Abstract: A process for the treatment of a hydrocracking unit bottoms stream containing heavy poly-nuclear aromatic (HPNA) compounds and/or a fresh hydrocracking feedstock stream containing HPNA precursors to produce coke. The HPNA and/or HPNA precursors are removed from the hydrocracking unit bottoms stream and/or a fresh hydrocracking feedstock stream by solvent washing, and the HPNA and/or HPNA precursors are subjected to delayed coking for the production of coke.

Abstract: A method of reducing the viscosity of a crude oil, the method comprising adding to the crude oil (i) a surfactant compound including at least two hydrophobic groups wherein the resultant mixture has a water content of less than 10 vol %.

Abstract: A system for removing oxygenates from a hydrocarbon stream includes a caustic wash unit comprising a plurality of caustic wash loops, and a hydrogenation reactor. The hydrogenation reactor is configured to receive a first gaseous stream from a first caustic wash loop of the plurality of caustic wash loops and pass a second gaseous stream from the hydrogenation reactor to a second caustic wash loop of the plurality of caustic wash loops, wherein the hydrogenation reactor comprises a sulfided catalyst.

Abstract: A process for slurry-phase hydrocracking of a heavy hydrocarbon feedstock in a reactor, such as an upflow bubble column reactor, includes separately introducing additive in two size ranges into the feedstock. A fine size particle additive is introduced upstream of a coarse size particle additive.

Abstract: The present invention provides a method for processing low-grade heavy oil, comprising: providing a riser-bed reactor; preheating the low-grade heavy oil and injecting it into the riser reactor to react with solid catalyst particles at the temperature of 550-610° C.; oil-gas, after reacting with the solid catalyst particles in the riser reactor, being introduced into the fluidized bed reactor to continue to react at temperature of 440-520° C. and weight hourly space velocity of 0.5-5 h?1; and the oil-gas, after reacting in the fluidized bed reactor, being separated from coked solid catalyst particles carried therein, and the separated oil-gas being introduced into a fractionation system. The method can effectively remove carbon residues, heavy metals, asphaltenes and other impurities from the low-grade heavy oil, and obtain high liquid product yield in a simple process.

Abstract: The invention generally relates to a hydrocarbon process for reducing condensation in a vapor-liquid amine or caustic acid gas scrubber. A first mixture is provided, the first mixture being superheated and comprising C2+ mono-olefin, acid gases, and diolefin molecules. The first mixture is divided into a first stream and a second stream, the first and second streams having substantially the same composition. The first stream is cooled to produce a gas phase and a liquid phase, the gas phase comprising less C6+, the liquid phase containing more C6+. The gas phase is separated to create a third stream. The third stream and the second stream are combined to form a second substantially superheated mixture. The second mixture is conducted to an acid gas scrubbing tower. The invention also relates to an apparatus for carrying out this process.

Abstract: An oil forming composition and a method of producing a synthetic crude oil are provided. The oil forming composition includes a mixture of an organic material selected from the group consisting of a member of the lactuca genus, nuts, nut derivatives, vegetable oils, pine tree derivatives, animal protoplasm, and combinations thereof; and a mineral aggregate selected from the group consisting of a silica containing mineral aggregate and a quartz containing mineral aggregate. The method of producing synthetic crude oil includes positioning a first heating enclosure adjacent to a heating surface, providing an oil forming composition within the first heating enclosure, positioning a lid over the oil forming composition, simultaneously applying pressure to the lid and heating the oil forming composition, cooling the oil forming composition to form a pre-volatile oil product, and heating the pre-volatile oil product while exposed to air to form the synthetic volatile fuel.

Abstract: An apparatus is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. Only the hot hydroprocessing effluent is heated in a fired heater prior to product fractionation, resulting in substantial operating and capital savings.

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: In one aspect, the inventive process comprises a process for pyrolyzing a hydrocarbon feedstock containing nonvolatiles in a regenerative pyrolysis reactor system. The process comprises: (a) heating the nonvolatile-containing hydrocarbon feedstock upstream of a regenerative pyrolysis reactor system to a temperature sufficient to form a vapor phase that is essentially free of nonvolatiles and a liquid phase containing the nonvolatiles; (b) separating said vapor phase from said liquid phase; (c) feeding the separated vapor phase and methane to the pyrolysis reactor system; and (d) converting the methane and separated vapor phase in said pyrolysis reactor system to form a pyrolysis product. In another aspect, the invention includes a separation process that feeds multiple pyrolysis reactors.

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: Processing schemes and arrangements are provided arrangements are provided for the processing a heavy hydrocarbon feedstock via hydrocarbon cracking processing with selected hydrocarbon fractions being obtained via absorption-based product recovery while minimizing or avoiding loss of light olefins via system purging.

Abstract: Methods for using supercritical water to convert hydrocarbons, particularly hydrocarbon fuels such as diesel fuel, jet fuel, or gasoline, into carbonaceous gases and hydrogen. The synthesis gas stream generated by the fuel reforming reaction can then be further refined to increase hydrogen content, and the resultant hydrogen can be utilized to power fuel cells.

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: In one aspect, the inventive process comprises a process for pyrolyzing a hydrocarbon feedstock containing nonvolatiles in a regenerative pyrolysis reactor system. The inventive process comprises: (a) heating the nonvolatile-containing hydrocarbon feedstock upstream of a regenerative pyrolysis reactor system to a temperature sufficient to form a vapor phase that is essentially free of nonvolatiles and a liquid phase containing the nonvolatiles; (b) separating said vapor phase from said liquid phase; (c) feeding the separated vapor phase to the pyrolysis reactor system; and (d) converting the separated vapor phase in said pyrolysis reactor system to form a pyrolysis product.

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: A process for conversion of a hydrocarbon feedstock comprising a relatively heavy main feedstock with a boiling point above approximately 350° C., and a relatively light secondary feedstock with a boiling point below approximately 320° C., wherein, the main feedstock, representing at least 50 wt. % of the hydrocarbon feedstock, is cracked in a fluidized-bed reactor in the presence of a cracking catalyst, the secondary feedstock is cracked in a fluidized bed with the same cracking catalyst, separately or mixed with the main feedstock, said secondary feedstock comprising oligomers with at least 8 carbon atoms of light olefins with 4 and/or 5 carbon atoms.

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: A retort heating apparatus includes a perimeter wall bounding a central compartment. A partition wall is disposed within the central compartment so as to separate the central compartment into at least a heating chamber and a vapor chamber. The partition wall has a plurality of spaced apart apertures formed thereon so as to provide fluid communication between the heating chamber and the collection chamber. A plurality of spaced apart baffles are disposed within the heating chamber between the perimeter wall and the partition wall. A collection plate is disposed within the vapor chamber at a downward curved or sloped orientation. The collection plate has lower end disposed at or adjacent to the partition wall and an opposing upper end disposed at or toward the perimeter wall.

Abstract: An improved system and method for providing reduced acid gas/dewatered light hydrocarbon gas to a light hydrocarbon gas liquefaction process wherein a plurality of light hydrocarbon gas liquefaction trains are used.

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: 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 catalyst suitable for hydrogenating organic compounds, essentially containing from 65 to 80% of nickel, calculated as nickel oxide, from 10 to 25% of silicon, calculated as silicon dioxide, from 2 to 10% of zirconium, calculated as zirconium oxide, and from 0 to 10% of aluminum, calculated as aluminum oxide, with the proviso that the sum of the content of silicon dioxide and aluminum oxide is at least 15% (percentages in % by weight, based on the total weight of the catalyst), obtainable by addition of an acidic aqueous solution of nickel, zirconium and, if desired, aluminum salts to a basic aqueous solution or suspension of silicon compounds and if desired aluminum compounds, the pH of the mixture thus obtained being decreased to at least 6.

Abstract: A method for processing chemical cleaning solvent waste that combines evaporation, purification, and detoxification. The method is mobile and thus allows the processing to be done at the site of the cleaning where the entire processing can be completed. Evaporation produces a concentrated solvent and vapor and gas. The concentrated solvent is detoxified to produce a dry residue for long term storage or disposal and a liquid that is filtered and then released to the surrounding environment. The vapor and gas are scrubbed and condensed to produce a gas that is suitable for release and a distillate. The distillate is purified by filtration and reverse osmosis to produce a distillate that is suitable for release.

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: 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: A process for treating an organic stream containing a non-distillable component to produce an organic vapor stream and a solid which process comprises the steps of: (a) contacting the organic stream containing a non-distillable component with a hydrogen-rich gaseous steam having a temperature greater than the organic stream in a flash zone at flash conditions thereby increasing the temperature of the organic stream and vaporizing at least a portion thereof to produce an organic vapor stream comprising hydrogen and a heavy stream comprising the non-distillable component; and (b) reacting at least a portion of the heavy stream comprising the non-distillable component in the presence of hydrogen in a pyrolysis zone to produce a thermally stabilized volatile organic stream comprising hydrogen and a solid.

Abstract: A process and apparatus for preheating and catalytic cracking of heavy oils is disclosed. Direct contact heat exchange of heavy feed, such as a resid, with hot product vapor from the cracking reactor provides an efficient way to preheat a heavy feed to an unusually high temperature, preferably in excess of 600.degree. F. Cooling hot cracked products from an FCC or TCC reactor upstream of the main fractionator reduces thermal cracking in the transfer line. High temperature preheat reduces the viscosity of the heavy feed, improves contact of heavy feed with cracking catalyst and reduces the amount of catalyst required to effect the catalytic cracking reaction. This improves yields, permits higher cracking reactor temperatures, and reduces cat:oil coke make.

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 process for treating a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component to produce a hydrogenated distillable hydrocarbonaceous product and a heavy product comprising the non-distillable component while minimizing thermal degradation of the hydrocarbonaceous stream which process comprises the steps of: (a) contacting the hydrocarbonaceous stream with a hot first hydrogen-rich gaseous stream having a temperature greater than the hydrocarbonaceous stream in a first flash zone at flash conditions including a first pressure thereby increasing the temperature of the hydrocarbonaceous stream and vaporizing at least a portion thereof to provide a first hydrocarbonaceous vapor stream comprising hydrogen and a first heavy product stream comprising the non-distillable component; (b) contacting the first heavy product stream comprising the non-distillable component with a hot second hydrogen-rich gaseous stream in a second flash zone at flash conditions including a second pressure

Abstract: A process for recovering heat from a tar-containing gas while simultaneously cooling the gas in a 3-stage cooling step by (1) directing a tar-containing gas through a jet cooler comprising a bed of solid particles so that the gas contacts the solid particles and forms a fluidized bed with the flow of the tar-containing gas, which jet cooler comprises a central draft tube into which the gas is directed and indirect heat exchange lines containing a liquid coolant therein disposed inside the central draft tube and wherein the gas and solid particles are cooled by such indirect heat exchange lines such that the tar from the gas condenses on the solid particles; (2) directing the gas through a tar cooler in the second stage wherein the gas-containing residual tars and other impurities resulting from the treatment in the jet cooler are sprayed with a circulating tar from a nozzle to remove a residual tars and impurities from the gas and wherein the gas is further cooled in said tar cooler by means of an indirect he

Abstract: A slurry feed pump which delivers a highly pressurized suspension of coal particles, coal oil and a catalyst to a liquefaction reactor is installed in a plenum chamber which is filled with pressurized coal oil and surrounds the pump housing. The suspension-supplying conduit sealingly extends into the chamber and is connected with the inlet of the pump housing, and a second conduit which delivers pressurized suspension to the reactor sealingly extends into the plenum chamber and is connected with the outlet of the pump housing. The pump is a vertical cantilevered centrifugal pump which is operated below first critical speed and its housing has holes for admission of coal oil from the plenum chamber to those parts in the pump housing which are most likely to undergo extensive wear under the action of coal particles in the suspension.

Abstract: A hydrocarbonaceous oil is introduced to a quench and scrubbing zone mounted on a fluid coking reactor. Heat from the coker vapor product vaporizes a portion of the hydrocarbonaceous oil. The unvaporized portion of the oil is used to quench and scrub the coker vapor product. The bottoms fraction of the quench and scrubbing zone is passed to a vacuum distillation zone to recover a heavy oil fraction and to produce a vacuum residuum for use as coker feed.