Abstract: Systems and methods are provided for improving the operation of a divided wall column for performing distillations. The systems and methods include using a separation stage in a fluid flow pathway for transporting an enriched intermediate stream from a first side of a dividing wall to a second side of a dividing wall. By using a separation stage, the benefit of transporting an enriched intermediate stream can be achieved without requiring precise knowledge of the local concentration profile on the first side of the dividing wall.

Abstract: It is provided solid, heterogeneous catalysts for the deoxygenation of esters of free fatty acids and triglycerides, and for the production of hydrocarbons that can be used as biofuels. More particularly, the catalyst comprises at least one metal oxide, the catalyst having a formula AlaCubNicSidTieZnfZrgLahCeiWjSnkGalFemMOnMnoCOpOx, wherein a, b, c, d, g, h, i, j, k, l, m n, o, p and x are the molar ratios of the respective elements, wherein a, b, c, d, h, i, j, k, l, m, n, o and p are >0, e, f and g are >0 and x is such that the catalyst is electrically neutral.

Abstract: A process increases the concentration of normal paraffins in a feed stream comprising separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream. A naphtha feed stream may be separated into a normal paraffin stream and a non-normal paraffin stream. An isomerization feed stream is taken from the non-normal paraffin stream and isomerized over an isomerization catalyst to convert non-normal paraffins to normal paraffins and produce an isomerization effluent stream. The isomerization effluent stream may be separated into a propane stream and a C4+ hydrocarbon stream optionally in a single column. The C4+ hydrocarbon stream may be recycled to the step of separating a naphtha feed stream.

Abstract: A dividing wall column system for producing hexane includes a dividing wall column including a dividing wall that divides the dividing wall column at least partially into a first side and a second side, with one side of the first and second sides configured to operate as a deisohexanizer column and the other side of the first and second side configured to operate as a hexane column to produce hexane.

Abstract: A method for producing an alternative gasoline fuel which contains 60% v/v or more of a combination of (a) a biologically-derived alcohol and (b) a mixture of C4 to C12 hydrocarbon fuel components, all of which hydrocarbon fuel components have been derived, whether directly or indirectly, from the catalytic conversion of a non-petroleum or biologically-derived oxygenate component, wherein the concentration of the alcohol (a) in the formulation is from 0.1 to 30% v/v.

Abstract: The present invention describes a process for the isomerization of a light naphtha with a view to forming high octane number gasolines, said process using a deisopentanizer and a deisohexanizer which are thermally integrated in a manner such as to reduce the consumption of the high temperature utilities employed in the process.

Abstract: The present invention describes a process for the production of high octane number gasoline by isomerization of a light naphtha cut, comprising two separation steps located downstream of the reaction step which can be used to improve the energy efficiency of said process.

Abstract: Disclosed is a method for storing and delivering ammonia, wherein a first ammonia adsorbing/absorbing material having a higher vapor pressure at a given temperature than a second ammonia adsorbing/absorbing material is used as an ammonia source for said second ammonia adsorbing/absorbing material when said second adsorbing/absorbing material is depleted of ammonia by consumption, and a device for performing the method.

Abstract: Embodiments of methods and apparatuses for isomerization of paraffins are provided. In one example, a method comprises the steps of separating an isomerization effluent into a product stream that comprises branched paraffins and a stabilizer vapor stream that comprises HCl, H2, and C6-hydrocarbons. C6-hydrocarbons are removed from the stabilizer overhead vapor stream to form a HCl and H2-rich stream. An isomerization catalyst is activated using at least a portion of the HCl and H2-rich stream to form a chloride-promoted isomerization catalyst. A paraffin feed stream is contacted with the chloride-promoted isomerization catalyst in the presence of hydrogen for isomerization of the paraffins.

Abstract: Processes for the disproportionation and isomerization of a C7 hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.

Abstract: Processes for the disproportionation and isomerization of a C5 hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a halocarbon carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.

Abstract: Processes for the disproportionation and isomerization of a hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.

Abstract: Embodiments of methods for making renewable diesel by deoxygenating (decarboxylating/decarbonylating/dehydrating) fatty acids to produce hydrocarbons are disclosed. Fatty acids are exposed to a catalyst selected from a) Pt and MO3 on ZrO2 (M is W, Mo, or a combination thereof), or b) Pt/Ge or Pt/Sn on carbon, and the catalyst decarboxylates at least 10% of the fatty acids. In particular embodiments, the catalyst consists essentially of 0.7 wt % Pt and 12 wt % WO3, relative to a mass of catalyst, or the catalyst consists essentially of a) 5 wt % Pt and b) 0.5 wt % Ge or 0.5 wt % Sn, relative to a mass of catalyst. Deoxygenation is performed without added hydrogen and at less than 100 psi. Disclosed embodiments of the catalysts deoxygenate at least 10% of fatty acids in a fatty acid feed, and remain capable of deoxygenating fatty acids for at least 200 minutes to more than 350 hours.

Abstract: A reaction-rectification process is performed in an integrated reaction-rectification system which combines catalytic isomerization and hydroisomerization reactors and distillations zones in an integral column.

Abstract: A method of making a diesel fuel from a renewable feedstock is described. Ammonia or an amine compound is used to neutralize the organic acids in the renewable feedstock. The ammonia or amine compound is removed from the product mixture before the isomerization zone so that it does not affect the isomerization catalyst.

Abstract: Embodiments of methods for making renewable diesel by deoxygenating (decarboxylating/decarbonylating/dehydrating) fatty acids to produce hydrocarbons are disclosed. Fatty acids are exposed to a catalyst selected from a) Pt and MO3 on ZrO2 (M is W, Mo, or a combination thereof), or b) Pt/Ge or Pt/Sn on carbon, and the catalyst decarboxylates at least 10% of the fatty acids. In particular embodiments, the catalyst consists essentially of 0.7 wt % Pt and 12 wt % WO3, relative to a mass of catalyst, or the catalyst consists essentially of a) 5 wt % Pt and b) 0.5 wt % Ge or 0.5 wt % Sn, relative to a mass of catalyst. Deoxygenation is performed without added hydrogen and at less than 100 psi. Disclosed embodiments of the catalysts deoxygenate at least 10% of fatty acids in a fatty acid feed, and remain capable of deoxygenating fatty acids for at least 200 minutes to more than 350 hours.

Abstract: Embodiments of methods for making renewable diesel by deoxygenating (decarboxylating/decarbonylating/dehydrating) fatty acids to produce hydrocarbons are disclosed. Fatty acids are exposed to a catalyst selected from a) Pt and MO3 on ZrO2 (M is W, Mo, or a combination thereof), or b) Pt/Ge or Pt/Sn on carbon, and the catalyst decarboxylates at least 10% of the fatty acids. In particular embodiments, the catalyst consists essentially of 0.7 wt % Pt and 12 wt % WO3, relative to a mass of catalyst, or the catalyst consists essentially of a) 5 wt % Pt and b) 0.5 wt % Ge or 0.5 wt % Sn, relative to a mass of catalyst. Deoxygenation is performed without added hydrogen and at less than 100 psi. Disclosed embodiments of the catalysts deoxygenate at least 10% of fatty acids in a fatty acid feed, and remain capable of deoxygenating fatty acids for at least 200 minutes to more than 350 hours.

Abstract: The service life and deactivation rate of a paraffin isomerization catalyst is improved through use of a new sulfur guard bed containing a chloride additive. This sulfur guard bed, which contains supported CuO material having an increased resistance to reduction, shows such improvement. Thus, the danger of run-away reduction followed by a massive release of water and deactivation of an isomerization catalyst is practically eliminated. The fact that the guard bed material preserves the active metal phase-copper in an active (oxide) form is an important advantage leading to very low sulfur content in the product stream. The sulfur capacity per unit weight of sorbent is also significantly increased, making this sorbent a superior cost effective sulfur guard product.

Abstract: A process for hydrocracking and hydro-isomerization of a paraffinic feedstock obtained by Fischer-Tropsch hydrocarbon synthesis comprising at least 50 wt % of components boiling above 370° C. to obtain a hydro-isomerized feedstock, the process comprising contacting the feedstock, in the presence of hydrogen, at elevated temperature and pressure with a catalyst comprising a hydrogenating compound supported on a carrier comprising amorphous silica-alumina, the carrier having a pore volume of at least 0.8 ml/g, wherein at most 40% of the pore volume comes from pores having a pore diameter above 35 nm and wherein at most 20% of the pore volume comes from pores having a pore diameter below 50 ? and above 37 ?, the carrier having a median pore diameter of at least 85 ?, wherein the product of (surface area per pore volume) and (median pore diameter as measured by mercury intrusion porosimetry) of the carrier is at least 34,000 ?·m2/ml.

Abstract: The invention relates to a process for producing base oils, comprisings the steps where feedstock selected from ketones, aldehydes, alcohols, carboxylic acids, esters of carboxylic acids and anhydrides of carboxylic acids, alpha olefins, metal salts of carboxylic acids and corresponding sulphur compounds, corresponding nitrogen compounds and combinations thereof, is subjected to a condensation step and subsequently subjected to a combined hydrodefunctionalization and isomerization step.

Abstract: The invention relates to a process for producing a new type of high-quality hydrocarbon base oil of biological origin. The process of the invention comprises ketonisation, hydrodeoxygenation, and isomerization steps. Fatty acids and/or fatty acid esters based on a biological raw material are preferably used as the feedstock.

Abstract: Process for isomerising a hydrocarbon feed containing at least C7 hydrocarbons, comprising steps of (a) in a separation column separating the feed into a heavy fraction comprising hydrocarbons having higher boiling point than n-heptane, an intermediate fraction being rich in n-heptane and/or mono-branched iso-heptanes and a light fraction being rich in multi-branched iso-heptanes; (b) withdrawing continuously from the separation column a portion of the intermediate fraction being rich in n-heptane and/or mono-branched iso-heptanes; (c) introducing the withdrawn portion into an isomerisation reactor and isomerising at isomerisation conditions the portion in presence of an isomerisation catalyst and a gas stream being rich in hydrogen; (d) withdrawing from the isomerisation reactor an isomerised effluent stream being enriched in multi-branched iso-heptanes together with cracked hydrocarbons and hydrogen; (e) purging the cracked hydrocarbons and hydrogen from the isomerised effluent to obtain a stabilised reacto

Abstract: Process to prepare simultaneously two or more base oil grades and middle distillates from a mineral crude derived feed, in particular a de-asphalted oil or a vacuum distillate feed or their mixtures, by performing the following steps: (a) hydrocracking the mineral crude derived feed, thereby obtaining an effluent; (b) distillation of the effluent as obtained in step (a) into one or more middle distillates and a full range residue boiling substantially above 340° C., (c) catalytically dewaxing the full range residue by contacting the residue with a dewaxing catalyst comprising a zeolite of the MTW type and a Group VIII metal, thereby obtaining a dewaxed oil; (d) isolating by means of distillation two or more base oil grades from the dewaxed oil obtained in step (c); and (e) isolating a dewaxed gas oil from the dewaxed-oil obtained in step (c); wherein the dewaxed oil as obtained in step (c) comprises between 10 and 40 wt % of a dewaxed heavy gas oil boiling for more than 70 wt % between 370 and 400° C.

Abstract: The process of producing middle distillates from effluents obtained by a Fischer-Tropsch synthesis, comprises a step for hydro-treatment and purification and/or decontamination by passage over a multi-functional guard bed prior to a step of hydrocracking/hydroisomerization. The guard bed reduces the amount of unsaturated compounds, oxygen-containing compounds, particulate mineral solids, and organometallic compounds.

Abstract: Process for the production of a RON isomerate that is at least equal to 80 and that contains less than 1% by weight of aromatic compounds and for co-production of an aromatic fraction that for the most part contains toluene, starting from a fraction with 7 carbon atoms containing paraffins, aromatic compounds and naphthenes.

Abstract: All catalytic process for producing white oils is provided. More particularly, medicinal grade white oils are produced from a process including hydrotreating and/or hydrocracking, catalytic dewaxing followed by hydrofinishing to produce a medicinal white oil.

Abstract: Pentanes are separated from a naphtha boiling range feedstock to provide a gasoline stock having a high RON and low RVP. The isopentane is isomerized to make normal pentane and normal pentane is withdrawn as a feed, preferably for a steam cracker.

Abstract: A process for the hydroisomerization of a waxy feed having a major portion boiling above 650° F. to produce a lubricating base oil having a lower pour point, said process comprising (a) passing the waxy feed along with hydrogen gas through a hydroisomerization zone maintained at a hydrogen partial pressure of between about 100 psia and about 400 psia, said hydroisomerization zone comprising a catalyst bed containing at least two active wax hydroisomerization catalysts, said catalysts comprising at least (i) a first catalyst comprising an active hydrogenation component and a 1-D, 10-ring molecular sieve having a maximum crystallographic free diameter of the channels equal to 6.2 ? units or greater and (ii) a second catalyst comprising an active hydrogenation component and a 1-D, 10-ring molecular sieve having a maximum crystallographic free diameter of the channels equal to 5.

Abstract: A process for the production of triptane, comprises: providing a hydrocarbon feedstock comprising at least 1 vol % of at least one cyclic hydrocarbon comprising a C5 and/or C6 ring; pre-treating the hydrocarbon feedstock by contacting the hydrocarbon feedstock with a catalyst in the presence of hydrogen, under conditions suitable for selectively opening the ring of the cyclic hydrocarbon; and isomerising the pre-treated feedstock by contacting the pre-treated feedstock with an isomerisation catalyst to produce a triptane-containing product stream.

Abstract: For producing very high quality base stock and for simultaneously producing high quality middle distillates, successive hydroisomerisation and catalytic dewaxmg steps are employed wherein the hydroisomerisation is carried out in the presence of a catalyst containing at least one noble metal deposited on an amorphous acidic support, the dispersion of the metal being 20%-100%. The support is preferably an amorphous silica-alumina. Catalytic dewaxing is carried out in the presence of a catalyst containing at least one hydrodehydrogenating element (group VIII) and at least one molecular sieve selected from ZBM-30, EU-2 and EU-11.

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: This invention relates to middle distillates having good cold flow properties, such as the Cold Filter Plugging Point (CFPP) measured in accordance with the IP method (309), and a high Cetane number, as well as to a process for production of such distillates. More particularly, this invention relates to middle distillates produced from a mainly paraffinic synthetic crude which is produced by the reaction of CO and H2, typically by the Fischer-Tropsch (FT) process. The middle distillates of the invention are predominantly isoparaffinic, the isoparaffins being methyl, ethyl and/or propyl branched. The invention also provides a diesel fuel composition including the middle distillates in accordance with the invention. A process for preparing the middle distillates is also included in the invention.

Abstract: A process for producing a high RON naphtha which comprises contacting a hydrocarbon feed stream comprising a mixture of the isomers of C5 and C6 paraffins with a CFI zeolite, such as CIT-5, in an adsorption zone, whereby the branched isomers of the C5 and C6 paraffins are preferentially adsorbed by the CFI zeolite as compared to the straight chain isomers, and recovering a naphtha product from the adsorption zone having a higher RON than the hydrocarbon feed stream, also including a hydroisomerization process and a hydrocracking process.

Abstract: A process for producing a high RON naphtha which comprises contacting a hydrocarbon feed stream comprising a mixture of the isomers of C5 and C6 paraffins with ATS zeolite, such as SSZ-55, in an adsorption zone, whereby the branched isomers of the C5 and C6 paraffins are preferentially adsorbed by the ATS zeolite as compared to the straight chain isomers, and recovering a naphtha product from the adsorption zone having a higher RON than the hydrocarbon feed stream, also including a hydroisomerization process and a hydrocracking process.

Abstract: A process to increase the octane number of a naphtha boiling range feed stock has been developed. Using a dividing wall column, the feed stock is separated into a light fraction comprising compounds containing five carbon atoms or less, an intermediate fraction containing largely compounds having six carbon atoms, and a heavy fraction which comprises compounds containing more than six carbon atoms. The light and heavy fractions are passes to a gasoline blending pool. The intermediate fraction is isomerized to increase the octane number of the intermediate fraction and form an isomerate. The isomerate is passed to the gasoline bending pool.

Abstract: A blend useful as a diesel fuel, as well as a method for its production, comprising a high quality Fischer-Tropsch derived distillate boiling in the range of a diesel fuel blended with a cracked stock boiling in the range of a diesel fuel wherein the final blend contains 10-35 wt. % aromatics and 1-20 wt. % polyaromatics and produces low regulated emissions levels.

Abstract: Clean distillate useful as a diesel fuel or diesel blending stock is produced from Fischer-Tropsch wax by separating wax into heavier and lighter fractions; further separating the lighter fraction and hydroisomerizing the heavier fraction and that portion of the light fraction below about 500° F. The isomerized product is blended with the untreated portion of the lighter fraction.

Abstract: A combination isomerization and liquid phase adsorptive separation process has been developed. In this arrangement, a C5+ naphtha stream is split into a heavy hydrocarbon stream comprising normal heptane and higher boiling hydrocarbons, an isomerization and adsorption zone feed stream comprising pentanes and lower boiling hydrocarbons, and a desorbent stream containing hexanes. The isomerization and adsorption zone feed stream is combined with an isomerization section effluent to form a combined feed to an adsorptive separation section. In the adsorption separation section, normal pentanes are selectively adsorbed on an adsorbent material, and a raffinate stream comprising hexanes and isoparaffins is recovered and passed to a deisohexanizer column. A desorbent stream containing normal hexane is recovered as a sidecut from the deisohexanizer column and is combined with the desorbent stream containing the hexanes from the naphtha splitter to supply the desorbent for the adsorptive separation section.

Abstract: A catalyst composition and process for the conversion of linear and/or branched paraffin hydrocarbons based on the use of an ionic liquid catalyst in combination with a Brønsted Acid, which provides a catalytic composition with an increased activity compared with said ionic liquid. Under suitable reaction conditions this conversion is leading to paraffin hydrocarbon fraction with higher octane number.

Abstract: The present invention discloses a process for producing a low haze heavy base oil including the steps of: (a) providing a heavy waxy feed stream having an initial boiling point greater than 900° F. and having a paraffin content of at least 80%; (b) separating the heavy feed stream into a heavy fraction and a light fraction by a deep cut distillation; and (c) hydroisomerizing the light fraction to produce a low haze heavy base oil.

Abstract: A procedure for the alkylation of isobutane by olefinic hydrocarbons, in which a first hydrocarbon charge (3) rich in isobutane is put in contact with a second hydrocarbon charge rich in light olefins (2), under conditions that will provoke the alkylation of the isobutane by the light olefins, the effluents that emanate from the reaction area in a fractionation column (6) are treated in order to extract therefrom at least a first cut rich in alkylate (7), a second cut rich in normal butane (8) and a third cut rich in isobutane (9), said third cut (9) is then recycled at the entry of the alkylation reaction area. The second cut (8) rich in normal butane is purified (12) so as to lower its content in compounds with 5 or more carbon atoms to a value that is less than or equal to 5% by weight, the cut thus purified (14) is treated in an isomerization reactor (16) of normal butane to isobutane, this cut is then recycled (21) at the entry of the alkylation effluents fractionation column (6).

Abstract: An improved process for producing very high quality base stock and for simultaneous production of high quality middle distallates, comprising successive hydroisomerisation and catalystic dewaxing steps wherein hydroisomerisation is carried out in the presence of a catalyst containing at least one noble metal deposited on an amorphous acidic support, the dispersion of the metal being less than 20%. The support is preferably an amorphous silica-alumina. Catalytic dewaxing is carried out in the presence of a catalyst containing at least one hydrodehydrogenating element (group VIII) and at least one molecular sieve (preferably zeolite). The sieve is preferable selected from NU-10, EU-1, EU-13, zeolite and ferrierite.

Abstract: A process for opening naphthenic rings of naphthenic ring-containing compounds, along with catalysts which can be used in that process. The naphthene ring opening catalyst is a catalyst comprising at least one Group VIII metal selected from Ir, Pt, Rh, and Ru, wherein these metals are supported on an alkali metal or alkaline-earth metal modified support in an amount effective for opening a naphthene ring-containing compound at a tertiary carbon site.

Abstract: A premium synthetic lubricating oil base stock having a high VI and low pour point is made by hydroisomerizing a Fischer-Tropsch synthesized waxy, paraffinic feed wax and then dewaxing the hydroisomerate to form a 650-750° F.+ dewaxate. The waxy feed has an initial boiling point in the range of about 650-750° F., from which it continuously boils up to at least 1050° F. and has a T90−T10 temperature difference of at least 350° F. The feed is preferably hydroisomerized without any pretreatment, other than optional fractionation. The 650-750° F.+ dewaxate is fractionated into two or more base stocks of different viscosity.

Abstract: A process for synthesis of lower isoparaffins from synthesis gas that is a mixture of hydrogen and carbon monoxide, wherein straight chain hydrocarbons are synthesized while isoparaffins and isoolefins are also produced through decomposition of hydrocarbons having a higher carbon number by use of a solid acid catalyst in the first stage, and isoparaffins are synthesized in the second stage. The straight chain hydrocarbons are produced by contacting the synthesis gas with a Fischer-Tropsch synthesis catalyst that is mixed with a solid acid catalyst for mainly hydrocracking long chain hydrocarbons. The isoparaffins are produced by contacting the straight chain hydrocarbons synthesized in the first stage, with a mixture of a hydrogenation catalyst for hydrogenating olefins and a solid acid catalyst for hydrocracking and isomerizing the straight chain hydrocarbons.

Abstract: Construction and operational costs of recovering the high-octane components of an isomerization raffinate product of a simulated moving bed adsorptive separation process units are reduced by employing a dividing wall column to perform the separation. The raffinate product stream is passed into the column at an intermediate point on the first side of the dividing wall, with the column delivering the low-octane raffinate components as a sidedraw from the opposite side of the dividing wall. A stream of higher octane components are removed both as an overhead stream and a bottoms stream. The sidedraw may be recycled to the isomerization zone.

Abstract: For producing three effluents which are respectively rich in straight chain paraffins, in mono-branched paraffins, and in di-branched and tri-branched paraffins possibly with naphthenic and/or aromatic compounds, from C5-C8 cuts or intermediate cuts (C5-C7, C6-C8, C7-C8, C6-C7, C7 or C8), comprising paraffinic and possibly naphthenic and/or aromatic hydrocarbons, and in some cases olefinic hydrocarbons, a chromatographic separation process uses a separation zone operating by adsorption. The process of the invention is of particular application when coupled with a hydro-isomerization process, which selectively recycles straight chain and mono-branched paraffins, necessary for paraffins containing at least 7 carbon atoms.

Abstract: For producing three effluents which are respectively rich in straight chain paraffins, in mono-branched paraffins, and in di-branched and tri-branched paraffins possibly with naphthenic and/or aromatic compounds, from C5-C8 cuts or intermediate cuts (C5-C7, C6-C8, C7-C8, C6-C7, C7 or C8), comprising paraffic and possibly naphthenic, aromatic and olefinic hydrocarbons, the separation process of the invention uses at least two separation units operating either by adsorption or by permeation. It is of particular application when coupled with a hydro-isomerization process, which selectively recycles straight chain and mono-branched paraffins, necessary with paraffins containing more than 7 carbon atoms.

Abstract: A process for isomerizing hydrocarbons is disclosed. The process includes contacting, under reaction conditions, a hydrocarbon-containing fluid containing a saturated hydrocarbon, preferably a normal paraffin containing in the range of from about 4 carbon atoms to about 10 carbon atoms per molecule, with a composition in a single-stage reaction zone. The process includes isomerizing such saturated hydrocarbon to thereby provide a product containing an isomerized hydrocarbon. The composition used in the process contains a zeolite and a metal carbide. The composition can be produced by combining a metal, preferably such metal is in a metal compound, with the zeolite to thereby provide a metal-promoted zeolite. The metal-promoted zeolite is then calcined or steamed followed by contacting the resulting zeolite with a hydrocarbon, preferably in the presence of hydrogen, to thereby provide a carburized metal-promoted zeolite.

Abstract: A lubricating base stock useful for forming lubricants such as a multigrade automotive oils, automatic transmission oils, greases and the like is prepared by hydroisomerizing a waxy hydrocarbon feed fraction having an initial boiling point in the 650-750.degree. F. range and an end point of at least 1050.degree. F., synthesized by a slurry Fischer-Tropsch hydrocarbon synthesis process. The hydroisomerization forms a hydroisomerate containing the desired base stock which is recovered, without dewaxing the hydroisomerate. The hydroisomerization is conducted at conditions effective to convert at least 67 wt. % of the 650-750.degree. F.+ waxy feed hydrocarbons to lower boiling hydrocarbons. When combined with a standard lubricant additive package, these base stocks have been formed into multigrade automotive crankcase oils, transmission oils and hydraulic oils meeting the specifications for these oils.