pressure for an ideal solution. 5. For nonideal vapor and liquid mixtures containing nonpolar components, certain P-u-7'equation-of-state models such as S-R-K, P-R, and L-K-P can be used to estimate density, enthalpy, entropy, fugacity coefficients, and k-values. 6. For nonideal liquid solutions containing nonpolar and/or polar components, certain free-energy models such as Margules, van Laar, Wilson, NRTL, UNIQUAC, and UNIFAC can be used to estimate activity coefficients, volume and enthalpy of mixing, excess entropy of mixing, and k-values.

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