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Controlling a reactive tray temperature with acceptable sensitivity but larger rangeability gives better robustness.
The use of the difference between two suitably chosen reactive tray temperatures, also referred to as ΔT, as the controlled variable significantly mitigates this non-linearity.
Results for the two synthesized control structures show that controlling the most sensitive reactive tray temperature results in poor robustness due to low rangeability causing "wrong" control action for large disturbances.
The fresh acetic acid and methanol feeds control a reactive and stripping tray temperature, respectively in CS1 (Roat et al., 1986) while in CS2, the reboiler duty replaces fresh acetic acid as the manipulation handle for reactive tray temperature control.
High non-linearity in the form of process gain 'sign reversal' causing the steady-state reactive tray temperature to move in the same direction for large opposite changes in the control input is observed.
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A two-temperature control structure is effective when the system is overdesigned in terms of number of reactive trays, holdup and/or catalyst load.
The optimal design of the RD process is obtained by minimizing the energy demand and the optimum number of reactive trays is found to be 10.
This pilot-scale plant consists of one RD column (10 reactive trays plus structured packing for separation) and a downstream stripper with a decanter in between.
It is also shown that controlling the difference in the temperature of two suitably chosen reactive trays further improves robustness of both the structures as input multiplicity is avoided.
Place the red wine vinegar in a non-reactive tray and lay the sardine fillets cut-side down in it.
We develop a generic steady-state design model for reactive distillation tray columns involving arbitrary liquid-phase reactions.
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