Dynamic control of a selective hydrogenation process with undesired MAPD impurities in the C3-cut streams

Process Synthesis and Optimization of Propylene/Propane Separation Using Vapor Recompression and Self-Heat Recuperation

“…According to the proprietary data from a local petrochemical company, a C3 splitter receives an 85:15 mol % liquid propylene/propane feed at 50 °C and 21 bar from the upstream C 3 H 4 hydrogenation unit. The required specifications for the product streams from the C3 splitter are 99.6 wt % propylene purity (polymer-grade propylene) with 99.0% recovery . These result in a 95.0 wt % pure propane product (HD-5 propane).…”

Estimation of Kinetic Parameters and Simulation of Methylacetylene and Propadiene Liquid-Phase Selective Hydrogenation Reactor Considering the Catalyst Deactivation

“…8 Wu et al determined the optimal operating conditions for maximizing the PR yield by solving the time-dependent optimization algorithm considering the catalyst deactivation. 9 Moreover, Marry et al had tried to simulate the liquid-phase reactor under the bubble flow regime using the gas-phase kinetic rate equations. They have tried to obtain the kinetic equations of the liquid phase by modifying the constants of the kinetic equations in the gas phase.…”

“…In another work, Samimi et al applied the statisicial approach response surface methodology (RSM) to investigate the effects of the fresh feed flow rate, MAPD inlet concentration, amount of recycling, and hydrogen flow rates on the PR yield . Wu et al determined the optimal operating conditions for maximizing the PR yield by solving the time-dependent optimization algorithm considering the catalyst deactivation . Moreover, Marry et al had tried to simulate the liquid-phase reactor under the bubble flow regime using the gas-phase kinetic rate equations.…”

“…In the literature, it has been acknowledged that the MA and PD hydrogenation reactions take place on the catalyst surface. Thus, both reactive molecules are adsorbed on the active surface of the catalyst and react with each other, and no reaction occurs in the fluid phase. − , Therefore, in the process under study, the ER model will not be able to explain the reaction rate equations, while the power-law ,, and LH-HW ,,,, models have been used in various studies.…”

“…The above literature has shortcomings such as data collection problems, , the paucity of data, , disregard for side reactions, − , disregard for catalyst deactivation, − ,− ,, pure mathematical fit, , and application of the not-so-correct assumption of two-phase flow in a trickle flow regime in a trickle bed reactor. ,, These drawbacks make the proposed models insufficient to be used in the simulation of industrial reactors.…”