Dispersion during bubble-train flow in capillaries

Thulasidas, T.C.; Abraham, Martín; Cerro, Ramón L.

doi:10.1016/s0009-2509(98)00240-1

Cited by 135 publications

(86 citation statements)

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“…In case where the reaction selectivity is important, this can result in signiÿcantly lower selectivities for a trickle-bed reactor in comparison to a monolithic reactor (Nijhuis, Kreutzer, Romijn, Kapteijn, & Moulijn, 2001). The residence time distribution in a monolithic reactor is narrow due to the Taylor-ow patters, in which the gas bubbles work as pistons separating the liquid slugs preventing backmixing (Thulasidas, Abraham, & Cerro, 1999).…”

Section: Comparisonmentioning

confidence: 99%

Modeling of monolithic and trickle-bed reactors for the hydrogenation of styrene

Nijhuis

Dautzenberg²,

Moulijn

2003

Chemical Engineering Science

122

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A kinetic study into the styrene hydrogenation over a palladium on alumina catalyst has been made. Styrene was used as a model component for pyrolysis gasoline. A kinetic rate expression has been derived and the inhibiting e ect of sulfur components has been included. Using this kinetics and mass-transfer models compiled from literature, the performance of two types of reactors for the styrene (pyrolysis gasoline) hydrogenation has been evaluated. A structured reactor such as a monolith has large advantages over a conventional trickle-bed reactor. For the monolithic reactor a more than 3 times higher volumetric productivity is obtained with much less catalyst. The modeling results indicate that deactivation by gum formation should be signiÿcantly less due to much better hydrogen mass transfer in the reactor. ?

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Section: Comparisonmentioning

confidence: 99%

Modeling of monolithic and trickle-bed reactors for the hydrogenation of styrene

Nijhuis

Dautzenberg²,

Moulijn

2003

Chemical Engineering Science

122

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“…The bubble length is usually several times of the channel diameter. The liquid slugs are separated by the bubbles and the two adjacent liquid slugs are connected only through a thin film (if present) between the bubble and the channel wall, which indicates a significant reduction in axial mixing [11]. The recirculation in the liquid slugs improves radial mixing [12,13].…”

Section: Introductionmentioning

confidence: 99%

Formation characteristics of Taylor bubbles in a microchannel with a converging shape mixing junction

Dang

Yue

Chen

et al. 2013

Chemical Engineering Journal

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“…1 The RTD can be determined from tracer injection experiments [2][3][4][5][6][7] and has been characterized for different reactors like microchannel reactors, 8 foam packed trickle flow reactors, 9 annular centrifugal extractors, 10 and the rotating disc reactor. 11 In this article, we present a single-phase model for a rotor-stator spinning disc reactor (SDR), which is based on residence time distribution measurements.…”

Section: Introductionmentioning

confidence: 99%

Residence time distribution in a single‐phase rotor–stator spinning disk reactor

et al. 2013

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A reactor model for the single-phase rotor-stator spinning disc reactor based on residence time distribution measurements is described. For the experimental validation of the model, the axial clearance between the rotor and both stators is varied from 1.0 3 10 23 to 3.0 3 10 23 m, the rotational disc speed is varied from 50 to 2000 RPM, and the volumetric flow rate is varied from 7.5 3 10 26 to 22.5 3 10 26 m 3 s 21 . Tracer injection experiments show that the residence time distribution can be described by a plug flow model in combination with 2-3 ideally stirred tanks-in-series. The resulting reactor model is explained with the effect of turbulence, the formation of Von K arm an and B€ odewadt boundary layers, and the effect of the volumetric flow rate.

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Dispersion during bubble-train flow in capillaries

Cited by 135 publications

References 0 publications

Modeling of monolithic and trickle-bed reactors for the hydrogenation of styrene

Modeling of monolithic and trickle-bed reactors for the hydrogenation of styrene

Formation characteristics of Taylor bubbles in a microchannel with a converging shape mixing junction

Residence time distribution in a single‐phase rotor–stator spinning disk reactor

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