Separation, characterization and catalytic cracking kinetics of aromatic fractions obtained from FCC feedstocks

Lappas, A. A.; Patiaka, D. Th.; Dimitriadis, B.D.; Vasalos, I.A.

doi:10.1016/s0926-860x(96)00337-7

Cited by 25 publications

(18 citation statements)

References 17 publications

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“…Due to many parameters contained in the kinetic model [14] the sequential consecutive regression method was applied rather than simultaneous regression. The estimated parameters were the kinetic constants k 1 to k 5 and the parameter n in deactivation function.…”

Section: Kinetic Analysis and Simulationmentioning

confidence: 99%

Kinetics of gas oil catalytic cracking

Sertić-Bionda

Gomzi

Fabulic-Ruszkowski³

2006

React Kinet Catal Lett

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In the present work catalytic cracking of gas oils has been studied in a standard MAT reactor. The cracking product distribution was measured at four different temperatures. Based on the experimental results, a 4-lump kinetic model was applied. Kinetic constants were estimated using the sequential step optimization method. Simulation results have shown to be in a good agreement with experimental data. An isothermal pseudo steady-state model for fixed bed MAT reactor is proposed.

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Section: Kinetic Analysis and Simulationmentioning

confidence: 99%

Kinetics of gas oil catalytic cracking

Sertić-Bionda

Gomzi

Fabulic-Ruszkowski³

2006

React Kinet Catal Lett

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“…Moreover, the quality of separation was verified by a gas chromatography mass spectroscopy procedure using a GC/MS apparatus (HP GC/MS 5859 MS ENGINE). According to this procedure, the aromatics which were separated by the ASTM D-2549-85 method, were analyzed in the GC/MS and their separation was found satisfactory (Lappas et al, 1997a;Lappas et al, 1997b).…”

Section: Resultsmentioning

confidence: 99%

“…The solvents are completely removed by evaporation and the residues are weighed and calculated as the non-aromatics and aromatics fractions of the sample. Full details for this method are given in the literature (Lappas et al, 1997a, Lappas et al, 1997b.…”

Section: Aromatics Determinationmentioning

confidence: 99%

Production of low aromatics and low sulfur diesel in a hydrodesulfurization (HDS) pilot plant unit

2013

Global NEST Journal

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The present work investigates the hydrotreating process of a diesel in order to achieve lower sulphur and aromatics content. The entire work was performed in a Hydrodesulphurization (HDS) pilot plant unit located in Chemical Process Engineering Research Institute (CPERI). For the tests, a commercial HDS catalyst (CoMo) was used while the feed was provided by the deep desulphurization unit of a Greek refinery (Motor-Oil refinery). For the determination of diesel aromatics, a method based on the ASTM D-2549-85 was applied. The objective of the work was to investigate the ability of a typical HDS catalyst for aromatics saturation. The effect of the main hydrotreating operating parameters (T, P, WHSV, H 2 /Oil ratio) on sulphur and aromatics removal was also investigated. In general, the data showed that the product density and the aromatic and sulphur content of diesel decreased as the temperature or pressure increased or space velocity decreased. It was concluded that with the present catalyst an aromatics saturation degree of up to 40% could be achieved, giving a diesel product with aromatics content of about 20-25% wt. However, high temperatures (>370°C) were required in order to achieve 500 ppmw sulphur in this feedstock.

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“…However, quinoline (and other nitrogenated poisons) are usually present in very small quantities in FCC feed, while polyaromatics, present in the feed or as a product of cracking, may represent a significant part of the so called unconverted feed. These components contribute to coke, and have a higher coke selectivity than feed gasoil as suggested by the craking of the heavy aromatic part of gasoil [38]. Nevertheless, they are not the principal contributors, since they only represent a small fraction of feed.…”

Section: Resultsmentioning

confidence: 99%

“…Soft coke is totally removed by an adequate stripping in most lab units, but may not be fully removed in the FCC www.elsevier.com/locate/apcata Applied Catalysis A: General 287 (2005) [34][35][36][37][38][39][40][41][42][43][44][45][46] stripper due to a limited efficiency derived from stripper geometry and vapour flow rate. The ratio of soft to hard coke obtained at the exit of the riser reactor depends on catalyst properties, especially vapour aging [20].…”

Section: Introductionmentioning

confidence: 99%