A CFB unit for skeletal isomerization of linear c4-c6 olefins on ferrierite catalysts

Sandelin, Fredrik; Eilos, I.; Harlin, E.; Hiltunen, J.; Jakkula, J.; Makkonen, J.; Karinen, Reetta

doi:10.1016/s0167-2991(04)80472-5

Cited by 6 publications

(4 citation statements)

References 2 publications

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“…The ferrierite catalyst (mean particle diameter of 120 µm) was deactivated in a 21-h skeletal isomerization run in a pilotscale reactor operating at 285 °C and 20 kPa. 16 The feed to the pilot reactor consisted of alkenes ranging from C 5 to C 7 .…”

Section: Methodsmentioning

confidence: 99%

Kinetic Modeling of Coke Oxidation of a Ferrierite Catalyst

Keskitalo

Lipiäinen

Krause

2006

Ind. Eng. Chem. Res.

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Kinetic models describing coke oxidation were derived for purposes of designing a catalyst regeneration unit and to gain information on coke oxidation kinetics. The coke was formed during an alkene skeletal isomerization reaction on a ferrierite catalyst. Experiments were performed according to the temperature-programmed oxidation technique at several oxygen concentrations and heating rates. The parameters of the models were estimated by nonlinear regression. A power-law model with parametrized order of oxygen concentration described the experimental results adequately. Three other successful models, which were based on assumed reaction mechanisms, shared two main characteristics: the formation of a reactive oxygen intermediate in a fast equilibrium reaction, and the formation of CO and CO 2 from one or more common precursors. All estimated parameters of the models were in a physically meaningful range.

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Section: Methodsmentioning

confidence: 99%

Kinetic Modeling of Coke Oxidation of a Ferrierite Catalyst

Keskitalo

Lipiäinen

Krause

2006

Ind. Eng. Chem. Res.

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“…The catalyst was a ferrierite zeolite, deactivated in skeletal isomerization of alkenes ranging from C 5 to C 7 . 3 The reaction was carried out in a pilot-scale reactor operating at 285 °C for 21 h. The catalyst was retrieved from the pilot reactor after flushing with nitrogen at 285 °C overnight. In this study, coke refers to any hydrocarbons present in the deactivated catalyst after the flushing.…”

Section: Methodsmentioning

confidence: 99%

“…Hydrocarbon processes in which coke formation plays an essential role could feasibly be designed with separate units for the main reaction and the regeneration. 3 In this design the deactivated catalyst is continuously fed to the regenerator, from which the regenerated catalyst is routed back to the main reactor. The coked catalyst passes through a dip leg, in which the particles remain as a bed until they are fed to the regenerator.…”

Section: Introductionmentioning

confidence: 99%

Evolution of Light Hydrocarbons from a Coked Ferrierite Catalyst during Temperature-Programmed Gasification

Keskitalo

Korhonen

Lipiäinen

et al. 2007

Ind. Eng. Chem. Res.

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The evolution of light hydrocarbons during temperature-programmed gasification with helium (TPHe) of a coked ferrierite catalyst was studied to gain information on partial coke removal by heat treatment under inert flow. The catalyst had been deactivated in the skeletal isomerization of alkenes. Characterization by DRIFTS, GC-MS, and 13 C CPMAS NMR revealed that the coke contained two-and three-ring aromatic hydrocarbons, as well as polyaromatics. Evolution predominantly of C 2 -C 5 hydrocarbons was observed during TPHe between 200 and 500 °C. The main components were propene and ethene. The carbon content of the catalyst dropped from 4.3 to 3.5 wt % during TPHe. Kinetic models suitable for the purpose of designing a coke removal unit were derived for the evolution of carbon fractions between C 2 and C 5 from the ferrierite zeolite. The results of the kinetic modeling suggest that one or several bimolecular reactions are relevant in the formation of light hydrocarbons from coke.

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“…To deal with the excessive coke formation during alkene IS, Sandelin et al designed a continuous circulating fluidised bed system comprising a reactor and a regenerator. 272 Using this system, the alkene-rich C 4 -C 6 fraction was successfully isomerised over ferrierite.…”

Section: Zeolitic Silica-alumina Catalystsmentioning

confidence: 99%

Catalysis in the Upgrading of Fischer–Tropsch Syncrude

2010

Catalysis in the Refining of Fischer-Tropsch Syncrude

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The catalysis of conversion technologies that are found in most commercial Fischer–Tropsch upgrading and refining facilities are discussed. Four main classes of catalysis are considered, namely a) alkene oligomerisation, b) isomerisation and hydroisomerisation of alkanes and alkenes, c) cracking and hydrocracking, and d) hydrotreating. The focus is on catalysis, with aspects such as oxygenates, oxygenate related deactivation, commercial processes and Fischer–Tropsch application specifics being highlighted.

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A CFB unit for skeletal isomerization of linear c4-c6 olefins on ferrierite catalysts

Cited by 6 publications

References 2 publications

Kinetic Modeling of Coke Oxidation of a Ferrierite Catalyst

Kinetic Modeling of Coke Oxidation of a Ferrierite Catalyst

Evolution of Light Hydrocarbons from a Coked Ferrierite Catalyst during Temperature-Programmed Gasification

Catalysis in the Upgrading of Fischer–Tropsch Syncrude

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