The gas-liquid contacting effect on the operation of small scale upflow hydrotreaters

Bellos, GD; Gotsis, KP; Papayannakos, NG

dc.contributor.author	Bellos, GD	en
dc.contributor.author	Gotsis, KP	en
dc.contributor.author	Papayannakos, NG	en
dc.date.accessioned	2014-03-01T01:27:25Z
dc.date.available	2014-03-01T01:27:25Z
dc.date.issued	2007	en
dc.identifier.issn	0920-5861	en
dc.identifier.uri	https://dspace.lib.ntua.gr/xmlui/handle/123456789/18441
dc.subject	Dispersion	en
dc.subject	Hydrodesulfurization	en
dc.subject	Mass transfer	en
dc.subject	Multiphase reactors	en
dc.subject	Packed bed	en
dc.subject	Scale-up	en
dc.subject.classification	Chemistry, Applied	en
dc.subject.classification	Chemistry, Physical	en
dc.subject.classification	Engineering, Chemical	en
dc.subject.other	Catalyst activity	en
dc.subject.other	Dispersions	en
dc.subject.other	Hydrodesulfurization	en
dc.subject.other	Mass transfer	en
dc.subject.other	Packed beds	en
dc.subject.other	Gas-liquid contacting effects	en
dc.subject.other	Multiphase reactors	en
dc.subject.other	Upflow mdoes	en
dc.subject.other	Flow visualization	en
dc.title	The gas-liquid contacting effect on the operation of small scale upflow hydrotreaters	en
heal.type	journalArticle	en
heal.identifier.primary	10.1016/j.cattod.2007.05.004	en
heal.identifier.secondary	http://dx.doi.org/10.1016/j.cattod.2007.05.004	en
heal.language	English	en
heal.publicationDate	2007	en
heal.abstract	The effect of reactor geometry and bed dilution on the extent of gas oil hydrodesulfurization was tested by conducting hydrodesulfurization experiments in two laboratory reactors of different scale with non-diluted and diluted beds in ascending flow. The superficial gas and liquid velocities and the catalyst bed height were kept constant while the main difference between the two reactor scales was the reactor diameter. The diluted bed of the mini-reactor showed the best performance and its results were identical in upflow and downflow mode. The differences between the performance of the mini- and the bench-scale reactor operating in upflow mode have been investigated. Reactor performance simulation was attempted by a mathematical model that takes into account axial dispersion of the liquid phase and gas-liquid mass transfer. Bench-scale reactor operation was characterized by lower mass transfer rates than the corresponding mini-scale one. Combining model predictions and mock up operation it is concluded that the stronger mass transfer resistances calculated for the bench-scale reactor are associated with poorer gas distribution through the catalyst bed. Reduction of the bed diameter results in better gas-liquid contact by forcing the gas bubbles to distribute more effectively into the liquid phase. (C) 2007 Elsevier B.V. All rights reserved.	en
heal.publisher	ELSEVIER SCIENCE BV	en
heal.journalName	Catalysis Today	en
dc.identifier.doi	10.1016/j.cattod.2007.05.004	en
dc.identifier.isi	ISI:000249653300011	en
dc.identifier.volume	127	en
dc.identifier.issue	1-4	en
dc.identifier.spage	103	en
dc.identifier.epage	112	en