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Packed Column Distillation

Packed Column Distillation. By Craig D. Mansfield. Some Background on Packed Column Distillation. Commonly uses High value products Heat sensitive products Usually run in small/medium batches Used since ~1907 Patent for Raschig rings by Dr. Raschig in 1907. Comparison to Tray Columns.

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Packed Column Distillation

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  1. Packed Column Distillation By Craig D. Mansfield

  2. Some Background on Packed Column Distillation • Commonly uses • High value products • Heat sensitive products • Usually run in small/medium batches • Used since ~1907 • Patent for Raschig rings by Dr. Raschig in 1907

  3. Comparison to Tray Columns Packed Advantages Tray Advantages Can handle solids High liquid rates Large column diameter Allows complex ops Easier alt. feed locations Better performance predictions Higher residence time Weigh less Better wetting • Lower • Smaller column diameter • Cheaper corrosive seps • Less foaming • Low liquid holdup • Efficient batch operation • Greater thermal control

  4. Research Problem Statement • Design/build a new packed distillation column for the UOL • Separate isopropanol and water • Operate in batch or continuous mode

  5. Basic Design Algorithm Used • Mixture properties • Flooding point data • Size/capacity of reboiler heat exchanger • Determine power source • Determine mass transfer performance • Size/capacity of reflux heat exchanger • Size/capacity of components and throughput • Volume of tanks/reboiler

  6. Mixture Properties • Used UniSim Design software • Viscosity, thermal cond., surface tension • Thermo models • gen. NRTL w/ PR • Diffusivity models • Wilke and Chang (diluted in water) • Sitaraman et al. (diluted in isopropanol) • Leffler and Cullinan (liquid mixture) • Gilliland (vapor mixture)

  7. T-X Diagram

  8. X-Y Diagram

  9. Viscosity vs X

  10. Flooding Point • Column filled w/ liquid holdup from high vapor flow • Common flooding models • Sherwood et al. • GPDC • Used Sherwood et al. as model for design • Determined flooding vapor/liquid flow rates

  11. Power Source • Required power is 6.34 KW • Choices are electric or steam • Electric power (via resistance) requires a min. 52.8 amps of current • Steam is already availableand efficient • Steam was chosen as the main power source

  12. Size of Reboiler Heat Exchanger • Used a vapor rate below flood point to find min. power requirement • Modeled reboiler w/ nucleate pool boiling • Correlations used: • Modified Thöme and Shakir model • Mostinski model • Calculated the area (“size”) required

  13. Mass Transfer Correlations • Onda et al. • Effective specific area • Interfacial Mass Transfer Coefficients

  14. Determination of Mass Transfer Performance (Transfer Units) • Used packed column design integral(s):

  15. vs

  16. Size of Reflux Heat Exchanger • Sized to match or exceed max reboiler power • At flood • At highest transfer capacity • Model used: Nusselt horizontal pipe theory • Size was the transfer area required (again)

  17. The Nominal Model Column/Operation Specs Reboiler/Condenser Specs = 94.96 W/K = 3.18 W/K Tube NPS = 0.5 in. = 0.320 m = 0.355 m = 0.01598 = 0.0177 • ID = 3 in. • = 2 m • = 1 • = 6.34 KW • = 0.577 m • = 0.154 m • = 3.42 • HETP = 0.21 m

  18. The Nominal Model Compositions Flow Rates B = 0.28 mol/s = 6.59 USGPH F = 0.34 mol/s = 10.42 USGPH D = 0.069 mol/s = 3.878 USGPH L = 0.069 mol/s = 3.878 USGPH • = 0.1 • = 0.6 • = 0.2 Average Efficiencies • = 0.80, z = 0.577 m • = 0.23, z = 2 m

  19. Core System Diagram

  20. Acknowledgements • Dr. Lewis E. Johns • Dr. Ranga Narayanan • Dr. Spyros Svoronos • The University of Florida

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