Abstract: A method and system for handling viscous liquid crude hydrocarbons is disclosed. The method involves (a) solvent deasphalting at least a portion of an asphaltene-containing liquid crude hydrocarbon feedstock to form an asphaltene fraction and a deasphalted oil (DAO) fraction essentially free of asphaltenes; (b) adjusting the density of the asphaltene fraction to substantially the same density of a carrier for the asphaltene fraction; (c) forming coated asphaltene particles from the asphaltene fraction of step (b); (d) slurrying the coated asphaltene particles with the carrier; and (e) transporting the slurry to a treatment facility or a transportation carrier.

Abstract: Disclosed herein are methods for isolating heavy saturated hydrocarbons from a subsurface shale formation comprising kerogen and an extractible organics component. These methods can be used to provide a bright stock product. The process comprises extracting an extractible organics component from subsurface shale formations comprising kerogen and the extractible organics component in an inorganic matrix and isolating a heavy hydrocarbon fraction comprising saturated beta-carotene. The methods utilize a hydrocarbon solvent to at least partially solubilize the extractible organics component. Among other factors, these processes are based on the discovery that the extractible organics is composed of a heavy hydrocarbon component containing saturated beta-carotene. The saturated beta-carotene product is a valuable commercial product. The presently disclosed processes are more environmentally benign, more economical, and more efficient in producing commercial products and in providing access to kerogen.

Abstract: Provided are multiple correlations for relationships between MI value for a brightstock extract and the distillation cut point temperature used for separation of the vacuum resid that is used to form the brightstock extract. Based on these correlations, a BSE having a desired MI value can be formed based on an adjustment of the distillation cut point temperature. A first correlation establishes a relationship between a fractional weight boiling temperature for a vacuum resid fraction and a distillation cut point temperature for separating the vacuum resid fraction from at least one distillate fraction in a feedstock. A second correlation establishes a relationship between a fractional weight boiling temperature for a brightstock extract derived from the vacuum resid fraction, and the fractional weight boiling temperature for the vacuum resid fraction. A third correlation has been established between the fractional weight boiling temperature for the brightstock extract and a mutagenicity index value.

Abstract: The invention is directed to a process for cleaning bitumen froth by mixing a sufficient amount of naphtha with the bitumen froth to provide a naphtha-to-bitumen ratio within the range of about 4.0 (w/w) to about 10.0 (w/w) and separating substantially dry diluted bitumen from the water and solids. Also provided is a process for cleaning diluted bitumen by mixing a sufficient amount of naphtha with the diluted bitumen to provide a naphtha-to-bitumen ratio equal to or greater than about 1.8 (w/w) and separating marketable fungible raw bitumen from the water and solids.

Abstract: A method and system for performing quantitative fractionation of a hydrocarbon sample is disclosed. The method includes introducing the hydrocarbon sample in a separation system having a first separation column and a second separation column. Separate fraction removal steps are performed for the elution of saturates, aromatic ring classes, sulfides, and polars fractions. The method allows to collect the separated fractions and obtain the material balance information of the hydrocarbon sample. The method further includes performing an analysis on the at least one aromatic ring class fraction to identify and quantify an olefins fraction in the hydrocarbon sample.

Abstract: Methods for preparing solvent-dry, stackable tailings. The methods may include a primary leaching or extraction process that separates most of the bitumen from a material comprising bitumen and produces first solvent-wet tailings. The first solvent-wet tailings are washed with a second solvent that removes the first solvent from the tailings. Second solvent remaining in the tailings is removed to thereby produce solvent-dry, stackable tailings.

Abstract: Systems and processes for producing one or more olefins. A feed containing 90% by weight or more C4 and higher hydrocarbons can be cracked at conditions sufficient to provide an olefinic mixture and an aromatic mixture. The olefinic mixture can comprise 90% by weight or more C1 to C3 hydrocarbons. The aromatic mixture can comprise 90% by weight or more C4 and higher hydrocarbons and one or more aromatics. The aromatic mixture can be contacted with one or more solvents to selectively separate at least a portion of the one or more aromatics therefrom to provide an aromatic-rich mixture and an aromatic-lean mixture. At least a portion of the aromatic-lean mixture can be recycled to the feed prior to cracking.

Abstract: A process oil comprising a 95/5 to 5/95 by weight mixture of: an extract having a DMSO extractable content less than 3 wt % obtained by solvent-extracting an oil obtained by deasphalting a vacuum distillation bottom; and either a mineral oil base having a DMSO extractable content less than 3 wt % which is a raffinate obtained by the solvent refining of a vacuum distillate or a mineral oil base having a DMSO extractable content less than 3 wt % obtained by subjecting a raffinate obtained by the solvent refining of a vacuum distillate to hydrorefining and/or dewaxing. The process oil has a kinematic viscosity at 100° C. of less than 32 mm2/s, % CA of 15 to 30, aniline point of 100° C. or lower, weight change through evaporation of 0.5% or less, and mutagenicity index of less than 1.

Abstract: A solvent deasphalting of crude oil or petroleum heavy fractions and residues is carried out in the presence of a solid adsorbent, such as clay, silica, alumina and activated carbon, which adsorbs the contaminants and permits the solvent and oil fraction to be removed as a separate stream from which the solvent is recovered for recycling; the adsorbent with contaminants and the asphalt bottoms is mixed with aromatic and/or polar solvents to desorb the contaminants and washed as necessary, e.g., with benzene, toluene, xylenes and tetrahydrofuran, to clean adsorbant which is recovered and recycled; the solvent-asphalt mixture is sent to a fractionator for recovery and recycling of the aromatic or polar solvent. The bottoms from the fractionator include the concentrated PNA and contaminants and are further processes as appropriate.

Abstract: A process to prepare a process oil with an aromatic content of more than 50 wt % (according to ASTM D 2007) and a polycyclic aromatics (PCA) less than 3 wt % (according to IP 346) by (a) contacting a feed mixture of a petroleum fraction boiling in the lubricating oil range and an aromatic rich hydrocarbon fraction with a polar solvent in a counter-current liquid-liquid extraction column, wherein the process oil is obtained by removing the polar solvent from the top product and an extract is obtained by removing the polar solvent from the top product and an extract is obtained by removing the polar solvent from the bottom product.

Abstract: An improved process for the recovery of aromatic compounds from a mixture containing aromatic and non-aromatic compounds and method for retrofitting existing equipment for the same is provided. The improved process comprises the steps of recovering aromatic compounds via parallel operation of a hybrid extractive distillation/liquid-liquid extractor operation and variations thereof. Methods of quickly and economically retrofitting existing recovery process equipment for use with the improved aromatics recovery process are also disclosed.

Abstract: An improved process for the recovery of aromatic compounds from a mixture containing aromatic and non-aromatic compounds and method for retrofitting existing equipment for the same is provided. The improved process comprises the steps of recovering aromatic compounds via parallel operation of a hybrid extractive distillation/liquid-liquid extractor operation and variations thereof. Methods of quickly and economically retrofitting existing recovery process equipment for use with the improved aromatic recovery process are also disclosed.

Abstract: A method of refining a petroleum product to remove aromatics and to separate paraffinic oils and waxes is provided. The method involves the utilization of phase equilibria wherein crystallized or solidified waxes, normally present in the petroleum product, are used to remove oils from a liquid solvent phase containing dissolved aromatics present in the unrefined petroleum product. The wax containing the oils is separated from the aromatic-containing solvent and is further processed to separate the waxes and oils. For petroleum products containing little, if any, wax, additional wax may be added and recycled back for further use in removing oils from the petroleum product. The method has particular application in preparing lubricating oils having a high viscosity index, where the presence of aromatics and wax can be detrimental.

Abstract: The processing oil contains polycyclic aromatic hydrocarbon, which is a substance known to be toxic to the human body, in an amount of less than 3 wt. % and an aromatic hydrocarbon in an amount of 25 wt. % or more, and has a kinematic viscosity at 100° C. of 10-30 mm2/s, a density of 0.870-970 g/cm3, and a 5 vol. % recovery temperature of 370-530° C. The processing oil exhibits excellent performance which has conventionally been obtained. The processing oil can be produced by a method in which oil mixture comprising an extract obtained through extraction from mineral oil by use of a polar solvent in an amount of 40-97 vol. % and lubricating base oil in an amount of 3-60 vol. % is subjected to extraction treatment by use of a polar solvent.

Abstract: An improved process for the recovery of aromatic compounds from a mixture containing aromatic and non-aromatic compounds and method for retrofitting existing equipment for the same is provided. The improved process comprises the steps of recovering aromatic compounds via parallel operation of a hybrid extractive distillation/liquid-liquid extractor operation and variations thereof. Methods of quickly and economically retrofitting existing recovery process equipment for use with the improved aromatics recovery process are also disclosed.

Abstract: The improved process and apparatus of the present invention for extracting high purity aromatics from gasoline using a glycol solvent based extraction process decrease liquid-vapor flashing, reduce reflux flow rate, and use heat of enthalpy produces at one point as a source of energy used at another point, decreasing energy consumption while significantly increasing purity and amount of product obtained.

Abstract: A process for reducing the Mutagenicity Index and/or the PCA content of a lubricating oil extract by re-extracting a lubricating oil extract with a second extraction solvent, different from the first extraction solvent, to form a secondary raffinate and a secondary extract mix; separating the secondary raffinate from the secondary extract mix; and separating the secondary raffinate and the secondary extract from said second extraction solvent.

Abstract: The high aromatic oil provided in the present invention is characterized by that a glass transition point is -45 to -20.degree. C. and an aromatic component measured by Clay-Gel method accounts for 55 to 90% by weight and that a polycyclic aromatic compound measured by IP 346 method accounts for less than 3% by weight based on the whole components of hydrocarbons contained in the oil.This high aromatic oil can suitably be used for various rubber compositions such as tires, rubber vibration insulators and fenders, oil extended synthetic rubbers, printing inks and writing inks.

Abstract: A method for producing a process oil is provided in which a napthenic rich feed is enriched with an aromatic extract oil. The enriched feed is then subjected to a solvent extraction thereby providing a process oil.

Abstract: The present invention is directed to an improved selective solvent extraction process wherein a hydrocarbon feed stream containing a mixture of aromatics and non-aromatics is contacted with an aromatics selective solvent in an extraction zone to produce an aromatics rich extract phase and an aromatics lean raffinate phase, water in a carefully controlled amount is added to the recovered extract phase resulting in the separation of the extract phase into a hydrocarbon rich pseudo-raffinate which is recycled to the extraction zone for processing with fresh feed and an increased yield of raffinate of higher quality than is obtained without pseudo-raffinate recycle.

Abstract: The invention relates to a process for separating extractable organic material from a composition comprising organic material intermixed with solids and water. The composition is contacted with a solvent and a dehydrating agent. The dehydrating agent removes water, improves the solvent extraction, and aids in later separation of the solids from the solvent. The process additionally provides a means for removing cyanide compounds from the composition and fixating the metals against leaching.

Abstract: Non-carcinogenic asphalts and asphalt blending stocks are produced from reduced hydrocarbon feedstocks. Such non-carcinogenic products are produced by establishing a functional relationship between mutagenicity index and a physical property correlative of hydrocarbon type for the asphalt or asphalt blending stock and determining a critical physical property level which, when achieved, results in a product having a mutagenicity index of less than about 1.0. Process conditions are established so that a product stream achieving the desired physical property level can be produced. Non-carcinogenic asphalts and asphalt blending stocks are then processed utilizing the conditions so established.

Abstract: A process for improving the performance of heavy oil refining units in a resid hydrotreating unit equipped for resid hydrotreating. The partially refined resid stream issuing from a train of ebullated bed reactor is first separated into high, medium, and low temperature components. The high temperature component is sent through a flash drum and then fractionated by solvent deasphalting in order to provide oil, resin, and asphaltene fractions. Thus, the asphaltene is eliminated before it can foul downstream equipment. This treatment of the heavy oil product has several benefits as compared to treating the vacuum tower bottoms. Among other things, one of these benefits is to debottleneck the resid hydrotreating unit, especially at the atmospheric tower.

Abstract: A refining process uses a two or four stage solvent separator coupled to receive an incoming feedstream of low sulfur resid and a solvent. In the preferred two stage separator, the mixture at the top of the first separator stage is fed to the second stage separator via a heat exchanger. The mixture at the bottom of the first stage separator includes resins and asphaltenes which are fed to a hydrotreater and then, in turn, to a fractionator. The output from the bottom of this fractionator can be fed back to the resid feedstream of the first stage separator for recycled separation. The material at the top of the second stage separator is fed back through the heat exchanger where it helps heat the mixture fed from the top of the first to the second stage separator, this feedback recovers the solvent for reuse in the first stage. The material settling to the bottom of the second stage separator is fed into a catalytic cracker or processed elsewhere.

Abstract: This invention provides for a process for separating extractable organic material from a feed composition comprising an oil-in-water emulsion comprising a continuous aqueous phase, a discontinuous organic liquid phase comprising said extractable organic material, and solids dispersed in said emulsion, the process comprising the steps of:(I) mixing said feed composition with sufficient shear to convert said feed composition to a water-in-oil emulsion; and(II) contacting said water-in-oil emulsion with at least one organic solvent, said organic solvent being capable of forming with said emulsion a system comprising at least two phases and being capable of dissolving at least about ten parts of said extractable organic material per million parts of said organic solvent at the temperature wherein at least about 50% by weight of said solvent boils at atmospheric pressure; forming a system comprising at least two phases, one of said phases being an emulsion phase comprising said emulsion and the other of said phase

Abstract: An improvement has been found in a process for producing Bright Stock from petroleum residuum by propane deasphalting and solvent refining. The extract of solvent refining is cooled to yield an aromatics-lean secondary raffinate which is recycled to propane deasphalting. An improved yield of Bright Stock is achieved over recycling extract to propane deasphalting.

Abstract: A lubricating oil stock is extracted with N-methyl-2-pyrrolidone to yield a primary raffinate useful as a high VI lubricating base oil and a primary extract. The primary extract is mixed with antisolvent and chilled to yield a secondary raffinate. This secondary raffinate is sufficiently reduced in aromatics that it is solvent extracted to yield medium to high VI lubricating base oil.

Abstract: Non-carcinogenic bright stock extracts and/or deasphalted oils are produced from reduced hydrocarbon feedstocks. Such non-carcinogenic products are produced by establishing a functional relationship between mutagenicity index and a physical property correlative of hydrocarbon type for the bright stock extract or deasphalted oil and determining a critical physical property level which, when achieved, results in a product having a mutagenicity index of less than about 1.0. Process conditions are established so that a product stream achieving the desired physical property level can be produced. Non-carcinogenic bright stock extracts and/or deasphalted oils are then processed utilizing the conditions so established. A bright stock extract and a deasphalted oil substantilly free from mutagenic activity, as well as processes for their production are also provided herein.

Abstract: This invention provides for a process for separating extractable organic material from a feed composition comprising said extractable organic material intermixed with solids and water, the process comprising the steps of: (A) contacting said feed composition with a first organic solvent, said first organic solvent being capable of dissolving at least about ten parts of said extractable organic material per million parts of said first organic solvent at the temperature wherein at least about 50% by weight of said first organic solvent boils at atmospheric pressure; dissolving at least part of said extractable organic material in said first organic solvent to form a first solution; and separating at least part of said first solution from said feed composition to provide an intermediate composition, part of said first organic solvent remaining intermixed with said intermediate composition; and (B) contacting said intermediate composition with a volatile organic solvent, said voltile organic solvent being capable

Abstract: A process is disclosed for separating an organic material from a composition comprising said organic material intermixed with particulate solids, the process comprising advancing a light hydrocarbon fluid through said particulate solids at an effective rate to drive said organic material from said particulate solids.

Abstract: A process is disclosed for separating an organic material from a composition comprising said organic material intermixed with particulate solids, the process comprising advancing a light hydrocarbon fluid through said particulate solids at an effective rate to drive at least some of said organic material from said particulate solids, adding water to said composition containing particulate solids and residual organic material to produce a second composition, and adding an oxidizing agent to said second composition in an amount sufficient to remove substantially all of the residual organic material.

Abstract: A carbonaceous material such as coal is conditioned by contact with a supercritical fluid prior to physical beneficiation. The solid feed material is contacted with an organic supercritical fluid such as cyclohexane or methanol at temperatures slightly above the critical temperature and pressures of 1 to 4 times the critical pressure. A minor solute fraction is extracted into critical phase and separated from the solid residuum. The residuum is then processed by physical separation such as by froth flotation or specific gravity separation to recover a substantial fraction thereof with reduced ash content. The solute in supercritical phase can be released by pressure reduction and recombined with the low-ash, carbonaceous material.

Abstract: A method of fractionating a mixture containing high boiling carbonaceous material and normally solid mineral matter includes processing with a plurality of different supercritical solvents. The mixture is treated with a first solvent of high critical temperature and solvent capacity to extract a large fraction as solute. The solute is released as liquid from solvent and successively treated with other supercritical solvents of different critical values to extract fractions of differing properties. Fractionation can be supplemented by solute reflux over a temperature gradient, pressure let down in steps and extractions at varying temperature and pressure values.

Abstract: Heavy oil derived from coal is diluted with organic solvent to a content of less than 10 weight percent of toluene-insoluble material. The mixture is then mixed with a non-aromatic solvent in a ratio of 1:3 to 5:1. With slow stirring of the heavy phase at a temperature of between 50.degree. and 200.degree. C., this mixture is separated into a pumpable TI-poor and a pumpable TI-rich fraction under the action of gravity, with a settling-surface load of up to 1 metric ton/m.sup.2 hour. No .beta.-resins are precipitated from these fluid fractions. No tacky, rubber-like sediment is formed from the TI-rich fraction. The fractions are distillatively separated from the solvents, which can be reused. The TI-poor fraction can be used, for example, as a carbon-black oil component or can be processed further to an impregnating agent for carbon shapes. Binders for carbon shapes or cokes are obtained from the TI-rich fraction.

Abstract: A process for the simultaneous separation of aromatics and non-aromatics from a heavy hydrocarbon stream and a light hydrocarbon stream in which process:(a) aromatics are extracted in a first extractor from the heavy hydrocarbon stream with the aid of a selective solvent which has a higher boiling point than that of said light hydrocarbon stream,(b) selective solvent is removed from the raffinate obtained from said first extractor, to yield heavy non-aromatics(c) aromatics are extracted from the light hydrocarbon stream in a second extractor with the aid of the extract phase obtained from the first extractor,(d) selective solvent is removed from the raffinate obtained from said second extractor to yield heavy aromatics and light non-aromatics(e) the extract phase from the second extractor is subjected to extractive distillation,(f) the bottom fraction of the extractive distillation is separated by distillation into light aromatics and selective solvent, and(g) the selective solvent obtained in step (f) is at

Abstract: A process for producing additional liquid products from a heavy hydrocarbon material by vis-breaking of a separated asphaltene-containing fraction under controlled conditions of temperature and pressure. The asphaltene-containing fraction is obtained by contacting the heavy hydrocarbon material with a first solvent under elevated temperature and pressure conditions to separate the asphaltenes as a heavy phase from the remainder of the heavy hydrocarbon material. The products of the vis-breaking operation comprise distillable and substantially nondistillable liquid products in association with a residue including organometallic compounds. The distillable and substantially nondistillable liquid products then are separated from the residue. The distillable products can be separated by distillation. The nondistillable products are separated from the residue employing a second solvent maintained under elevated temperature and pressure conditions and then recovered as a liquid phase product.

Abstract: A process for increasing the fuel yield of coal liquefaction products by extracting the asphaltenes, resins and aromatic compounds from said coal liquefaction products. This is accomplished by contacting said coal liquefaction products with a halogenated aliphatic solvent to form two phases, one containing tar and the other containing said solvent and the remainder of said coal liquefaction products, separating said phases from each other and treating said tar phase with a second solvent to recover asphaltenes, resins and/or aromatics in said tar phase. The resulting asphaltenes, resins and/or aromatics are suitable for upgrading to produce additional synthetic fuel.