A comparison of the catalytic partial oxidation of C1 to C16 normal paraffins

The catalytic partial oxidation (CPO) of C1 through C16 normal alkanes is examined on Pt and Rh-coated α-Al2O3 ceramic foam supports. New data for heavy liquid fuels (≥ C6) are combined with previously reported data for lighter hydrocarbons to explore the effects of reactant fuel molecular weight, catalyst metal, and support structure on the CPO of normal paraffins. These results show that, independent of catalyst metal and support geometry, fuel conversion and the total selectivity to olefin products increase with increasing chain length of the reacting fuel. Conversely, the selectivities of H2 and CO decrease with increasing molecular weight of the reacting fuel. Pt catalysts generate higher selectivities to ethylene and other olefins than Rh catalysts, but Rh is the better catalyst for synthesis gas (H2 + CO) production. Catalyst supports with lower internal surface area to volume ratio produce lower selectivities of H2 and CO and higher selectivities of H2O, ethylene, and other olefins than high surface area to volume catalysts. © 2006 American Institute of Chemical Engineers AIChE J 2007

[1]  L. Schmidt,et al.  Contributions of heterogeneous and homogeneous chemistry in the catalytic partial oxidation of octane isomers and mixtures on rhodium coated foams , 2006 .

[2]  L. Schmidt,et al.  Partial oxidation of n-hexadecane at short contact times: Catalyst and washcoat loading and catalyst morphology , 2006 .

[3]  Kenneth A. Williams,et al.  Catalytic autoignition of higher alkane partial oxidation on Rh-coated foams , 2006 .

[4]  C. Leclerc,et al.  A dual catalyst bed for the autothermal partial oxidation of methane to synthesis gas , 2005 .

[5]  J. Richardson,et al.  Properties of ceramic foam catalyst supports: mass and heat transfer , 2003 .

[6]  L. Schmidt,et al.  Catalytic partial oxidation of higher hydrocarbons at millisecond contact times: decane, hexadecane, and diesel fuel , 2003 .

[7]  L. Schmidt,et al.  C6 oxygenates from n-hexane in a single-gauze reactor , 2000 .

[8]  L. Schmidt,et al.  High yields of synthesis gas by millisecond partial oxidation of higher hydrocarbons , 2000 .

[9]  Laxminarayan L. Raja,et al.  A critical evaluation of Navier–Stokes, boundary-layer, and plug-flow models of the flow and chemistry in a catalytic-combustion monolith , 2000 .

[10]  Lanny D. Schmidt,et al.  Modeling homogeneous and heterogeneous chemistry in the production of syngas from methane , 2000 .

[11]  L. Schmidt,et al.  Oxygenates and olefins from alkanes in a single-gauze reactor at short contact times , 1999 .

[12]  L. Schmidt,et al.  Oxidative dehydrogenation of isobutane at short contact times 1 This research was supported by NSF C , 1999 .

[13]  L. Schmidt,et al.  The Effect of Ceramic Supports on Partial Oxidation of Hydrocarbons over Noble Metal Coated Monoliths , 1998 .

[14]  L. Schmidt,et al.  Partial Oxidation of C5and C6Alkanes over Monolith Catalysts at Short Contact Times , 1998 .

[15]  L. Schmidt,et al.  Partial oxidation of alkanes over noble metal coated monoliths , 1994 .

[16]  L. Schmidt,et al.  Comparison of monolith-supported metals for the direct oxidation of methane to syngas , 1994 .

[17]  L. Schmidt,et al.  Partial Oxidation of CH4, C2H6, and C3H8 on Monoliths at Short Contact Times , 1994 .

[18]  L. Schmidt,et al.  Ethylene formation by oxidative dehydrogenation of ethane over monoliths at very short contact times , 1993 .

[19]  Daniel A. Hickman,et al.  Synthesis gas formation by direct oxidation of methane over Rh monoliths , 1993 .

[20]  Daniel A. Hickman,et al.  Steps in CH4 oxidation on Pt and Rh surfaces: High‐temperature reactor simulations , 1993 .

[21]  L. Schmidt,et al.  Production of Syngas by Direct Catalytic Oxidation of Methane , 1993, Science.

[22]  Daniel A. Hickman,et al.  Synthesis gas formation by direct oxidation of methane over Pt monoliths , 1992 .