The catalytic hydrogenolysis of n-butane was investigated in an integral packed bed reactor (0.70 mi. ID by 25 cni. long). The catalyst was 105; nickel on silica gel. A block factorial set of experiments was performed at hydrogen-to-butane feed ratios of 4. to 9., temperatures of 240% to 282OC and feed flowrates of 1.0 to 1.8 ml/sec. T h e predominant reaction appeared to be the r e m a d of terminal methyl groups.Kinetic rate expressions were developed to predict the product distribution, taking into account a five-fold change in catalytic activity. A parameter estimation strategy, applying non-linear regression theory, was used to obtain the ten kinetic parameters. Error analysis of the parameters was performed using likelihood ratios. Models were developed to describe the catalyst activity changes observed during experinrentation. The kinetic model predicts the experimental observations very accurately over all conversions and shows some deviation only a t the combination of high temperature and low feed ratio.nvestigations have been reported in the literature

This study was undertaken to obtain experience in developing steady‐state mathematical models of full‐scale chemical reactors through the use of a combination of bench‐scale experiments and actual plant operating data. In this case, the hydrogenolysis of n‐butane on a nickel on silica gel catalyst was studied in a %inch diameter pilot plant fluidized bed reactor. The kinetic parameters in a mechanistic reaction model were obtained in a bench‐scale integral reactor and these rate equations were included in a simple two‐phase fluidized bed model. The parameter relating to interchange of gas between bubbles and emulsion was determined from the fluidized bed data. A comparison of the predicted and observed selectivities suggested a weakness in the kinetic model. This shortcoming was then partially corrected by using the fluidized bed data. In this way, a reactor model was achieved which was satisfactory for overall plant simulations.