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Optimal Control Structure Design for Distillation Columns Sequence

Explore control strategies for two distillation columns in a sequence under varying conditions. Utilize a self-optimizing method with active constraint regions and systematic modeling. Consider potential disturbances and examine the effect of candidate controlled variables. Investigate the impact of measurement errors on temperature, concentration, and flow rates.

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Optimal Control Structure Design for Distillation Columns Sequence

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  1. Master project: Control structure design for a sequence of distillation columns Tor Anders Marvik Supervisor: Sigurd Skogestad Co-supervisors: Vladimoros L. Minasidis Johannes Jäschke Name, title of the presentation

  2. Optimal controlstructureoftwodistillationcolums in a sequence Varying marked conditions Computer model Active constraint regions Self-optimizing variables Region 1: V2, V1, xD2,B active Region 2: xD2,B active General/systematic approach?

  3. The model Based on column A by Skogestad 41 tray Feed on tray 21 Assumtions: Constant pressure Constant relative volatility Constant molar flows, No vapor holdup, Equlibrium on all stages Total condenser Steady state model in Matlab Conditions from Jacobsen

  4. Jacobsen’s map

  5. V2, V1, xD2,B active

  6. V2, V1, xD2,B active

  7. Approach to findself-optimizing variables? • Brute force • Null space HF=0 • Exactlocalmethod • Possibledisturbances • F,q,zF, prices, • CV candiates • Traytemparature, composition, L1, V1, D1, L2, V2 D2, B2 • Combination

  8. Brute force

  9. Combinations as CV • Combination ofTemperature (As RoalBræck Leer) • All stages • Every 5th stage • Ratio withfeedflow

  10. Sizeofthemeasurementerror • Temperature: 1 K • Consentraiton: 5% • Flow: 10%

  11. To do • A LOT • Standard approach • Brute force  exactlocalmethod • See how L changes to disturbanceswhenthecandiadate CV is fixed

  12. Thankyou Feedback and questions?

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