The synthesis of 19 carefully selected Pt/γ-Al 2 O 3 À Cl formulations was followed by high-throughput catalytic testing in order to unravel the effect of an active phase formulation change on nheptane reforming performances. Pt/γ-Al 2 O 3 À Cl catalysts were prepared with different Pt (0.3-1 % wt ) and Cl (0.1-1.4 % wt ) contents and using two γ-Al 2 O 3 supports so that both sites concentrations and sites locations at the crystallite surface vary among the catalyst pool. Catalytic tests were conducted in mild conditions for a comparison of catalysts in kinetic regime.Results show that Pt and Cl concentrations control the competition between hydroisomerisation, hydrogenolysis and hydrocracking pathways. Aromatisation, on the contrary, is poorly affected by formulation changes. Non-monotonous trends linking Pt/Cl ratio to isomerisation selectivity are found for both γ-Al 2 O 3 supports. This study provides new insights for the description of bi-functional transformations in catalytic naphtha reforming.

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Packed bed reactors with diameters below 1 cm, millipacked beds hereafter, are often used to test catalysts. The prospect of using these reactors for catalytic kinetic measurements is quite attractive, but it requires a better knowledge of the flow characteristics of these reactors. This study focuses on the main hydrodynamic features of millipacked bed reactors in single phase gas flow. The effects of the bed length, gas velocity, reactor/particle diameter ratio (d) and the use of fine inert powder as porosity filler are investigated via residence time distribution measurements and reactive tests. When using spherical particles, for values of reactor/particle diameter ratios between 1 < d < 3, the behavior of the Peclet number, Pe, is not monotonous. Lower values of the Pe number for specific values of d corresponding to large void spaces between the particles and/or between the particles and the walls, have been observed. For values of d > 3 higher Pe numbers are observed, in particular at high gas velocities, due to the transition to a more uniform packing where the walls are no longer the major constraint. When using cylindrical particles, higher dispersion is observed when the cylinders align on each other along the reactor axis, as compared to when they are randomly arranged in the reactor. A criterion to calculate the maximum conversion that can be achieved neglecting dispersion effects has been proposed, highlighting the situations where it has to be used with caution. The dispersion in these reactors can often be neglected. In case the criterion is not fulfilled, filling the porosity of the beds with powder reduces the dispersion. Using porosity fillers in reactors with internal diameters between 2 and 4 mm showed an improvement of the conversions for n-heptane reforming and methylcyclohexane dehydrogenation, which is attributed to external mass transfer improvement. Fine and spherical powders fill better the porosity and yield lower dispersion and higher mass transfer.