Abstract: A process for upgrading a hydrocarbon feed includes passing the hydrocarbon feed and an aromatic bottoms stream to an FCC unit including an FCC reactor and a catalyst regenerator. The hydrocarbon feed is hydrogen-rich having at least 12 wt. % hydrogen, and the aromatic bottoms stream is a bottoms stream produced from an aromatics recovery complex for processing reformate from naphtha reforming. The hydrocarbon feed and aromatic bottoms stream are cracked over the FCC catalysts to produce an effluent and spent FCC catalysts having coke deposits. The spent FCC catalyst is regenerated through combustion of the coke deposits. The hydrogen-rich hydrocarbon feed does not produce enough coke to satisfy the heat demand of the FCC reactor. Cracking the aromatic bottoms stream increases the amount of coke so that combustion of the additional coke during regeneration produces additional heat to satisfy the heat demand of the FCC reactor.

Abstract: Methods for processing a hydrocarbonaceous feedstock flows are provided. In one embodiment, the method includes providing two or more hydroprocessing stages disposed in sequence, each hydroprocessing stage having a hydroprocessing reaction zone with a hydrogen requirement and each stage in fluid communication with the preceding stage. The hydrocarbonaceous feedstock flow may be separated into portions of fresh feed for each hydroprocessing stage, and the first portion of fresh feed to the first hydroprocessing stage is heated. The heated first portion of fresh feed may be supplied with hydrogen from the hydrogen source in an amount satisfying substantially all of the hydrogen requirements of the hydroprocessing stages to a first hydroprocessing zone. The unheated second portion of fresh feed is injected counter current to the process flow as quench at one or more locations in one or more of the reaction zones.

Abstract: The present invention is an improved process for stripping HPNA's from hydroprocessed streams in a fractionation column having a split shell configuration. Only one vapor stripping feed is required to the split shell of the fractionation column. The resulting reduction in steam requirement provides a superior fractionation in the column.

Abstract: The present invention is an improved process for stripping HPNA's from hydroprocessed streams in a fractionation column having a split shell configuration. Only one vapor stripping feed is required to the split shell of the fractionation column. The resulting reduction in steam requirement provides a superior fractionation in the column.

Abstract: A contactor/separator is formed from a vessel; an inlet for receiving a vapor/liquid mixture; an inlet for receiving a superheated vapor; a hub located within the vessel, the hub including a plurality of vanes for imparting a centrifugal motion to the vapor/liquid mixture or the superheated vapor; an outlet in a bottom of the vessel for removing liquid; and an outlet for removing vapor from the vessel. A method is also provided for heating and separating liquid and vapor from a hydrocarbon feedstock comprising introducing a hydrocarbon feedstock into a contactor/separator: introducing a superheated vapor into the contactor/separator such that it contacts and vaporizes a portion of the feedstock within the contactor/separator; separating unvaporized feedstock from vaporized feedstock in the contactor/separator; removing the vaporized feedstock and the superheated vapor through a first outlet; and removing the unvaporized feedstock through a second outlet.

Abstract: A method and apparatus for the cracking of a petroleum oil feedstock to produce a desulfurized full-range gasoline product. The petroleum oil feedstock is contacted with a base cracking catalyst and an FCC additive in an FCC unit, wherein the catalyst includes a stable Y-type zeolite and a rare-earth metal oxide and the additive includes a shape selective zeolite. The catalyst, additive and petroleum oil feedstock can be contacted in a down-flow or riser fluid catalytic cracking unit, that can also include a regeneration zone, a separation zone, and a stripping zone. The FCC unit includes an integrated control and monitoring system that monitors at least one parameter selected from FCC operating parameters, feed rate, feedstock properties, and product stream properties, and adjusts at least one parameter in response to the measured parameter to increase production of desulfurized products.

Abstract: The present invention provides a process for treating a hydrocarbon feed gas stream containing acid gases (CO2, H2S and mercaptans) by contacting the feed gas stream in a multi-section caustic tower, the bottom sections employing a recirculating caustic solution to remove the CO2 and H2S down to low single digits parts per million concentration and the upper sections employing a stronger caustic solution on a once-through basis to produce a mercaptans depleted gas stream.

Abstract: A process for the recovery and purification of a contaminated hydrocarbons, wherein the contamination includes metals, finely divided solids and non-distillable components. The process further includes hydroprocessing the oil to remove deleterious compounds, to produce high quality reusable lubricants, solvents and fuels and to improve the quality of water byproduct.

Abstract: Process for the work-up of naphtha, wherein a) naphtha or a stream produced from naphtha in a pretreatment step is separated in a membrane unit into a stream A which is depleted in aromatics and a stream B which is enriched in aromatics, with the aromatics concentration in stream A being from 2 to 12% by weight (step a), b) at least part of the substream A is fed to a steam cracker (step b), c) at least part of the substream B is fed to a unit in which it is separated by means of a thermal process into a stream C which has a lower aromatics content than stream B or a plurality of streams C?, C?, C?? . . . which each have lower aromatics contents than stream B and a stream D which has a higher aromatics content than stream B or a plurality of streams D?, D?, D?? . . .

Abstract: For producing basic oils and in particular very high quality oils, i.e. oils possessing a high viscosity index (VI), a low aromatics content, good UV stability and a low pour point, from oil cuts having an initial boiling point higher than 340° C., possibly with simultaneous production of middle distillates (in particular gasoils and kerosene) of very high quality, i.e. having a low aromatics content and a low pour point, the invention provides a flexible procedure for producing oils and middle distillates from a charge containing heteroatoms, i.e. containing more than 200 ppm by weight of nitrogen, and more than 500 ppm by weight of sulphur. The procedure comprises at least one hydrorefining stage, at least one stage of catalytic dewaxing on zeolite, and at least one hydrofinishing stage.

Abstract: The invention relates to a process for the production of gasoline with a low sulfur content comprising at least three stages: a first stage in which the sulfur-containing compounds present in the gasoline are at least partially transformed into H2S and into saturated sulfur-containing compounds; a second stage whose purpose is to eliminate the H2S from the gasoline produced in the first stage; and a third stage in which the saturated sulfur-containing compounds remaining in the gasoline are transformed into H2S. The process according to the invention optionally also comprises a pretreatment stage whose purpose is to hydrogenate the diolefins of the feedstock before the first stage.

Abstract: An inline, high-shear mixer is provided in a cracked gas stream upstream of a caustic tower in an ethylene production unit. Spent caustic is withdrawn from the bottom of the caustic tower and pumped to the mixer, where the spent caustic mixes with and absorbs acid gas components from the cracked gas stream. The spent caustic is separated from the cracked gas, forming a partially treated cracked gas stream. The partially treated cracked gas stream is then fed to the caustic tower. Polymer deposition in the caustic tower is reduced because polymeric material is formed when the cracked gas stream is mixed with the spent caustic and is removed before the cracked gas stream is fed to the caustic tower.

Abstract: A three stage hydroprocessing process includes two liquid and one vapor reaction stages, both of which produce an effluent comprising liquid and vapor. Both vapor effluents comprise vaporized hydrocarbonaceous material. Fresh hydrogen is used for the hydroprocessing in both liquid stages. The second stage liquid effluent comprises the product liquid. The first stage liquid effluent is the feed for the second stage. The first stage vapor effluent is hydroprocessed in the vapor stage and then cooled to condense and recover at least a portion of the processed vapor as additional product liquid.

Abstract: In an integrated lube oil process, a lube oil stock is hydrotreated over a non-noble metal containing hydrotreating catalyst in an HDN/HDS unit to remove sulfur and nitrogen from the lube oil stock and produce an HDN/HDS unit effluent. The effluent comprises hydrodesulfurized, hydrodenitrogenated lube oil stock, hydrogen sulfide and ammonia. The hydrogen sulfide and ammonia are stripped from the hydrodesulfurized, hydrodenitrogenated lube oil stock to form a liquid stream comprising stripped lube oil stock and a first gas stream comprising hydrogen sulfide, ammonia and molecular hydrogen. The stripped lube oil stock is hydrotreated over a noble-metal containing hydrotreating catalyst in an HDW unit to produce an HDW unit effluent comprising a dewaxed lube oil stock. A second gas stream comprising molecular hydrogen is separated from the dewaxed lube oil stock. The first gas stream is combined with the second gas stream to form a third gas stream.

Abstract: A hydroprocessing process includes two hydroprocessing reaction stages, both of which produce a liquid and a vapor effluent, and a liquid-vapor contacting stage. The first stage vapor effluent contains impurities, such as heteroatom compounds, which are removed from the vapor by contact with processed liquid effluent derived from one or both reaction stages and, optionally, also liquid recovered from processed vapor. The first and contact stage liquid effluents are passed into the second stage to finish the hydoprocessing. The contact and second stage vapor effluents are cooled to recover additional hydroprocessed product liquid.

Abstract: A process for producing normally gaseous olefins from two different process units sharing common downstream quench and fractionation facilities, wherein one of the process units is a short contact time mechanically fluidized vaporization unit for processing petroleum residual feedstocks and the other is a conventional steam cracking unit.

Abstract: The present invention provides a process for hydrodelayed thermal cracking in combination with hydrostripping, which comprises feeding crude oil from a surge tank to a crude oil stripper via a feed line; separating the crude oil into a lighter fraction and a heavier fraction in the crude oil stripper; subjecting the lighter fraction to hydrodesulfurization; feeding the heavier fraction from the crude oil stripper to a first storage tank; hydrothermally cracking the heavier fraction for at least 10 minutes under a hydrogen pressure in the first storage tank; introducing a bottom residue of the first storage tank into a second storage tank or the feed line, and subjecting a cracked and vaporized fraction of the first storage tank to hydrodesulfurization; hydrothermally cracking the residue introduced into the second storage tank under a higher hydrogen pressure than the hydrogen pressure of the first storage tank; subjecting a portion of a bottom residue of the second storage tank to hydrodemetallization, hydro

Abstract: The invention involves visbreaking heavy oil under mild conditions in a vertical vessel containing a vertical elongate ring spaced inwardly from the vessel wall to form an outer open-ended annular chamber and an inner open-ended soak chamber. Heavy oil at 220.degree.-600.degree. F. is fed to top of annular chamber. A mixture of visbroken residuum and heavy oil at 730.degree.-800.degree. F. is fed to top of soak chamber. There is heat transfer through the ring from the soak liquid to the annulus liquid to assist in maintaining mild temperature in the soak chamber. The two streams mix in the base of the vessel whereby the visbreaking reaction is quenched. Part of the product is recycled and heated to provide the feed to the soak chamber.

Abstract: A simultaneous recovery of pure benzene and pure toluene is performed by extractive distillation with N-formylmorpholine and/or other N-substituted morpholines whose substituents contain not more than seven C-atoms as a solvent. From the entry product by predistillation, a benzene fraction boiling in the region between 75.degree. and 85.degree. C. and a toluene fraction boiling in the region between 99.degree. and 111.degree. C. is separated. The benzene fraction is supplied in the lower part, and the toluene fraction is supplied in the upper part of the extractive distillation column separated by a chimney plate into two parts.

Abstract: A heat integrated hydrotreating process has been invented. The feedstock is a cracked hydrocarbon stock which is mixed with hydrogen to suppress coking before heating in a multiple tube furnace to reactor inlet temperature. A minor portion of the feedstock is mixed with hydrogen and heated to reactor inlet temperature by quenching the hot reactor effluent. The minor portion is fed directly to the hydrogenation reactor, bypassing the furnace. By the process, high level heat is recovered.

Abstract: Process for thermal cracking of residual hydrocarbon oils by(1) feeding the oil and a synthesis gas to a thermal cracking zone, the gas having a temperature sufficiently high to maintain the temperature in the cracking zone by direct heat exchange at 420.degree.-645.degree. C.;(2) separating the cracked products into (a) a gas, (b) at least one distillate fraction and (c) a cracked residue;(3) separating the cracked residue into a heavy hydrocarbon oil poor in asphaltenes and a heavy hydrocarbon oil rich in asphaltenes;(4) gasifying the oil rich in asphaltenes in the presence of oxygen and steam to produce synthesis gas; and(5) recycling synthesis gas from step 4 as feed to step 1.

Abstract: A catalytic hydrocracking process which comprises: (a) contacting a hydrocarbonaceous feedstock having a propensity to form heavy polynuclear aromatic compounds and a liquid recycle stream in a hydrocracking zone to convert a substantial portion of the hydrocarbonaceous components in the feedstock to lower boiling products; (b) recovering a hydrocarbon effluent from the hydrocracking zone and partially condensing the hydrocarbon effluent from the hydrocracking zone and separating the same into a lower boiling hydrocarbon product stream and an unconverted hydrocarbon stream having at least a portion boiling above about 400.degree. F. (204.degree. C.