The direct hydrogenation of CO2 into dimethyl-ether (DME) has been studied in presence of zeo- lite-based hybrid catalysts, prepared through gel-oxalate coprecipitation of copper, zinc and zirconium pre- cursors (in an atomic ratio of 60 : 30 : 10 respectively) in a solution containing different home-made zeolites (i.e., Sil-1, MFI, Y, FER, BEA, MOR), for a final CuZnZr/zeolite weight composition of 1:1. All the samples were properly characterized with different techniques for determining the textural, structural and morpho- logical nature of the catalytic surface. N2 physisorption highlighted a variation both in the specific surface area and in the pore size distribution from the parent zeolites to the hybrid catalyst. TEM analyses disclosed how the pre-formed zeolite architecture affects the distribution of the oxides on the surface, significantly controlling not only the activity-selectivity pattern under the adopted experimental conditions (TR, 200– 260°C; PR, 30 bar, GHSV: 8.800 NL/kgcat/h), but also the catalyst stability during time on-stream.

Promoting Direct CO2 Conversion to DME over Zeolite-based Hybrid Catalysts

Giordano, G.;Migliori, M.;
2020

Abstract

The direct hydrogenation of CO2 into dimethyl-ether (DME) has been studied in presence of zeo- lite-based hybrid catalysts, prepared through gel-oxalate coprecipitation of copper, zinc and zirconium pre- cursors (in an atomic ratio of 60 : 30 : 10 respectively) in a solution containing different home-made zeolites (i.e., Sil-1, MFI, Y, FER, BEA, MOR), for a final CuZnZr/zeolite weight composition of 1:1. All the samples were properly characterized with different techniques for determining the textural, structural and morpho- logical nature of the catalytic surface. N2 physisorption highlighted a variation both in the specific surface area and in the pore size distribution from the parent zeolites to the hybrid catalyst. TEM analyses disclosed how the pre-formed zeolite architecture affects the distribution of the oxides on the surface, significantly controlling not only the activity-selectivity pattern under the adopted experimental conditions (TR, 200– 260°C; PR, 30 bar, GHSV: 8.800 NL/kgcat/h), but also the catalyst stability during time on-stream.
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Utilizza questo identificativo per citare o creare un link a questo documento: http://hdl.handle.net/20.500.11770/304239
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