Phillips Petroleum Company

Dean P Montgomery

James W Gall

Ed D Davis

John W Myers

In a crude oil refining apparatus, heavy cycle oil from the catalytic cracking unit employed in the crude oil refining apparatus is recycled to a hydrofining process. Such recycling improves the value of the product mix obtained from the crude oil refining apparatus with respect to an apparatus in which the heavy cycle oil withdrawn from the catalytic cracking units is recycled to the catalytic cracking units.

Crude oil refining apparatus

In a crude oil refining process, heavy cycle oil from the catalytic cracking unit employed in the crude oil refining process is recycled to a hydrofining process. Such recycling improves the value of the product mix obtained from the crude oil refining process with respect to a process in which the heavy cycle oil withdrawn from the catalytic cracking units is recycled to the catalytic cracking units.

Crude oil refining

In a normally endothermic naphtha reformer reactor, using a fixed bed of particulate catalyst, to determine if catalyst by-passing is occurring, the feed rate to the reactor is decreased, e.g., by such as about 30 percent, to a rate found previously still to produce an endothermic reaction. If the reactor outlet temperature now exceeds the reactor inlet temperature, the reaction is exothermic, and catalyst by-passing is occurring.

Detection of catalyst by-passing in fixed bed naphtha reformer

Prior to subjecting a butene-1 containing stream isomerization to produce butene-2 in the presence of a catalyst, e.g., a palladium catalyst, the feedstream is subjected to pretreatment in the presence of a contact mass adapted to remove under pretreatment conditions from the feedstream impurities which adversely affect the catalyst, e.g., sulfur and arsenic.

Pretreatment of butene-1 in isomerization of it to butene-2

Aliphatic monoolefins which can be normal or branched are isomerized at temperatures in the approximate range 500.degree.-1200.degree. F. in presence of a high surface area activated alumina containing a relatively low amount of sodium oxide (Na.sub.2 O) to form 1-olefin. Generally, from about 0.13 to about 0.39 milliequivalents of Na.sub.2 O per gram of the activated alumina containing the Na.sub.2 O, supplied by such sodium compounds as are disclosed, the activated alumina having a large surface area, i.e., about 300-400 m.sup.2 per gram, is used as a catalyst for the isomerization of, say, isomeric n-butenes. Generally, the olefin treated will have from 4 to about 20 carbon atoms per molecule.

Olefin double bond isomerization

A noble metal hydrogenation catalyst suited for removal of acetylene by hydrogenating the same selectively as when it is in the presence of ethylene from which it is to be removed, e.g., palladium, which has been poisoned by arsenic is reactivated by purging the same with an arsenic-free gas, e.g., an arsenic-free ethylene containing acetylene together with hydrogen, in one embodiment at an elevated temperature, until substantial acetylene removal is occurring as one indication of restoration of activity and selectivity for removal of acetylene. The catalyst can then be employed for the selective removal of acetylene as from a gas containing it and ethylene.

Reactivation of arsenic-poisoned noble metal catalyst for removal of

A magnesium oxide-containing catalyst which has been used to isomerize butene-2 to butene-1 is regenerated at a localized bed temperature to not exceed about 1000.degree. F., preferably not to exceed about 900.degree. F., by steps involving purging the catalyst with an inert gas, then admixing with said gas oxygen or oxygen-containing gas to produce a final mixture to contain not more than about 0.5 volume percent O.sub.2, and passing said mixture through the catalyst, controlling flow of the mixture to maintain the catalyst at a localized temperature not exceeding substantially about 1000.degree. F., preferably not exceeding about 900.degree. F., increasing the O.sub.2 content of the mixture gradually, but not sufficiently to substantially exceed said temperature of about 1000.degree. F., preferably 900.degree. F., continuing to pass said mixture through the catalyst until substantially no more carbon oxides are detected in the gas exiting the catalyst, arresting flow of oxygen to the catalyst, continuing to pass said inert gas through the catalyst until substantially all O.sub.2 has been purged therefrom, then purging said catalyst to prepare it for isomerization use.

Regeneration of isomerization catalysts containing magnesium oxide

A process for the selective hydrogenation of acetylene present in acetylene-rich gases which comprises carrying out the hydrogenation in the presence of a liquid phase inert hydrocarbon reaction medium and a metal hydrogenation catalyst.

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Bartlesville, OK, United States of America

Dean P Montgomery