Abstract: A process and apparatus for fractionation of a superheated vapor in a fractionation column is disclosed. A conventional fractionator, having an inlet for hot vapors at the base, and a plurality of products withdrawn via side draws is modified by physically inverting some parts of the column. The superheated vapors are charged to an upper portion of the column, to contact and vaporize a liquid fraction pumped up from a lower portion of the column. The vaporized liquid is discharged as a vapor fraction to the base of the column from which the liquid fraction was obtained. Superheated vapor fed to the column is fractionated, but in a fractionator in which the hottest part of the column is not in the base of the column. The inverted fractionator, when used in conjunction with a riser cracking FCC reactor, greatly reduces thermal cracking in a transfer line moving superheated, cracked vapor from the reactor to the fractionator.

Abstract: Hydrocarbon feeds are dewaxed and hydrotreated in a two-stage dewaxing-hydrotreating reactor system with interstage separation of olefinic and naphtha and light olefins. Separation of the naphtha and olefins is carried out by stripping the effluent from the dewaxing reactor with a stripping medium such as make-up hydrogen or vapor from the hydrotreater effluent. Hydrogen recycle for the dewaxer and the hydrotreater is taken from the stripper/separator after removal of the olefinic naphtha and removal of contaminants. Separation of the lighter olefins from the olefinic naphtha may be improved by the use of an oil solvent such as naphtha introduced into the top of the interstage stripper/separator so that the recycle gas from the stripper/separator is essentially free of wet gas and heavier fractions.

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: High octane gasoline and high quality distillate are co-produced by a hydrocracking process in which a catalytic cracking light cycle oil is hydrocracked under conditions of low to moderate hydrogen pressure and severity to produce a high octane, hydrocracked gasoline. The distillate fraction which boils immediately above the gasoline fraction is recycled to the hydrocracker to increase the paraffinic content of this fraction by partial saturation and cracking of the aromatics contained in it so as to form a paraffinic distillate of low sulfur and high cetane index which is useful as a road diesel fuel. A higher boiling distillate fraction of relatively lower aromaticity may also be produced for use as a low sulfur fuel oil. The recycled fraction may be cooled to provide quench for the hydrocracker.

Abstract: A hydrotreating process uses a separation section that reduces the loss of C.sub.5 and higher hydrocarbons through the use of a low hydrogen to hydrocarbon ratio in the reactor and the adsorptive removal of a majority of hydrogen sulfide from a liquid phase hydrotreater effluent. Sulfurous hydrocarbon feed is admixed with hydrogen to maintain a hydrogen to hydrocarbon ratio of less than 50 SCFB. The hydrogen and hydrocarbons are passed through a hydrotreater reactor to convert sulfur compounds to H.sub.2 S. The hydrotreater effluent is cooled and after flashing of any excess hydrogen or light ends the cooled effluent is contacted with an adsorbent material for the removal of H.sub.2 S. A hydrotreated hydrocarbon product is withdrawn from the adsorption section. The low hydrogen to hydrocarbon ratio permits the process to be used without the recycle of hydrogen thereby eliminating the need for separators and compressors that were formerly used to recycle hydrogen to the hydrotreater.

Abstract: A process and apparatus for preheating and catalytic cracking of heavy oils is disclosed. Direct contact heat exchange of heavy feed, such as a resid, with hot product vapor from the cracking reactor provides an efficient way to preheat a heavy feed to an unusually high temperature, preferably in excess of 600.degree. F. Cooling hot cracked products from an FCC or TCC reactor upstream of the main fractionator reduces thermal cracking in the transfer line. High temperature preheat reduces the viscosity of the heavy feed, improves contact of heavy feed with cracking catalyst and reduces the amount of catalyst required to effect the catalytic cracking reaction. This improves yields, permits higher cracking reactor temperatures, and reduces cat:oil coke make.

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 hydrocarbonaceous feedstock is hydrocracked by contacting the feedstock in a first reaction stage at elevated temperature and pressure in the presence of hydrogen with a first hydrocracking catalyst to obtain a first effluent, separating from the first effluent a gaseous phase and a liquid phase at substantially the same temperature and pressure as prevailing in the first reaction stage, contacting the liquid phase of the first effluent in a second reaction stage at elevated temperature and pressure in the presence of hydrogen and a second hydrocracking catalyst to obtain a second effluent, obtaining at least one distillate fraction and a residual fraction from the combination of the gaseous phase and the second effluent by fractionation, and recycling at least a part of the residual fraction to a reaction stage.

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: A process is disclosed for converting a gaseous or vaporized hydrocarbon feedstock to a product comprising ethylene, acetylene or a mixture thereof.

Abstract: A process for treating a hydrocarbonaceous stream containing a non-distillable component to produce a hydrogenated distillable hydrocarbonaceous product while minimizing thermal degradation of the hydrocarbonaceous stream which process comprises the steps of: (a) contacting the hydrocarbonaceous stream with a hot first hydrogen-rich gaseous stream having a temperture greater than the hydrocarbonaceous stream in a flash zone at flash conditions thereby increasing the temperature of the hydrocarbonaceous stream without indirect heat exchange and vaporizing at least a portion thereof to provide a hydrocarbonaceous vapor stream comprising hydrogen and a heavy stream comprising the non-distillable component; (b) contacting the hydrocarbonaceous vapor stream comprising hydrogen with a hydrogenation catalyst in a hydrogenation reaction zone at hydrogenation conditions to increase the hydrogen content of the hydrocarbonaceous compounds contained in the hydrocarbonaceous vapor stream; (c) condensing at least a portion

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 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 gain a substantial conversion to lower boiling products; (b) 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 boiling above about 400.degree. F. (204.degree. C.) and comprising trace quantities of 11.sup.+ ring heavy polynuclear aromatic compounds; (c) introducing at least a portion of the unconverted hydrocarbon stream boiling above about 400.degree. F. (204.degree. C.) and comprising trace quantities of 11.sup.+ ring heavy polynuclear aromatic compounds into a 11.sup.

Abstract: A process for the production of hydrogen-enriched hydrocarbonaceous products which process comprises: (a) converting a heavy, asphaltene-containing hydrocarbonaceous residual oil, wherein at least 80% of the residual oil boils above 650.degree. F. (343.degree. C.), in the presence of hydrogen and a particulate catalyst at residual oil conversion conditions in a reaction zone to produce a liquid effluent stream comprising particulate catalyst and normally liquid hydrocarbonaceous compounds; (b) contacting at least a portion of the liquid effluent stream from step (a) with water and a hydrocarbonaceous solvent comprising at least one aromatic hydrocarbon; and (c) gravitationally separating the resulting admixture from step (b) into a solvent phase comprising the normally liquid hydrocarbonaceous compounds and essentially free of solids, and an aqueous phase comprising essentially all of the particulate catalyst.

Abstract: A process for converting a gas oil range petroleum feedstock into lighter petroleum products by:(a) charging the gas oil range petroleum feedstock and hydrogen to a first fixed bed hydrocracking zone containing a hydrocracking catalyst at hydrocracking conditions to produce a first hydrocracking zone product stream;(b) separating the first fixed bed hydrocracking zone product stream in a fractionation zone into a petroleum products stream and a bottoms stream;(c) charging the bottoms stream and hydrogen to a second fixed bed hydrocracking zone containing a hydrocracking catalyst at hydrocracking conditions to produce a second fixed bed hydrocracking zone product stream;(d) cooling the second fixed bed hydrocracking zone product stream to a temperature below about 250.degree. F.;(e) recycling a first portion of the cooled second fixed bed hydrocracking zone product stream to the fractionation zone; removing materials having a boiling range from about 500.degree. to about 650.degree. F.

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: An effective, economical catalytic cracking process is provided to produce quality gasoline and other hydrocarbons from whole crude oil. The catalytic cracking process is operable and particularly useful during maintenance or shutdown of associated pipestills, vacuum tower, and/or atmospheric tower.

Abstract: A method for hydrocracking a heavy fraction oil characterized by cracking a heavy fraction oil in the presence of a hydrogen donating solvent and hydrogen gas and circulating a fraction having a specific boiling range as the circulating solvent through the cracking reactor whereby the formation of carbonaceous substances is greatly inhibited, the supply of a makeup hydrogen donating solvent is disposed with and the concentration of tetralin in the circulating solvent is maintained at a fixed or higher level.

Abstract: Liquid dewaxing product recycled back as input feed in, for example, a lube dewaxing or distillate dewaxing process, provides improved catalyst performance, improved V.I. and improved yield.

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: An effective hydrotreating process is provided to minimize precipitation of asphaltenic solids in the product oil. In the preferred process, an aromatic diluent, preferably comprising decanted oil, is injected into one or more of the fractionators downstream of the reactor.

Abstract: An improved method for producing a hydrotreated oil from a naphthenic feed is described. The process comprises passing the naphthenic feed through the multistage hydrotreating process with intermediate removal of hydrogen sulfide and/or ammonia.

Abstract: An apparatus and process for catalytically upgrading an FCC effluent is described, wherein the FCC effluent is contacted with a shape-selective catalyst at low severity conditions prior to fractionation.

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 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: A process for recovering heat from a tar-containing gas while simultaneously cooling the gas in a 3-stage cooling step by (1) directing a tar-containing gas through a jet cooler comprising a bed of solid particles so that the gas contacts the solid particles and forms a fluidized bed with the flow of the tar-containing gas, which jet cooler comprises a central draft tube into which the gas is directed and indirect heat exchange lines containing a liquid coolant therein disposed inside the central draft tube and wherein the gas and solid particles are cooled by such indirect heat exchange lines such that the tar from the gas condenses on the solid particles; (2) directing the gas through a tar cooler in the second stage wherein the gas-containing residual tars and other impurities resulting from the treatment in the jet cooler are sprayed with a circulating tar from a nozzle to remove a residual tars and impurities from the gas and wherein the gas is further cooled in said tar cooler by means of an indirect he

Abstract: A catalytic hydrocracking process which comprises (a) introducing a reduced crude into a fractionation zone to produce a vacuum gas oil stream having a propensity to form polynuclear aromatic compounds in a hydrocracking zone and a slop wax stream; (b) contacting the vacuum gas oil stream in a hydrocracking zone with added hydrogen and a metal promoted hydrocracking catalyst at elevated temperature and pressure sufficient to gain a substantial conversion to lower boiling products; (c) partially condensing the hydrocarbon effluent from the hydrocracking zone and separating the same into a low boiling hydrocarbon product stream and an unconverted hydrocarbon stream boiling above about 650.degree. F. (343.degree. C.

Abstract: A process for catalytically cracking a hydrocarbon-containing feed stream, preferably having an API.sup.60 gravity of about 5-30, wherein at least a portion of off-gases is treated so as to remove C.sub.2 -C.sub.4 olefins therefrom, and the off-gas stream having a reduced olefin content is then recycled to the catalytic cracking zone.

Abstract: Vacuum resid and cracked residuum such as decant oil or thermal tar are processed together to reduce the ultimate yield of coke, asphalt and fuel oil. The vacuum resid is donor cracked, and the donor cracker effluent is quenched with decant oil or thermal tar and then fractionated. Fractionator bottoms are vacuum distilled, and vacuum tower overheads are hydrogenated to produce donor for the donor cracker.

Abstract: A process for providing a hydrogen-rich gas stream from a reaction zone effluent comprising hydrogen and hydrocarbons is disclosed.

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: There is disclosed a system for measuring and controlling the concentration of hydrogen in hydrogen recycle processes used in oil refineries and petrochemical plants. The system is intended to reduce the amount of hydrogen and hydrocarbon vapor circulating in such systems, thus reducing the quantity of utilities needed to operate such systems. Specifically, there is a savings of compressor power and fuel required for heating. The system is dependent on the recognition that a decrease in cooling medium temperature results in an increase in hydrogen flow, which can be decreased to the minimum permissible without endangering catalyst activity and stability and product yield if hydrogen concentration is monitored, and that partial pressure is the key parameter.

Abstract: There is disclosed a system for measuring and controlling the concentration of hydrogen in hydrogen recycle processes used in oil refineries and petrochemical plants. The system is intended to permit reduction in hydrogen use in hydrogen-consuming hydrogen recycle processes. The system is dependent on the recognition that a decrease in cooling medium temperature results in an increase in vent gas flow, which can be decreased to the minimum permissible without endangering catalyst activity and stability and product yield if hydrogen concentration is monitored, and that partial pressure is the key parameter.

Abstract: A delayed coking process is provided in which the fresh hydrocarbonaceous oil feed is divided into at least two streams. One stream is introduced directly into the preheating zone of the coking zone and one stream is introduced into the coker product fractionator. The fractionator bottoms fraction is recycled to the preheating zone as a separate stream from the fresh feed stream. The separate preheated fresh feed stream is introduced into the top of the coking zone and the preheated recycled fractionator bottoms fraction is introduced into the bottom of the coking zone. The given fresh feed splitting configuration permits decreasing the recycle rate of the heavy coker product and increasing liquid yield while the top and bottom feeding to the coking zone permit subjecting the given streams to different severity of coking.

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: A process for converting high-boiling crude oil having a high content of nondistillable residue which crude oil contains metals and asphaltenes by donor solvent hydrovisbreaking is disclosed wherein the process is carried out near the carbonization temperature limit in the presence of a hydrogen donor. The hydrogen donor can be one derived from the crude itself, from a similar crude oil, or from the distillate product of said donor solvent hydrovisbreaking.

Abstract: Visbreaking a mixture of petroleum residuum, coal and catalytic cracking catalyst under conditions severe enough to effect conversion but not so severe as to produce substantial quantities of coke produces a range of products including gaseous olefins and gasoline distillate. The solids recovered from the visbreaking operation can be processed to produce a synthesis gas of carbon monoxide and hydrogen.

Abstract: A process for the isomerization of acyclic hydrocarbons and alkylaromatic hydrocarbons is disclosed. The mixed-phase feed stream is heated and the liquid-phase portion of the feed stream is simultaneously vaporized by indirect heat exchange against the effluent of the reaction zone. Prior to this exchange, the effluent of the isomerization zone is heated in a fired heater to a temperature above that employed in the reaction zone. The inventive concept eliminates the need to pass mixed-phase feed streams through fired multi-pass heaters.

Abstract: An economic route to transport fuels from low grade feedstocks containing organic polycyclic components and mineral and/or metallic components comprises separating the feedstock into (a) a residue containing fuel values and substantially all of the mineral and metallic components and (b) a liquid hydrocarbon fraction; hydrogenating the liquid hydrocarbon fraction; providing hydrogen for the hydrogenation by steam reforming methane-containing gas recovered from the hydrogenated material; and providing the heat for the steam reforming by immersing the reformer reactor tubes in a fluidized bed heated by combustion of residue from the separation step. If the fluidized bed is pressurized, the process can be made substantially self-contained with all the heat and power requirements for steam generation and feedstock compression for hydrogenation and steam reforming being recovered from the flue gas.

Abstract: Hydrocracked, low pour lubricating oils of good stability are manufactured by passing a suitable hydrocarbon feed and hydrogen sequentially through a hydrocracking zone, a catalytic dewaxing zone, and a hydrotreating zone, all at high pressure and in that order, with purification of the hydrogen gas prior to passage to the dewaxing zone. By maintaining all zones at high pressure, the efficiency of the process is augmented.

Abstract: Hydrocracked, low pour lubricating oils of good stability are manufactured by passing a suitable hydrocarbon feed sequentially through a hydrocracking zone, a catalytic dewaxing zone, and a hydrotreating zone, all at high pressure and in that order, and with separation of hydrocrackate from recycle hydrogen prior to dewaxing. Only clean makeup hydrogen is fed to the dewaxer, passed through the hydrotreater, and then on to the hydrocracker, thereby providing an exceptionally efficient process.

Abstract: A petroleum distillate feed is upgraded and a substantial C.sub.3 -C.sub.4 olefin product fraction produced by contacting the feed with ZSM-5 type zeolite at (1) a temperature in the 500.degree.-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, and fractionating the effluent product stream.

Abstract: Problems associated with heating the mixed-phase feed stream of a hydrocarbon conversion process are reduced by a method of operation which includes heating the feed stream to a sufficient temperature for passage into a reaction zone by indirect heat exchange. The effluent stream of the reaction zone is then further heated in a fired heater and is passed through the indirect heat exchange zone in which the feed stream was heated.

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: This invention provides a continuous process for separating a gaseous phase from a hydrocarbon liquid containing carbonaceous particulates and gases. The liquid is fed to a cylindrical separator, with the gaseous phase being removed therefrom as an overhead product, whereas the hydrocarbon liquid and the particulates are withdrawn as a bottoms product. By feeding the liquid tangentially to the separator and maintaining a particulate-liquid slurry downward velocity of from about 0.01 to about 0.25 fps in the separator, a total solids weight percent in the slurry of from about 0.1 to about 30%, a slurry temperature of from about 550.degree. to about 900.degree. F., a slurry residence time in the separator of from about 30 to about 360 seconds, and a length/diameter ratio for the separator of from about 20/1 to about 50/1, so that the characterization factor, .alpha., defined as ##STR1## DOES NOT EXCEED ABOUT 48 (.degree.R sec.sup.

Abstract: The liquid product of a slurry hydrogen treating zone is separated into fractions in the same separation zone used to obtain the heavy hydrocarbonaceous oil fraction used as feed for the hydrogen treating zone. A separate portion of coarser solids is withdrawn from the hydrogen treating zone.

Abstract: A vapor-liquid separator is provided which is adapted to be connected directly to the exit of a fixed reactor bed, and includes a vertically disposed housing, an upper portion of which is connected to vapor-liquid inlet means which may be provided by the fixed bed reactor so that a vapor-liquid mixture may be introduced downwardly into the housing.