Gulf Research & Development Company

Robert D Christman

Stephen J Yanik

John A Paraskos

Jordan S Lasher

William S Bonnell

Joel D McKinney

Kirk J Metzger

Thomas C Readal

Geoffrey R Wilson

Matt Christman

Golf putter head

A process and apparatus for the hydrodesulfurization of residual oil in a plurality of catalyst zones in series with the upstream reactor being removed periodically for a catalyst change. When an upstream zone is taken off-stream for a catalyst change, the fresh feed oil is passed to a succeeding downstream zone so that the downstream catalyst zone is upstaged to the status of an upstream catalyst zone. When a zone is returned to service after a catalyst change, it enters the process as a downstream reactor in the series.

Hydrodesulfurization apparatus with upstaged reactor zones

A process for the hydrodesulfurization of residual oil in a plurality of catalyst zones in series with the upstream reactor being removed periodically for a catalyst change. When an upstream zone is taken off-stream for a catalyst change, the fresh feed oil is passed to a succeeding downstream zone so that the downstream catalyst zone is upstaged to the status of an upstream catalyst zone. When a zone is returned to service after a catalyst change, it enters the process as a downstream reactor in the series.

Hydrodesulfurization process with upstaged reactor zones

A multiple stage process for hydrodesulfurizing a residual oil comprising passing the oil downwardly through a plurality of stages in series with an interstage flashing step. A portion of the fresh feed oil continuously or intermittently by-passes the first stage and flows directly to the second stage.

Multiple stage hydrodesulfurization process including partial feed oil

A multiple stage process for hydrodesulfurizing a residual oil while passing the oil downwardly through a plurality of stages in series with an interstage flashing step. After the catalyst in the downstream stage is deactivated by coke deposition, fresh feed oil is passed directly to the deactivated catalyst to obtain an extended life in the downstream catalyst.

Multiple stage hydrodesulfurization process with extended downstream

A process is described for fixed bed hydrodesulfurizing a non-asphaltic oil feed blend for a zeolitic FCC riser cracking system in which cracking occurs at a space velocity sufficiently high to prevent formation of a catalyst bed. It is shown that sulfur dioxide emissions from the zeolite catalyst regenerator associated with the riser are reduced to a lower extent than total sulfur removal from the feed oil. This indicates uneven sulfur removal in the hydrodesulfurization step whereby a smaller portion of sulfur is removed from the heavy portion of the feed from which the coke is derived than from the lighter portion of the feed. The present invention demonstrates a synergistic effect upon sulfur removal from the heavy portion of the feed by widening the boiling range of the feed and this synergistic effect is converted to practical advantage by reducing the amount of hydrodesulfurization catalyst in proportion to said synergistic effect, thereby keeping hydrocracking to a specified low level. The boiling range of the feed is widened by adding to the higher boiling portion of the feed a portion of a second stream to lower the average boiling point of the hydrodesulfurization feed whereby the sulfur content of the remaining portion of the second stream is sufficiently low that the second stream does not require desulfurization. The further discovery is demonstrated herein that the ratio of gasoline to total conversion during the subsequent riser cracking step of the hydrodesulfurizer effluent is enhanced by reducing the amount of the hydrodesulfurization catalyst as permitted by said synergistic effect.

Hydrodesulfurization process involving blending high boiling streams

Aromatic hydrocarbons are hydrogenated in the presence of hydrogen and a catalyst composite comprising at least two hydrogenating agents and an alumina support having a controlled bayerite concentration, average pore radius, and pore volume distribution and further having been calcined at a temperature in the range of 800.degree. - 1600.degree. F. (427.degree. - 871.degree. C.) prior to impregnation of the hydrogenating agent.

Hydrogenation of aromatics

An improved method for sulfiding a petroleum distillate desulfurization catalyst which comprises sulfiding the catalyst composite with a sulfur-containing petroleum distillate at a temperature in excess of 660.degree.F. and thereafter conducting the desulfurization process at a temperature less than 650.degree.F.

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Pittsburgh, PA, United States of America

Robert D Christman