Standard Oil Company (indiana)

Amoco Corporation

David F Tatterson

John M Forgac

Ronald Coates

Thomas M O'Grady

Lewis E Grimes

Albert L Hensley, Jr

Gary P Hagen

George A Huff

Cecelia A Radlowski

James L Taylor

Iacovos A Vasalos

Robert L Mehlberg

Ken K Robinson

William D Ford

Robert H Walker

Paul A Willems

James S Meyer

A catalyzed, continuous vapor phase process to convert a C.sub.2 or higher alcohol and, optionally, one or more C.sub.1 or higher alcohols, for example methanol and ethanol, to a mixture containing at least one higher molecular weight alcohol, for example, isobutanol, over a catalyst which is essentially magnesium oxide. The process also may have a lower aldehyde and/or ketone in the feed.

Catalyzed vapor phase process for making alcohols

A method for stabilizing oil is provided. An oil fraction having hydrocarbons with an initial boiling point of about 200.degree. F. to about 1050.degree. F. is hydrotreated to reduce the nitrogen content of the oil fraction to be stabilized. Subsequently, condensed aromatic compounds are selectively extracted from the hydrotreated oil fraction to yield a stable oil fraction.

Oil stabilization

A method for converting methane to higher molecular weight hydrocarbons wherein hot oxidative coupling reactor effluent is briefly contacted with a C.sub.2 to C.sub.20 alkane quench material to remove part of the heat contained in the raw reactor effluent, and is then further quenched by thermal quenching means to achieve a temperature which discourages retrograde reactions.

Oxidative coupling process for converting methane and/or natural gas to

A process is provided to produce and stabilize shale oil. In the process, raw oil shale is retorted with heat carrier material to liberate an effluent product stream comprising hydrocarbons and entrained particulates of oil shale dust. In order to minimize polymerization of the product stream and enhance agglomeration of the shale dust, the product stream is stabilized with a hydrogen donor quench upon exiting the retort. The quenched stream is subsequently dedusted and upgraded.

Shale oil stabilization with a hydrogen donor quench

A process is provided to produce and stabilize shale oil. In the process, raw oil shale is retorted with heat carrier material to liberate an effluent product stream comprising hydrocarbons and entrained particulates of oil shale dust. In order to minimize polymerization of the product stream and agglomerate the shale dust, the product stream is stabilized with a hydrogen donor quench in the presence of a hydrogen transfer catalyst upon exiting the retort. The quenched stream is subsequently purged of catalyst, dedusted, and upgraded.

Shale oil stabilization with a hydrogen donor quench and a hydrogen

A method is disclosed for recovering liquids and gases by a rapid hydropyrolysis of carbonaceous solids which comprises subjecting the carbonaceous material in a stream of carrier gas to a first pressure and a first temperature below the decomposition temperature of the carbonaceous material; reducing substantially in a single step the pressure on the stream of carbonaceous material from the first pressure to a second pressure, the ratio of the first pressure to the second pressure being at least 1.6, thereby accelerating the carrier gas in the stream of carbonaceous material; permitting the accelerated stream of carbonaceous material to expand as a free jet and mixing hot gas with the accelerated and expanded stream of carbonaceous material to raise the temperature of the carbonaceous material by heat exchange with the hot gas, to a second temperature of at least the aforesaid decomposition temperature, thereby initiating decomposition of the carbonaceous material; and reducing the temperature of the reaction mixture to below said decomposition temperature, with the total time for heating the carbonaceous material from the first temperature to the second temperature, decomposing the carbonaceous material and cooling the reaction mixture to below said decomposition temperature being from about 1 millisecond to about 10 seconds.

Rapid hydropyrolysis of carbonaceous solids

A process for (i) fluid catalytic cracking in a cracking zone of residuum and other heavy oils comprising gas oil, petroleum residue, reduced and whole crudes, and shale oils with high metals content, (ii) wherein the coke deposits on the used cracking catalyst are reduced in amount by regeneration and wherein (iii) contaminant metals comprising nickel, vanadium, copper and iron deposited on the used cracking catalyst are deactivated in sufficient amount to reduce hydrogen and coke formation during the cracking process whereby the said catalyst is suitable for re-use wherein (A) the catalyst particles are contacted with fresh feed and associated recycle feed, and wherein (B) the feed is cracked in a cracking zone, wherein (C) the used catalyst particles are subjected to alternate exposures of up to 30 minutes in duration of conditions comprising (a) an oxidizing zone at a temperature of above 900.degree. F. wherein molecular oxygen in flue gas emitted from the oxidizing zone is over 0.1 volume percent, and (b) a reducing zone at a temperature within the range of from about 900.degree. F. to about 1450.degree. F., wherein the reducing atmosphere is a material selected from the group consisting of hydrogen, hydrocarbons, carbon monoxide, and mixtures thereof and is present in a concentration of from about 4 to 100 volume percent, and wherein (D) the regenerated catalyst can be returned to the cracking zone.

Fluid catalytic cracking of heavy petroleum fractions

A process for fluid catalytic cracking of residuum and other heavy oils comprising gas oil, petroleum residue, reduced and whole crudes and shale oil with high metals contents wherein contaminant metals comprising nickel, vanadium, copper and iron are deactivated, organic sulfur compounds deposited on the cracking catalyst are removed, wherein the said contaminant metals are deactivated by contact with a high temperature reducing atmosphere comprising carbon monoxide in a range of from about 4 to about 14 volume percent, the temperature being at least 900.degree. F. and preferably greater than 1200.degree. F., wherein the catalyst is modified with at least one inorganic sulfur oxide absorbent which reacts with sulfur oxides under regeneration conditions to form non-volatile inorganic sulfur compounds, the said sulfur oxide absorbent being present in sufficient amount to effect said reduction of said sulfur oxides.

Growing community of inventors

Downers Grove, IL, United States of America

David F Tatterson