Comparison of performance of microreactor and semi-batch reactor for catalytic hydrogenation of o-nitroanisole

Experimental studies on hydrogenation of anthraquinone derivative in a microreactor

“…The values of K L a found in a microreactor by Losey et al was in the range 5-15 s À1 whereas the values in a laboratory trickle bed reactor is 0.01-0.08 s À1 . Work done in our lab by Tadepalli et al [11] for a different hydrogenation reaction also showed that the mass transfer coefficient, K L a value in a packed bed microreactor is similar to that obtained by Losey et al in the range of parameters studied in this work. The flow velocity used in the prersent work is higher than than that used by Losey et al and hence the mass transfer coefficient in our reactor would even be higher than that obtained by Losey et al Also, in the microreactor periodic drying of the catalyst bed might happen.…”

Microchannel Reactor System Design & Demonstration For On-Site H2O2 Production by Controlled H2/O2 Reaction

“…The mass transfer coefficient increases with velocity, as expected for a reaction limited by external mass transfer (Kreutzer et al, 2001). The range of mass transfer parameters is similar to that obtained by Tadepalli et al (2007). Figure 5.10 have a greater discrepancy than typical for the other graphs.…”

Cycloaddition of Isoamylene and ?-Methylstyrene in a Microreactor using Filtrol-24 catalyst: Microreactor Performance Study and Comparison with Semi-Batch Reactor Performance

“…From this figure, it seems that there are external mass transfer effects at stirrer speeds below 1000 rpm. Tadepalli et al (2007) also showed that the mass transfer parameter values for a microreactor were two orders of magnitude higher than those obtained in the semi-batch reactor for the catalytic hydrogenation of o-nitroanisole. A similar increase in yield and reactant conversion with temperature that was observed in the microreactor up to a temperature of 140 o C, is also observed in the semi-batch reactor, as shown in Figure 10.…”

“…Not only is spent aqueous acid catalyst environmentally unfriendly, the organic effluent also has to be purified. (Tadepalli et al, 2007). Both steps increase the generation of liquid waste and greatly increase process and disposal costs.…”

“…Both steps increase the generation of liquid waste and greatly increase process and disposal costs. Better heat and mass transfer in a microreactor for this exothermic reaction can improve selectivity, safety, yield, product quality, and also improve energy efficiency Tadepalli and Lawal, 2008;Tadepalli et al, 2007;Voloshin et al, 2007). Eliminating the use of the corrosive acid catalyst will also eliminate the need to use expensive corrosion resistant materials of construction.…”