Abstract: In an integrated lube oil process, a lube oil stock is hydrotreated over a non-noble metal containing hydrotreating catalyst in an HDN/HDS unit to remove sulfur and nitrogen from the lube oil stock and produce an HDN/HDS unit effluent. The effluent comprises hydrodesulfurized, hydrodenitrogenated lube oil stock, hydrogen sulfide and ammonia. The hydrogen sulfide and ammonia are stripped from the hydrodesulfurized, hydrodenitrogenated lube oil stock to form a liquid stream comprising stripped lube oil stock and a first gas stream comprising hydrogen sulfide, ammonia and molecular hydrogen. The stripped lube oil stock is hydrotreated over a noble-metal containing hydrotreating catalyst in an HDW unit to produce an HDW unit effluent comprising a dewaxed lube oil stock. A second gas stream comprising molecular hydrogen is separated from the dewaxed lube oil stock. The first gas stream is combined with the second gas stream to form a third gas stream.

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 method of producing hydrocarbon diluent from heavy crude oil, comprises pre-heating the crude oil to produce a heated crude oil, separating in a separator vessel by flashing the heated crude oil to produce a first vapor fraction and a first liquid fraction, thermally cracking in a cracking unit at least a portion of the first liquid fraction to produce a first liquid effluent, quenching the first liquid effluent, introducing at least a portion of the quenched first liquid effluent into a separator, condensing the first vapor fraction, and separating in a separator vessel the condensed vapor fraction to produce the hydrocarbon diluent and gas.

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 benzene content of hydrocarbon gasolines is accomplished by (a) fractionating at least one hydrocarbon gasoline into a light fraction A, with an increased benzene content, and a heavy fraction B, with a reduced benzene content; (b) contacting the light fraction A at a temperature below room temperature with a gas containing at least a fraction of olefins in which the number of carbon atoms is from 2 to 5 per molecule so that at least a fraction of said olefins is absorbed in light fraction A; at the end of stage (b), separating a residual gas with a reduced olefin content from a liquid fraction C, with an increased olefin content; (d) passing the fraction C from stage (c) into an alkylation reactor so that at least a fraction of the benzene is alkylated by at least a fraction of the olefins; (e) fractionating the mixture emerging from stage (d) so as to produce, firstly, a gas phase chiefly comprising gases which were not converted during stage (d) and, secondly, a liquid phase, at least partly containing

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: Catalytic Cracking is effected by feeding thereto (i) a deasphalted vacuum resid together with (ii) a solvent treated virgin vacuum gas oil, the two being preferably mixed prior to solvent treating.

Abstract: The present invention provides a process for decreasing the energy consumption of a catalytic cracking process product recovery section while improving gasoline yield by integrating multistage vapor compression and product recovery with deacidification and conversion of C.sub.2 -C.sub.4 aliphatics to C.sub.5 + normally liquid hydrocarbons.

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).

Abstract: Recarburizer coke containing not more than 0.1 weight percent sulfur and not more than 0.1 weight percent nitrogen is prepared by severe catalytic hydrotreating, followed by thermal cracking, and delayed coking of vacuum gas oil obtained from the vacuum distillation of FCC decant oil.

Abstract: The invention relates to a process for hydrocarbon fractionation and extraction making it possible to obtain a petrol with an improved octane number and a kerosene with an improved smoke point.According to the invention a charge with a final boiling point of at least 220.degree. C. is fractionated into three fractions:a light petrol containing less than 10% aromatics and boiling points at 25.degree. to 80.degree. C.,a medium petrol (80.degree. C. and at the most 150.degree. C.), whose end point is determined by a nitrogen content below 50 ppm,a heavy petrol with an end point equal to or below 220.degree. C.,be a selective liquid solvent aromatics are then extracted from the heavy petrol producing a refined product which is poured into the kerosene pool or diesel fuel,the solvent is regenerated by reextraction using light petrol so as to produce an aromatics-enriched petrol fraction with an improved octane number.

Abstract: A process for treating an organic stream containing a non-distillable component to produce an organic vapor stream and a solid which process comprises the steps of: (a) contacting the organic stream containing a non-distillable component with a hydrogen-rich gaseous steam having a temperature greater than the organic stream in a flash zone at flash conditions thereby increasing the temperature of the organic stream and vaporizing at least a portion thereof to produce an organic vapor stream comprising hydrogen and a heavy stream comprising the non-distillable component; and (b) reacting at least a portion of the heavy stream comprising the non-distillable component in the presence of hydrogen in a pyrolysis zone to produce a thermally stabilized volatile organic stream comprising hydrogen and a solid.

Abstract: A process is disclosed for increasing the octane number of an FCC unit gasoline pool by upgrading selected gasoline boiling-range streams. FCC gasoline is mixed with the feed to a light olefin upgrading reactor. Upgraded gasoline is then fractionated in an existing FCC gas plant.

Abstract: A heavy crude oil is fractionated into at least three liquid fractions which include a distillate fraction boiling in the 400.degree. F.-650.degree. F. range and a 650.degree. F.+ boiling range residuum. The distillate cut is hydrodesulfurized and the residuum is hydrodemetallized. The cuts thus hydrotreated, and at least a part of the third liquid fraction, are then combined to form an upgraded synthetic crude oil of relatively low sulfur content and relatively low vanadium and nickel content.

Abstract: A process for producing a pumpable syncrude from a Fischer-Tropsch wax by fractionating the wax into relatively low boiling fraction containing oxygenate compounds and a relatively high boiling fraction which is substantially free of oxygenate compounds and thereafter isomerizing/hydrocracking the low boiling fraction in the presence of hydrogen and a fluorided Group VIII metal-on-alumina catalyst. The preferred Group VIII metal is platinum.The pumpable syncrude is thereafter fractionated to produce a low boiling fraction which is thereafter isomerized/hydrocracked in the presence of hydrogen and a fluorided Group VIII metal-on-alumina catalyst to produce upgraded middle distillate fuel products. The preferred catalyst for middle distillate production is a fluorided platinum-on-alumina catalyst where a major portion of the fluoride within the catalyst is present as aluminum fluoride hydroxide hydrate.

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 reforming a full boiling range naptha feed to enhance benzene yield is disclosed which first separates the feed into a C.sub.6 fraction containing at least 10% by volume of C.sub.7 + hydrocarbons and a C.sub.7 + fraction, then subjecting the C.sub.6 fraction to a catalytic aromatization process and subjecting the C.sub.7 + fraction to a catalytic reforming process, followed by recovering the aromatics produced.

Abstract: Residual oils from steam-cracking or catalytic cracking, oils from coal liquefaction and oils from bituminous sands and shales are converted to gasoline by a process comprising the fractionation of the feed charge to a naphtha and a middle distillate: the naphtha, admixed with a gasoline cut "E", is hydrotreated and then dehydrogenated to gasoline; the middle distillate is hydrotreated and fractionated to gasoline and a heavier fraction, the heavier fraction is hydrocracked and fractionated, thus producing a gasoline cut which constitutes the above cut "E".

Abstract: An integrated combination of fluid catalytic cracking and hydrocracking select fractions of crude oil and FCC cycle oils to conserve hydrogen process requirements in the production of gasoline is discussed. Liquid products of hydrocracking are separated into low boiling components and a high boiling fraction is recycled to the FCC operation. Select fractions obtained from hydrocracking, FCC and crude oil distillation are upgraded by reforming and alkylation.

Abstract: Method and means for converting organic materials, such as garbage, sewage sludge, wood and agricultural products, and the like, to fuels are disclosed which include pre-drying the organic feed material and feeding the same to a reactor for the pyrolysis thereof. Pyrolytic off-gases are fed to a condenser where a condensable fraction comprising, generally, oil and water is removed. The gas phase from the condenser is scrubbed by means of a scrubber, passed through an activated charcoal filter, and burned to supply heat for at least partially drying the reactor feed material.First gravity separating means separates the liquid phase from the condenser into oil and water fractions. Similarly, second gravity separating means, to which scrubber liquid is supplied, separates the scrubber liquid into oil and water fractions. The water fraction from the second gravity separating means is supplied as scrubbing liquid for scrubbing the gas phase.

Abstract: Heavy high-sulfur crude oil is subjected to distillation to produce gas and liquid hydrocarbon products and a residuum. The gas and liquid products are desulfurized. Part of the residuum is coked in a delayed coker, and sulfur in the coke is removed by high temperature calcination. The remainder of the residuum is air-blown to produce an asphalt product, and sulfur recovered from the other products is added to the asphalt to produce a sulfur-enriched asphalt product.

Abstract: A process of producing a solvent useful in coal liquefaction which includes separating the heavy liquid produced from the liquefaction of coal into a fraction boiling at 200.degree. to 210.degree. C., a fraction boiling at 211.degree. to 230.degree. C., and a fraction boiling at not less than 231.degree. subjecting the fraction boiling at 211.degree. to 230.degree. C. to a hydrogenation treatment to produce a hydrogenated fraction, mixing the hydrogenated fraction with the fraction boiling at 200.degree. to 210.degree. C. to form a resultant mixture, and mixing a portion of the resultant mixture with a portion of the fraction boiling at not less than 231.degree. C. Alternately, the solvent is produced from the heavy liquid by separating it into a fraction boiling at 200.degree. C. to 210.degree. C., a fraction boiling at 211.degree. C. to 230.degree. C., a fraction boiling at 231.degree. C. to 250.degree. C., a fraction boiling at 251.degree. C. to 350.degree. C. and a fraction boiling at not less than 351.

Abstract: Whole crude and residual fractions from distillation of petroleum and like feed stocks are subjected to selective vaporization to prepare heavy fractions of reduced Conradson Carbon and/or metals content by short-term, high temperature riser contact with a substantially inert solid contact material of low surface area in a selective vaporization zone. High boiling point components of the charge which are of high Conradson Carbon number and/or high metal content remain on the contact material as a combustible deposit which is then burned off in a combustion zone whereby the contact material is heated to a high temperature for return to the selective vaporization zone to supply the heat required therein. The system is dynamically controlled for fuel supply in the combustion zone by the lower hydrogen content, least valuable components of the feed.

Abstract: A solvent useful in coal liquefaction is obtained by separating the heavy liquid resulting from coal liquefaction into a fraction boiling at temperatures of between 200.degree. to 210.degree. C., a fraction boiling at temperatures between 211.degree. to 250.degree. C., and a fraction boiling at not less than 250.degree. C., subjecting the fraction boiling at between 211.degree. C. to 250.degree. C. to two hydrogenation treatments, mixing the hydrogenated product with the fraction boiling at between 200.degree. to 210.degree. C. which optionally has been hydrogenated to form a resultant mixture and mixing a portion of the resultant mixture with the fraction boiling at not less than 250.degree. C. which has been optionally hydrogenated.

Abstract: Hydrocarbons are preheated, particularly for a hydrodesulfurization process by first heating the hydrocarbon stream to produce a vapor and a liquid stream, thereafter superheating at least some of the vapor phase and mixing the superheated vapor phase with the liquid phase to generate the hydrocarbon feedstream at the desired temperature. By this procedure only the evaporated hydrocarbons are subjected to a high temperature, but not the heavier hydrocarbons.

Abstract: The present invention is directed to a process for desulfurizing petroleum oils and for improving the performance of known catalytic hydrodesulfurization processes. In accordance with the process, a narrow boiling fraction of a typical hydrodesulfurization feedstock is selectively removed prior to the introduction of said feedstock into the hydrodesulfurization unit. Feedstocks include gas oils, residual oils or other fractions which contain sulfur in the form of sulfides, disulfides and a part of a substituted ring such as thiophene, benzothiophene and dibenzothiophene. The invention embodies the discovery that certain intermediate sulfur compounds are the most refractory or difficult to remove.

Abstract: Whole crude and bottoms fractions from distillation of petroleum are upgraded by high temperature, short time contact with a fluidizable solid of essentially inert character to deposit high boiling components of the charge on the solid whereby Conradson Carbon values, salt content and metal content are reduced. The upgraded hydrocarbon fraction may be supplied to fractionator, in which case the high temperatue contactor serves as a heater, e.g. crude heater for crude distillation, in addition to improving quality of the fractions derived by distillation. For charge stocks boiling above about 500.degree.-650.degree. F., the upgrading process yields a product suitable for charge to catalytic cracking in that Conradson Carbon, salts and metals are reduced to levels tolerable in catalytic cracking.

Abstract: A process which comprises fractionating a wide-boiling range naphtha feedstock into a low-boiling, light-naphtha fraction having an end or maximum boiling point within the range of about 190.degree. to about 200.degree. F. (88.degree. to about 104.degree. C.), and a high-boiling, heavy-naphtha fraction having an initial boiling point within a range of about 190.degree. to about 220.degree. F. (88.degree. to about 104.degree. C.), and contacting the light-naphtha fraction in an isomerization zone with added hydrogen and a catalyst comprising tantalum pentafluoride and hydrogen halide to produce effluent yielding naphthene components which are blended with the heavy-naphtha fraction. The resulting blended material can be processed by reforming to produce an aromatic-rich naphtha product and hydrogen.

Abstract: Production of motor gasoline and a BTX-enriched reformate by fractionating a naphtha feedstock into a mid-boiling BTX-precursor fraction, a relatively high-boiling fraction and a relatively low-boiling fraction; catalytically reforming the BTX-precursor fraction in a first reforming zone; combining the relatively high-boiling and low-boiling fractions and catalytically reforming the combined fractions in a second reforming zone.

Abstract: Heavy petroliferous stocks such as vacuum and atmospheric resids, tar sand oils, shale oils, liquids from conversion of coal and the like are concurrently distilled and hydroprocessed for removal of sulfur, nitrogen and metals and are hydrocracked or otherwise hydroprocessed in a packed distillation column under hydrogen pressure wherein the packing is constituted, at least to a substantial extent in both stripping and rectifying sections by catalyst suited to the desired conversions. In a specific application to catalytic hydrodewaxing of lubricating oil stocks, improvement of Viscosity Index (VI) of dewaxed product results.

Abstract: Distillate petroliferous stocks such as neutral lubricating stocks and distillate fuels are hydroprocessed for dewaxing and/or removal of sulfur, nitrogen and metals under hydrogen pressure in a downflow reactor packed with a catalyst suited to the desired conversions in which lighter portions of the charge are introduced to respectively lower levels of the catalyst bed, whereby product withdrawn from the bottom of the reactor is reconstituted distillate of which lighter portions have received milder treatment. In a specific application to catalytic hydrodewaxing of lubricating oil stocks, improvement of Viscosity Index (VI) of dewaxed product results.

Abstract: A process for the production of a gasoline having a low benzene content. A catalytic reformate and a stripped liquid produced in the gas concentration unit of an FCC unit are fractionated in a dehexanizer to concentrate the benzene and C.sub.3 -C.sub.4 olefins these two streams contain into a single stream. This stream is passed into an alkylation zone wherein at least some of the benzene is alkylated with the olefins. The alkylation zone effluent is stripped and recombined with C.sub.7 -plus dehexanizer bottoms stream to form a gasoline product stream.

Abstract: A processing arrangement for upgrading crude oil by the combination of hydrodewaxing, and fluid catalytic cracking or hydrocracking to maximize the production of low pour, high quality distillate fuel oil is particularly described. Cracking of atmospheric bottoms of residua, hydrodewaxing atmospheric heavy gas oil and hydrodesulfurizing light gas oil material to produce diesel fuel oil products are primary components of the processing arrangement.

Abstract: A hydrocarbon charge stock boiling below 500.degree. F. is converted into aromatic hydrocarbons and isobutane via a combination process involving catalytic reforming, hydrocracking and subsequent catalytic reforming without the immediate separation of the product effluent from the lead reformer and hydrocracking zone.

Abstract: Process for treatment of tars and oil, the process being characterized by distillation of the oil to form a vacuum distillate and vacuum residue, hydrocracking of the distillate, deasphalting of the residue, and hydrodemetallizing and hydrodesulphurizing the deasphalted residue.

Abstract: Refining of crude petroleum by fractionally distilling the crude into lighter cuts and distillate bottoms constituting more than 50% of the crude. Hydrogenating the distillate bottoms at a temperature above 700.degree. C. in a tubular reactor to produce saturated hydrocarbons, some gas and a solid carbonaceous material. Separating the solid material in a cyclone and returning the hydrogenated oil to the fractionating column. Passing the solid carbonaceous material by an extruder to a second tubular reactor in contact with a mixture at a temperature above 750.degree. C. of steam, 1 and 2 carbon atom gases, and combustion products containing O.sub.2 from a third cyclone. Discharging the reaction products containing unreacted carbonaceous material together with substantially no O.sub.2, production of H.sub.2 and increased amounts of CO and CO.sub.2 into a second cyclone. Separating the gaseous products from the solid, recovering H.sub.2 and passing it to the first reactor tube.

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: Benzene, which is toxic and carcinogenic, is removed from a gasoline or gasoline precursor stream, such as a mixture of a reformate and a naphtha produced in a fluidized catalytic cracking unit, in a process which includes fractionating the precursor stream into a light hydrocarbon stream containing the benzene and a heavy hydrocarbon stream. The light hydrocarbon stream is then admixed with an olefinic hydrocarbon, passed through an alkylation zone and then remixed with the heavy hydrocarbon stream.

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: This process applies to effluents from syntheses of the Fischer-Tropsch type; it comprises several treatments applied to the three cuts obtained from these effluents, i.e. a "light fraction", a "light oil" and a "decanted oil". These treatments comprise such steps as distillation, polymerization, alkylation, hydrotreatment, cracking-decarboxylation, isomerization and hydro reforming. The products are mainly gasoline, kerosene and gasoil.

Abstract: Process for producing low density low-sulfur crude oil as feedstock to refinery processes in which a high density, starting crude oil is divided into a base stream and a dilution stream. The dilution stream is separated into a straight run light fraction, at least a medium fraction and an asphaltic residue. At least the medium fraction is subjected to hydrocracking. The hydrocracked fraction and the light fraction are mixed with the base stream and a crude oil of low density and low sulfur content is recovered.

Abstract: Upgrading of 350.degree. F plus product of Fischer-Tropsch Synthesis is accomplished by hydrotreating the Fischer-Tropsch Synthesis product and selective cracking the hydrotreated material boiling above about 600.degree. F. A product slate is recovered comprising LPG, gasoline, jet fuel, light and heavy oil fractions.

Abstract: High grade, low-sulfur needle coke is produced from heavy high-sulfur aromatic mineral oil feedstocks by a sequence of (1) fractionating the feedstock into a minor heavy fraction, and a major lighter fraction, (2) subjecting the lighter fraction to mild hydrofining, (3) blending the heavy fraction separated in step (1) with the heavy fraction of hydrofined oil from step (2), (4) subjecting the resulting blend to delayed thermal coking, and preferably (5) recycling to the coking step heavy coker gas oil recovered from the coker effluent. If desired, the aromaticity of the heavy hydrofined oil from step (2) can be increased by subjecting the same to thermal cracking prior to step (3).

Abstract: Upgrading a Fischer-Tropsch synthesis product by separating a 350.degree. to 850.degree. F product fraction thereof into a 650.degree. F minus fraction and a 650.degree. F plus fraction; separating the 650.degree. F minus fraction to provide a more narrow 350.degree. to 650.degree. F fraction; combining the 650.degree. F plus fraction with a portion of the 350.degree. to 650.degree. F fraction to form a wide boiling range feed material; contacting this formed wide boiling range feed material, together with hydrogen, with a special catalyst comprising a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least 12 and a constraint index of 1 to 12, at a temperature of about 500.degree. to 800.degree. F, a hydrogen partial pressure of about 100 to 800 psia and a space velocity of about 0.5 to 5 LHSV to produce a converted product thereof separating the zeolite conversion product to recover a 350.degree. F minus fraction from a 350.degree. F plus fractions; and separating the 350.degree.

Abstract: The product of Fischer-Tropsch Synthesis is separated to recover a C.sub.5 -400.degree. F liquid fraction which is thereafter hydrogenated in order to saturate diolefins and contacted with a ZSM-5 type zeolite under conditions of elevated temperature and pressure so as to obtain gasoline of a higher octane rating. The contact with the ZSM-5 zeolite is preferably in the presence of added hydrogen.

Abstract: The products of Fischer-Tropsch synthesis boiling below a separated decant oil fraction are subjected to cooling to a temperature of about 100.degree. F and separation of the cooled product to recover Fischer-Tropsch produced water comprising oxygenates, a normally liquid hydrocarbon phase comprising absorbed oxygenates and a gaseous phase normally comprising a substantial amount of C.sub.5 hydrocarbons in combination with lower boiling materials including unreacted synthesis gas and carbon dioxide. Each of said gaseous phase and said normally liquid hydrocarbon phase are thereafter contacted with a selected crystalline zeolite catalyst particularly selective for the formation of gasoline boiling material of high octane.

Abstract: The product effluent of a Fischer-Tropsch synthesis is subjected to cooling sufficient to separate a high boiling product fraction boiling above about 400.degree. F from lower boiling product effluent material and comprising water product with formed oxygenates. The total lower boiling product effluent thus obtained is passed in contact with a special class of selective crystalline zeolite catalyst maintained under conditions to improve upon the hydrocarbon products contacted and convert oxygenates for hydrocarbons.

Abstract: Hydrocarbon mixtures containing 1-80% wax, e.g. shale oil, can be transported in a pipeline by distilling the mixture into an overheads fraction and a bottoms fraction, cooling the overheads fraction to a temperature above its pour point, but to a temperature sufficiently low so that when it is admixed with the bottoms fraction, the composite temperature of the mixture will be at or below the temperature at which the mixture is to be transported, and admixing the overheads fraction with the bottoms fraction (at a temperature above that at which wax crystals form) while imparting to the mixture a shear rate less than about 20 sec.sup.-1 to form a pumpable slurry. The slurry is preferably transported in a pipeline at conventional temperatures.

Abstract: A process for reforming a full boiling range naptha feed to enhance benzene yield is disclosed which first separates the feed into a .[.C.sub.6 .]. .Iadd.lighter .Iaddend.fraction .[.containing at least 10% by volume of C.sub.7+ hydrocarbons.]. .Iadd., comprising at least one member selected from the group consisting of C.sub.6, C.sub.7, and C.sub.8 hydrocarbons, .Iaddend.and a .[.C.sub.7 +.]. .Iadd.heavier .Iaddend.fraction, then subjecting the .[.C.sub.6 .]. .Iadd.lighter .Iaddend.fraction to a catalytic aromatization process .[.and subjecting the C.sub.7 + fraction to a catalytic reforming process, followed by recovering the aromatics produced.]..Iadd.in the presence of a non-acidic catalyst.Iaddend..