Comparison between MAT Flow Fixed Bed and Batch Fluidized Bed Reactors in the Evaluation of FCC Catalysts. 1. Conversion and Yields of the Main Hydrocarbon Groups

Passamonti, Francisco Javier; Puente, Gabriela de la; Sedrán, Ulises

doi:10.1021/ef8008103

Cited by 15 publications

(23 citation statements)

References 34 publications

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“…More specifically, in the pilot unit an increase in the C/O augments the space-velocity, which ultimately leads to more pronounced deltas in feed conversion. In the bench scale testing, in contrast, the space time is independent of the C/O and the variation in the conversion is induced by changes in the degree of catalyst deactivation by coke, as was stated elsewhere [21,29]. Also noted in Figs.…”

Section: Bench Scale Versus Pilot Scalementioning

confidence: 75%

“…The cracking of heavy fraction, given in terms of the bottoms selectivity, is not significantly different for the two reactor configurations. Most of these trends are [23,28,29]. A hydrodynamics effect, presumably associated to a lower concentration of catalyst particles in a pilot plant riser than that in a non circulating bench scale reactor, is a reasonable explanation for the smaller conversion observed in the pilot plant testing [23].…”

Section: Bench Scale Versus Pilot Scalementioning

confidence: 92%

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Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

et al. 2011

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Besides offering an adequate product distributions, a cracking catalyst must exhibit a reasonable resistance to the combined effect of high temperature, steam and metals. Two commercial catalysts, poisoned with Ni ? V (*2,500 ppm), are subjected to a large scale cyclic deactivation with steam, then characterized using mostly basic techniques and finally tested via bench scale and pilot scale cracking experiments. As examples of industrial deactivation, corresponding equilibrium catalysts (E-CATs) are investigated in parallel. Depending on their specific formulation, catalysts deactivate differently due to the exposition to high temperature steam and metals. The intrinsic deviations in the catalytic properties of cyclic deactivated catalysts (CD-CATs) related to E-CATs are further biases by the particular history of the latter and the particular reactor configuration and hydrodynamics, such deviations being magnified in the bench scale testing. Relative differences in activity and product yields (except for coke and hydrogen) of CD-CATs referred to E-CATs are below 10% at the pilot scale, and within 23% at the bench scale. Relative biases in hydrogen and coke yield of may be as high as 75 and 26% in the pilot plant and as much as 150 and 32% at the bench scale.

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Section: Bench Scale Versus Pilot Scalementioning

confidence: 75%

Section: Bench Scale Versus Pilot Scalementioning

confidence: 92%

Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

et al. 2011

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“…The lower unit cell size and content of rare earth elements that provide a higher hydrothermal resistance to FCC catalysts 39,40 in catalyst ECAT-D, as compared to those in catalyst ECAT-R, are typical in octane-barrel catalysts, where both the gasoline yield and quality (RON) are expected to be maximized. 38 The results of acidity characterization are shown in Table 3 and Figure 1. It can be seen that the total acidity in catalyst ECAT-D, as given by the amount of pyridine remaining adsorbed after desorption at 150 °C, was significantly higher than that in catalyst ECAT-R.…”

Section: Resultsmentioning

confidence: 99%

“…In this sense, the fluidized bed in the CREC Riser Simulator reactor allows for a more efficient catalyst−reactants contact, thus avoiding the high coke yields observed in fixed bed reactors. 8,38 Figure 2 shows the conversions of all the feedstocks on the equilibrium catalysts as a function of reaction time. Even though the absolute values of conversion do not match those found in the commercial operation, 4 given the operating conditions chosen for these experiments, distinctive behaviors can be observed.…”

Section: Resultsmentioning

confidence: 99%

Performance of Equilibrium FCC Catalysts in the Conversion of the SARA Fractions in VGO

et al. 2020

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Two equilibrium FCC catalysts of the octane-barrel (ECAT-D) and resid (ECAT-R) types were used in the cracking of a typical vacuum gasoil (VGO) and its saturated (SF), aromatic (AF), and resin (RF) fractions. The experiments were carried out in a batch, fluidized bed laboratory CREC Riser Simulator reactor. The reaction temperature was 500 °C, the catalyst-to-oil relationship was 1, with 0.2 g of the catalyst being used in each experiment, and the reaction times were 0.7, 1.5, and 3 s. The ranking of the reactivities of the different feedstocks was SF > VGO > AF > RF over both catalysts. While the AF and RF fractions yielded more gasoline than the SF fraction, the latter showed the highest yields of LPG. The coke forming trend followed the order SF < VGO < AF < RF. Even though catalyst ECAT-D, with a higher and stronger acidity, was more active than catalyst ECAT-R, which has less acidity and better textural properties (higher mesoporosity and pore diameter), the latter was less affected by coke deposition, considering the changes in the specific surface area and acidic properties after use. Coke impacted more severely on Bronsted acid sites than on Lewis sites, particularly when the AF and RF fractions were used. The stronger acid sites were more severely affected by coke, particularly in catalyst ECAT-D. The negative effect on strong acidic sites was consistent with the increasing basic character of the feedstocks, following the order SF < VGO < AF < RF.

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“…Additional descriptive details can be found in Bidabehere and Sedran (2006), Al-Khattaf (2007), and Passamonti et al (2009).…”

Section: Reactor Setup and Operation Modementioning

confidence: 99%

Reliable Laboratory Reactor Data Analysis: Evaluation of Commercial FCC Catalysts in a Batch Fluidized Bed Reactor

Río

Passamonti

Sedrán

2015

Chemical Engineering Communications

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Statistical techniques for the treatment and analysis of experimental data from laboratory reactors were considered, as applied to a CREC Riser Simulator reactor for the example of FCC catalyst evaluation. Deviations in mass balances were reconciliated considering the variance in each product mass. After reconciliations, simple OPE curves were used to fit the data due to their simplicity and proper representation of the yield curves. In the data fitting step, errors in both dependent and independent variables were considered by using information obtained in the reconciliation procedure. The impact of different levels of confidence bands in the models on the discrimination of experimental results was discussed. Significant improvements in catalyst evaluation could be achieved either in the CREC Riser Simulator or other types of laboratory reactors with the help of the statistical procedures described here without increasing substantially the number of experiments.

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Comparison between MAT Flow Fixed Bed and Batch Fluidized Bed Reactors in the Evaluation of FCC Catalysts. 1. Conversion and Yields of the Main Hydrocarbon Groups

Cited by 15 publications

References 34 publications

Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

Cyclic Deactivation with Steam of Metallated Cracking Catalysts: Catalytic Testing at the Bench Scale and the Pilot Scale

Performance of Equilibrium FCC Catalysts in the Conversion of the SARA Fractions in VGO

Reliable Laboratory Reactor Data Analysis: Evaluation of Commercial FCC Catalysts in a Batch Fluidized Bed Reactor

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