Dehydrogenative cracking of n-butane using double-stage reaction

Wakui, Kenichi; Satoh, Koichi; Sawada, Goro; Shiozawa, Koji; Matano, Koichi; Suzuki, Kenzi; Hayakawa, T.; Yoshimura, Y.; Murata, Kazuhisa; Mizukami, Fujio

doi:10.1016/s0926-860x(01)01014-6

Cited by 28 publications

(8 citation statements)

References 7 publications

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“…Three primary strategies for achieving these properties include element modification (Liu et al 2011;Wakui et al 2002), preparation of nano-zeolites (Song et al 2004;Morales-Pacheco et al 2007;Viswanadham et al 2009;Mochizuki et al 2011), and introduction of mesopores between zeolites crystals (Zheng et al 2009;Tang et al 2012;Groen et al 2004). Element modification of zeolites, such as non-metal, alkali metal, alkaline earth metal, transition metal, and rare earth metal modification can adjust acidity and product selectivity, improve catalytic activity (Xue et al 2007;Wang et al 1994Wang et al , 2007Maia et al 2010).…”

Section: Introductionmentioning

confidence: 99%

HZSM-5/MCM-41 composite molecular sieves for the catalytic cracking of endothermic hydrocarbon fuels: nano-ZSM-5 zeolites as the source

Sang

Jiao

et al. 2014

J Nanopart Res

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A series of HZSM-5/MCM-41 composite molecular sieves (HZM-Ns (x)) were prepared by employing nano-ZSM-5 zeolites with the SiO 2 /Al 2 O 3 ratios (x) of 50, 100 and 150 as the source. These materials were characterized by X-ray diffraction, Fourier transform infrared spectroscopy, scanning electron microscopy, energy dispersive spectroscopy, transmission electron microscopy, N 2 adsorptiondesorption measurement, and NH 3 temperature-programmed desorption. The catalytic cracking of endothermic hydrocarbon fuels over the HZM-Ns with ndecane as model was evaluated at atmospheric pressure and 500°C. The effect of the parent zeolite, mesopore and SiO 2 /Al 2 O 3 ratio on the structure, acidity, and catalytic performance of HZM-Ns was investigated. The HZM-Ns exhibited a skeletal matrix with nano-sized HZSM-5 particles (200-300 nm) with a controllable acidity well dispersed in and microporous-mesoporous hierarchical pores. The mesoporous structure improved the diffusion of the reactants and products in the pores, and the HZSM-5 nanoparticles uniformly dispersed in the MCM-41 matrix supplied a proper acidity, shorter channels, and a higher specific surface area for reaction. These resulted in a high catalytic activity, a high selectivity to light olefins and a long lifetime for n-decane catalytic cracking. The HZM-N (150) exhibited the excellent conversion, a high selectivity to light olefins and a long lifetime due to low diffusion resistance, high specific surface area, and appropriate acid distribution and strength, with the increasing SiO 2 / Al 2 O 3 ratio.

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Section: Introductionmentioning

confidence: 99%

HZSM-5/MCM-41 composite molecular sieves for the catalytic cracking of endothermic hydrocarbon fuels: nano-ZSM-5 zeolites as the source

Sang

Jiao

et al. 2014

J Nanopart Res

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“…This good performance of the HZSM-5 zeolite in the cracking of n-butane has been observed by different authors with catalysts based on this zeolite with different SiO 2 /Al 2 O 3 ratios and prepared based on different modifications. [16][17][18] The combined cracking of n-butane with methanol has been studied in a previous paper (Figure 1), which has the advantage of being energetically neutral when a suitable ratio of reactants is used, thus avoiding the high energy requirements of the cracking. Significant synergies have been found between the two reactions when they are carried out jointly in the same reactor.…”

Section: Introductionmentioning

confidence: 99%

Kinetic Modeling of n-Butane Cracking on HZSM-5 Zeolite Catalyst

Mier

Aguayo

Gamero

et al. 2010

Ind. Eng. Chem. Res.

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A kinetic model of lumps has been established for n-butane cracking over HZSM-5 zeolite catalyst (SiO2/Al2O3 = 30) in the 400−550 °C range, based on the results obtained in a fixed bed reactor (space time, up to 2.4 (g of catalyst) h (mol CH2)−1; He/n-butane molar ratio in the feed, up to 6/1; time on stream, 5 h). The model allows quantifying the distribution of the lumps of products (C2−C4 olefins, C2−C4 paraffins, methane, and C5−C10 components) in a wide range of temperatures, partial pressures of hydrocarbons in the reaction medium, and space times. The kinetic model steps for the transformation of n-butane into olefins and of olefins into paraffins and C5−C10 are second order with respect to the reactant, whereas the remaining steps are first order with respect to each reactant. When the target is the production of C2−C4 olefins, the yield is limited to 12%, at 550 °C.

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“…Moreover, with decreasing aluminum content in the zeolite structure, the relative contribution of the protolytic mechanism increases vs. the bimolecular mechanism. [13][14][15][16][17][18][19][20] Kinetic modeling is a very useful tool to develop a better understanding of catalytic cracking reactions. 7,8,14 This type of zeolite also enhances protolytic cracking reactions over secondary reactions because of its special shape selectivity, moderate acidic strength, and low capacity for hydrogen transfer.…”

Section: Introductionmentioning

confidence: 99%

“…Hence, many authors have investigated the mechanism and kinetics behind the catalytic cracking of butanes. [13][14][15][16][17][18][19][20] Kinetic modeling is a very useful tool to develop a better understanding of catalytic cracking reactions. Several authors have investigated the kinetics of paraffin catalytic cracking over HZSM-5 zeolite catalysts, using microkinetic modeling.…”

Section: Introductionmentioning

confidence: 99%

Chemical kinetic modeling of i‐butane and n‐butane catalytic cracking reactions over HZSM‐5 zeolite

et al. 2011

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A chemical kinetic model for i‐butane and n‐butane catalytic cracking over synthesized HZSM‐5 zeolite, with SiO2/Al2O3 = 484, and in a plug flow reactor under various operating conditions, has been developed. To estimate the kinetic parameters of catalytic cracking reactions of i‐butane and n‐butane, a lump kinetic model consisting of six reaction steps and five lumped components is proposed. This kinetic model is based on mechanistic aspects of catalytic cracking of paraffins into olefins. Furthermore, our model takes into account the effects of both protolytic and bimolecular mechanisms. The Levenberg–Marquardt algorithm was used to estimate kinetic parameters. Results from statistical F‐tests indicate that the kinetic models and the proposed model predictions are in satisfactory agreement with the experimental data obtained for both paraffin reactants. © 2011 American Institute of Chemical Engineers AIChE J, 58: 2456–2465, 2012

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Dehydrogenative cracking of n-butane using double-stage reaction

Cited by 28 publications

References 7 publications

HZSM-5/MCM-41 composite molecular sieves for the catalytic cracking of endothermic hydrocarbon fuels: nano-ZSM-5 zeolites as the source

HZSM-5/MCM-41 composite molecular sieves for the catalytic cracking of endothermic hydrocarbon fuels: nano-ZSM-5 zeolites as the source

Kinetic Modeling of n-Butane Cracking on HZSM-5 Zeolite Catalyst

Chemical kinetic modeling of i‐butane and n‐butane catalytic cracking reactions over HZSM‐5 zeolite

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