Abstract: Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Abstract: Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Abstract: Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Abstract: Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude.

Abstract: Systems and methods are provided for slurry hydroconversion of a heavy oil feedstock, such as an atmospheric or vacuum resid, in the presence of an enhanced or promoted slurry hydroconversion catalyst system. The slurry hydroconversion catalyst system can be formed from a) a Group VIII non-noble metal catalyst precursor/concentrate (such as an iron-based catalyst precursor/concentrate) and b) a Group VI metal catalyst precursor/concentrate (such as a molybdenum-based catalyst precursor/concentrate) and/or a Group VI metal sulfided catalyst.

Abstract: Systems and methods are provided for slurry hydroconversion of a heavy oil feedstock, such as an atmospheric or vacuum resid, in the presence of an enhanced or promoted slurry hydroconversion catalyst system. The slurry hydroconversion catalyst system can be formed from a) a Group VIII non-noble metal catalyst precursor/concentrate (such as an iron-based catalyst precursor/concentrate) and b) a Group VI metal catalyst precursor/concentrate (such as a molybdenum-based catalyst precursor/concentrate) and/or a Group VI metal sulfided catalyst.

Abstract: A process for generating refrigeration, electricity or work utilizing a sorption system is disclosed. The sorption system includes a sorbent material and a fluid, in which the sorbent material and fluid in combination have a pressure index of at least 1.2.

Abstract: A sorption system is disclosed that includes a sorbent material and a fluid, in which the sorbent material and fluid in combination have a pressure index of at least 1.2.

Abstract: A sorption system is disclosed that includes a sorbent material and a fluid, in which the sorbent material and fluid in combination have a pressure index of at least 1.2.

Abstract: A process for isomerization dewaxing of a hydrocarbon feed which includes contacting the hydrocarbon feed with a large pore size, small crystal size, crystalline molecular sieve and an intermediate pore size, small crystal size, crystalline molecular sieve to produce a dewaxed product with a reduced pour point and a reduced cloud point. In a preferred embodiment, the feed is contacted with the molecular sieves sequentially, first with the large pore sieve followed by the intermediate pore sieve.

Abstract: A process for isomerization dewaxing of a hydrocarbon feed which includes contacting the hydrocarbon feed with a large pore size, small crystal size, crystalline molecular sieve and an intermediate pore size, small crystal size, crystalline molecular sieve to produce a dewaxed product with a reduced pour point and a reduced cloud point. In a preferred embodiment, the feed is contacted with the molecular sieves sequentially, first with the large pore sieve followed by the intermediate pore sieve.

Abstract: The present invention is a coated hydrogenation catalyst that includes a porous support material, an active metal component and a silica precursor, wherein the support material is impregnated with the active metal component and then contacted with the silica precursor. After impregnation, the support material is calcined to form a SiO2 layer. The active metal component can be one or more Group VIII metals, metal oxides, metal sulfides or metal carbides. The support material for the coated catalyst is kieselguhr, alumina, silica or silica-alumina. In a preferred embodiment, the active metal component is platinum, palladium, rhodium, rhenium or iridium and the catalyst includes a zeolite component. The coated catalyst is prepared by first impregnating the support material with the active metal component and then contacting the silica precursor to form an impregnated catalyst. The impregnated catalyst is then calcined to form the coated catalyst having a SiO2 layer.

Abstract: The present invention relates to the removal of mercury and other heavy metals from a hydrocarbon feedstream. The process involves contacting the hydrocarbon feedstream with a feedstream-soluble sulfur compound and then contacting the hydrocarbon feedstream and solubilized sulfur compound with an adsorbent.

Abstract: Akylation product is contacted with a purification medium in a liquid phase pre-reaction step to remove impurities and form a purified stream. The purified stream may then be further processed by liquid phase transalkylation to convert the polyalkylated aromatic compound to a monoalkylated aromatic compound. The process may use a large pore molecular sieve catalyst such as MCM-22 as the purification medium in the pre-reaction step because of its high reactivity for alkylation, strong retention of catalyst poisons and low reactivity for oligomerization under the pre-reactor conditions. Olefins, diolefins, styrene, oxygenated organic compounds, sulfur containing compounds, nitrogen containing compounds and oligomeric compounds are removed.

Abstract: Petroleum wax feeds are converted to high viscosity index lubricants by a two-step hydrocracking-hydroisomerization process in which the wax feed which exhibits branchingis initially subjected to hydrocracking under mild conditions with a conversion to non-lube range products of no more than about 30 weight percent of the feed. The hydrocracking is carried out at a hydrogen pressure of at least 1000 psig (7000 kPa) using an amorphous catalyst which preferentially removes the aromatic components present in the initial feed. The hydrocracked effluent is then subjected to hydroisomerization in a second step using a low acidity zeolite beta catalyst which effects a preferential isomerization on the paraffin components to less waxy, high VI isoparaffins. The second stage may be operated at high pressure by cascading the first stage product into the second stage or at a lower pressure, typically from 200 to 1000 psig.

Abstract: Petroleum waxes are converted to high viscosity index lubricants by a hydroisomerization process in which the wax feed is subjected to hydroisomerization over a low acidity molecular sieve isomerization catalyst (the molecular sieve being preferably a zeolite) which effects a preferential isomerization on the paraffin components in the feed to less waxy, high VI isoparaffins. The hydroisomerization is operated at high pressure, at least 1000 psig hydrogen partial pressure (reactor inlet) using a zeolite catalyst, preferably a noble metal containing zeolite beta catalyst which contains boron as a framework component of the zeolite to give a low alpha value, typically below 10. The hydroisomerization is carried out at with a 650° F.+ conversion in the range of 10 to 40 weight percent of the feed. A final dewaxing step to target pour point may be used with relatively low loss, typically no more than 15 weight percent, during this dewaxing.

Abstract: This invention discloses a process for producing a high Viscosity Index lubricant having a VI of at least 125 from a waxy hydrocarbon feed having a wax content of at least 40 wt %. The process comprises catalytically dewaxing waxy paraffins present in the feed by isomerization in the presence of hydrogen and in the presence of a low acidity large pore zeolite isomerization catalyst. This catalyst has a ratio of SiO.sub.2 /Al.sub.2 O.sub.3, as synthesized, of at least 50:1, wherein the catalyst is prepared in the absence of boron. The alpha value of the catalyst is no greater than 20. The catalyst comprises a noble metal hydroisomerization catalyst such as Pt. The feed may be hydrocracked prior to dewaxing with the large pore zeolite. The effluent of the process may also be further dewaxed by either solvent or catalytic means in order to achieve target pour point.

Abstract: A catalyst composition which comprises a crystalline metallosilicate having the structure of zeolite Beta, phosphor and a matrix that is substantially free of crystalline aluminum phosphate which has improved resistance to steam deactivation which has higher cracking activity than analogous catalysts prepared without phosphorus. The crystalline metallosilicate be used in the as-synthesized form or in the calcined form. included is the method to produce the catalyst composition and methods for the use of catalysts prepared by the present method in organic conversion processes. Specific embodiments of the invention involve various techniques for preparation of catalyst containing phosphorus and crystalline metallosilicates having the structure of zeolite Beta. Catalysts prepared according to the method of this invention are useful for organic compound, e.g., hydrocarbon compound, conversion processes. Organic compound conversion processes include cracking, hydrocracking, and transalkylation, among others.

Abstract: Petroleum wax feeds having a low oil content are converted to high viscosity index lubricants by a two-step hydrocracking-hydroisomerization process in which the wax feed is initially subjected to hydrocracking under mild conditions with a conversion to lube range products of between generally 30 and 40 weight percent of the feed. The hydrocracking is carried out at a hydrogen pressure of at least 800 psig using an amorphous catalyst which preferentially removes the aromatic components present in the initial feed. The hydrocracked effluent is then subjected to hydroisomerization in a second step using a low acidity zeolite beta catalyst. The second stage may be operated at high pressure by cascading the first stage product into the second stage or at a lower pressure, typically from 200 to 1000 psig. The second stage catalyst is preferably a noble metal containing zeolite beta catalyst. The second stage is carried out at relatively low temperature, typically from 600.degree. to 650.degree. F.

Abstract: Long chain alkyl substituted naphthalenes are produced by alkylating naphthalene with an olefin or other alkylating agent with at least 6, and usually 12 to 20 carbon atoms, in the presence of an alkylation catalyst comprising a zeolite having rare earth cations, and both ammonium and protonic species, associated with the exchangeable sites of the zeolite. The zeolite is usually a large pore size zeolite such as USY. The presence of rare earths and both ammonium and protonic species increases selectivity for production of long chain mono-alkyl substituted naphthalenes in preference to more highly substituted products.