Abstract: A process is disclosed for the isomerization of a C.sub.4 feedstock and a C.sub.5 -C.sub.6 feedstock that reduces equipment and operating expenses by utilizing a process flow scheme that provides beneficial heat integration and facilitates the use of a common recovery zone while permitting a wide variation in the relative ratio of a C.sub.4 to a C.sub.5 -C.sub.6 feedstock. The isomerization of the C.sub.4 feedstock takes place in a separate reaction zone. The effluent from the C.sub.4 isomerization zone is heat exchanged against or mixed with the C.sub.5 -C.sub.6 feedstock ahead of an additional isomerization zone that converts the C.sub.5 -C.sub.6 hydrocarbons, and if present, normal C.sub.4 hydrocarbons, to more highly branched hydrocarbons. Effluents from both isomerization zones enter a common separation section that removes light gases from the isomerate product.This invention simplifies the simultaneous isomerization of C.sub.4 and C.sub.5 -C.sub.6 feedstocks.

Abstract: A combination isomerization and liquid phase adsorptive separation process is given increased efficiency and cost effectiveness while also improving the product quality by eliminating the columns for the separation of desorbent material from extract and raffinate streams. In this arrangement a C.sub.5 + naphtha stream is split into a heavy hydrocarbon stream comprising normal hexane and higher boiling hydrocarbons and an isomerization zone feedstream comprising isohexane and lower boiling hydrocarbons. The heavy hydrocarbon stream goes directly to a deisohexanizer column. The isomerization zone feedstream is combined with an excess desorbent stream and the extract stream from an adsorptive separation section to form a combined feed. Hydrocarbons in the combined feed are isomerized and after stabilization pass directly into the adsorption section.

Abstract: A combination isomerization and liquid phase adsorptive separation process is given increased efficiency and cost effectiveness by the elimination of a column for the separation of desorbent material from selectively retained components. By decreasing the ratio of normal paraffin desorbent to the selective pore volume circulation rate, the extract column can be eliminated without providing other means for the rejection or recovery of desorbent material. This reduction in the ratio of normal paraffin desorbent to selective pore volume circulation rate has been found not to decrease the recovery from the adsorption section. The elimination of the column provides a substantial decrease in the cost of the equipment to operate a combination isomerization zone and liquid phase adsorption section. In an alternate arrangement, the extract column is replaced with a deisohexanizer column. The deisohexanizer column can be used to produce a C.sub.5 -C.sub.6 product stream having research octane numbers of 93 or greater.

Abstract: A combined process for hydrotreating and isomerizing a C.sub.4 -C.sub.7 feedstock is simplified and made more efficient by the use of a common hydrogen source and low hydrogen to hydrocarbon ratio in both the hydrotreating and isomerization steps of the invention. The method supplies hydrogen to a combined hydrotreatment and isomerization process for the isomerization of a feed stream comprising C.sub.4 -C.sub.7 hydrocarbons. The hydrocarbon feed stream contains sulfur and oxygen contaminants and is combined with a hydrogen-containing stream in an amount that produces a maximum hydrogen to hydrocarbon ratio of 0.9 stdm.sup.3 m.sup.3 (50 SCFB). The hydrotreater feed is contacted in a hydrotreater reactor with a catalyst comprising a Group VIB metal and a Group VIII metal on an alumina support.

Abstract: An improved catalyst particle is disclosed for the conversion of hydrocarbons which comprises a refractory inorganic-oxide support, a Friedel-Crafts metal halide, and a surface-layer platinum-group metal component, wherein the concentration of platinum-group metal component on the surface layer of each catalyst particle is at least 1.5 times the concentration in the central core of the catalyst particle. An isomerization process also is disclosed which is particularly effective for the conversion of C.sub.4 -C.sub.7 alkanes.

Abstract: Waxy distillates, or raffinates containing from as little as 10% wax but more typically about 30% wax or more are upgraded by a process comprising the steps of hydrotreating the waxy oil under conditions which convert less than 20% of the feed into products boiling lower than the feed to reduce the sulfur and nitrogen content of the oil followed by hydroisomerizing the hydrotreated waxy oil to reduce the wax content and increase the viscosity index. This oil having a waxy content of less than 30%, preferably less than 25%, can now be more easily dewaxed using conventional solvent dewaxing procedures. The advantage of the present process resides in the increased yield and/or stability of oil as compared to other upgrading, dewaxing processes which convert wax to light products. The isomerization catalyst is preferably a low fluorine content catalyst, more preferably a noble metal on 0.1 to less than 2 wt % fluorine on alumina catalyst, most preferably a noble Group VIII metal (e.g.

Abstract: Fischer-Tropsch wax is converted to a lubricating oil having a high viscosity index and a low pour point by first hydrotreating the wax under relatively severe conditions and thereafter hydroisomerizing the hydrotreated wax in the presence of hydrogen on a particular fluorided Group VIII metal-on-alumina catalyst. The hydroisomerate is then dewaxed to produce a premium lubricating oil base stock.

Abstract: A combined process for hydrotreating and isomerizing a C.sub.4 -C.sub.7 feedstock is simplified and made more efficient by the use of a common hydrogen source and low hydrogen to hydrocarbon ratio in both the hydrotreating and isomerization steps of the invention. The method supplies hydrogen to a combined hydrotreatment and isomerization process for the isomerization of a feed stream comprising C.sub.4 -C.sub.7 hydrocarbons. The hydrocarbon feed stream contains sulfur and oxygen contaminants and is combined with a hydrogen-containing stream in an amount that produces a maximum hydrogen to hydrocarbon ratio of 0.9 stdm.sup.3 /m.sup.3 (50 SCFB). The hydrotreater feed is contacted in a hydrotreater reactor with a catalyst comprising a Group VIB metal and a Group VII metal on an alumina support.

Abstract: Butane is isomerized in the presence of substantial quantities of C.sub.5 and C.sub.6 hydrocarbons using an alumina catalyst having from 0.01 to 0.25 wt. % platinum and 2 to 10 wt. % of a chloride component. The process operates at temperatures ranging from 180.degree.-225.degree. C. (355.degree.-435.degree. F.) and produces a high yield of isobutane while at the same time providing a high level of C.sub.5 and C.sub.6 hydrocarbon isomerization without a significant increase in yield loss of C.sub.5 and higher hydrocarbons. The process can be carried out in a single reaction zone or in a series of reaction zones to increase the production of isoparaffins.

Abstract: A process for producing a pumpable syncrude from a Fischer-Tropsch wax by fractionating the wax into relatively low boiling fraction containing oxygenate compounds and a relatively high boiling fraction which is substantially free of oxygenate compounds and thereafter isomerizing/hydrocracking the low boiling fraction in the presence of hydrogen and a fluorided Group VIII metal-on-alumina catalyst. The preferred Group VIII metal is platinum.The pumpable syncrude is thereafter fractionated to produce a low boiling fraction which is thereafter isomerized/hydrocracked in the presence of hydrogen and a fluorided Group VIII metal-on-alumina catalyst to produce upgraded middle distillate fuel products. The preferred catalyst for middle distillate production is a fluorided platinum-on-alumina catalyst where a major portion of the fluoride within the catalyst is present as aluminum fluoride hydroxide hydrate.

Abstract: A process for the isomerization of C.sub.4 -C.sub.6 paraffins that uses a highly active catalyst to isomerize the feed in the presence of very little hydrogen. The process is characterized by good stability and high conversion with effluent hydrogen to hydrocarbon ratios of 0.05 or less. Continued operation at low hydrogen concentrations is made possible by the remarkably low coking tendency of the catalyst, especially during periods of temporary sulfur deactivation. The low hydrogen to hydrocarbon ratio simplifies the process and makes it cheaper to operate by eliminating facilities for the recovery and recycle of hydrogen.

Abstract: A C.sub.4 -C.sub.6 feed to an isomerization zone containing substantial amounts of cyclic hydrocarbons is contacted with a high chloride, platinum alumina catalyst to simultaneously open cyclic hydrocarbon rings and isomerize paraffins to more highly branched paraffins. The process can operate at relatively low severity conditions that provide favorable equilibrium conditions for isoparaffin conversion. The ring opening is also obtained without excessive generation of light hydrocarbons. Multiple stage reaction zones may be used to operate the first stage at slightly higher severity than the second stage to maximize ring opening and obtain favorable equilibrium of iso to normal paraffins.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with an acidic multimetallic catalytic composite comprising a combination of catalytically effective amounts of a platinum group component, a cobalt component, a tin component, a phosphorus component and a halogen component with a porous carrier material. The platinum group, cobalt, tin, phosphorus and halogen components are present in the multimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal, about 0.05 to about 5 wt. % cobalt, about 0.01 to about 5 wt. % tin, about 0.01 to about 5 wt. % phosphorus and about 0.1 to about 3.5 wt. % halogen. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and a hydrogen stream are contacted with the acidic multimetallic catalyst disclosed herein at reforming conditions.

Abstract: These catalysts comprise:A refractory oxide-mineral carrier;a halogen element, present in combined form; and,in free or combined form,(a) a platinum-group metal, and(b) tin.They are characterized in that they contain, moreover, a metal from groups Ia and IIa of the periodic table of the elements.Specifically, said metal from groups Ia and IIa may be sodium, lithium, potassium, calcium or barium.

Abstract: Isomerizable hydrocarbons are isomerized using a catalytic composite comprising a combination of a catalytically effective amount of a pyrolyzed rhenium carbonyl component with a porous carrier material containing a uniform dispersion of catalytically effective amounts of a platinum group component, which is maintained in the elemental metallic state during the incorporation and pyrolysis of the rhenium carbonyl component, of a tin component, and of a halogen component and from about 1 to about 100 weight percent of a Friedel-Crafts metal halide calculated on a Friedel-Crafts metal halide-free basis.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a novel activated multimetallic catalytic composite comprising a combination of a catalytically effective amount of a pyrolyzed ruthenium carbonyl component with a porous carrier material containing a uniform dispersion of a catalytically effective amount of a platinum group component, which is maintained in the elemental metallic state during the incorporation and pyrolysis of the ruthenium carbonyl component, and of a rhenium component. In a highly preferred embodiment, this novel catalytic composite also contains a catalytically effective amount of a halogen component. The platinum group component, pyrolyzed ruthenium carbonyl component, rhenium component and optional halogen component are preferably present in the multimetallic catalytic composite in amounts, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % of the uniformly dispersed platinum group metal, about 0.01 to about 2 wt.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a novel attenuated superactive multimetallic catalytic composite comprising a combination of a catalytically effective amount of a pyrolyzed rhenium carbonylcomponent with a porous carrier material containing a uniform dispersion of a catalytically effective amount of a platinum group component, which is maintained in the elemental metallic state during the incorporation and pyrolysis of the rhenium carbonyl component, and of a tin component. In a highly preferred embodiment, this novel catalytic composite also contains a catalytically effective amount of a halogen component. The platinum group component, pyrolyzed rhenium carbonyl component, tin component and optional halogen component are preferably present in the multimetallic catalytic composite in amounts, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal, about 0.01 to about 5 wt. % rhenium, about 0.005 to about 5 wt.

Abstract: Isomerizable light paraffinic hydrocarbon feeds are isomerized in an improved process using a particular super-chlorided reforming catalyst under isomerizing conditions. A chloride source in the feed stabilizes the catalyst. This process provides for a material octane improvement of the feed without excessive loss thereof to normally gaseous hydrocarbons.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a novel superactive multimetallic catalytic composite comprising a reduced combination of a catalytically effective amount of an adsorbed rhenium-oxygen complex with a porous carrier material containing a catalytically effective amount of a conventional rhenium component and a uniform dispersion of a catalytically effective amount of a platinum group component which is maintained in the elemental metallic state during the adsorption and reduction of the rhenium-oxygen complex. A key feature associated with the preparation of the subject catalytic composite is reaction of a rhenium-oxygen complex with a porous carrier material containing a conventional rhenium component and a uniform dispersion of a platinum group component maintained in the elemental state, whereby the interaction of the rhenium-oxygen complex with the platinum group metal moiety is maximized due to the platinophilic (i.e.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a novel superactive multimetallic catalytic composite comprising a combination of a catalytically effective amount of a pyrolyzed rhenium carbonyl component with a porous carrier material containing a catalytically effective amount of a conventional rhenium component and a uniform dispersion of a catalytically effective amount of a platinum group component, which is maintained in the elemental metallic state during the incorporation of the rhenium carbonyl component. A key feature associated with the preparation of the subject catalytic composite is reaction of a rhenium carbonyl complex with a porous carrier material containing a conventional rhenium component and a uniform dispersion of a platinum group metal maintained in the elemental state, whereby the interaction of the rhenium carbonyl complex with the platinum group moiety is maximized due to the platinophilic (i.e.

Abstract: Isomerizable hydrocarbons including paraffins, cycloparaffins, olefins and alkyl aromatics are isomerized by contacting the hydrocarbon at isomerization conditions with a catalytic composite comprising a platinum group metal on an alpha-alumina monohydrate support wherein said support is prepared by admixing an alpha-alumina monohydrate with an aqueous amoniacal solution having a pH of at least about 7.5 to form a stable suspension and commingling said suspension with a salt of a strong acid to form an extrudable paste or dough. Upon extrusion, the extrudate is dried and calcined to form said alumina support.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a novel activated multimetallic catalytic composite comprising a combination of a catalytically effective amount of a pyrolyzed ruthenium carbonyl component with a porous carrier material containing a uniform dispersion of a catalytically effective amount of a platinum group component which is maintained in the elemental metallic state. In a highly preferred embodiment, this novel catalytic composite also contains a catalytically effective amount of a halogen component. The platinum group component, pyrolyzed ruthenium carbonyl component and optional halogen component are preferably present in the multimetallic catalytic composite in amounts, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % of the uniformly dispersed platinum group metal, about 0.01 to about 2 wt. % of carbonyl-derived ruthenium and about 0.1 to about 3.5 wt. % of halogen.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a novel attenuated superative multimetallic catalytic composite comprising a combination of a catalytically effective amount of a pyrolyzed rhenium carbonyl component with a porous carrier material containing a uniform dispersion of catalytically effective amounts of a platinum group component, which is maintained in the elemental metallic state, and of a tantalum component. In a highly preferred embodiment, this novel catalytic composite also contains a catalytically effective amount of a halogen component. The platinum group component, pyrolyzed rhenium carbonyl component, tantalum component and optional halogen component are preferably present in the multimetallic catalytic composite in amounts, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal, about 0.01 to about 5 wt. % rhenium, about 0.01 to about 5 % tantalum and about 0.1 to about 3.5 wt. % halogen.