Fluid catalytic cracking: modelling of an industrial riser

Landeghem, F. van; Nevicato, David; Pitault, Isabelle; Forissier, M.; Turlier, P.; Derouin, C.; Bernard, J.R.

doi:10.1016/0926-860x(95)00309-6

Cited by 62 publications

(39 citation statements)

References 26 publications

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“…As a result, very little dispersion on solid particle residence time is observed, with Peclet numbers above 1000. Note that this is significantly better than in industrial risers, were some degree of backmixing exists, and Peclet numbers of 5 to 16 were measured [32]. The narrow size of the reactor also improves the isothermicity of the reaction.…”

Section: Fixed Fluid Bed Solid Well Mixed Gas: Berty Type Reactors Rmentioning

confidence: 92%

FCC testing at bench scale: New units, new processes, new feeds

Corma

Sauvanaud

2013

Catalysis Today

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As the FCC process has evolved over decades, several laboratory scale equipment have appeared to maintain a proper assessment of catalysts activity. Several laboratory equipments are available for simulating the FCC process, from the well known fixed bed, MicroActivity Test to newer, fluid bed or transported bed units. As well, a number of units have been created to simulate other parts of the process such as regenerator or stripper, The increased pressure for treating non-conventional feeds, from reprocessing gasoline to extra-heavy feeds or oils produced from biomass containing large amounts of heteroatoms, increase the needs to have a laboratory test which is as close as possible to the process so that data extraction from the laboratory test are simplified, thus less prone to errors or misunderstanding. KeywordsLaboratory testing, catalytic cracking, naphtha cracking, coked catalyst, biooil cracking Highlights• FCC process is adapting to new feeds and new processes• Heavy resid feeds and biomass-derived feeds are being extensively tested • Significant operation and process changes are contemplated to squeeze maximum value from feeds: naphtha reprocessing, use of partially coked catalysts, several independent risers. 3

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Section: Fixed Fluid Bed Solid Well Mixed Gas: Berty Type Reactors Rmentioning

confidence: 92%

FCC testing at bench scale: New units, new processes, new feeds

Corma

Sauvanaud

2013

Catalysis Today

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“…This work confirmed the validity of lumping strategy even for the hydrotreating process. The usage of lumping strategy is not limited to hydrocracking and some works have been done in the similar fields like modeling of fluid catalytic cracking process [19], hydroconversion [20] and catalytic [21,22] as well as thermal cracking [23] of heavy oils which the latter is in the field of petrochemical processes.…”

Section: Introductionmentioning

confidence: 99%

4-Lump kinetic model for vacuum gas oil hydrocracker involving hydrogen consumption

Sadighi

Ahmad

Rashidzadeh³

2010

Korean J. Chem. Eng.

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A 4-lump kinetic model including hydrogen consumption for hydrocracking of vacuum gas oil in a pilot scale reactor is proposed. The advantage of this work over the previous ones is consideration of hydrogen consumption, imposed by converting vacuum gas oil to light products, which is implemented in the kinetic model by a quadratic expression as similar as response surface modeling. This approach considers vacuum gas oil (VGO) and unconverted oil as one lump whilst others are distillate, naphtha and gas. The pilot reactor bed is divided into hydrotreating and hydrocracking sections which are loaded with different types of catalysts. The aim of this paper is modeling the hydrocracking section, but the effect of hydrotreating is considered on the boundary condition of the hydrocracking part. The hydrocracking bed is considered as a plug flow reactor and it is modeled by the cellular network approach. Initially, a kinetic network with twelve coefficients and six paths is considered. But following evaluation using measured data and order of magnitude analysis, the three route passes and one activation energy coefficient are omitted; thus the number of coefficients is reduced to five. This approach improves the average absolute deviation of prediction from 7.2% to 5.92%. Furthermore, the model can predict the hydrogen consumption for hydrocracking with average absolute deviation about 8.59% in comparison to those calculated from experimental data.

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“…Arandes et al [13] used the 10-lump kinetic model [9] to predict steady states and dynamics of cracking units, the original model was completed with pressure balance in the riser, however it is considered only at the riser outlet. Derouin et al [14] considered the impact of hydrodynamics during catalytic cracking by extending previous works by the same research group [15,16]. Nonetheless, in their last paper they do not include an explicit pressure balance along the riser, as it was the case in the paper by Van Landeghem et al [15].…”

Section: Introductionmentioning

confidence: 93%

“…Derouin et al [14] considered the impact of hydrodynamics during catalytic cracking by extending previous works by the same research group [15,16]. Nonetheless, in their last paper they do not include an explicit pressure balance along the riser, as it was the case in the paper by Van Landeghem et al [15]. In the modelling of the previous generation of cracking units, that also included a riser, the only reference to a pressure balance inside this reactor is due to McFarlane et al [17].…”

Section: Introductionmentioning

confidence: 98%