Ring opening of hydrocarbons for diesel and aromatics production: Design of heterogeneous catalytic systems

Galadima, Ahmad; Muraza, Oki

doi:10.1016/j.fuel.2016.05.024

Cited by 46 publications

(26 citation statements)

References 140 publications

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“…Consequently, the hydrogenation of the polyaromatic components of the heavy oil reduces the viscosity of the upgraded oil [8], and as a consequence, the fuel distillate fractions are increased [6,10]. Therefore, the hydrogenation of polyaromatic compounds in heavy oil improves the API (American Petroleum Institute) gravity, increases fuel distillate fractions in the upgraded oil, facilitates the removal of heteroatoms such as sulfur and nitrogen, and suppresses coke formation in order to extend the catalyst lifetime [11,12]. On the other hand, introducing pure hydrogen gas into the oil formation is very challenging.…”

Section: Introductionmentioning

confidence: 99%

Hydrogenation and Dehydrogenation of Tetralin and Naphthalene to Explore Heavy Oil Upgrading Using NiMo/Al2O3 and CoMo/Al2O3 Catalysts Heated with Steel Balls via Induction

et al. 2020

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This paper reports the hydrogenation and dehydrogenation of tetralin and naphthalene as model reactions that mimic polyaromatic compounds found in heavy oil. The focus is to explore complex heavy oil upgrading using NiMo/Al2O3 and CoMo/Al2O3 catalysts heated inductively with 3 mm steel balls. The application is to augment and create uniform temperature in the vicinity of the CAtalytic upgrading PRocess In-situ (CAPRI) combined with the Toe-to-Heel Air Injection (THAI) process. The effect of temperature in the range of 210–380 °C and flowrate of 1–3 mL/min were studied at catalyst/steel balls 70% (v/v), pressure 18 bar, and gas flowrate 200 mL/min (H2 or N2). The fixed bed kinetics data were described with a first-order rate equation and an assumed plug flow model. It was found that Ni metal showed higher hydrogenation/dehydrogenation functionality than Co. As the reaction temperature increased from 210 to 300 °C, naphthalene hydrogenation increased, while further temperature increases to 380 °C caused a decrease. The apparent activation energy achieved for naphthalene hydrogenation was 16.3 kJ/mol. The rate of naphthalene hydrogenation was faster than tetralin with the rate constant in the ratio of 1:2.5 (tetralin/naphthalene). It was demonstrated that an inductively heated mixed catalytic bed had a smaller temperature gradient between the catalyst and the surrounding fluid than the conventional heated one. This favored endothermic tetralin dehydrogenation rather than exothermic naphthalene hydrogenation. It was also found that tetralin dehydrogenation produced six times more coke and caused more catalyst pore plugging than naphthalene hydrogenation. Hence, hydrogen addition enhanced the desorption of products from the catalyst surface and reduced coke formation.

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Section: Introductionmentioning

confidence: 99%

Hydrogenation and Dehydrogenation of Tetralin and Naphthalene to Explore Heavy Oil Upgrading Using NiMo/Al2O3 and CoMo/Al2O3 Catalysts Heated with Steel Balls via Induction

et al. 2020

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“…Catalytic reforming is a matured industrial process to produce aromatics from paraffins and olefins which cause low‐octane and automobile emission problems [4,5] . The naphtha aromatization process involves the conversion of low‐octane hydrocarbons into benzene, toluene, ethyl benzene and xylene (BTEX) having high octane values [6] . The conversion of paraffin to aromatics is hindered by the inertness of the C−H/C−C bonds and the unfavorable thermodynamics; which result in high reaction temperatures and low product yields and selectivity.…”

Section: Introductionmentioning

confidence: 99%

Aromatization of Commercial Full Range Naphtha Over Modified Hierarchical ZSM‐5 Catalyst

et al. 2021

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Aromatization of commercial full range naphtha has been studied in a fixed bed reactor using the synthesized hierarchical zeolite catalysts. Desilication was carried out on H‐ZSM‐5 support with Silica to Alumina (SiO2/Al2O3) molar ratio 30 to generate additional meso‐porosity and active metal Gallium was incorporated by wetness impregnation method. Various concentrations of sodium hydroxide solutions and two different initial calcination temperature were used during the modification to understand the effect of these parameters on the catalysts. All the catalysts were characterized using nitrogen adsorption, X‐ray diffraction, temperature programmed ammonia desorption, elemental and surface imaging techniques. Catalytic evaluation is done in a fixed bed reactor operated at a temperature of 550 °C, atmospheric pressure and liquid hourly space velocity of 6.0 h−1. Product streams from the fixed bed reactor are analyzed using both online and offline gas chromatographs using ASTM D7833 and D6729 respectively to report product selectivity and mass balance. It is observed that the additional meso porosity and the retention of crystallite phase lead to 62.4 % enhancement in aromatic selectivity and 52.2 % decrease in off‐gas generation for the developed catalyst compared to its non‐desilicated analogue during the aromatization process of full range real naphtha.

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“…Monofunctional acid (mainly different kinds of zeolites), monofunctional metallic, and bifunctional catalysts have been proposed for performing the selective ring opening (SRO) …”

Section: Introductionmentioning

confidence: 99%

“…Despite the significant effort made by several research groups, the selective opening of naphthenic rings has not yet been applied industrially. This could be due to the low yields to ring opening (RO) products.…”

Section: Introductionmentioning

confidence: 99%

Ru‐Pt catalysts supported on Al₂O₃ and SiO₂─Al₂O₃ for the selective ring opening of naphthenes

et al. 2019

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Alumina and silica-alumina supported Ru-Pt catalysts were evaluated for the ring opening of naphthenes. Pt, Ru, and Ru-Pt catalysts were prepared by the impregnation of inorganic precursors over γ-alumina and silica-alumina supports. The catalysts were evaluated by temperature programmed reduction (TPR), pyridine temperature programmed desorption (TPD), CO-FTIR, and by test reactions of 33DM1B isomerization, cyclohexane dehydrogenation, cyclopentane hydrogenolysis, and the ring opening of decalin. The strong interaction between the metals (Pt-Ru) was attributed to their reductions occurring simultaneously. The acidity and strength of the acid sites of the monometallic Ru catalyst were higher than those of the monometallic Pt catalyst. The total acidity (Lewis and Brønsted) and the strength of the acid sites were higher for the silica-alumina supported catalysts. The silica-alumina catalysts had 10 times more Brønsted acidity than the γ-alumina ones and an increased activity and selectivity to decalin ring opening products. Supported monometallic Ru had the best performance for the ring opening reaction. K E Y W O R D Sdecalin, Ru-Pt catalysts, selective ring opening

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Ring opening of hydrocarbons for diesel and aromatics production: Design of heterogeneous catalytic systems

Cited by 46 publications

References 140 publications

Hydrogenation and Dehydrogenation of Tetralin and Naphthalene to Explore Heavy Oil Upgrading Using NiMo/Al2O3 and CoMo/Al2O3 Catalysts Heated with Steel Balls via Induction

Hydrogenation and Dehydrogenation of Tetralin and Naphthalene to Explore Heavy Oil Upgrading Using NiMo/Al2O3 and CoMo/Al2O3 Catalysts Heated with Steel Balls via Induction

Aromatization of Commercial Full Range Naphtha Over Modified Hierarchical ZSM‐5 Catalyst

Ru‐Pt catalysts supported on Al₂O₃ and SiO₂─Al₂O₃ for the selective ring opening of naphthenes

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Ring opening of hydrocarbons for diesel and aromatics production: Design of heterogeneous catalytic systems

Cited by 46 publications

References 140 publications

Hydrogenation and Dehydrogenation of Tetralin and Naphthalene to Explore Heavy Oil Upgrading Using NiMo/Al2O3 and CoMo/Al2O3 Catalysts Heated with Steel Balls via Induction

Hydrogenation and Dehydrogenation of Tetralin and Naphthalene to Explore Heavy Oil Upgrading Using NiMo/Al2O3 and CoMo/Al2O3 Catalysts Heated with Steel Balls via Induction

Aromatization of Commercial Full Range Naphtha Over Modified Hierarchical ZSM‐5 Catalyst

Ru‐Pt catalysts supported on Al2O3 and SiO2─Al2O3 for the selective ring opening of naphthenes

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Ru‐Pt catalysts supported on Al₂O₃ and SiO₂─Al₂O₃ for the selective ring opening of naphthenes