Info

simulated

IrtMctwy.-SIOL

Figure 4.17. Experimental (symbol and dotted lines) and Calculated (full lines) Profiles of (a) Manipulated Flow rates and (b) Compositions in the Vesselsb.

Table 4.14. Input Data for Example 2

No. of Plates

(including reboiler, total condenser) Total fresh feed in the feed tank, B0, kmol Component

Feed composition, xgg, mole fraction: Column holdup, kmol:

Condenser = 0.07 Reboiler

Internal plates, total Vapour load, kmol/hr

Flow rate from feed tank to the feed plate, kmol/hr = 5.0

Relative volatility, a

(with ki = 2kf, Xj is the mole fraction of the ith component)

4.3.4. Multivessel Batch Distillation Column (MultiBD)

Referring to Figure 2.3 of multivessel batch distillation (MultiBD) column, the model equations for condenser, reboiler and internal plates are the same as those presented for conventional batch distillation column (section 4.2). The model equations for the vessels are the same as those presented for feed tank of the MVC column (section 4.3.3). Note however, that there are no feed plate model equations as in the case of an MVC column.

Skogestad et al. (1997) simulated a MultiBD column with a similar to type III model using a total reflux operation. The input data for the column is presented in Table 4.15.

The column was operated until composition in each vessel (including the condenser and the reboiler) reaches steady state values (more than 3 hr of operation). The final product compositions in each vessel are shown in Figure 4.20.

Distillate Accumulator

Distillate Accumulator

Time.hr
Figure 4.18. MVC with Chemical Reaction - Composition Profiles

Time, hr

Figure 4.19. MVC with Chemical Reaction - Holdup Profiles

Time, hr

Figure 4.19. MVC with Chemical Reaction - Holdup Profiles

Table 4.15. Input Data for MultiBD Column

No. of column sections

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