Abstract: Disclosed is a method of manufacturing high-quality naphthenic base oil by subjecting, as a feedstock, light cycle oil (LCO) and slurry oil (SLO) obtained through fluidized catalytic cracking (FCC) to hydrotreating and dewaxing.

Abstract: Processes for reforming of naphtha feedstocks are described. Briefly, a two stage naphtha reforming process is described. The first stage uses a low acidity beta zeolite catalyst under relatively mild reforming conditions to form an effluent. This effluent is passed to a subsequent stage where further reforming occurs using a catalyst containing ZSM-5 zeolite. The second stage is run under mild reforming conditions. The low pressures employed in the reforming process described maximize liquid product yield by avoiding unwanted cracking reactions and production of light products.

Abstract: The process as described herein produces a moderately aromatic isoparaffinic base oil from a distillate range product. This process comprises: (a) providing a distillate range paraffin feed comprising paraffins and cycloparaffins; (b) mildly reforming the distillate range paraffin feed to convert at least a portion of the cycloparaffins to alkylaromatics and provide a mildly reformed distillate range stream; (c) treating a stream comprising the mildly reformed distillate range stream in a molecular redistribution reactor to provide a distributed stream; (d) dewaxing at least a portion of the distributed stream to provide a dewaxed stream; (e) combining at least a portion of the dewaxed stream with the stream to be processed in the molecular redistribution reactor to provide the distributed stream; and (f) isolating a moderately aromatic isoparaffinic base oil from the dewaxed stream.

Abstract: A process for the fluid catalytic cracking of mixed hydrocarbon feeds from different sources is described, such as feeds A and B of different crackability, the process being especially directed to obtaining light fractions such as LPG and comprising injecting feed A in the base of the riser reactive section and feed B, of lower crackability, at a height between 10% and 80% of the riser, with feed B comprising between 5% and 50% of the total processed feed. The process requires that the feeds present differences in the contaminant content, improved dispersion of feeds A and B and feed B injection temperature same or higher than that of feed A.

Abstract: Process to prepare a haze free base oil having a cloud point of below 0° C. and a kinematic viscosity at 100° C. of greater than 10 cSt by performing the following steps: (a) hydroisomerisation of a Fischer-Tropsch synthesis product, (b) isolating one or more fuel products and a distillation residue, (c) reducing the wax content of the residue by contacting the feed with a hydroisomerization catalyst under hydroisomerization conditions, and (d) solvent dewaxing the product of step (c) to obtain the haze free base oil.

Abstract: The present invention relates to a multistage reforming process to produce a high octane product. A naphtha boiling range feedstock is processed in a multi-stage reforming process, in which said process involves at least 1) a penultimate stage for reforming the naphtha feedstock to produce a penultimate effluent 2) a separation step for separating the penultimate effluent into at least an intermediate stream and a heavy stream based on boiling point and 3) a final stage for further reforming the intermediate stream.

Abstract: The invention concerns a regenerative reforming process in 3 or 4 reforming reactors, wherein: for 3 reactors, the catalyst distribution between the 3 reactors is such that in the range 30% to 36% by weight of catalyst is present in each of the 3 reactors; for 4 reactors: the catalyst distribution between the 4 reactors is such that in the range 22% to 28% by weight of catalyst is present in each of the 4 reactors.

Abstract: The present invention provides an improvement in the process of producing hydrogen from hydrocarbon-containing streams. A cyclic reforming process, referred to as pressure swing reforming, provides an efficient means for producing a hydrogen containing synthesis gas for fuel cell applications. Pressure swing reforming may be integrated with shift reactions, preferential oxidation, and membrane separation, achieving thermal and material efficiencies relative to conventional hydrogen production. In one embodiment, at least some synthesis gas which is first produced in the pressure swing reforming process is combusted with air to provide the heat for the regeneration step of the pressure swing reforming process.

Abstract: A method of filtering contaminants from a chemical process stream is disclosed. The method includes a step of passing the process stream over a filtration medium including a plurality of discrete filtration elements, each element having parallel first and second faces and a multi-cellular structure of substantially uniform parallel channels running from the first face to the second face. The cross-sectional shape of the channels preferably defines a polygon having angles less than or equal to 90°.

Abstract: A process for reforming a hydrocarbon feed containing precursors of ethylbenzene, e.g., C8 isoalkane and/or C8 isoalkene precursors of ethylbenzene, that results in the formation of reduced amounts of ethylbenzene. The process is carried out in a catalytic reforming unit comprised of a plurality of operatively connected reactors comprising at least one lead reforming reactor and a tail reforming reactor. The process is carried out by reforming the feed in at least one lead reactor which contains a first reforming catalyst and a catalyst effective for converting ethylbenzene and further reforming the product of the lead reactor in the tail reactor that contains a second reforming catalyst.

Abstract: Processes for reforming, and in particular aromatising, hydrocarbons from a petroleum source may be carried out by contacting the hydrocarbons with a catalyst of a zeolite KL impregnated with a metal promotor such as platinum, in which the zeolite crystals are of hockeypuck shape. The processes have a good yield and selectivity for the desired reformed products and the catalyst is stable, is associated with a low rate of coke formation, and has a long catalytically active life before regeneration is required.

Abstract: This patent presents a two-stage process for production of high-octane gasoline from a hydrocarbon stream comprising C4-C12 hydrocarbon mixtures of paraffins, optionally including cycloalkanes, aromatics and olefins. During the first step linear molecules are activated and converted predominantly to mono-branched isomers. Present cyclic molecules and olefins are hydrogenated, but conversion must be sufficiently low to avoid ring opening. Only such (low) amount of multi-branched isomers is formed in the first reaction zone that extent of cracking is still acceptable. Concentration of multi-branched isomers is consecutively increased in the second step. Reaction of mono-branched isomers requires lower activation energy than cracking and isomerisation of linear molecules. Monomethyl-paraffins readily react to their multi-branched counterparts with a high selectivity under mild reaction conditions with catalysts having a Hammet acidity value lower than −10 at temperature of maximum 100° C.

Abstract: Systems, processes, and reactors for the catalytic reforming of naphtha are provided. Embodiments of the invention include reactors comprising monolithic catalyst having honeycomb-type structure that allows for improved efficiency, productivity, and reaction selectivity over conventional catalytic reforming technology.

Abstract: A substantially water-free hydrocarbon feed is charged to a multiple-reactor reformer system being operated under reforming conditions and comprising at least two reformer reactors serially connected in fluid-flow communication and each containing a reformer catalyst; and, simultaneously with the charging step, a chloriding agent is sequentially introduced, without simultaneously introducing water, immediately upstream from the inlets of all the reformer reactors in an amount and for a period of time that are effective to inhibit the deactivation of the reformer catalyst.

Abstract: The patent application discloses an integrated process for reformate upgrading. Such a process enables production of a high value product slate, by incorporating the step of reforming along with reaction/diffusion with a zeolite.

Abstract: Process for the catalytic steam reforming of a hydrocarbon feed stock with a content of higher hydrocarbons and oxygen comprising the steps of catalytic pre-reforming the feed stock and steam reforming the pre-reformed feed stock, the pre-reforming step is carried out in presence of a fixed bed catalyst comprising at least a portion of a noble metal catalyst being active in oxidation of hydrocarbons to carbon oxides and conversion of higher hydrocarbons to methane, wherein the noble metal catalyst is supported on a carrier of MgO and/or MgAl2O4 spinel.

Abstract: A process combination is disclosed to selectively upgrade hydrocarbons in a manner to essentially eliminate olefins in product from the combination. Preferably the hydrocarbons comprise naphtha which is reformed to upgrade its octane number and/or to produce aromatic intermediates, followed by hydrogenation of olefins in the reformate. Olefin saturation optimally is effected by catalytic reaction on an olefin-containing reformate taken at an intermediate point from the effluent side of the reforming-process feed-effluent heat exchanger. Saturation is performed in a defined temperature range which results in selective hydrogenation.

Abstract: The patent application discloses an integrated process for reformate upgrading. Such a process enables production of a high value product slate, by incorporating the step of reforming along with reaction/diffusion with a zeolite.

Abstract: A process combination is disclosed to selectively upgrade naphtha to obtain a component for blending into gasoline. A naphtha feedstock is subjected to formation of olefins from paraffins using a nonacidic catalyst followed by aromatization of the resulting olefin-containing product to obtain improved yields of an aromatics-rich, high-octane gasoline product.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a first bifunctional-catalyst reforming zone, a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic zeolite, and a terminal bifunctional catalyst reforming zone. The first and terminal bifunctional catalysts preferably comprise a lanthanide-series metal component. The process combination permits higher severity, higher aromatics yields and/or increased throughput relative to the known art, and is particularly useful in connection with moving-bed reforming facilities with continuous catalyst regeneration.

Abstract: This process relates to reforming a full-boiling range hydrocarbon feed in two parallel stages while maximizing the catalyst life of the heavy cut reformer and/or reducing the complexity of the plant by preferentially sending the higher purity Aromax.RTM. hydrogen to the heavy cut reformer.

Abstract: This invention is a reforming process that employs at least two moving bed reaction zones. One of the reaction zones, called the lead reaction zone, passes catalyst particles and a hydrocarbon-containing effluent to the other reaction zone, which operates at an inlet temperature that is at least 60.degree. F. (33.degree. C.) hotter than the lead reaction zone. In a preferred embodiment, this invention employs no heating between the combined feed exchanger and the lead reaction zone. This invention is particularly applicable to reforming processes that employ continuous regeneration sections.

Abstract: A full boiling hydrocarbon feed is reformed to enhance para-xylene and benzene yields. First, the hydrocarbon feed is separated into a C.sub.5- cut, a C.sub.6 -C.sub.7 cut, and a C.sub.8+ cut. The C.sub.6 -C.sub.7 cut has less than 5 lv. % of C.sub.8+ hydrocarbon, and the C.sub.8+ cut has less than 10 lv. % of C.sub.7- hydrocarbon. The C.sub.6 -C.sub.7 cut is subjected to catalytic aromatization at elevated temperatures in a first reformer in the presence of hydrogen and using a non-acidic catalyst comprising at least one Group VIII metal and a non-acidic zeolite support to produce a first reformate stream; and the C.sub.8+ cut is subjected to catalytic aromatization at elevated temperatures in a second reformer in the presence of hydrogen and using an acidic catalyst comprising at least one Group VIII metal and a metallic oxide support to produce a second reformate stream. Less than 20 wt. % of the total amount of C.sub.

Abstract: A catalytic reforming process comprises a prereactor which provides an intermediate stream to a riser reactor with multiple catalyst injection points to obtain high aromatics yields from a naphtha feedstock. Product from the riser reactor typically is discharged into a fluidized-bed reforming reactor, in which the reforming reaction is completed and catalyst is separated from hydrogen and hydrocarbons. Hydrocarbons from the reactor are separated to recover an aromatized product. Catalyst is regenerated to remove coke and reduced for reuse in the reforming process.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic L-zeolite and an aromatics-isomerization zone containing a catalyst comprising a medium-pore molecular sieve, a platinum-group metal and a refractory inorganic oxide. Optionally, the zeolitic-reforming zone is preceded by a continuous-reforming zone associated with continuous catalyst regeneration, The process combination features high selectivity in producing a high-purity BTX product from naphtha.

Abstract: A large pore volume catalyst was used for reforming heavy cracked naphtha. The average pore diameter is preferably between about 110 to 150 Angstroms. Improved catalytic stability and improved liquid yield was achieved. As a result of the improvement a 101 RON debutanized naphtha reformate is produced at a reduced catalyst aging rate.

Abstract: A hydrocarbon feed is reformed to enhance para-xylene yield and to minimize ethylbenzene production. The hydrocarbon feed is subjected to catalytic aromatization at elevated temperatures in the presence of hydrogen, using a non-acidic catalyst having at least one Group VIII metal on a non-acidic zeolite support, to produce a reformate stream containing ethylbenzene and xylenes in which the para-xylene content of the xylene fraction is less than equilibrium. Then, at least some of the reformate is reacted at elevated temperatures in the presence of hydrogen, using an intermediate pore size zeolitic catalyst having a modifier in the absence of a Group VIII metal, to isomerize the non-equilibrium xylene fraction. The modifier can be magnesium, calcium, barium, or phosphorus. At least 20 wt. % of the ethylbenzene in the reformate is converted by hydrodealkylation.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a first bifunctional-catalyst reforming zone, a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic zeolite, and a terminal bifunctional catalyst reforming zone. The first and terminal bifunctional catalysts preferably comprise a lanthanide-series metal component. The process combination permits higher severity, higher aromatics yields and/or increased throughput relative to the known art, and is particularly useful in connection with moving-bed reforming facilities with continuous catalyst regeneration.

Abstract: The invention concerns a jet engine fuel having the following characteristics:i) distilling range from 140 to 300.degree. C.;ii) cis-decalin/trans-decalin ratio greater than 0.2;iii) aromatics content less than 22% by volume;iv) sulfur content less than 100 ppm, andv) lower heating value per unit volume greater than 34.65 Mj/liter.Also process for making the same wherein for example a cut from catalytic cracking distilling between 140 and 300.degree.0 C. is subjected to a hydrotreatment step and then to a dearomatization step.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a continuous-reforming zone, consisting essentially of a moving-bed catalytic reforming zone and continuous regeneration of catalyst particles, and a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic zeolite. The process combination permits higher severity, higher aromatics yields and/or increased throughput in the continuous-reforming zone, thus showing surprising benefits over prior-art processes, and is particularly useful in upgrading existing moving-bed reforming facilities with continuous catalyst regeneration.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a first bifunctional-catalyst reforming zone, a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic zeolite, and a terminal bifunctional catalyst reforming zone. The process combination permits higher severity, higher aromatics yields and/or increased throughput relative to the known art, and is particularly useful in connection with moving-bed reforming facilities with continuous catalyst regeneration.

Abstract: This is a process for upgrading a petroleum naphtha fraction. The naphtha is subjected to reforming and the reformate is cascaded to a benzene and toluene synthesis zone over a benzene and toluene synthesis catalyst comprising a molecular sieve of low acid activity. The preferred molecular sieve is steamed ZSM-5. The benzene and toluene synthesis zone is operated under conditions compatible with the conditions of the reformer such as pressures of above about 50 psig (446 kPa) and temperatures above about 800.degree. F. (427.degree. C). In one aspect of the invention, the benzene and toluene synthesis catalyst includes a metal hydrogenation component such as cobalt, nickel, platinum or palladium. In one mode of operation, the benzene and toluene synthesis catalyst replaces at least a portion of the catalyst of the reformer. The process produces a product containing an increased proportion of benzene and toluene, and a reduced proportion of C8 aromatics, particularly ethylbenzenes, as compared to the reformate.

Abstract: A hydrocarbon feedstock is catalytically reformed in a process which comprises at least three catalyst zones. The feedstock contacts a catalyst comprising platinum, a halogen, and a metal promoter on a solid catalyst support in a first catalyst zone. Effluent from the first catalyst zone contacts a catalyst comprising platinum, germanium and halogen on a solid catalyst support in an intermediate catalyst zone to obtain an intermediate effluent, which contacts a catalyst having the essential absence of germanium and comprising platinum, halogen and a metal promoter on a solid catalyst support in a terminal catalyst zone to obtain a reformate.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a continuous-reforming zone associated with continuous catalyst regeneration, a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic L-zeolite and an aromatics-isomerization zone containing a catalyst comprising a platinum-group metal, a metal attenuator and a refractory inorganic oxide. The process combination features high selectivity in producing a high-purity BTX product from naphtha.

Abstract: A hydrotreating apparatus comprising (a') a fixed-bed reactor packed with a hydrotreating catalyst for hydrotreating a heavy oil and (b') a suspended-bed reactor packed with a hydrotreating catalyst for further hydrotreating the heavy oil hydrotreated in the fixed-bed reactor. According to the apparatus of the present invention, (a) feeding of a heavy oil to a fixed-bed reactor is disclosed packed with a hydrotreating catalyst to thereby effect hydrotreating of the heavy oil and (b) feeding of the heavy oil hydrotreated in the fixed-bed reactor to a suspended-bed reactor packed with a hydrotreating catalyst to thereby effect further hydrotreating of the heavy oil can be conducted, and therefore the period of hydrotreating of the heavy oil can be prolonged.

Abstract: A process combination is disclosed to selectively upgrade naphtha to obtain an isoparaffin-rich product for blending into gasoline. A naphtha feedstock is subjected to ring cleavage to convert naphthenes to paraffins using a nonacidic catalyst followed by isomerization of paraffins to obtain an increased proportion of isoparaffins. Ring cleavage also may be effected on the product of isomerization and separation by fractionation or adsorption.

Abstract: Naphthenic rings in naphthenic ring-containing compounds in a feedstream are selectively opened wherein at least about 50 wt. % of the ring compounds in the feedstream are characterized as containing at least one C.sub.6 ring having at least one substituent containing 3 or more carbon atoms. The naphthenic rings are opened without significant dealkylation of any pendant substituents on the ring. The feedstream, containing such compounds, is contacted with a supported catalyst containing a metal selected from Ir, Ru, or a mixture thereof, which catalyst when reacted with a feed comprised of 20 wt. % n-butylcyclohexane in heptane diluent will result in: a) at least a 10% yield of C.sub.10 paraffin yield/%C.sub.10 ring disappearance.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a continuous-reforming zone, consisting essentially of a moving-bed catalytic reforming zone and continuous regeneration of catalyst particles, and a zeolitic-reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic zeolite. The process combination permits higher severity, higher aromatics yields and/or increased throughput in the continuous-reforming zone, thus showing surprising benefits over prior-art processes, and is particularly useful in upgrading existing moving-bed reforming facilities with continuous catalyst regeneration.

Abstract: This invention deals with a process for converting aliphatic C.sub.2 -C.sub.6 hydrocarbons into C.sub.6.sup.+ aromatics and C.sub.3.sup.= /C.sub.4.sup.= olefins. The process involves combining dehydrocyclodimerization (DHCD) with dehydrogenation. Thus, the feedstream is first sent to a DHCD zone which produces an effluent stream which contains C.sub.6.sup.+ aromatics along with C.sub.1 -C.sub.5 hydrocarbons. This effluent stream is separated into a stream containing C.sub.1 -C.sub.4 hydrocarbons and one containing C.sub.6.sup.+ aromatics. The C.sub.1 -C.sub.4 containing stream is flowed to a dehydrogenation zone to produce C.sub.3.sup.= /C.sub.4.sup.= olefins.

Abstract: The present invention is directed to an improved isomerization process employing a catalyst wherein the catalyst comprises a pair of catalyst particles of different acidity utilized either as distinct beds of such discrete particles or as a mixture of such discrete particles. The isomerization process utilizing such a catalyst produces a product which exhibits higher VI as compared to products produced using either catalyst component separately or using a single catalyst having the average acidity of the two discrete catalysts.

Abstract: A catalytic reforming process uses a riser reactor with multiple catalyst injection points to obtain high aromatics yields from a naphtha feedstock. Product from the riser reactor typically is discharged into a fluidized-reforming reactor, in which the reforming reaction is completed and catalyst is separated from hydrogen and hydrocarbons. Hydrocarbons from the reactor are separated to recover an aromatized product. Catalyst is regenerated to remove coke and reduced for reuse in the reforming process.

Abstract: Catalytic reforming wherein the lead reactor contains a catalsyt comprised of platinum and a relatively low level of Re on an inorganic oxide support. The tail reactor contains a platinum rhenium catalyst wherein the rhenium content is at higher levels.

Abstract: An integrated process for increasing C.sub.6 to C.sub.8 aromatics content in reformate prepared from C.sub.9.sup.+ aromatics-containing feed comprises:1) pretreating a raw naphtha feedstream containing C.sub.9.sup.+ aromatics and sulfur by contacting with a) a hydrodesulfurization catalyst under hydrodesulfurization conditions to produce a hydrodesulfurized feedstream and thereafter b) cascading said hydrodesulfurized feedstream over a noble metal- and/or Group VIA metal-containing porous crystalline inorganic oxide catalyst comprising pores having openings of 12-member rings under conditions sufficient to effect conversion of C.sub.9.sup.+ aromatics, thereby providing a pretreated effluent stream of enhanced C.sub.8.sup.- aromatics content relative to that obtained in the absence of said cascading; and2) reforming at least a portion of said pretreated effluent stream to provide a reformate stream.

Abstract: Reforming is effected with a combination of a primary supported noble-metal catalyst and a catalyst containing one or more medium pore non-zeolite molecular sieves (MP-NZMS). The latter reforming and dehydrocyclization comprise a Group VIII metal and at least one bound MP-NZMS characterized in the calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20.degree. C. and characterized by an adsorption of triethylamine less than about 5 percent by weight at a partial pressure of 2.6 torr and a temperature of 22.degree. C., The MP-NZMS catalyst binder preferably is alumina and/or silica, and the Group VIII metal preferably is platinum.

Abstract: A hydrocarbon feedstock is catalytically reformed to effect dehydrocyclization of paraffins in a process combination comprising a first reforming zone, a sulfur-removal zone containing a mixed reforming catalyst and sulfur sorbent comprising a manganese component to preclude sulfur from the feed to a second reforming zone. The process combination shows substantial benefits over prior art processes in achieving reforming-catalyst stability.

Abstract: Aliphatic feeds are converted to olefins and/or aromatics in a multi pressure reactor system. A high pressure first stage reactor generates much or all of the hydrogen needed to reduce catalyst coking in lower pressure downstream reactors. High pressure operation protects catalyst stability in the first reactor, while produced hydrogen helps protect downstream catalyst. Low pressure downstream operation improves yields.

Abstract: A hydrocarbon feedstock is catalytically reformed in a sequence comprising a reforming zone containing a catalyst comprising a platinum-group metal and a nonacidic L-zeolite and an aromatics-isomerization zone containing a catalyst comprising a platinum-group metal, a metal attenuator and a refractory inorganic oxide. The process combination features high selectivity in producing a high-purity BTX product from naphtha.

Abstract: A process combination is disclosed to selectively upgrade naphtha to obtain an isoparaffin-rich product for blending into gasoline. A naphtha feedstock is subjected to ring cleavage to convert naphthenes to paraffins using a nonacidic catalyst followed by isomerization of paraffins to obtain an increased proportion of isoparaffins.

Abstract: A process is disclosed for removing residual sulfur from a hydrotreated naphtha feedstock. The feedstock is contacted with molecular hydrogen under reforming conditions in the presence of a less sulfur sensitive reforming catalyst to convert trace sulfur compounds to H.sub.2 S, and to form a first effluent. The first effluent is contacted with a solid sulfur sorbent to remove the H.sub.2 S and form a second effluent. The second effluent is then contacted with a highly selective reforming catalyst under severe reforming conditions. Also disclosed is a method using a potassium containing sulfur sorbent made from nitrogen-free potassium compounds.

Abstract: A process for reforming a gasoline boiling range naphtha stream using a reforming process unit comprised of two independent process units, each of which are operated in two stages. The first stage is operated in a fixed-bed mode and is comprised of a plurality of serially connected fixed bed reactors, and the second stage is operated in a moving bed continuous catalyst regeneration mode. A hydrogen-rich stream is recycled through both stages for each process unit and the moving-bed reforming zones share a common regeneration zone.