Abstract: An improved process for separating hydrogen from hydrocarbons. The process includes a pressure swing adsorption step, a compression/cooling step and a membrane separation step. The membrane step relies on achieving a methane/hydrogen selectivity of at least about 2.5 under the conditions of the process.

Abstract: Processes and apparatus for providing improved contaminant removal and hydrogen recovery in hydrogenation reactors, particularly in refineries and petrochemical plants. The improved contaminant removal is achieved by selective purging, by passing gases in the hydrogenation reactor recycle loop or purge stream across membranes selective in favor of the contaminant over hydrogen.

Abstract: Processes and apparatus for providing improved contaminant removal and hydrogen reuse in reactors, particularly in refineries and petrochemical plants. The improved contaminant removal is achieved by selective purging, by passing gases in the reactor recycle loop across membranes selective in favor of the contaminant over hydrogen.

Abstract: Processes and apparatus for providing improved catalytic reforming, specifically improved recovery of reformate and hydrogen from catalytic reformers. The improvement is achieved by passing portions of the reactor effluent or streams derived from the reactor effluent across membranes selective in favor of light hydrocarbons over hydrogen.

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: High-vacuum oil refinery systems and process are disclosed in this invention. The systems and process enables to carry out vaporization and distillation of oils under the condition of 1-10.sup.-4 Torr of high vacuum and at the temperature of not higher than 360.degree. C. and thereby removing possibility of thermal cracking while heating to be vaporized and easily produces high quality oil. The vaporized gases are centrifugally separated and liquefied by specific gravity using high-vacuum gas specific gravity centrifugal separators and thereby producing high purity oil of uniform quality. The process also carries out vaporization and distillation of the oil at the temperature of not higher than 360.degree. C. so that the process prevents vaporization of sulfur components of the oil, but simply drains the sulfur components along with the concentrated sludge oil and thereby distilling and desulfurizing the crude or heavy oil at the same time without using expensive conventional desulfurizing process.

Abstract: The viscosity of quench oil circulated in a pyrolysis fractionation unit is controlled by contacting pyrolysis furnace effluent with a slip stream of 0.1-0.5 kg/kg of the quench oil, separating the resulting vapor-liquid mixture to remove tarry liquid, and feeding the remaining vapor to the fractionator. Removing the tarry liquid from the fractionator feed in this manner allows operation of the fractionator with less reflux, a higher bottoms temperature, and more heat recovery at a higher temperature.

Abstract: Discloses high purity solvent compositions constituted of n-paraffins and isoparaffins, with the isoparaffins containing predominantly methyl branches, and having an isoparaffin:n-paraffin ratio sufficient to provide superior low temperature properties and low viscosities. The solvent compositions are made by a process wherein a waxy, or long chain paraffinic feed, especially a Fischer-Tropsch wax, is reacted over a dual function catalyst to produce hydroisomerization and hydrocracking reactions at 700.degree. F.+ conversion levels ranging from about 20 to 90 wt. % to provide a C.sub.5 -1050.degree. F. crude fraction. The C.sub.5 -1050.degree. F. crude fraction is then topped via atmospheric distillation to produce a low boiling fraction with an upper end point boiling between about 650.degree. F. and 750.degree. F. The low boiling fraction is fractionated and a narrow boiling range solvent obtained therefrom; one which can be further divided into solvent grades of various boiling ranges.

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: 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: Purified hydrogen is recovered from the effluent of a catalytic dehydrogenation zone using an integrated cold absorption process. The effluent, which contains olefinic hydrocarbons and hydrogen is compressed, cooled and contacted with a liquid absorbent. The purified hydrogen can be recycled to the dehydrogenation zone and the olefinic hydrocarbons are recovered as product. The present invention will recover higher purity hydrogen and liquefiable hydrocarbons more economically than prior art processes.

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: 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: A process for recovering hydrogen-rich gases and increasing the recovery of liquid hydrocarbon products from a hydrocarbon conversion zone effluent is improved by a particular arrangement of a refrigeration zone, a pressure swing adsorption (PSA) zone, and up to two separation zones. The admixing of at least a portion of the tail gas from the PSA zone with a hydrogen-rich gas stream recovered from a first vapor-liquid separation zone results in significantly improved hydrocarbon recoveries and the production of a high purity hydrogen product. The process is especially beneficial in the integration of the catalytic reforming process with vapor hydrogen consuming processes such as catalytic hydrocracking in a petroleum refinery.

Abstract: Basically, the present invention is predicated on the discovery that zeolites that have a high silica to alumina ratio, e.g., a ratio of 20 and above, pore diameters of greater than about 5.0.ANG., and which have substantially no active acid sites, i.e., zeolites which are non-reactive toward olefin isomerization and oligomerization, are especially useful in substantially separating linear olefins and paraffins from hydrocarbon mixtures containing at least linear and branched aliphatic hydrocarbons and optionally containing aromatic and other hydrocarbons.

Abstract: The impurity content, e.g. propionitrile, in a fraction containing C.sub.5 or C.sub.6 tertiary olefins obtained by cracking hydrocarbons is reduced by distilling with an alkanol and removing the impurity as a higher boiling point fraction.

Abstract: The present invention is an integrated catalytic reforming/hydrodealkylation process that maximizes benzene recovery by incorporating refrigeration and pressure swing adsorption separation units. In the refrigeration separation unit, liquid reformate is used as a sponge oil to recover benzene from a hydrodealkylation purge gas stream, which in the past has been vented. The pressure swing adsorption unit remove impurities from a hydrogen-rich gas stream prior to use in the hydrodealkylation unit.

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: The present invention is a catalytic hydrocracking process which minimizes the fouling of the process unit with 11.sup.+ ring heavy polynuclear aromatic compounds by means of hydrogenating and converting at least a portion or slipstream of the hydrocarbon effluent from the hydrocracking zone containing trace quantities of 11.sup.+ ring heavy polynuclear aromatic compounds in a 11.sup.+ ring heavy polynuclear aromatic compound conversion zone containing a hydrogenation catalyst having a hydrogenation component at hydrogenation conditions to selectively reduce the concentration of 11.sup.+ ring heavy polynuclear aromatic compounds before the hydrocracking zone effluent is cooled below about 400.degree. F. At least a portion of the effluent from the 11.sup.+ ring heavy polynuclear aromatic compound conversion zone is cooled and separated to produce at least a portion of the unconverted recycle stream.

Abstract: The present invention relates to a hydrocracking and isomerization process for preparing low pour point middle distillate hydrocarbons and lube oil from a hydrocarbonaceous feedstock boiling above about 600.degree. F. by contacting the feedstock with a catalyst containing an intermediate pore size silicoaluminophosphate molecular sieve and a hydrogenation component.

Abstract: Potential problems associated with the formation of polynuclear aromatic compounds during hydrocracking of residual oils are eliminated by operating at high conversion rates with a high hydrogen concentration followed by a unique separation method. The feed to the final product recovery column is preferably highly vaporized before or within the column. All of the net bottoms stream of the product recovery column, which is equal to less than 5 vol. percent of the feed, is withdrawn from the process. Only PNA free distillate is recycled.

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: A hydroconversion effluent separation process is provided.The effluent from the hydroconversion zone is passed to a hot high pressure separation zone. The gas phase from that zone is then passed to a cold high pressure separation zone while the liquid hydrocarbon bottoms is passed to a hot low pressure separation zone. The gas phase is partially condensed in the cold high pressure separation zone to obtain a hydrogen-rich gas and a liquid hydrocarbon bottoms. A portion of the hydrogen-rich gas is recycled to the hydroconversion zone. A second portion is sent to a hydrogen purification step, most preferably by membrane separation, and the purified gas is recycled to the hydroconversion zone. The overhead from the hot low pressure separation is fed to a cold low pressure separation zone. The gas phase from the cold low pressure separation zone is recycled to the hydroconversion zone. Preferably, two cold low pressure separation zones are utilized in the process.

Abstract: Heavy crude oil emulsions are converted to lighter essentially sulphur-free and nitrogen-free hydrocarbons by Group VI B or Group VIII B metal compounds or complexes along with carbon monoxide, hydrogen or mixtures of carbon monoxide and hydrogen, and broken without the necessity for prior emulsion treatment and separation.

Abstract: A catalytic hydrocracking process which minimizes the fouling of the process unit with 11.sup.+ ring heavy polynuclear aromatic compounds by means of hydrogenating and converting at least a portion of the recycle hydrocarbon liquid containing trace quantities of 11.sup.+ ring heavy polynuclear aromatic compounds in a 11.sup.+ ring heavy polynuclear aromatic compound conversion zone containing a zeolite hydrogenation catalyst having pore openings in the range from about 8 to about 15 Angstroms, a hydrogenation component and an intercalated clay component at hydrogenation conditions to selectively reduce the concentration of 11.sup.+ ring heavy polynuclear aromatic compounds.

Abstract: The quality and yield of dewaxed, hydrotreated lube oil base stocks are improved by reducing the top temperature in the hydrotreated lube stripper so as to increase the proportion of heavy kerosene components in the lube oil base stock. The separation system provides for a two stage stripping of the lube oil fraction such that the kerosene fraction stripped from the lube product in the primary product stripper under vacuum is stripped in a second stage stripper at a higher pressure with recycle of the heavy kerosene fraction as a reflux stream to the primary vacuum stripper so that a product with improved viscosity index and flash point is separated in the primary stripper.

Abstract: Potential problems associated with the formation of polynuclear aromatic compounds during hydrocracking of residual oils are eliminated by operating at high conversion rates with a high hydrogen concentration followed by a unique separation method. The feed to the final product recovery column is highly vaporized. All of the net bottoms stream of the product recovery column, which is equal to less than 5 vol. percent of the feed, is withdrawn from the process. Only PNA free distillate is recycled.

Abstract: A catalytic hydrocracking process which comprises: (a) contacting a hydrocarbonaceous feedstock having a propensity to form 11.sup.+ ring heavy polynuclear aromatic compounds and a liquid recycle stream in a hydrocracking zone with added hydrogen and a metal promoted hydrocracking catalyst at elevated temperature and pressure sufficient to convert a substantial portion of the feedstock to lower boiling hydrocarbon products; (b) partially condensing the hydrocarbon effluent from the hydrocracking zone to produce a gaseous hydrocarbon stream comprising hydrogen, and an unconverted hydrocarbon stream having components boiling above about 400.degree. F. (204.degree. C.) and comprising trace quantities of 11.sup.

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 removing catalyst fines from slurry oil is disclosed. A settling reagent, such as coal, alumina, or coke, is added to a fines containing heavy oil bottoms product from a fractionator downstream of a catalytic cracking unit. The settling reagent promotes rapid settling and removal of fines from heavy oil product. Settling may be performed in a slurry settler, or a centrifuge. A catalytic cracking process for heavy, metals laden oil is also disclosed using a settling reagent to clarify slurry oil, then recycling settled settling reagent to contact the heavy oil in the catalytic cracking process.

Abstract: In a first condensation stage (which is on the rising current end of the low-temperature carbonization drum and the equipment for which is integrated) quenching is done with a cooled low-temperature carbonization oil fraction containing solids. Simultaneously the whole discharge opening placed on the rising current end in the base region of the low-temperature carbonization drum for the volatile components of the low-temperature carbonization process is continuously scrubbed clean with the low-temperature carbonization oil fraction containing solids. Additionally, the volatile and liquid components are also drawn off simultaneously.

Abstract: Resid hydrotreating conversion of resid can be substantially increased by blending the resid with high-temperature flash drum oil before being hydrotreated in a train of ebullated bed reactors. The high-temperature flash drum oil also improves the overall thermal efficiency of the process.

Abstract: A hydrotreatment method, for example, hydroviscoreduction or hydrodesulfurization in which the charge of hydrocarbons is reacted with hydrogen in contact with a catalyst finely dispersed in the liquid phase. To separate the product from the catalyst, the effluent freed from its accompanying free gas is passed along, and in contact with the upstream wall of a porous inorganic membrane. The oil that has not been filtered contains a concentrate of catalyst and is recycled to the hydrotreatment reactor. The filtered oil constitutes the product of the method.

Abstract: An improved process for removing free liquid from a hydrocarbon-rich gas stream is disclosed. Liquid is injected into the gas stream upstream of a chiller and downstream of an acid-gas removal system and any equipment that may affect the water content of the gas stream: compressors, columns, additional knockout drums, heat exchangers or the like. This enhances heat and mass transfer in a manner that both minimizes the formation of small droplets and encourages the coalescence of small droplets in the chiller. As a result, small droplets which would normally pass through a knockout drum and a standard mist eliminator are increased in size, prior to their arrival at a vapor-liquid separator to larger drops which are easily removed by the vapor-liquid separator, and the mist eliminator.

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: Disclosed is a method and apparatus for separating and stabilizing a hydrotreater effluent into a stabilized liquid product and a dry gas product. The hydrotreater effluent is expanded in a first expansion drum from a high pressure to an intermediate pressure, evolving both gaseous and liquid phase components. The gaseous phase components are withdrawn as the gas product and the liquid phase components are further processed. The liquid phase components are further expanded in a second expansion drum, evolving further gas products which are compressed, cooled and returned to the first expansion drum. The second expansion drum liquid phase can comprise the liquid product output or can be further treated by an additional expansion stage.

Abstract: A process for high hydroconversion of petroleum residua containing at least about 25 V % material boiling above 975.degree. F. to produce lower boiling hydrocarbon liquid products and avoid undesirable precipitation of asphaltene compounds. In the process, the feedstock is at least about 80 percent catalytically hydroconverted to material boiling below 975.degree. F. and containing a mixture of gas and liquid fractions, after which the gas fraction is removed while maintaining the resulting liquid fractions temperature above about 730.degree. F. to avoid precipitation of asphaltene compounds which causes operations difficulties in the downstream equipment. Alternatively, the pressure-reduced liquid fraction can be stripped of material boiling below about 650.degree. F. before cooling the liquid to a temperature below about 730.degree. F. to prevent such precipitation of asphaltene compounds in the downstream equipment.

Abstract: A process for high hydroconversion of petroleum residua containing at least about 25 V % material boiling above 1000.degree. F. to produce lower boiling hydrocarbon liquid products and avoid undesirable precipitation of asphaltene compounds. In the process, the feedstock is at least about 50 percent catalytically hydroconverted to material boiling below 975.degree. F. and containing a mixture of gas and liquid fractions, after which the gas fraction is removed and the resulting liquid fractions is pressure-reduced and quenched to a temperature below about 775.degree. F. To avoid precipitation of asphaltene compounds which causes operational difficulties in the downstream equipment, the quench liquid used should have an API gravity not more than about 22.degree. API higher than the API gravity of the first pressure-reduced liquid fraction.

Abstract: A process for high hydroconversion of heavy hydrocarbon liquid feedstocks such as petroleum residua containing at least about 50 V % material boiling above 975.degree. F. to produce lower boiling hydrocarbon liquid and gas products, wherein heavy RCR materials and metals compounds are removed in-situ from the reactor effluent liquid by solvent vapor extraction using a process-derived solvent vapor at supercritical conditions. In the process, the feedstock is catalytically hydroconverted at 780.degree.-860.degree. F. temperature, and the resulting liquid fraction is contacted with a process-derived solvent vapor fraction having a normal boiling range of 250.degree.-400.degree. F. and heated to supercritical temperature to dissolve and extract substantially all the hydrocarbon liquid fractions, and separate heavy RCR materials and the metals compounds contained therein.

Abstract: Coal, petroleum residuum and similar carbonaceous feed materials are subjected to hydroconversion in the presence of molecular hydrogen to produce a hydroconversion effluent which is then subjected to one or more separation steps to remove lower molecular weight liquids and produce a heavy bottoms stream containing high molecular weight liquids and unconverted carbonaceous material. The viscosity of the bottoms streams produced in the separation step or steps is prevented from increasing by treating the feed to the separation step or steps with hydrogen sulfide gas prior to or during the separation step or steps. The viscosity of the heavy bottoms stream produced in the final separation step is also controlled by treating these bottoms with hydrogen sulfide gas.

Abstract: Unreacted hydrogen contained in the gaseous effluent from a high pressure hydrogenation process is reduced in pressure, followed by purification of the hydrogen at the lower pressure, and recompression to a high pressure for use in a hydrogenation process. Liquid effluent is also reduced in pressure, hydrogen stripped therefrom, and combined with the recovered hydrogen gas at the lower pressure for purification.

Abstract: A petroleum distillate feed is upgraded and an olefinic product is produced by contacting the feed with ZSM-5-type zeolite at (1) a temperature in the 500.degree. F.-800.degree. F. range; (2) a pressure below about 13 atmospheres gauge; and (3) an LHSV in the 0.1-15 V/V/Hr range.

Abstract: Efficient utilization of hydrogen in a hydrocracking system is obtained by recovering in a first gas-liquid separation zone hydrogen by gas-liquid separation of hydrocrackate at a pressure of at least about 75 percent of the pressure in the hydrocracking zone, and recovering in a second gas-liquid separation zone hydrogen from the separated liquid phase from the first gas-liquid separation zone, said second gas-liquid separation zone being at a pressure less than 75 percent of the pressure in the first gas-liquid separation zone and at conditions sufficient to provide a separated vapor phase containing at least about 50 volume percent of hydrogen and having a hydrogen partial pressure of at least about 20 atmospheres. At least a portion of the separated vapor phase from the second gas-liquid separation zone is contacted with the feed side of a polymeric membrane exhibiting a high selectivity to the permeation of hydrogen as compared to the permeation of methane. The opposite side, i.e.

Abstract: This invention relates to a hydrocarbon conversion process effected in the presence of hydrogen, especially a hydrogen-producing hydrocarbon conversion process. More particularly, this invention relates to the catalytic reforming of a naphtha feedstock, and is especially directed to an improved recovery of the net excess hydrogen, and to an improved recovery of a C.sub.3 + normally gaseous hydrocarbon conversion product and a C.sub.5 + hydrocarbon conversion product boiling in the gasoline range.

Abstract: A hydrocrackate from a hydrocracking zone operating under hydrocracking conditions is separated into at least one liquid phase and a separated vapor phase wherein the separated vapor phase has a greater concentration of hydrogen than the minimum concentration of hydrogen in the vapor phase in the hydrocracking zone. At least a portion of the separated vapor phase is contacted with the feed side of a polymeric membrane selective to the permeation of hydrogen as compared to the permeation of methane, and the opposite side of the polymeric membrane is maintained at a pressure sufficiently below the pressure at the feed side of the polymeric membrane to permeate hydrogen to the opposite side of the polymeric membrane and to provide a hydrogen permeate having a concentration of hydrogen greater than the concentration of hydrogen in the separated vapor phase and greater than the concentration of hydrogen in the hydrogen feed gas. The hydrogen permeate is compressed and recycled to the hydrocracking zone.