This paper uses Aspen Plus software to carry out steady?state simulations of a new process for the reactive distillation of hydrogen peroxide isopropylbenzene (CHP) and subsequent refining processes for phenol and acetone. The operating pressure, feed position and number of plates of the reactive distillation column and the refining process were economically optimised with the objective of minimising the total annual cost (C_TAC). The results show that the optimal operating parameters of the process are as follows : the total number of trays of RD was 34, the number of trays in the distillation section was 27, the number of trays in the reaction section was 6, the feed position was 28, and the operating pressure was 3.0×10⁴ Pa. The total plate numbers of acetone refining tower (T101), cumene top tower (T102), tar tower (T103) and phenol refining tower (T104) were 25, 61, 23 and 22, respectively. The feed positions are 16, 45, 9 and 9, respectively. The operating pressures were 5.2×10⁴, 5.0×10³, 5.5×10⁴, 6.0×10³ Pa. The minimum C_TAC of the new process was 2 239.03×10⁴ yuan/year. At the same time, the steady?state simulation and economic optimization of the traditional CHP decomposition and subsequent phenol and acetone refining process were also carried out, and the minimum C_TAC value was 2 608.13×10⁴ yuan/year. By comparing the reactive distillation process with the traditional process, it can be seen that C_TAC can save 14.15% and energy consumption can save 9.01%.