Abstract: A process is disclosed for producing distillate range hydrocarbons using MTW and/or SSZ-41x catalysts.

Abstract: Naphtha boiling range compositions are provided that can have improved combustion properties (relative to the research octane number of the composition) in spark ignition engines and/or compression ignition engines. The improved combustion properties can be achieved by controlling the total combined amounts of n-paraffins and isoparaffins that include a straight-chain propyl group (R1—CH2—CH2—CH2—R2). For such a straight-chain propyl group, R2 can correspond to any convenient CxHy group that can appear in a paraffin or isoparaffin. R1 can correspond to a hydrogen atom, making the straight-chain propyl group a terminal n-propyl group; or R1 can correspond to any convenient CxHy group that can appear in a paraffin or isoparaffin.

Abstract: A process and apparatus is disclosed for pretreating a hydrocarbon stream in a hydrotreating reactor and separating the diesel materials from the pretreated effluent before the heavier liquid materials are fed to a hydrocracking unit. Thus diesel materials are preserved but recovered along with the hydrocracked effluent. A recovered diesel stream can be sent to a hydrotreating unit to improve its cetane rating.

Abstract: One exemplary embodiment can be a process for treating a hydroprocessing fraction. The process can include obtaining a bottom stream from a fractionation zone, and passing at least a portion of the bottom stream to a film generating evaporator zone for separating a first stream containing less heavy polynuclear aromatic compounds than a second stream.

Abstract: Processing schemes and arrangements are provided for the processing a heavy hydrocarbon feedstock via fluidized catalytic cracking with selected hydrocarbon fractions including light olefins being obtained via absorption and separation product recovery.

Abstract: Process for the conversion of heavy feedstocks selected from heavy crude oils, distillation residues, heavy oils coming from catalytic treatment, thermal tars, oil sand bitumens, various kinds of coals and other high-boiling feedstocks of a hydrocarbon origin known as black oils, by the combined use of the following three process units: hydroconversion with catalysts in slurry phase (HT), distillation or flash (D), and deasphalting (SDA).

Abstract: Processing schemes and arrangements are provided arrangements are provided for the processing a heavy hydrocarbon feedstock via hydrocarbon cracking processing with selected hydrocarbon fractions being obtained via absorption-based product recovery while minimizing or avoiding loss of light olefins via system purging.

Abstract: A method for the efficient conversion of heavy oil to distillates using sequential hydrocracking in the presence of both supported and colloidal catalyst immediately followed by a high temperature-short residence time thermal treatment. The hydrocracker reaction products or a heavy oil and hydrogen donor diluent may be advantageously heated by direct contact with high velocity combustion products.

Abstract: The invention concerns a process for treating a hydrocarbon feed comprising a series of a first upstream process for hydrocarbon hydroconversion comprising at least one reaction chamber, the reaction or reactions occurring inside said chambers and employing at least one solid phase, at least one liquid phase and at least one gas phase, and a second downstream steam reforming process comprising at least one reaction chamber, characterized in that the said upstream process is carried out in a “slurry” and/or an ebullated bed mode and in that the downstream process comprises a first step for at least partial conversion of hydrocarbons heavier than methane into methane, termed the pre-reforming step, and in that the reaction or reactions occurring inside the chambers of the downstream stream reforming process enables the production of a reagent, namely hydrogen, which is necessary for the reactions in the first upstream process.

Abstract: Process for treatment of a hydrocarbon feedstock that comprises a hydrocarbon-containing liquid phase and hydrogen, in which the feedstock is separated under a pressure P1 into a liquid L1 and a gas G1, that is compressed and brought into contact with a portion of L1 under a pressure P2>2×P1 to recover a liquid L2 and a hydrogen-rich gas G2; L2 is fractionated to obtain a stabilized liquid L4a that is free of LPG and lighter products, a liquid stream of LPG, and a gas stream G4 that is recycled, and in which one of gas streams: recompressed G1 and G4 is in counter-current contact with an unstabilized liquid AL that is obtained from or extracted from L1 or L2, whereby this unstabilized liquid is supercooled by at least 10° C. below its bubble point at pressure P2.

Abstract: A process for selectively producing C3 olefins from a catalytically cracked or thermally cracked naphtha stream is disclosed herein. The naphtha stream is introduced into a process unit comprised of a reaction zone, a stripping zone containing a dense phase, a catalyst regeneration zone, and a fractionation zone. The naphtha feedstream is contacted in the reaction zone with a catalyst containing from about 10 to about 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, and are then recycled to the reaction zone.

Abstract: This invention is an improved distillation sequence for the separation and purification of ethylene from a cracked gas. A hydrocarbon feed enters a C2 distributor column. The top of the C2 distributor column is thermally coupled to an ethylene distributor column, and the bottoms liquid of a C2 distributor column feeds a deethanizer column. The C2 distributor column utilizes a conventional reboiler. The top of the ethylene distributor is thermally coupled with a demethanizer column, and the bottoms liquid of the ethylene distributor feeds a C2 splitter column. The ethylene distributor column utilizes a conventional reboiler. The deethanizer and C2 splitter columns are also thermally coupled and operated at a substantially lower pressure than the C2 distributor column, the ethylene distributor column, and the demethanizer column. Alternatively, a hydrocarbon feed enters a deethanizer column.

Abstract: A catalytic hydrocracking process for the production of ultra low sulfur diesel wherein a hydrocarbonaceous feedstock is hydrocracked at elevated temperature and pressure to obtain conversion to diesel boiling range hydrocarbons. The resulting hydrocracking zone effluent is 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. The first gaseous hydrocarbonaceous stream containing diesel boiling range hydrocarbons is introduced into a desulfurization zone and subsequently partially condensed to produce a hydrogen-rich gaseous stream and a second liquid hydrocarbonaceous stream containing diesel boiling range hydrocarbons. At least a portion of the first liquid stream is separated in a dividing wall column to produce a liquid hydrocarbonaceous stream containing diesel boiling range hydrocarbons which is also introduced into the desulfurization zone.

Abstract: A catalytic hydrocracking process for the production of lube base oil wherein a hydrocarbonaceous feedstock is contacted with hydrogen and a metal promoted hydrocracking catalyst in a hydrocracking reaction zone at elevated temperature and pressure to obtain conversion to higher hydrogen-content hydrocarbons including lube base oil. The resulting hot, uncooled effluent from the hydrocracking reaction zone is hydrogen stripped in a hot, high pressure 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 gaseous hydrocarbonaceous stream is condensed to produce a second liquid hydrocarbonaceous stream and a second hydrogen-rich gaseous stream. The first liquid hydrocarbonaceous stream is preferably separated at a pressure greater than atmospheric pressure to provide at least one lube base oil product stream.

Abstract: Processes for providing improved methane removal and hydrogen reuse in reactors, particularly in refineries and petrochemical plants. The improved methane removal is achieved by selective purging, by passing gases in the reactor recycle loop across membranes selective in favor of methane over hydrogen, and capable of exhibiting a methane/hydrogen selectivity of at least about 2.5 under the process conditions.

Abstract: The present invention provides a process for the preparation of a catalyst composition which comprises, as first cracking component, a zeolite beta with a silica to alumina molar ratio of at least 20 comprising crystals less than 100 nm in size, and a second cracking component selected from (i) crystalline molecular sieves having pores with diameters greater than 0.6 nm, and (ii) clays, the process comprising the steps of:(i) preparing a mixture comprising the first cracking component and the second cracking component, the first cracking component being in the form of a sol,(ii) extruding the mixture into catalyst extrudates, and(iii) calcining the extrudates.

Abstract: A process for converting a heavy hydrocarbon fraction comprises treating the hydrocarbon feed in a hydroconversion section in the presence of hydrogen, the section comprising at least one three-phase reactor containing at least one ebullated bed hydroconversion catalyst, operating in liquid and gas riser mode, said reactor comprising at least one means for removing catalyst from said reactor and at least one means for adding fresh catalyst to said reactor.

Abstract: A process for converting a heavy hydrocarbon fraction comprises treating the hydrocarbon feed in a hydroconversion section in the presence of hydrogen, the section comprising at least one three-phase reactor containing at least one ebullated bed hydroconversion catalyst, operating in liquid and gas riser mode, said reactor comprising at least one means for removing catalyst from said reactor and at least one means for adding fresh catalyst to said reactor.

Abstract: A process and apparatus for separating a hydrocarbon gas into fractions containing predominant portions of hydrogen, methane, and C.sub.2 and heavier components, where the methane and lighter components are separated from the feed gas under non-cryogenic conditions to produce a hydrogen-rich fraction, a first fraction rich in C.sub.2 and heavier components and a hydrocarbon-rich fraction, the hydrocarbon-rich fraction then being separated under cryogenic conditions into a second fraction rich in C.sub.2 and heavier components and a methane-rich fraction.

Abstract: The invention is a process for reducing capital and energy costs in ethylene recovery. Moderate pressure processing and thermally coupled fractionation steps are achieved through the use of integrator columns. Ethylene separation from cracked gas originating from ethane through gas oil feeds can now be done with thermodynamically efficient fractionation at capital cost competitive with low efficiency designs. Acetylene hydrogenation may be done before demethanization where desired, and dephlegmation is preferred to accomplish high-efficiency rectification of hydrogen and methane from ethylene. Open loop heat pumps can optionally be incorporated into the ethane/ethylene splitter fractionation step, whose desirability is controlled by optimization of capital and energy costs.

Abstract: A method of processing a cracked gas feedstream containing hydrogen and C.sub.1 to C.sub.6 and heavier hydrocarbons is described using a relatively low pressure as compared to conventional cryogenic separation processes. At pressures below 27 bars, the feedstream is dried and cooled in a series of steps to initially separate out essentially all of the C.sub.6 and heavier hydrocarbons forming a vapor stream containing the hydrogen, the C.sub.1 to C.sub.3 hydrocarbons and at least some of the C.sub.4 and C.sub.5 hydrocarbons. The C.sub.4 and C.sub.5 components act as an absorption liquid to lower the light ends partial pressure permitting the condensation of C.sub.2 and C.sub.3 components at higher temperature levels and permitting the operation at lower pressures. The vapor stream is then further cooled and separated in another series of steps and processed in a demethanizer column in a manner to provide a high pressure hydrogen and methane overhead product and a high recovery of C.sub.2 and C.sub.

Abstract: A straight run naphtha is fractionated to yield on intermediate naphtha and the heaviest 10-25 vol % as heavy naphtha. The heavy naphtha is subjected to hydrocracking to yield liquid fuel and lighter, including C.sub.4 isoparaffins and a cracked naphtha having a 90 vol % temperature (T90) of 310.degree. F. (155.degree. C.).

Abstract: A method of converting a hydrocarbon feed with a catalyst and regenerating the catalyst by contact with an oxygen-containing stream is disclosed. The hydrocarbon conversion process employs a purification zone that purifies a net gas stream and that also removes water from a circulating regeneration gas stream. This method is useful for the regeneration of reforming catalysts comprising L-zeolite.

Abstract: An integrated three-column process for recovering hydrocarbon distillate products from a hydroprocessing or hydrocracking reactor effluent stream and a hydrocarbon distillate product recovery train are disclosed. According to the present recovery process, an effluent stream from the cracking reactor is cooled and separated into light and heavy phase streams. The heavy phase stream is depressurized and stripped of light end components in a steam stripping column. The light phase stream is further cooled to separate a liquid stream which is combined with the light ends from the stripper and fed to a debutanizer. A C.sub.4 -rich light end stream taken overhead from the debutanizer is condensed to produce LPG product stream(s). A C.sub.4 -lean heavy end stream removed from the bottoms of the debutanizer is combined with a heavy end bottoms stream from the stripper and fed to a fractionator for fractionation into product distillate streams such as light and heavy naphtha, jet fuel, diesel oil, and the like.

Abstract: In an ebullated bed process reactor effluent is subjected to high pressure followed by intermediate flash separation. An ebullation liquid is formed by educting high pressure flash separation liquid into an intermediate flash separation liquid. The ebullation liquid is recycled to the reactor to expand the catalyst bed to 110 vol % to 200 vol % of a settled catalyst bed volume. As a result of recycle pressure balance is advantageously maintained. Carry over catalyst and catalyst fines are recycled to the reactor and kept out of downstream equipment.

Abstract: The recovery of distillate products from a hydrocracking process includes passing the liquid-phase portion of the reaction zone effluent into a stripping column. A naphtha sidecut stream is recovered off the stripping column and combined with the net overhead liquid of the column. These combined streams are then combined with the naphtha recovered from the primary product recovery column. This minimizes the hydrogen sulfide present in the total naphtha product.

Abstract: A catalytic hydrocracking process which minimizes the fouling of the process unit with 11.sup.+ ring heavy polynuclear aromatic compounds by means of partially condensing the hydrocarbon effluent from the hydrocracking zone to produce an unconverted hydrocarbon stream comprising trace quantities of 11.sup.+ ring heavy polynuclear aromatic compounds and contacting the unconverted hydrocarbon stream with an adsorbent which selectively retains the 11.sup.+ ring heavy polynuclear aromatic compounds before the unconverted hydrocarbon stream is recycled to the hydrocracking zone.

Abstract: An improved hydrocracking process, in a process for conversion of components of a heavy hydrocarbon feed to lighter, more valuable products, wherein the feed comprises foulant, the process comprising: (a.) contacting the feed with hydrogen, in the presence of a hydrocracking catalyst, at an elevated temperature and pressure in a hydrocracker, to produce a hydrocracker effluent comprising foulant; (b.) cooling and depressurizing the hydrocracker effluent to form a cooled, depressurized hydrocracker effluent comprising foulant; (c.) separating the cooled, depressurized hydrocracker effluent into the products of the conversion and an unconverted portion of the hydrocracker effluent which comprises foulant; and (d.) recycling, as effluent recycle to the hydrocracker, the unconverted portion of the hydrocracker effluent to the hydrocracker, wherein the concentration of foulant in the hydrocracker effluent is increased; the improvement comprising: (i.

Abstract: This invention relates to a process for the separation of fine catalyst particles from a hydrocarbon feedstock coming from a catalytic cracking unit by filtration through mineral barriers and a filtration loop.The process consists of filtering the feedstock through mineral barriers that are resistant to heat and have a porosity adapted to the minimum diameter of the particles to be retained. The porosity is generally between 0.1 and 100 microns.

Abstract: An improvement has been found in the gas recovery section of a delayed coking process. In the improvement the compressor discharge is amine scrubbed to remove hydrogen sulfide. The compressor discharge is the entire vapor feed to the gas recovery section and contains about 90% of the hydrogen sulfide. This has been found to cause a significant drop in both the depropanizer and debutanizer pressure and allow a saving in the investment cost of the pressure vessel. Synergistically a reduced amount of hydrogen sulfide is present in the entire gas recovery section. The remaining 10% of the hydrogen sulfide is removed by amine scrubbing the fuel gas and propane/propylene fractions.

Abstract: A catalytic hydrocracking process which comprises: (a) contacting a hydrocarbonaceous feedstock having a propensity to form heavy polynuclear aromatic compounds and a liquid recycle stream in a hydrocracking zone to convert a substantial portion of the hydrocarbonaceous components in the feedstock to lower boiling products; (b) recovering a hydrocarbon effluent from the hydrocracking zone and partially condensing the hydrocarbon effluent from the hydrocracking zone and separating the same into a lower boiling hydrocarbon product stream and an unconverted hydrocarbon stream having at least a portion boiling above about 400.degree. F. (204.degree. C.

Abstract: Process for separating a mixed-phase hydrocarbonaceous effluent originating from the conversion of a hydrocarbonaceous feedstock in the presence of hydrogen at elevated temperature and pressure in a multiple separator system, which effluent contains hydrogen, normally liquid hydrocarbonaceous components and normally gaseous hydrocarbonaceous components by(i) separating in a first separation zone the effluent into a first liquid phase (L1) and a first vapor phase (V1),(ii) cooling the first vapor phase obtained to a temperature in the range between 25.degree. and 85.degree. C.

Abstract: A process for converting a feedstock containing 1 to about 6 carbon atoms per molecule which includes (a) contacting the feedstock with a solid composition comprising a crystalline microporous three dimensional solid catalyst having pores and being capable of promoting the conversion, and matrix material at conditions effective to convert the feedstock, to produce at least one desired product, and to at least partially deactivate the solid composition; (b) contacting the deactivated solid composition with regeneration medium at conditions to at least partially regenerate the solid composition; and (c) repeating step (a), the improvement which comprises (d) contacting the regenerated solid composition prior to step (c) to condition the regenerated solid composition to have increased effectiveness in step (c).

Abstract: Method and apparatus for fractionating a hot vaporous hydrocarbon feed from a fluid catalytic cracking reactor wherein the hot vaporous feed is introduced into a fractionator zone near one end thereof and liquid is removed from a liquid collection zone and cooled in a heat extraction zone. A first portion of the cooled liquid is returned to a location between the liquid collection zone and the point of introduction of the vaporous feed and sprayed directly on hot condensed liquid flowing downwardly over an inclined baffle plate to quickly quench the liquid below the temperature at which polymerization of the constituents of the liquid can occur.

Abstract: An improved method for processing the effluent of a hydrocarbon conversion zone. The invention is particularly useful in a catalytic reforming reaction, wherein practice of the invention results in an increased recovery of butane and propane. The effluent is separated into vapor and liquid components, which are then recontacted at a higher pressure. Several recontacting steps may be employed. Liquid product is then subjected to fractionation. Overhead vapor from the fractionation zone is recycled back to a recontacting step in order to recover a portion of the hydrocarbons contained therein, instead of routing the vapor to the plant fuel gas system.

Abstract: A process for visbreaking a heavy petroleum fraction wherein the effluent of the visbreaking heater is quenched by admixture with an overhead liquid produced by condensation of the overhead vapors of a secondary flash zone. The visbreaker effluent is then passed into a rectified flash zone, with the bottoms liquid of the rectified flash zone forming the feed stream to the secondary flash zone.

Abstract: Hydrocarbonaceous black oils are converted into lower-boiling hydrocarbons via a process which utilizes two separate catalytic reactor systems interconnected by way of a multiple-stage separation facility. Fresh feed charge stock is reacted in the first reactor system in admixture with hydrogen recovered from the second reactor system. Conversely, unconverted material from the first reactor system is reacted in the second system with make-up hydrogen and all the recycle hydrogen recovered from both reactor systems.

Abstract: Multiple-stage separation of a mixed-phase product effluent resulting from the hydrocracking and/or hydrorefining conversion of a hydrocarbonaceous charge stock. Reaction product effluent is initially separated in a high temperature, high pressure first separation zone, the vapor phase from which is cooled and separated in a second separation zone to provide a hydrogen-rich vaporous phase. The liquid phase from the second separation zone is increased in temperature and separated in a third separation zone at a substantially lower pressure. At least a portion of the liquid phase from the third separation zone is combined with the vaporous phase from the first separation zone prior to cooling and separation in the second separation zone. A savings of about 10.0% in hydrogen loss is realized or about 12 standard cubic feet per barrel of charge stock.

Abstract: Separation of the catalyst-containing product effluent from a fluid catalytic cracking unit is effected in the main column by a technique which involves removing a light naphtha fraction as the single overhead stream and separately withdrawing a heavy naphtha fraction as a lower side-cut. The latter is stripped of light naphtha (for recycle to the main column) and recovered as a product stream. Preferably a portion of the heavy naphtha fraction (as withdrawn) is cooled and combined with the light naphtha overhead reflux stream.

Abstract: A reaction product effluent, containing hydrogen, normally gaseous hydrocarbons and normally liquid hydrocarbons, is separated into desired component streams in a system which incorporates a low-pressure flash zone, a debutanizer and a deethanizer. The net overhead vaporous product from the deethanizer is introduced into the flash zone, the liquid phase from which serves as a portion of the feed to the debutanizer. Preferably, the net overhead vaporous product from the debutanizer is also introduced into the flash zone.