Response time as a function of the MeOH feed flowrate

The second statement can be explained by following the same reasoning. In a distillation (separation) process the driving force (top-bottom) is specified and the fiux remains to influence. Thus, in nonreactive sections flux should be manipulated to control the unit. The results of these observations fully agrees with the analysis given by Luyben et al. (1999) and Meeuse (2003) for a reactor and distillation column. 

Meaningfulness and validity of results. Note that in the current approach a continuous range of disturbances for one input variable is considered for the computation of the responsiveness time constant. In comparison with the generalized definition of 

In the course of this chapter the economic-driven design (classical design) was implicitly compared with a new bi-optimized design (green design) for the case of a MTBE RD column. A set of indicators can be used to compare both designs ( ) exergy loss and a) closed loop control performance. 

The exergy loss (or entropy produced) can be extracted from the Pareto curve presented in figure 8.9. The relevant data for the classical and green designs and for the fully exergy-driven design i.e. w = [0 l] ) are hsted in table 8.7. 

The shadow prices can be computed directly out from the data in table 8.7 or from the Pareto curve in figure 8.9. It was foimd that, when compared to the classical case, 

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Figure 8.13. Response time as a function of the MeOH feed flowrate. Remarks MeOH feed flowrate varies from the nominal value (168 mol xs ) to 150 mol xs the optimal design variables and sizing parameters corresponds to a /econ — /esxesrgy design, with w = [0.3 O. ]". ...

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