Abstract: Process for the manufacture of lubricating base oils wherein a hydrocarbon feedstock is catalytically treated in the presence of hydrogen at elevated temperature and pressure and wherein at least part of a heavy fraction of the material obtained is subjected to dewaxing, in which process a hydrocarbon feedstock is used containing flashed distillate produced via a residue conversion process.

Abstract: A process is described for removing mineral or ash constituents from heavy hydrocarbon residues, such as those resulting from coal-oil coprocessing, residue hydrocracking or coal liquifaction. The process comprises the steps of: (a) intimately mixing the ash-containing heavy hydrocarbon oil residue with a surfactant and a pH-conditioned aqueous solution under high shear mixing conditions to disperse the ash-containing residue in the aqueous phase thereby creating a fine oil-in-water emulsion, (b) adding a strong oxidizing agent to the emulsion to thereby break the emulsion and release the ash into the aqueous phase and (c) separating the ash-containing aqueous phase from the oil phase. The HLB method for characterizing the emulsion forming activity of a surface active material is described in M. J. Rosen, Surfactants and Interfacial Phenomena, John Wiley & Sons, New York (1989), incorporated herein by reference.

Abstract: Hydrocarbon lubricants having a high viscosity index (V.I.) and low pour point are produced by hydroisomerizing a waxy lube feed such as slack wax or a waxy gas oil over zeolite beta after which aromatic components are removed by extraction, e.g. with furfural. The raffinate is then dewaxed, preferably by solvent dewaxing to target pour point with a final hydrofinishing step. The hydroisomerization coupled with the aromatics extraction and dewaxing increases the range of crudes that can be processed into high V.I. lubes while maintaining equivalent product qualities. Hydrogen consumption in the process is relatively low.

Abstract: A method of processing hydrocarbon substances including coal, heavy crude oil, and bitumen by hydrogenating the hydrocarbon substance with a gas containing from 20%-100% hydrogen at a pressure in the range of from 50 bar to 700 bar and at a temperature in the range of from 250.degree. C. to 600.degree. C. to produce a hydrogenation residue which is treated in a secondary stripping operation using hydrogen gas at a pressure between about 1.2 bar and 150 bar to recover light hydrocarbon gases from the hydrogenation residue.

Abstract: An improved process for hydrogenation of heavy oil is provided by the use of a mixed catalyst. In the process of the present invention, a mixture of a direct desulfurization catalyst and a spent FCC catalyst which is free of molybdenum is used as the mixed catalyst. In accordance with the process of the present invention, a middle distillate fraction having a boiling point falling within the range of 171.degree. to 343.degree. C. can be obtained in high yield.

Abstract: A process is disclosed for reprocessing contaminated oils, such as used crankcase oil from automobile engines, by thermal treatment, such as visbreaking, in the presence of other hydrocarbon feedstocks, followed by fractional distillation for the recovery of a gasoline fraction, a carboxylic acid fraction, a gas oil fraction containing chlorinated hydrocarbons and a high boiling bottoms fraction. The gas oil fraction is subjected to catalytic hydrocracking with the simultaneous destruction of chlorinated hydrocarbons. The resulting hydrocracked oils, after separation of hydrogen chloride, are free from chlorine compounds and other contaminants.

Abstract: An improvement has been found in the gas recovery section of a delayed coking process. In the improvement the compressor discharge is amine scrubbed to remove hydrogen sulfide. The compressor discharge is the entire vapor feed to the gas recovery section and contains about 90% of the hydrogen sulfide. This has been found to cause a significant drop in both the depropanizer and debutanizer pressure and allow a saving in the investment cost of the pressure vessel. Synergistically a reduced amount of hydrogen sulfide is present in the entire gas recovery section. The remaining 10% of the hydrogen sulfide is removed by amine scrubbing the fuel gas and propane/propylene fractions.

Abstract: High viscosity index, low pour point lubricants are produced by the oligomerization of a wax-derived lubricant fraction. The fraction may be produced from slack wax or de-oiled wax by hydroisomerization over zeolite beta or hydrocracking/isomerization over an amorphous catalyst followed by selective dewaxing, preferably by catalytic dewaxing over a highly shape selective zeolite such as ZSM-23. The preferred peroxides are ditertiary alkyl peroxides such as ditertiary butyl peroxide (DTBP) and are typically used at temperatures of 100.degree.-300.degree. C.

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: Heavy hydrocarbon oil, containing asphaltene, sulfur and metal contaminants, is hydrotreated in the presence of a hydrotreating catalyst having a small pore diameter in an initial process step to remove sulfur and metal contaminants. Removal of additional metal and sulfur contaminants is then accomplished in a second process step by solvent deasphalting, wherein the size of the pore diameter of the hydrotreating catalyst utilized in the initial hydrotreating step affects the metals rejection in the subsequent solvent deasphalting step. In a third process step the deasphalted oil is catalytically cracked substantially in the absence of added hydrogen to provide lower boiling hydrocarbon products.

Abstract: A multistep process is disclosed for the manufacture of synthetic lubricants from the C.sub.8 to C.sub.24 linear olefin components of below liquid fuel value petroleum distillate fractions derived via the high temperature thermal cracking of petroleum residua. Such feeds contain major amounts of 1-n-olefins, n-paraffins and greater than 0.1% concentration of sulfur mostly in the form aromatic, thiophene type sulfur compounds.In the first step of the present process such feeds are enriched in the straight chain aliphatic hydrocarbon components by one or more separation processes, preferably via urea adduction or by crystallization. In the second step, the olefin components are oligomerized to sulfur containing C.sub.30 to C.sub.60 polyolefins, preferably in the presence of BF.sub.3 complex catalysts. In the third step, the polyolefins are hydrogenated to novel isoparaffin lubricants in the presence of sulfur resistant catalysts, preferably transition metal sulfides.

Abstract: Hydrocarbon feeds are dewaxed and hydrotreated in a two-stage dewaxing-hydrotreating reactor system with interstage separation of olefinic and naphtha and light olefins. Separation of the naphtha and olefins is carried out by stripping the effluent from the dewaxing reactor with a stripping medium such as make-up hydrogen or vapor from the hydrotreater effluent. Hydrogen recycle for the dewaxer and the hydrotreater is taken from the stripper/separator after removal of the olefinic naphtha and removal of contaminants. Separation of the lighter olefins from the olefinic naphtha may be improved by the use of an oil solvent such as naphtha introduced into the top of the interstage stripper/separator so that the recycle gas from the stripper/separator is essentially free of wet gas and heavier fractions.

Abstract: A hydrodesulfurization process for catalytically hydrosulfurizing highly aromatic feeds, especially catalytically cracked feeds such as light cycle oils from catalytic cracking processes and aromatic extracts, employs a hydrodesulfurization catalyst containing zeolite beta. The zeolite beta based catalyst is more effective for effecting desulfurization than comparable amorphous catalysts or catalysts based on other large pore size zeolite and is capable of achieving a high degree of desulfurization at relatively low levels of conversion. The hydrodesulfurization catalyst comprises a transition metal hydrogenation component, preferably Co/Mo, on zeolite beta together with an inert matrix. The zeolite beta based catalyst may be mixed with amorphous catalyst such as Co/Mo/alumina. The low sulfur products are useful as blending components for road diesel fuels and other distillate fuels.

Abstract: This invention provides a fixed bed of nonuniformly sized grade catalyst particles for hydrocracking or hydrodesulfurization. The graded particles are arranged with the largest particles in either the upstream or the downstream portion of the bed. In either case, when compared with the conventional bed of uniformly sized particles, the graded bed of this invention shows enhanced hydrocarbon conversion activity for heavy oils over a useful range of conversion. Such catalyst bed is particularly useful in moderate hydrocracking operating at less than 1000 psig (7000 kPa) pressure.

Abstract: The quality and yield of dewaxed, hydrotreated lube oil base stocks are improved by reducing the top temperature in the hydrotreated lube stripper so as to increase the proportion of heavy kerosene components in the lube oil base stock. The separation system provides for a two stage stripping of the lube oil fraction such that the kerosene fraction stripped from the lube product in the primary product stripper under vacuum is stripped in a second stage stripper at a higher pressure with recycle of the heavy kerosene fraction as a reflux stream to the primary vacuum stripper so that a product with improved viscosity index and flash point is separated in the primary stripper.

Abstract: High octane gasoline and high quality distillate are co-produced by a hydrocracking process in which a catalytic cracking light cycle oil is hydrocracked under conditions of low to moderate hydrogen pressure and severity to produce a high octane, hydrocracked gasoline. The distillate fraction which boils immediately above the gasoline fraction is recycled to the hydrocracker to increase the paraffinic content of this fraction by partial saturation and cracking of the aromatics contained in it so as to form a paraffinic distillate of low sulfur and high cetane index which is useful as a road diesel fuel. A higher boiling distillate fraction of relatively lower aromaticity may also be produced for use as a low sulfur fuel oil. The recycled fraction may be cooled to provide quench for the hydrocracker.

Abstract: Lubricant basestocks of high viscosity index, typically with V.I. of at least 130 or higher, and low pour point, typically below 5.degree. F., are produced by hydroisomerizing petroleum waxes such as slack wax or de-oiled wax, over zeolite beta and then dewaxing to target pour point. A preferred process employs a solvent dewaxing after the hydroisomerization step to effect a partial dewaxing with the separated waxes being recycled to the hydroisomerization step; dewaxing is then completed catalytically, typically over ZSM-5 or ZSM-23.

Abstract: A process for removing catalyst fines from slurry oil is disclosed. A settling reagent, such as coal, alumina, or coke, is added to a fines containing heavy oil bottoms product from a fractionator downstream of a catalytic cracking unit. The settling reagent promotes rapid settling and removal of fines from heavy oil product. Settling may be performed in a slurry settler, or a centrifuge. A catalytic cracking process for heavy, metals laden oil is also disclosed using a settling reagent to clarify slurry oil, then recycling settled settling reagent to contact the heavy oil in the catalytic cracking process.

Abstract: An improved process for the flexible production of high-quality gas oil from two crude gas oil feedstocks deriving from primary fractionation consisting of subjecting the heavy crude gas oil feedstock to catalytic dewaxing in the presence of hydrogen, adding a lighter crude gas oil feedstock to the actual effluent from the dewaxing stage and subjecting these feedstocks simultaneously to catalytic desulphurization.

Abstract: I disclose a single stage, multilayered catalyst system capable of hydrodehazing and hydrofinishing a solvent dewaxed lube oil base stock. In the first layer, I catalytically dewax the solvent dewaxed stock. In the second layer, I hydrofinish the catalytically dewaxed stock. My invention also relates to a process for hydrodewaxing and hydrofinishing a solvent dewaxed lube oil base stock.

Abstract: Using a catalyst comprising a silicoaluminophosphate molecular sieve such as SAPO-11 and SAPO-41, and platinum or palladium, a hydrogenation component, heavy oils are simultaneously subjected to hydrocracking and isomerization reactions. The process selectively produces middle distillates in high yields having good low temperature fluid characteristics, especially reduced pour point and viscosity.

Abstract: A process is provided wherein premium fuels are manufactured from a high sulfur, low pour point feed and a low sulfur, high pour point feed. The feeds are treated individually (blocked operation) in a catalytic reactor that desulfurizes or dewaxes the feed, depending on temperature, and the effluents are combined. Since cut point limitations due to sulfur or pour point are removed by the process, yield of a fuel (e.g. jet fuel) is materially enhanced.

Abstract: The severity of a visbreaking operation is increased by treating product to remove a heavier phase in an amount of less than 15 weight percent and recycling treated product.

Abstract: We disclose a single stage, multilayered catalyst system capable of hydrodewaxing and hydrofinishing a solvent-dewaxed lube oil base stock. In the first layer we catalytically dewax the solvent-dewaxed stock. In the second layer we hydrofinish the catalytically dewaxed stock. Our invention also relates to a process for hydrodewaxing and hydrofinishing a solvent-dewaxed lube oil base stock.

Abstract: A proces for hydrocracking 343.degree. C..sup.+ feedstock which contains polycyclic aromatics to form a lube base stock having enhanced oxidation stability and viscosity index is disclosed. The process employs a catalyst which comprises a layered silicate, such as magadiite which contains interspathic polymeric silica and interspathic polymeric oxides of one or more elements selected from the group consisting of Al, B, Cr, Ga, In, Mo, Nb, Ni, Ti, Tl, W and Zr, preferably Al. The catalyst may also contain a hydrogenation component, e.g., palladium.

Abstract: The process of the invention relates to the production of dehazed white oil possessing long-term low temperature storage stability. The white oil is dehazed with a dehazing catalyst comprising a Group VIII metal incorporated with a shape-selective molecular sieve selected from the Group consisting of a ZSM-5 type zeolite and a crystalline borosilicate molecular sieve.

Abstract: Relatively heavy or relatively light lube chargestocks are dewaxed in two parallel, separate reactors. The reactor used for dewaxing the relatively light chargestocks contains a crystalline aluminosilicate zeolite exemplified natural or synthetic ferrierite, ZSM-22, ZSM-23 and ZSM-35 zeolites and/or mixtures thereof. The reactor used for dewaxing the relatively heavy chargestocks contains a crystalline aluminosilicate zeolite exemplified by ZSM-5, ZSM-11 zeolites, ZSM-5/ZSM-11 intermediates and/or mixtures thereof.

Abstract: A process for improving the storage stability of hydrocracked neutral oil lubricating oil stocks comprising a dewaxing step utilizing a high silica zeolite catalyst to produce a dewaxer effluent and two stabilizing steps utilizing hydrofinishing and nonhydrogenative stabilization by an acidic catalyst.

Abstract: This invention relates to a non-oxidative method of sweetening a sour hydrocarbon fraction. The method comprises treating a sour hydrocarbon fraction containing mercaptans with an acid-type catalyst in the presence of an unsaturated hydrocarbon at reaction conditions thereby converting said mercaptans to thioethers. Acid type catalysts which may be used include polymeric sulfonic acid resins, intercalate compounds, sollid acid catalysts and acidic inorganic oxide catalysts.

Abstract: This invention relates to an efficient process for shape-selective conversion of organic feedstock with a catalyst comprising a Clathrate Group tectosilicate such as ZSM-39 and a highly siliceous, shape selective zeolite such as ZSM-5. In one embodiment, a stabilized, dewaxed lube stock is prepared by catalytically dewaxing a hydrocrackate.

Abstract: The severity of a visbreaking operation is increased by treating product to remove a heavier phase in an amount of less than 15 weight percent and provide a remaining product having a Shell Hot Filtration number of less than 0.25.

Abstract: An integrated refining scheme for hydroprocessing high boiling fractions such as gas oil and catalytically cracked cycle oils to produce premium quality distillates, especially jet fuels and naphthas suitable for reforming into high octane gasoline. In addition, unconverted, high boiling fractions suitable for processing by conventional refining techniques into high quality, low pour point lube base stocks are obtained. The integrated hydroprocessing comprises a first stage hydrocracking step employing an aromatic selective hydrocracking catalyst based on a large pore size acidic component such as amorphous alumina or silica alumina or a large pore size zeolite such as zeolite X or zeolite Y. The hydrocracking may be operated either in a naphtha directing mode under conditions of moderate to high severity or under conditions of low to moderate severity to produce a relatively higher proportion of product boiling in the middle distillate range.

Abstract: A process for improving the color and oxidation stability of feed characterized as an admixture of liquid hydrocarbon compounds, inclusive of fused multi-ring aromatic and hydroaromatic hydrocarbons. This feed, which boils within a range of from about 224.degree. C. to about 538.degree. C. and contains moderate to high concentrations of organic sulfur and organic nitrogen compounds, is (1) hydrotreated over a hydrotreating catalyst at hydrotreating conditions, or (2) hydrotreated over a hydrotreating catalyst at hydrotreating conditions and the high boiling product therefrom hydrocracked over a hydrocracking catalyst at hydrocracking conditions, to obtain a low sulfur, low nitrogen product which is contacted as a feed in the presence of hydrogen, over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals components at hydrogen partial pressure and temperature sufficient to improve product color, or stablize the product against light and oxygen degradation, or both.

Abstract: A process for dewaxing and stabilizing a hydrocracked bright stock, comprising hydrodenitrification, catalytic dewaxing, and mild hydrofinishing.

Abstract: A method and apparatus for the recovery of bitumen oils from oil shale. The method comprises crushing the oil shale to a predetermined particle size and mixing with an organic solvent to form a slurry. The slurry is then subjected to supercritical temperatures and pressures whereby the kerogen materials break down into bitumen oils which solubilize in the solvent. The liquid and solids are separated and the solid components are further treated under supercritical temperatures and pressures to yield further bitumen oils. The extracted bitumen oils are separated from solvent by fractionation, and upgraded by removing an asphaltenes residue. Off-gases and asphaltenes residue from the system are burned in a limestone fluidized bed combustor, which results in environmentally acceptable emissions and supplies process heat and power. The apparatus includes a high pressure autoclave-type vessel with an internal venturi draft tube, and a plurality of high pressure decantation vessels with internal lamellae thickeners.

Abstract: A process for separating finely divided solid particles from a hydroprocessing liquid product which comprises treating a heavy hydrocarbon feed having an asphaltene content of at least 1 wt. % so as to obtain an unstable product characterized by heavy molecular weight molecules which promote the agglomeration of said finely divided solid particles and thereafter feeding said unstable product to a precipitating zone provided with a centrifugal decanter for precipitating the agglomerated solid particles and said heavy molecular weight molecules in said precipitating zone wherein at least 80 wt. % of the finely divided solid particles is recovered.

Abstract: A catalytic dewaxing process in which a hydrocarbon feed, usually a lubricant feed, is catalytically dewaxed in at least two catalytic dewaxing stages with an interstage separation of the light ends which are subjected to hydrogenation to saturate the olefins before the hydrotreated product is passed to the second dewaxing stage. The hydrotreated fraction may be the entire fraction below the lube boiling range with a lube feed or a lower boiling portion of it with separated higher boiling portions such as naphtha and distillate by-passing the second dewaxing step.

Abstract: A process for the conversion of residual asphaltene-containing hydrocarbonaceous charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption.

Abstract: A catalytic hydrocracking process which comprises (a) introducing a reduced crude into a fractionation zone to produce a vacuum gas oil stream having a propensity to form polynuclear aromatic compounds in a hydrocracking zone and a slop wax stream; (b) contacting the vacuum gas oil stream in a hydrocracking zone with added hydrogen and a metal promoted hydrocracking catalyst at elevated temperature and pressure sufficient to gain a substantial conversion to lower boiling products; (c) partially condensing the hydrocarbon effluent from the hydrocracking zone and separating the same into a low boiling hydrocarbon product stream and an unconverted hydrocarbon stream boiling above about 650.degree. F. (343.degree. C.

Abstract: A spindle oil is hydrotreated and then hydrodewaxed in the presence of a catalyst containing at least 70 percent by weight of an intermediate pore molecular sieve in the support so as to produce a selected fraction having a low pour point and viscosity comparable to the original spindle oil, said fraction being then suitable as a "cutter stock" for lowering the pour point of fuel oils.

Abstract: An improved multistage hydrodewaxing process for hydrodewaxing a hydrocarbon feedstock, such as a heavy or light distillate, is disclosed. A two-phase mixture of a hydrogen-rich gas stream and a liquid hydrocarbon is passed through a series of spaced catalyst beds in a single reactor, reaction vapors containing olefins, are withdrawn at each interspace between beds and replaced with hydrogen-rich saturated gas.

Abstract: A moderate pressure hydrocracking process is disclosed in which substantially dealkylated heavy distillate feedstocks are processed directly to high octane gasoline over a catalyst, preferably comprising a crystalline silicate zeolite hydrocracking component having a Constraint Index less than 2. The bottoms fraction produced from the contacting may be passed to an FCC unit for further processing. In another embodiment, the substantially dealkylated heavy distillate feedstock may be fractionated into a lighter boiling stream and a heavier boiling stream for better ease of processing.

Abstract: An improved nickel-tin hydrogenation catalyst additionally comprising palladium provides a highly active catalyst more easily activated than conventional nickel hydrogenation catalysts, and a process employing the improved catalyst to stabilize lubricating oils to ultraviolet radiation is disclosed.

Abstract: The instant invention discloses a method of removing heterocyclic basic nitrogen compounds from petroleum oils which comprises first enhancing the concentration of the heterocyclic basic nitrogen compounds in a portion of the petroleum oil and then extracting the enhanced portion of the heterocyclic basic nitrogen compounds with a two phase system having an aliphatic carboxylic acid as the extracting agent. In the hydrotreating embodiment of this invention a portion of all of the nitrogen compounds are converted to heterocyclic basic nitrogen compounds and thereby more feasibly extracted. In the distillation embodiment of this invention the nitrogen compounds are actually concentrated and thereby result in a more feasible extraction with the aliphatic carboxylic acid.

Abstract: This invention relates to a method for catalytically manufacturing a low pour point petroleum product from distillates of crude oil, and more particularly to a method for economically manufacturing a low pour point petroleum product, such as the insulating oil, the lubricating oil used for various types of freezing devices, or the base oil for such lubricating oil, from a paraffin-based crude oil as the starting material without using any special rare crude oil such as naphthene-based crude oil. The catalyst comprises zeolite TSZ.

Abstract: A process for stabilizing a lubricating oil base stock derived from a nitro-aromatic-containing hydrocracked bright stock, comprising a three-step stabilizing process utilizing hydrodenitrification followed by mild hydrofinishing followed by nonhydrogenative acid stabilization.

Abstract: An improved method and apparatus are disclosed for hydrodewaxing hydrocarbon feedstock, such as heavy distillate or residual feed. The feedstock is hydrodewaxed in a first step. The resulting first effluent is separated to form a first vapor stream containing olefinic products and a first liquid stream, with a pour point of about 30.degree. to about 100.degree. F. The first liquid stream is then introduced into a second catalytic reaction, where the first liquid stream is hydrodewaxed to a specification pour point less than about 30.degree. F. The method and apparatus may also comprise routing primary products of hydrodewaxing, which contain olefins, as they are removed from the dewaxed first effluent, through an MOGDL unit to convert the olefins to additional high quality lubes. Improvements are due to removal of primary by-products containing olefins which inhibit dewaxing and accelerate catalyst aging and may cause reactor upsets. The addition of the MOGDL unit increases lube yields.

Abstract: An improved sulfur trap for the sulfur level reduction of a reformer feed leaving a hydrofiner to render it suitable for use in a reforming unit employing a sulfur-sensitive reforming catalyst. The nickel catalyst contained in said sulfur trap is one wherein the average crystallite size of the nickel is at least about 75.ANG., and at greater than 50 percent of the nickel is in reduced state, based on the total weight of the supported component.

Abstract: A process for stabilizing a lubricating oil base stock derived from a nitro-aromatic-containing hydrocracked bright stock, comprising a two-step stabilizing process utilizing hydrodenitrification followed by mild hydrofinishing.

Abstract: A method for the two-step catalytic hydrogenation treatment of a heavy hydrocarbon oil which comprisesfirst contacting the heavy hydrocarbon oil with a first solid catalyst comprising a metal component having catalytic activity for hydrogenation supported on a zeolite having catalytic activity for cracking a hydrocarbon, said zeolite having a (i) pore size distribution curve with two peaks, one peak in the range of 5 to 50 nm pore diameter and the other peak in the range of 50 to 1000 nm pore diameter and (ii) the volume of the pores having a diameter of 100 nm or larger is at least 0.05 ml/g; andthen contacting the heavy hydrocarbon oil which had been contacted with said first catalyst, with a second catalyst, said second catalyst having hydrogenation activity and which is different from said first catalyst.