OP-II-3

PP-II-30Fig. 1. Axial profile of methane conversion (%)with varying inlet temperatureFig. 2. Methane conversion (%) versus reactorpressureFig. 3. Temperature profile in the reactor atdifferent pressureFig. 4. Axial temperature profile inthe reactorTable 1. Temperature differences along the reactor at various inlet temperaturesT in T out ∆T750 K 1032.8 K 282.8800 K 1042.3 K 242.3850 K 1049.8 K 199.8Reference:[1]. Chen, Z.; Prasad, P.; Yan, Y.; Elnashaie, S. Simulation for reforming of natural gas with oxygeninput in novel membrane reformer. Fuel Processing Technology. 2003, 83, 235-252.[2]. Pedernera, M.N.; Piña, J.; Borio, D.O.; Bucalá, V. Use of a heterogeneous two-dimensional model toimprove the primary steam reformer performance. Chemical Engineering Journal. 2003, 94, 29-40.[3]. Huang, T.J.; Yu, T.C.; Jhao, S.Y. Weighting Variation of Water-Gas Shift in Steam Reforming ofMethane over Supported Ni and Ni-Cu Catalysts. Ind. Eng. Chem. Res. 2006, 45, 150-156.[4]. Gallucci, F.; Paturzo, L.; Basile, A. A simulation study of the steam reforming of methane in adense tubular membrane reactor. International Journal of Hydrogen Energy. 2004, 29, 611-617.[5]. Grevskott, S.; Rusten, T.; Hillestad, M.; Edwin, E.; Olsvik, O. Modelling and simulation of a steamreforming tube with furnace. Chemical Engineering Science. 2001, 56, 597-603.[6]. Levent, M.; Budak, G.K.; Karabulut, A. Estimation of concentration and temperature profiles formethane-steam reforming reaction in a porous catalyst. Fuel Processing Technology. 1998, 55,251-263.[7]. Hou, K.; Hughes, R. The kinetics of methane steam reforming over a Ni/a-Al2O catalyst. ChemicalEngineering Journal. 2001, 82, 311-328.387