Abstract: A stable distillate fuel blend useful as a fuel or as a blending component of a fuel that is suitable for use in an internal combustion engine, said fuel blend prepared from at least one highly paraffinic distillate fuel component and at least one highly aromatic petroleum-derived distillate fuel component and a process for preparing same involving the blending of at least two components having antagonistic properties with respect to one another.

Abstract: Processes for converting C1 to C3 alkanes into high purity C6 to C24 normal alpha olefins and internal combustion engine grade fuels and/or lubricating oils comprising a sequence of fractionation and thermal cracking and/or hydrocracking operations. The C6 to C24 normal alpha olefin fractions generally have a purity of at least about 90 wt. %.

Abstract: The invention provides a process for the production of a synthetic naphtha fuel suitable for use in compression ignition (CI) engines, the process including at least the steps of hydrotreating at least a fraction of a Fischer-Tropsch (FT) synthesis reaction product of CO and H2, or a derivative thereof, hydrocracking at least a fraction of the FT synthesis product or a derivative thereof, and fractionating the process products to obtain a desired synthetic naphtha fuel characteristic. The invention also provides a synthetic naphtha fuel made by the process as well as a fuel composition and a Cloud Point depressant for a diesel containg fuel composition, said fuel composition and said depressant including the synthetic naphtha of the invention.

Abstract: A catalytic hydrocracking process which provides for the simultaneous production of LPG and distillate hydrocarbons. The feedstock is introduced into a denitrification and desulfurization zone and then passed directly to a hot, high pressure stripper utilizing a hot, hydrogen-rich stripping gas to produce a first liquid stream boiling in the range of the feedstock and a first vapor stream comprising hydrocarbonaceous compounds boiling at a temperature below the boiling range of the feedstock. The first liquid stream is hydrocracked in a first hydrocracking zone and then passed to the denitrification and desulfurization zone. At least a portion of the first vapor stream is condensed to produce a second liquid stream comprising hydrocarbonaceous compounds boiling at a temperature below the boiling range of the feedstock.

Abstract: This invention relates to a process to produce propylene from a hydrocarbon feed stream, preferably a naphtha feed stream, comprising C5 and C6 components wherein a light portion having a boiling point range of 120° C. or less is introduced into a reactor separately from the other components of the feed stream.

Abstract: A catalytic hydrocracking process wherein a first hydrocarbonaceous feedstock is contacted with a hydrogen and a metal promoted hydrocracking catalyst in a hydrocracking reaction zone at elevated temperature and pressure to obtain conversion to lower boiling hydrocarbons. The resulting hot, uncooled effluent from the hydrocracking reaction zone is hot hydrogen stripped in a stripping zone maintained at essentially the same pressure as the hydrocracking zone to produce a first gaseous hydrocarbonaceous stream and a first liquid hydrocarbonaceous stream. At least a portion of the first liquid hydrocarbonaceous stream is preferably recycled to the hydrocracking reaction zone. A second hydrocarbonaceous feedstock having a boiling temperature range lower than that of the first hydrocarbonaceous feedstock is introduced into an upper end of the stripper to serve as reflux.

Abstract: Heavy hydrocarbons are upgraded to higher value distillates in a hydrocarbon conversion process which employs several parallel reaction zones which each contain both hydrotreating and hydrocracking catalyst beds. The feed and liquid recycle from the bottom of the reaction zone is charged to the top of the uppermost catalyst bed. Hydrogen flow is countercurrent to the descending liquid, and products are removed overhead through vapor-liquid contactors. The flow of feed to one of the reaction zones is periodically stopped to allow sequential on-stream hydrogenative regeneration of the catalysts within the reaction zone.

Abstract: A method to rapidly characterize the hydrocarbon chemistry of heavy residual petroleum mixtures uses three model equations for predicting aromatic carbon content, aromatic hydrogen content and total hydrogen content of the heavy residual oil. The predictive equations are based on three easily measured bulk properties including refractive index, specific gravity and the Watson K factor.

Abstract: Disclosed is a catalytic cracking process that includes more than one catalytic cracking reaction step. The process integrates catalytic cracking steps with hydroprocessing in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, one hydroprocessing step is included between the cat cracking reaction steps, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step.

Abstract: The invention relates to Fluid Catalytic Cracking (FCC) for producing liquid fuels and light olefins from liquid hydrocarbon mixtures such as petroleum fractions.

Abstract: A high efficiency FCC process obtains the necessary regenerated catalyst temperature for a principally thermal cracking stage by cracking a light feedstock such as naphtha or a middle distillate in a first riser that principally performs thermal cracking and then cracks a heavy FCC feed in a second riser with a blend of catalyst from the principally thermal cracking step and recycle catalyst from the heavy feed to provide the necessary coke content on the catalyst that will produce high regenerated catalyst temperatures. The high temperature of the regenerated catalyst in the first riser provides a convenient means of cracking naphtha under high severity conditions and then using the remaining activity of the contacted catalyst for the principally catalytic reaction of the heavier feed. A separate thermal cracked product may be recovered from an intermediate blending vessel downstream of the first riser.

Abstract: A large difficult to process hydrocracking feed stream may be processed at lower overall pressure and therefore in a unit of reduced capital cost by first dividing the feed stream into a light fraction and a smaller heavy fraction and then processing these fractions in separate reactors. The heavy fraction will normally contain the more difficult to process species and is processed in a once through reaction zone. The light fraction is processed in a higher conversion reaction zone which also receives the recycle stream produced in the product fractionation/recovery zone. The effluents of the two reaction zones may be charged into a common separator or into different separators to reduce ammonia levels in the recycle reactor.

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: Hydrocarbon feedstocks are hydroprocessed in parallel reactors, while hydrogen flows in series between the reactors. A first hydrocarbon feedstock and a hydrogen-rich recycle gas stream are introduced to a first reactor, where a first reactor effluent stream is produced and fed to a first separator, which separates the first reactor effluent stream into a first hydrogen-rich gas stream and a first hydroprocessed product stream. The first hydrogen-rich gas stream and a second hydrocarbon feedstock are fed to a second reactor, where a second reactor effluent stream is produced and fed to a second separator, which separates the second reactor effluent stream into a second hydrogen-rich gas stream and a second hydroprocessed product stream. A make-up hydrogen stream is added to the second hydrogen-rich gas to form the hydrogen-rich recycle gas stream that is compressed and fed to the first reactor.

Abstract: A process for the dual riser contacting of a primary feed and a secondary recycle feed fraction uses independent recovery of the separate streams from the riser cracking zone to improve the product yields and properties. Separate recovery segregates the upgraded recracked components from the rest of the primary cracked products. The benefits of selective of recracking are lost if the upgraded products from the recycle stream become recombined with the primary cracked product. The selectively recovered recycle feed may undergo hydroprocessing to hydrogenate, hydrocrack and/or hydrotreatmement before recracking. The process can also make highly efficient use of the high residual activity in the catalyst that has contacted the secondary feed.

Abstract: A large hydrocracking feed stream is processed without resorting to full dual reaction trains by passing a portion of the feed stream into each of two reaction zones, with the effluents of the two reaction zones being charged into a common separation and product recovery facility. Unconverted hydrocarbons recovered in the product recovery facility are passed into only one of the reaction zones.

Abstract: An integrated process is provided for preparing a dewaxed heavy lube base oil product and a dewaxed light lube base oil product from a waxy feedstock. The process includes separating the waxy feedstock into two or more fractions. A light fraction is upgraded to increase its VI, and dewaxed in an isomerization process using a wax isomerization catalyst such as SAPO-11, SAPO-31 or SAPO-41. A heavy fraction is upgraded to increase its VI, and dewaxed in the presence of a wax cracking catalyst such as ZSM-5.

Abstract: There is provided a process and a device with a convection zone (A) and a radiation zone (B) in a furnace (10), whereby the process includes: a first stage of precracking a feedstock of light hydrocarbons (1) and a second stage of final co-cracking of the mixture that is composed of this precracked light feedstock (7) and a feedstock of heavy hydrocarbons (2). The process further includes: separate heating of the two feedstock streams (1 and 2) in the convection zone (A), in which the preheating temperature of each feedstock stream remains below the initial cracking temperature in each case; precracking (5) of the preheated light hydrocarbons; mixing of precracked light hydrocarbon stream (8) while a mixed stream (9) is formed; intense heating of mixed stream (9) to a temperature that is higher than the initial cracking temperature by virtue of the fact that the mixture is introduced into the radiation zone (B) of the furnace (10); and cooling (15) of cracked gases outside the furnace (10).

Abstract: Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing step between the catalytic cracking reaction steps in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, the hydroprocessing step is included between the reaction stages, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step.

Abstract: Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing process step between the catalytic cracking reaction steps in order to maximize olefins production, mid-distillate quality and naphtha octane level in the cracked products. Preferably, a first cracked hydrocarbon product is obtained from a first cracking stage and separated into a mid-distillate and gas oil containing fraction having an initial boiling point of at least 300.degree. F., the distillate and gas oil containing fraction is hydroprocessed, and a naphtha fraction and a gas oil containing bottoms fraction of the hydroprocessed material are cracked in a second cracking stage.

Abstract: A process for contemporaneously catalytically cracking a paraffin rich feedstock and a heavy feedstock wherein the feedstocks are segregated prior to catalytic cracking in separate reactors with regenerated particulate catalyst solids. The process provides for the separate optimal cracking of paraffinic constituents and heavy naphthenic constituents while maintaining an overall heat balance.

Abstract: A process for simultaneously removing heteroatoms, such as sulfur, from a virgin distillate stream and a light catalytic cyclic stream in two reaction zones in a hydrotreating process unit. One reaction zone will be a low temperature reaction zone and the other will be the high temperature zone. In the low temperature reaction zone, the cracked stream is reacted with a hydrotreating catalyst at a predetermined temperature and in high temperature reaction zone, the virgin distillate stream is reacted with a catalyst which is less reactive than that of the first reaction zone. When catalyst in the high reaction zone is replaced with fresh catalyst the temperature is lowered so that it now becomes the low temperature zone in which the cracked stream is redirected.

Abstract: A method for controlling the manufacture of lubricating oils involving the steps of distillation, extracting, dewaxing and optionally hydrofining; or for controlling operating units associated with refinery or chemical processes with feed stocks and products boiling above 350.degree. C. The method comprises selecting one or more chemical or perceptual or physical or performance properties of the lubricating oil or the feedstock, distillate or raffinate used in the manufacturing process; or of the refinery or chemical process feed stocks or products; creating a training set from reference samples which contain characteristic molecular species present in the lubricating oil, feedstock, distillate or raffinate used in the manufacturing process or from the refining or chemical operations. The reference samples are subjected to GC/MS analysis wherein the often collinear data generated is treated by multivariate correlation methods.

Abstract: Disclosed is a one-step process intended as an alternative to catalytic reforming which upgrades naphthas by simultaneously saturating aromatics, isomerizing paraffins and selectively cracking heavier hydrocarbons which comprises contacting heavy naphtha feedstock in a reforming zone with a catalyst comprising a solid acid, optionally with a binder of Group III and/or IV of the Periodic Table, having a metal from Group VIII of the Periodic Table deposited thereon, wherein the reaction conditions are much milder than those typically used in catalytic reforming.

Abstract: A naphtha or a middle distillate hydrocarbon is hydrodearomatized by hydrotreating in the presence of a catalyst containing a carbon support bearing (i) molybdenum or tungsten, (ii) a metal or non-noble Group VIII, and (iii) chromium.

Abstract: A fluid catalytic cracking unit equipped with multiple feed injection points along the length of the riser is operated such that portions of the same fresh feed are charged to different feed injection points. Preferably, the hydrocarbon fresh feed can be split into two or more non-distinct fractions, with one fraction charged to the bottom injection point along the length of the riser reactor, and the remaining fractions charged to injection points progressively higher up along the length of the riser reactor with the temperature of the upper injection feed fractions being different from that of the lowest injection point fraction prior to entry into the FCC riser reactor. Hydrocarbon products from the cracking process can be recycled to one or more of the various injection points along the length of the riser.

Abstract: Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing step between the catalytic cracking reaction steps in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, the hydroprocessing step is included between the reaction stages, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step.

Abstract: This invention discloses an enhanced process for the hydroprocessing of a feed, the feed comprising a highly aromatic refinery distillate stream boiling in the range between 300.degree. and 900.degree. F. The feed is separated into light and heavy streams such that the light stream contains from 0.1 to 5 wt. % dibenzothiophene, substituted dibenzothiophenes, and heavier polycyclic thiophenes. The lighter stream is hydrotreated at pressures from 300.degree. to 1000.degree. F. with a commercial catalyst having a hydrogenation component. The heavier stream is treated in the presence of hydrogen at higher pressure, from 600 to 2000 psig with a catalyst comprising active material having a Constraint Index of less than 2 in addition to a hydrogenation component in order to achieve over 35% conversion of material boiling above 630.degree. F. The active material of the catalyst is a highly siliceous zeolite or an acidic amorphous silica-alumina material.

Abstract: Disclosed is a method which combines catalytic cracking and olefin production using a coked catalytic cracking catalyst as a dehydrogenation catalyst to dehydrogenate an alkane feed stream and form an olefin rich product stream. The method uses a staged backmixed regeneration system to form the dehydrogenation catalyst and to fully reactivate deactivated cracking catalyst for reuse in the cracking reaction. The catalyst preferably comprises a crystalline tetrahedral framework oxide component.

Abstract: A process for contemporaneously catalytically cracking a paraffin rich feedstock and a heavy feedstock wherein the feedstocks are segregated prior to catalytic cracking in separate reactors with regenerated particulate catalyst solids. The process provides for the separate optimal cracking of paraffinic constituents and heavy naphthenic constituents while maintaining an overall heat balance.

Abstract: Hydrotreated and hydrocracked liquid/vapor effluents are separated in a common separating vessel under elevated pressure. High quality middle distillates and low-sulfur/low-hydrogen-containing FCC feedstocks are produced.

Abstract: A process combination is disclosed to selectively upgrade catalytically cracked gasoline to obtain products suitable for further upgrading to reformulated fuels. A naphtha feedstock, preferably heavy naphtha, is hydrogenated to saturate aromatics, followed by selective isoparaffin synthesis to yield light and heavy synthesis naphtha and isobutane. The heavy synthesis naphtha may be processed by reforming, light naphtha may be isomerized, and isobutane may be upgraded by dehydrogenation, etherification and/or alkylation to yield gasoline components from the process combination suitable for production of reformulated gasoline.

Abstract: A process for multi-stage catalytic cracking is disclosed. A first stage cracks a first feed at atmospheric to 100 psig over a shape selective zeolite to convert from 10 to 90%, by volume, to lighter products rich in iso-compounds which may be used to make ethers. A second feed, which may include 700.degree. F.+ liquid from the selective cracking reaction, is cracked in a catalytic cracking (FCC) unit. Preferably all or some of the products from the shape selective cracking reactor are fractionated in the FCC main column.

Abstract: A process combination is disclosed to selectively upgrade naphtha to obtain gasoline which is in accordance with current standards for reformulated fuels. A naphtha feedstock is fractionated to selectively direct light naphtha to isomerization or blending, a head-cut fraction to reforming, and a heavy potion to selective isoparaffin synthesis to yield light and heavy synthesis naphtha and isobutane. The heavy potion of the synthesis naphtha is processed by reforming. Light naphtha may be isomerized, with or without recycle of low-octane components of the product. A gasoline component is blended from light, synthesis, and reformate products from the process combination.

Abstract: A method of hydrotreatment of heavy hydrocarbon oil in the presence of catalysts which comprises hydrodemetallizing and hydrocracking the heavy hydrocarbon oil successively and thereafter hydrodesulfurizing and hydrodenitrogenating the treated heavy hydrocarbon oil. The hydrocracking is carried out in the presence of a catalyst comprising at least one metal or metal compound of the group VIA or the group VIII of the Periodic Table supported on a carrier comprising 10 to 90 weight % of an iron-containing aluminosilicate and 90 to 10 weight % of an inorganic oxide. Other methods of treatment of heavy hydrocarbon oil comprise the hydrotreatment in conjunction with fluid catalytic cracking and/or thermal hydrocracking. The methods provide a naphtha fraction, a kerosene fraction and a gas oil fraction which can be obtained from the heavy hydrocarbon oil efficiently with high yield.

Abstract: A process for feed oil refining for production of lubricating oil, by using an equipment for lubricating oil production including a fulfural refining unit, a hydrotreating unit and a ketone dewaxing unit, all connected in series. In this process, operations associated with the switch of feed oil are conducted by carrying out the first to seventh step groups successively. Each step group is initiated when a given time has passed since the start of the previous step group, or when the value of a particular measurement item has reached a target value, or when the value of a particular measurement item has shown a change. First, in the first step group, the amount of feed oil supplied to each unit, etc. is adjusted and, in the second step group, the feed oil to the furfural refining unit is switched.

Abstract: This invention provides an integrated process for converting a hydrocarbon feedstock having components boiling above 300.degree. F. into liquid fuel products boiling in the range of from about 80.degree. F. to about 700.degree. F.

Abstract: A catalytic cracking process and apparatus wherein particles of cracking catalyst circulate continuously between a reaction zone and a regeneration zone and hot regenerated catalyst from the regeneration zone contacts hydrocarbon feed in the reaction zone to produce cracked hydrocarbon products and spent catalyst. The spent catalyst is recovered and subjected to stripping in a stripping zone to remove strippable material therefrom. The stripped spent catalyst is circulated to the regeneration zone for oxidative exothermic regeneration. Some hot regenerated catalyst is passed directly from the regenerator to the stripping zone via a conduit provided for this purpose. Another hydrocarbon stream is passed into contact with the hot regenerated catalyst in this conduit. The said other hydrocarbon stream is converted to products of enhanced value (e.g., olefins) during contact with catalyst in the conduit, and the said products are recovered.

Abstract: A staged catalytic cracking process and apparatus is disclosed where each stage has a catalyst to oil ratio of at least 15 and there are individual hydrocarbon feeds to each stage and product removal from each stage. There is a residence time profile with the first stage having a short residence time and the successive stages having progressively longer residence times. Further, there is a feed profile with the lighter components of the total feed going to the first stage and the heavier components being fed to the later stages. The apparatus has a generally vertical orientation which permits it to be incorporated into existing cracking units for upgrading and also easily provides for both short and long residence times.

Abstract: FCC process uses an open reactor vessel to house cyclones or other separation devices that reduce the carry through of product gases with the catalyst into the reactor vessel to less than 10 wt. % so that the catalyst in the reactor vessel provides a secondary dealkylation zone. By using a highly efficient separation device to remove product from the catalyst, the environment in the reactor vessel receives a low volume of cracked hydrocarbons from the riser conversion zone and provides a convenient secondary reaction zone that receives a recycled heavy gasoline fraction separated from the riser product stream. Dealkylation in the secondary reaction zone provides additional light gasoline to satisfy T90 requirements.

Abstract: A process for the production of distillate hydrocarbon from atmospheric fractionation residue and waste lubricants by means of contacting the waste lubricant with a hot hydrogen-rich gaseous stream to increase the temperature of this feed stream to vaporize at least a portion of the distillable hydrocarbonaceous compounds thereby producing a distillable hydrocarbonaceous stream which is immediately hydrogenated in an integrated hydrogenation zone. The vaporization of the waste oil is also conducted in the presence of a vacuum fractionation residue which is produced in the integrated process. The resulting effluent from the integrated hydrogenation zone and a distillable hydrocarbon stream recovered from the atmospheric fraction residue is catalytically converted to produce lower molecular weight hydrocarbon compounds.

Abstract: A process combination is disclosed to selectively upgrade naphtha to obtain gasoline which is in accordance with current standards for reformulated fuels. A naphtha feedstock is fractionated to selectively direct light naphtha to isomerization or blending, a heart-cut fraction to reforming, and a heavy portion to selective isoparaffin synthesis to yield light and heavy synthesis naphtha and isobutane. The heavy portion of the synthesis naphtha is processed by reforming. Light naphtha may be isomerized, with or without recycle of low-octane components of the product. A gasoline component is blended from light, synthesis, and reformate products from the process combination.

Abstract: A process combination is disclosed to reduce the aromatics content and increase the oxygen content of a key component of gasoline blends. A naphtha feedstock having a boiling range usually suitable as catalytic-reforming feed is processed by selective isoparaffin synthesis to yield lower-molecular weight hydrocarbons including a high yield of isobutane. The isobutane is processed to yield an ether component by dehydrogenation and etherification. The cracked light naphtha may be upgraded by isomerization. The heavier portion of the cracked naphtha is processed in a reformer. A gasoline component containing oxygen as ether and having a reduced aromatics content and increased volumetric yield relative to reformate of the same octane number is blended from the net products of the above processing steps. The process combination is particularly suited for use in an existing refinery.

Abstract: A process combination is disclosed to reduce the aromatics content and increase the oxygen content of a key component of gasoline blends. A naphtha feedstock having a boiling range usually suitable as catalytic-reforming feed is processed by selective isoparaffin synthesis to yield lower-molecular weight hydrocarbons including a high yield of isobutane. A portion of the isobutane is processed to yield an ether component by dehydrogenation to yield isobutene followed by etherification. Part of the isobutane and isobutene are alkylated to produce an alkylate component. The synthesis light naphtha may be upgraded by isomerization. The heavier portion of the synthesis naphtha is processed in a reformer. A gasoline component containing oxygen as ether and having a reduced aromatics content and increased volumetric yield relative to reformate of the same octane number is blended from the net products of the above processing steps.

Abstract: The conventional wye (where the clean regenerated catalyst returns from the regenerator to contact the feed as it enters the riser) is replaced with two or more wyes, all connected between the regenerator outlet and the inlet to a common short cracking riser. Each wye has a separate injector which can inject; e.g., diesel oil, so that neat (unmixed) diesel contacts clean catalyst and the mixture rises up a smaller riser before entering a short main riser where the largely cracked mixture is admixed with similar cat-vacuum bottoms, etc. mixtures from the other wyes. Most cracking occurs before entering the common riser so the effect is similar to a riser cracker operating on a single unmixed feed.

Abstract: An improvement in iso-olefin etherification is obtained in an integrated process combining a fluidized catalytic cracking reaction and a fluidized catalyst etherification reaction wherein zeolite catalyst particles are withdrawn in partially deactivated form from the ether reaction stage and added as part of the catalyst in the FCC reaction.

Abstract: An FCC process uses an open reactor vessel to house cyclones or other separation devices that reduce the carry though of product gases with the catalyst into the reactor vessel to less than 5 wt. % so that the catalyst in the reactor vessel can contact a secondary feedstock. By using a highly efficient separation device to remove product from the catalyst the environment in the reactor vessel receives a low volume of feed hydrocarbons and riser by-products. These by products comprise mainly C.sub.2 and lighter gases which are inert to a variety of other feedstreams. Possible secondary feedstreams include hydrotreated heavy naphtha, hydrotreated light cycle oil, light reformate and olefins. It is highly useful to use the secondary feedstream to heat the catalyst in the reactor vessel to facilitate hot stripping of the catalyst. Heat may be introduced in this manner by heating the secondary feedstream or using a feedstream that produces an exothermic reaction in the reactor vessel.

Abstract: Process for producing gasoline components from a hydrocarbonaceous feed containing hydrocarbons comprising at least 4 carbon atoms, and hydrocarbons obtained thereby. The process comprises:a. separating feed into a heavy fraction containing hydrocarbons comprising at least 7 carbon atoms and a light fraction containing hydrocarbons comprising at most 7 carbon atoms,b. isomerizing at least part of the light fraction at a temperature between 50.degree. and 300.degree. C.,c. separating effluent of step b) into a stream containing branched hydrocarbons and a stream containing normal hydrocarbons, andd. isomerizing at least part of the stream containing normal hydrocarbons at a temperature which is higher than the temperature applied in step b).

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 for producing gasoline components from a hydrocarbonaceous feed containing hydrocarbons comprising at least 4 carbon atoms is disclosed. The process comprises the following steps:a) separating feed into a heavy fraction containing hydrocarbons comprising at least 7 carbon atoms, an intermediate fraction containing mainly hydrocarbons comprising 6 or 7 carbon atoms, and a light fraction containing hydrocarbons comprising at most 6 carbon atoms,b) isomerizing at least part of the light fraction,c) combining effluent of step b) with the intermediate fraction, separating off a stream containing normal hydrocarbons and a stream containing branched hydrocarbons, andd) passing at least part of the stream containing normal hydrocarbons to isomerization step b).