Kinetic analysis of vacuum residue hydrocracking in early reaction stages

Purón, H.; Arcelus-Arrillaga, Pedro; Chin, Ken K.; Pinilla, J.L.; Fidalgo, Beatriz; Millán, Marcos

doi:10.1016/j.fuel.2013.09.053

Cited by 44 publications

(47 citation statements)

References 26 publications

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“…It can be found that H 2 and CO 2 contents are higher than that of non‐catalytic cracking when iron‐containing mixed oxides were added, which is consistent with the results obtained from Wang et al and Fumoto et al They used iron oxide based catalysts for the catalytic cracking of heavy oil, and found that the H 2 and CO 2 contents are much higher in the presence of iron oxide based catalysts than in the non‐catalytic cracking. The condensation of polyaromatic hydrocarbons on the catalyst surface may produce H 2 . The second oxide in the catalysts suppressed the oxidation of the tar and promoted its hydrogenation .…”

Section: Resultsmentioning

confidence: 99%

Steam catalytic cracking of coal tar over iron‐containing mixed metal oxides

Wang

Jin

et al. 2018

Can J Chem Eng

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Steam catalytic cracking is deemed as a promising method for the catalytic cracking of coal tar. In this study, a serial of iron-containing mixed metal oxides including ceria, zirconia, alumina, cobalt, nickel, and barium oxides were prepared for steam catalytic cracking of coal tar and characterized by N 2 adsorption-desorption, X-ray diffraction, H 2 temperature programmed reduction, and Raman spectroscopy, respectively. It was found that the specific surface area and pore volume increase while the crystal size decreases when Fe 2 O 3 was doped with the investigated metal oxides. Among these, iron-alumina mixed oxide (FeAl) shows the highest specific surface area and pore volume. The H 2 -TPR analysis indicated that most of the mixed metal oxides have lower reduction temperature, especially for iron-ceria mixed oxide (FeCe). The reduction temperature of FeCe is around 500 8C, and its reduction peak shifts to a lower temperature and becomes narrower as compared to other iron-containing mixed metal oxides. The steam catalytic cracking of coal tar at 550 8C showed that the light tar content (below 360 8C) over FeCe, FeCo, and FeAl are 68.5, 67.0, and 66.5 %, respectively. The increase of CO 2 and H 2 over iron-containing mixed metal oxides suggested that oxygen species from iron-containing mixed metal oxides and steam could participate in the steam catalytic cracking of coal tar.

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Section: Resultsmentioning

confidence: 99%

Steam catalytic cracking of coal tar over iron‐containing mixed metal oxides

Wang

Jin

et al. 2018

Can J Chem Eng

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“…Various kinetic models have been proposed by several researchers (Froment, 2005;Botchway et al, 2004;Browning et al, 2016;Ancheyta et al, 2005;Elizalde et al, 2010;Puron et al, 2014) to study the product distribution in hydrocracking. A commonly used approach is to consider the mixture in terms of selected lumps, which can be specified in terms of structural characteristics, such as boiling point.…”

Section: Introductionmentioning

confidence: 99%

Optimization of Kinetic Lumping Model Parameters to Improve Products Quality in the Hydrocracking Process

Naderi¹,

Shokri²,

Ahmadpanah³

2018

Braz. J. Chem. Eng.

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In this study a typical continuous lumping model with five parameters has been used for kinetic modeling of thermal and catalytic hydrocracking. Model parameters have been optimized according to experimental product distributions using a particle swarm optimization (PSO) algorithm. Experimental data from the hydrocracker setup have been employed to validate the proposed model. In this setup hydrogen and vacuum gasoil feed were introduced from the top of a vertical reactor and, after passing through a catalyst bed, the liquid and gas products were separated and analyzed. Temperature of the reactor was adjusted in the range of 440-470ºC for thermal hydrocracking, and 410-430ºC for catalytic hydrocracking. Liquid hourly space velocities (LHSV) were in the range of 0.5-1.5 feed flow rate per catalyst volume in both sets of experiments. Results of optimization showed that the parameters were only temperature dependent. The comparison between model results and experimental data indicates that the model is capable of predicting product yield with maximum errors of 0.986 and 0.041 for RMSE and AARE values, respectively.

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“…Theoretically, the required kinetic model should consider all the elementary reactions occurring during hydrogenation [7], but practical application is impossible because of the complexity of the reaction mixture consisting of numerous components. Thus, existing modeling technologies of hydrogenation are primarily based on the lumped method [8][9][10][11][12][13][14][15][16], in which the complex mixture is usually divided into smaller groups of pseudo components with respect to their properties, such as boiling point, and http://dx.doi.org/10.1016/j.apenergy.2014. 10.009 0306-2619/Ó 2014 Elsevier Ltd. All rights reserved.…”

Section: Introductionmentioning

confidence: 99%