Abstract: A fluid coking-gasification process for converting heavy hydrocarbonaceous chargestocks to lower boiling products in which an inorganic metal composition is used to mitigate slagging in the gasifier, wherein the metal is selected from the alkaline-earths, the rare earths, and zirconium. The inorganic metal composition is added either directly into the gasifier or it is mixed with the coke passing from the heating zone to the gasification zone.

Abstract: An improved spiral wound element for separations is disclosed wherein the improvement comprises using as the feed/retentate space one or more layers of a material having an open cross-sectional area in the range 30 to 70% and as the permeate spacer material at least three layers of material two of which are fine and have an open cross-sectional area of about 10 to 50% surrounding a coarse layer having an open cross-sectional area of about 50 to 90%.

Abstract: A multi-element housing is disclosed for the containment of multiple membrane separation elements in parallel. The multi-element housing is characterized in that the elements are grouped in parallel with a feed/retentate zone, defined by a space enclosed by two tube sheets arranged at the same end of the elements. The central mandrels of the elements pass through the feed/retentate zone space defined by the two tube sheets and empty permeate outside the defined space into a permeate collection zone from which it is removed, while the tube sheet directly attached to the element is in open relationship to the interior of the membrane element and retentate accumulates in the space between the top tube sheet and the bottom tube sheet from which it is removed.

Abstract: Hydrocarbon solvents used or the dewaxing and/or deasphalting of oils can be recovered by the selective permeation of said solvents through an interfacially polymerized membrane under reverse osmosis conditions.

Abstract: Raffinate yield from solvent extraction is improved when the extract phase recovered from the solvent extraction process is subjected to a membrane separation step wherein a saturates/1-ring aromatics rich retentate is produced and a 2+ ring aromatics rich permeate are produced and the saturates/1-ring aromatic rich retentate phase is recycled to the solvent extraction process.

Abstract: Non-normal, branched paraffins (isoparaffins) are separated from hydrocarbon feeds comprising mixtures of isoparaffins and normal paraffins by the procedure involving the steps of contacting the hydrocarbon feed with one face of a non-selective, microporous partition barrier membrane while simultaneously contacting the opposite face of said membrane, preferably in countercurrent flow, with a polar solvent. The isoparaffins in the feed selectively permeate across the porous partition barrier membrane in response to the polar solvent to the solvent side of the membrane whereby a permeate enriched in isoparaffins and a retentate of decreased isoparaffin content as compared to the feed are obtained.

Abstract: Olefins are selectively separated from hydrocarbon feeds containing mixtures of olefins and paraffins by contacting said hydrocarbon feed mixture with one side of a micro-porous, non-selective partition barrier membrane while simultaneously passing, preferably in countercurrent flow, along the opposite side of said membrane a polar solvent. The olefin preferentially passes through said micro-porous non selective partition barrier in response to the polar solvent yielding a permeate enriched in olefin and a retentate enriched in paraffin as compared to the original feed stream.

Abstract: Naphthenic hydrocarbons are separated from aliphatic rich hydrocarbon feeds comprising mixtures of naphthenes with paraffinic hydrocarbons by a membrane extraction process whereby the hydrocarbon feed is contacted with one face of a porous, non-selective partition barrier membrane while simultaneously contacting the other side of said membrane with a polar solvent such as ethylenediamine. The naphthenic hydrocarbon preferentially migrates through the porous membrane partition barrier in response to the polar solvent present on the permeate side of the barrier.

Abstract: The yield, raffinate product quality, and throughput of the selective solvent extraction of hydrocarbon feeds is improved by subjecting the hydrocarbon feeds from which aromatic hydrocarbons are to be selectively solvent extracted to a membrane separation process which selectively permeates aromatics through the membranes to produce a permeate rich in aromatics and a retentate rich in saturates and 1-ring aromatics and subjecting this retentate to the selective solvent extraction process.

Abstract: A fluid coking-gasification process for converting heavy hydrocarbonaceous chargestocks to lower boiling products in which calcium silicate is used to mitigate bogging, slagging, or both. The calcium silicate can be added directly to the heavy hydrocarbonaceous chargestock to mitigate both bogging and slagging or it can be added directly into the gasifier to mitigate slagging.

Abstract: Multi-ring aromatic hydrocarbons and/or toxins are selectively solvent extracted from hydocarbon feed streams by the process comprising contacting the aromatics and/or toxins containing hydrocarbon stream with one side of a porous, non-selective partition barrier membrane while simultaneously contacting the other side of said membrane with an aromatics selective extraction solvent whereby the multi-ring aromatic hydrocarbons and/or toxins selectively migrate through the porous partition barrier membrane in response to the selective solvent. A preferred extraction solvent is ethylenediamine. The permeate comprising multi-ring aromatics in solvent can be subjected to a membrane separation process to separate the extraction solvent from the aromatics.

Abstract: A fluid coking-gasification process for converting heavy hydrocarbonaceous chargestocks to lower boiling products in which a zeolitic material is use to mitigate slagging in the gasifier, especially when the zeolite material is spent catalytic cracking catalyst. The zeolite material is added either directly into the gasifier on it is mixed with the coke passing from the heating zone to the gasification zone.