Catalytic Hydrocracking of an Asphaltenic Coal Residue

Benito, Ana M.; Martínez, María Teresa

doi:10.1021/ef9600467

Cited by 14 publications

(11 citation statements)

References 19 publications

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“…Suppression of coke formation due to hydrogen addition is widely thought of as a capping of free radical coke precursors formed when carbon-to-carbon bonds split leading to lower molecular weight compounds than the original THAI feed oil molecules. 44,45 A significant effect of hydrogen in this study was its ability to suppress the formation of coke compared to nitrogen as the flowing gas atmosphere (Figures 9a,b and 10), and as is commonly practiced in the refining industry the phenomenon is known to increase the yield of distillates and its quality. 46 Table 3S shows the composition of the produced gases when hydrogen was injected as the reaction atmosphere.…”

Section: Resultsmentioning

confidence: 82%

Optimization of the CAPRI Process for Heavy Oil Upgrading: Effect of Hydrogen and Guard Bed

Hart

Shah

Leeke

et al. 2013

Ind. Eng. Chem. Res.

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Toe-to-heel air injection (THAI) and its catalytic version CAPRI are relatively new technologies for the recovery and upgrade of heavy oil and bitumen. The technologies combine horizontal production well, in situ combustion, and catalytic cracking to convert heavy feedstock into light oil down-hole. The deposition of asphaltenes, coke, and metals can drastically deactivate the catalyst in the CAPRI process. A fixed bed microreactor was used to experimentally simulate the conditions in the catalyst zone of the oil well of CAPRI. In this study, oil upgrading and catalyst deactivation in the CAPRI process were investigated in the temperature range of 350−425°C, pressure of 20 barg and residence time of 9.2 min. Additionally, a guard bed consisting of activated carbon particles prior to the active catalyst in a microreactor and/or the addition of hydrogen to the gas feed were used to minimize coke formation and catalyst deactivation through respectively removing and hydrocracking the coke precursors. It was found that depending on the upgrading temperature, the viscosity of the produced oil reduced significantly by 42−82% and (American Petroleum Institute) API gravity increased by ∼2 to 7°API relative to the feedstock of 0.49 Pa·s and 13°API, respectively. Conversely, the use of hydrogen further increased the API gravity by 2°API and the viscosity by 5.3%. Notably, the coke content of the catalyst reduced from 57.3 wt % in nitrogen to 34.8 wt % in hydrogen atmosphere. The use of a guard bed increased the API gravity of the produced oil by a further 2°and reduced the viscosity by an average of 8.5% further than achieved with the active HDS catalyst CoMo/alumina.

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Section: Resultsmentioning

confidence: 82%

Optimization of the CAPRI Process for Heavy Oil Upgrading: Effect of Hydrogen and Guard Bed

Hart

Shah

Leeke

et al. 2013

Ind. Eng. Chem. Res.

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“…Benito and Martínez [9] followed a simple first-order kinetic model in which the heavy fraction is cracked to produce middle distillates. The feed was an asphaltenic residue from coal liquids, and was hydrocracked using a NiO-MoO 3 /Al 2 O 3 catalyst in a tubular reactor.…”

Section: Introductionmentioning

confidence: 99%

Kinetic model for hydrocracking of heavy oil in a CSTR involving short term catalyst deactivation

Martínez

Ancheyta

2012

Fuel

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“…Many process of cracking were done simultaneously with hydrogenation, called hydrocracking. Hydrocracking process needs two components of catalyst, which are metal component as hydrogenation catalyst and acid component as cracking catalyst (Benito, 2000). For this purpose, the catalyst often used is the combination of transition metal and active Zeolite.…”

Section: Articlementioning

confidence: 99%

Synthesis of Catalyst Cobalt Impregnated on Activated Natural Zeolite, Co/ANZ

Dewi¹,

Fanani²

2017

ijfac

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Research has been done on the synthesis of catalyst Co/Activated Natural Zeolite. The variables studied were the mass ratio of Cobalt to Zeolite and temperature of reduction during catalyst activation. The catalyst produced were analysed in their acidity and surface area. Acidity was presented in the form of ammonia and pyridine adsorption on the catalyst surface. The results showed the increasing Cobalt to Zeolite mass ratio will increase acidity of the catalyst produced. Reduction temperature during catalyst activation also gave same effect as Cobalt to Zeolite mass ratio did. Best ratio within the range of this study was Cobalt to Zeolite mass ratio of 6:20, which was found at reduction temperature of 400 C. This ratio gave catalyst acidity correspond to ammonia adsorption of 6.4615 mmol/g, and to pyridine adsorption of 2.6047 mmol/g catalyst. The best reduction temperature was 450 C at ratio of 6:20. The acidity of this catalyst was of 7.5202 mmol/g as in ammonia adsorption, and was of 3.662 mmol/g as in pyridine adsorption. Catalyst surface area of the best ratio was 32.63 m2/g, whilst catalyst surface area of the best reduction temperature was 38.95 m2/g.

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Catalytic Hydrocracking of an Asphaltenic Coal Residue

Cited by 14 publications

References 19 publications

Optimization of the CAPRI Process for Heavy Oil Upgrading: Effect of Hydrogen and Guard Bed

Optimization of the CAPRI Process for Heavy Oil Upgrading: Effect of Hydrogen and Guard Bed

Kinetic model for hydrocracking of heavy oil in a CSTR involving short term catalyst deactivation

Synthesis of Catalyst Cobalt Impregnated on Activated Natural Zeolite, Co/ANZ

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