Catalytic coal liquefaction systems are modeled by the model compound system consisting of 1-methylnaphthalene and its hydrogenated products of naphthalene, tetralin, and decalin. The kinetics and product distributions for the conversion of 1-methylnaphthalene to products are obtained for ten proprietary coal liquefaction catalysts. Four of the catalysts were fresh; six were removed from a coal liquefaction reactor after extended runs processing coal slurry. Conversion of 1-methylnaphthalene to products was adequately described by first-order kinetics. The concentration of tetralin, an important hydrogen donor molecule, in the product was found to be proportional to the concentration of naphthalene. This proportionality is believed to be due to a reversible reaction sequence between naphthalene and tetralin proceeding through dihydronaphthalene. The decrease in activity as measured by 1methylnaphthalene conversion for the spent catalysts compared to fresh catalyst activity corresponds well with loss in activity recorded during the coal liquefaction run, as measured by decrease in hydrogen consumption.Most forecasts of future energy supply and demand show a projected shortfall in liquid hydrocarbons that becomes relatively severe by about 1990 (ERDA, 1975). Considerable research is currently being undertaken to develop economically competitive, high capacity processes for the conversion of coal into liquid fuels. Various processes, such as SRC, Exxon, Consol, Synthoil, H-Coal,

The effect of catalyst bed length at constant liquid hourly space velocity or of liquid flowrate on the performance of a trickle bed reactor in hydrodesulfurization of 53% reduced Kuwait crude has been evaluated experimentally. Two different catalyst sizes, 7-8 mesh and 20-30 mesh (U.S. sieves), have been employed. The experimental results were obtained at a temperature of 750°F, a liquid hourly space velocity of 1 hr-1, and pressures of 1000 and 2000 psig. The experimental data have been evaluated on the basis of the axial dispersion model of Mears (1971), the holdup model of Henry and Gilbert (1973), and the effective catalyst wetting model of Mears (1974).

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