This paper focuses on the simulation

optimization and control of the reactive dividing wall column for the production of n-butyl acetate through ester exchange reaction. The optimal operating conditions are obtained with the minimum total annual cost(TAC) as the target function. Different matching relationships between manipulate variables and control variables are determined through the sensitive analysis of steady state relative gain and the Relative Gain Array(RGA) criterion

and then three control structures are built in Aspen Dynamics. It shows that the use of the reactant feed ratio to control the stage temperature is effective to handle the feed disturbances

which presents superior ability in maintaining stability of this system. At last

an improved control structure(CS3) is proposed

which deletes the ratio of reboiler duty and mixture feed rate and shows a great advantage in reducing overshoot of product purities. The specific control structure of CS3 is as follows: the reboiler load of reactive distillation column controls the temperature of the 16th plate of the reactive distillation column directly; ratio of feed rate for n-butanol and methyl acetate/methanol mixture controls the temperature of 28th plate of the reactive distillation column; and the reboiler load of stripping column controls that of the 3rd plate of stripping column directly.