Abstract: The present invention discloses a process for increasing the selectivity of the production of isobutylene in an admixture of C.sub.4 olefins, in a process comprising producing isobutylene, with high selectivity, comprising catalytically producing a first composition comprising at least one C.sub.4 olefin selected from the group consisting of 1-butene, cis-2-butene, trans-2-butene, admixtures thereof and 2-methylpropene admixed with at least one of said 1-butene, cis-2-butene, and trans-2-butene, by passing paraffin containing feed, which feed is free of aromatics, and in which the paraffin contains 5 to 20 carbon atoms, in the vapor phase, over a first catalyst composition, wherein the catalyst comprises ZSM-5 or ZSM-12, and increasing the isobutylene content of the first composition by producing a second composition, by contacting the first composition with a second catalyst composition comprising ZSM-23 under conditions in which the second composition is in the vapor phase, while maintaining the total C.

Abstract: A process for naphtha cracking employing new synthetic catalyst of ultra-large pore crystalline material. The new crystalline material exhibits unusually large sorption capacity demonstrated by its benzene adsorption capacity of greater than about 15 grams benzene/100 grams at 50 torr and 25.degree. C., a hexagonal electron diffraction pattern that can be indexed with a d.sub.100 value greater than about 18 Angstrom Units and a hexagonal arrangement of uniformly sized pores with a maximum perpendicular cross section of at least about 13 Angstrom units.An improved cracking reaction is provided for catalytic conversion of hydrocarbon feedstock which comprises contacting the feedstock under catalytic conversion conditions with acid metallosilicate solid catalyst having the structure of MCM-41 with hexagonal honeycomb lattice structure consisting essentially of uniform pores in the range of about 20 to 100 Angstroms. The cracking reaction is very selective, especially when conducted at temperature of about 425.

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: An improved process for upgrading paraffinic naphtha to high octane fuel by contacting a naphtha feedstock, such as virgin naphtha feedstock stream containing predominantly C.sub.7 -C.sub.12 alkanes and naphthenes, with solid medium pore acid zeolite cracking catalyst under low pressure selective cracking conditions effective to produce at least 10 wt % selectivity C.sub.4 -C.sub.5 isoalkene. Cracking effluent is separated to obtain a light olefinic fraction rich in C.sub.4 -C.sub.5 isoalkene and a C.sub.6 + liquid fraction of enhanced octane value containing less than 50 wt % aromatic hydrocarbons. In a multistage operation enhanced octane products are obtained by etherifying the isoalkene fraction and by contacting the C.sub.6 + normally liquid fraction with reforming catalyst under moderate reforming conditions at elevated temperature to obtain a reformate product of enhanced octane value.

Abstract: A process for upgrading of unstable olefins, naphthas, and dienes, such as coker naphthas, is disclosed. The olefins in the unstable naphthas are oligomerized over a shape selective zeolite to gasoline and distillate products. The dienes are catalytically converted by the same zeolite. Preferably, hydrogen is added to increase catalyst life. Feed pretreatment, to remove basic nitrogen compounds also improves catalyst life. Water washing of coker naphtha is the preferred method of removing basic nitrogen compounds.

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 is disclosed for dewaxing a waxy hydrocarbon feedstock and for upgrading the olefinic interstage by-product to a high-octane gasoline blending stream. Waxy hydrocarbon feedstock is catalytically dewaxed until the catalyst is deactivated. Hydrogen-rich gas or, optionally, oxygen-containing gas, is then circulated to at least partially reactivate the catalyst. The interstage by-product, stored during the dewaxing run, is then upgraded in the reaction zone to a high-octane gasoline blending component.

Abstract: A process for oligomerizing C2 to C10 olefins obtained by catalytic cracking of heavy crude oil is disclosed. The olefins are oligomerized in the presence of added hydrogen over a shape selective zeolite to gasoline and distillate products. Feed pretreatment, to remove basic nitrogen compounds present in light olefin stream in refinery, with water wash or a guard bed is practiced improves catalyst life.

Abstract: Process and apparatus for upgrading light olefinic crackate gas from a fluidized catalytic cracking unit having a riser reactor for contacting hot solid cracking catalyst with a heavy hydrocarbon feedstock, said light crackate gas containing ethene, propene and other C.sub.1 -C.sub.4 lower aliphatics, comprising the steps of:reacting the light olefinic gas in contact with a fluidized bed of acid medium pore zeolite catalyst particles under oligomerization and/or aromatization conditions to produce a hydrocarbon effluent stream rich in C.sub.5.sup.+ hydrocarbons and a byproduct light gas rich in C.sub.1 -C.sub.4 saturated hydrocarbons;separating the oligomerization reaction effluent stream to provide a second light gas stream and a condensed liquid hydrocarbon product stream; andrecycling at least a portion of the second gas stream to the fluidized catalytic cracking unit as a lift gas for fluidizing solid cracking catalyst particles in a lower riser portion of said cracking unit.

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 dual-mode hydrocarbon conversion process is provided which comprises reforming a sulfur-, nitrogen- and/or olefin-containing hydrocarbon feedstock, e.g. an FCC gasoline, in a conversion unit operated under reforming conditions employing as catalyst a noble metal-containing crystalline silicate having a Constraint Index of not greater than about 2 and a framework SiO.sub.2 /Al.sub.2 O.sub.3 ratio of at least about 50 to provide a relatively high yield of high octane reformate and a relatively low yield of C.sub.3-4 hydrocarbons prior to or following hydrocracking the feedstock in the unit operated under hydrocracking conditions in the presence of the aforesaid catalyst to provide a relatively low yield of high octane hydrocrackate and a relatively high yield of C.sub.3-4 hydrocarbons. The latter can be separated from the liquid product and processed in a gas plant to provide LPG products.

Abstract: The present invention discloses a catalytic cracking operation featuring a single riser in which a variety of hydrocarbon conversion reactions takes place, a stripping unit in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises:(a) converting a relatively high boiling charge material introduced to the riser at a lower level thereof in the presence of a first catalyst component which is an amorphous cracking catalyst and/or a large pore crystalline silicate cracking catalyst to provide lighter products including significant quantities of naphtha; and,(b) converting a naphtha charge material introduced to the riser at a higher level thereof in the presence of a second catalyst componet which is a shape selective medium pore crystalline silicate zeolite catalyst to provide a relatively high octane gasoline product.

Abstract: A catalytic cracking process is described featuring multiple risers in which a variety of hydrocarbon conversion reactions takes place, a stripping unit in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises:(a) converting a relatively high boiling hydrocarbon charge material in a first riser in the presence of a catalyst mixture comprising, as a first catalyst component, an amorphous cracking catalyst and/or a large pore crystalline cracking catalyst and, as a second catalyst component, a shape selective medium pore crystalline silicate to provide lighter products including naphtha and C.sub.3 and/or C.sub.4 olefin;(b) converting an ethylene-rich charge material introduced to a second riser at a lower level thereof in the presence of said catalyst mixture to provide heavier products and to increase the temperature of the catalyst in said region; and,(c) converting C.sub.3 and/or C.sub.

Abstract: A fluid catalytic cracking method which comprises:(a) cracking a hydrocarbon feed stock in the presence of a mixed catalyst system which comprises particles of a first, amorphous cracking catalyst and/or large crystalline cracking catalyst component which requires frequent regeneration in a catalyst regeneration zone and particles of a second, shape selective crystalline silicate zeolite catalyst component which is less coke deactivated than the first catalyst component and requires less frequent regeneration than the latter, there being a sufficient difference between one or more of the characterizing physical properties of each catalyst component that the rate of circulation of particles of second catalyst component through the regeneration zone is, on the average, less than that of particles of first catalyst component, said cracking providing a product rich in C.sub.2-6 olefins; and,b) catalytically converting C.sub.2 -C.sub.6 olefins obtained from step (a) to a product containing gasoline and distillate.

Abstract: A catalytic cracking process is provided featuring multiple risers in which a variety of hydrocarbon conversion reactions take place, a stripping unit in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises:(a) converting a relatively high boiling hydrocarbon charge material in a first riser in the presence of a first catalyst component which is an amorphous cracking catalyst and/or a large pore crystalline zeolite cracking catalyst to provide lighter products;(b) converting an ethylene-rich charge material introduced to a second riser at a lower level thereof in the presence of a second catalyst component which is a shape selective medium pore crystalline silicate zeolite catalyst to provide heavier products and to increase the temperature of the catalyst in said region; and,(c) converting a naphtha charge material introduced to the second riser at a higher level thereof in the presence of said second catalyst c

Abstract: There is provided a catalytic cracking operation featuring a single riser reaction zone having a lower and an upper section wherein a variety of hydrocarbon conversion reactions takes place, a stripping zone in which entrained hydrocarbon material is removed from catalyst and a regeneration zine in which spent cracking catalyst is regnerated, which comprises:(a) thermally cracking a C.sub.

Abstract: An improvement in gasoline octane without substantial decrease in overall yield is obtained in an integrated process combining a fluidized catalytic cracking reaction and a fluidized catalyst olefin oligomerization reaction when crystalline medium pore shape selective zeolite catalyst particles are withdrawn in partially deactivated form from the oligomerization reaction stage and added as part of the active catalyst in the FCC reaction.

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: Olefin containing gasolines are upgraded to improve octane number with less than 5 wt.% yield loss by contacting such gasolines at elevated temperatures with acidic zeolites having alpha values between 5 and 100.

Abstract: An upgrading process for paraffinic naphthas subjects a full range naphtha to hydrocracking over a zeolite beta hydrocracking catalyst to effect a selective, partial hydrocracking in which the higher molecular weight n-paraffinic components of the naphtha are hydrocracked preferentially to the lower molecular weight components with concurrent isomerization of n-paraffins to isoparaffins, to form a hydrocracked effluent which comprises isobutane, C.sub.5 to C.sub.7 paraffins and relatively higher boiling naphthenes and paraffins. The hydrocracked effluent is split to remove the isobutane and the C.sub.5 and C.sub.7 paraffins with the balance of the higher boiling components being used as a reformer feed. Removal of the C.sub.5 and C.sub.7 paraffins permits improved reformer operation with the production of a higher octane product. The isomerization of the paraffins which occurs in the hydrocracking step provides a C.sub.5 to C.sub.

Abstract: A reactor sequencing technique is useful for multi-stage hydrocarbon conversion systems employing a number of fixed bed catalytic reactors at various process temperatures and catalytic activity levels. An apparatus for oligomerizing lower olefins (e.g., C.sub.2 -C.sub.6) is disclosed wherein catalyst partially inactivated in a primary stage is employed to effect conversion at higher temperature in a secondary stage prior to catalyst regeneration.

Abstract: By-product effluent streams from pyrolytic hydrocarbon cracking processes, containing monoolefins and diolefins, are treated to hydrogenate the olefins and to aromatize the aliphatics, with a catalyst comprising silicoaluminophosphates (SAPO-5, SAPO-11 etc.).

Abstract: By-product effluent streams from pyrolytic hydrocarbon cracking processes, containing monoolefins and diolefins, are treated to hydrogenate the olefins and to aromatize the aliphatics, with a catalyst comprising the aluminophosphates of U.S. Pat. No. 4,310,440.

Abstract: A process is provided for catalytically dewaxing a middle distillate with a ZSM-5 type catalyst. In this process the olefinic by-product is separated and catalytically converted to additional fuel oil and gasoline of good quality.

Abstract: A method for reducing the pour point of a hydrocarbon oil which comprises contacting said oil under dewaxing conditions with a zeolite dewaxing catalyst thereby forming a dewaxed oil that contains olefins, and contacting said dewaxed oil and said contained olefins with a solid acidic catalyst under conditions effective to increase the stability of said oil.

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: A combination process for upgrading hydrocarbon fractions obtained from raw shale oil, oil products of coal processing and select fractions of crude oils comprising sulfur, nitrogen and metal contaminants to produce jet fuel product fractions such as JP4, JP5, JP8 and other turbine-type fuel materials provided. The combination of integrated processing steps involving hydrotreating, acid extraction of basic nitrogen compounds and hydrofining thereof to produce a feed composition suitable for catalytic reforming in the absence of significant hydrocracking whereby jet fuel boiling range material is produced significantly reduces by the combination the hydrogen requirements of the process.

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 cracking a carbo-metallic oil feed having an initial boiling point of about 450.degree. F. or below comprising a naturally-occurring crude or a portion of such crude, including a portion boiling above 1000.degree. F. The 650.degree. F. portion is characterized by a carbon residue on pyrolysis of at least about 1 and containing at least about 4 ppm of Nickel Equivalents. The process comprises bringing the feed under cracking conditions in a progressive flow-type reactor into contact with a cracking catalyst bearing more than about 1500 parts per million of Nickel Equivalents of heavy metal(s). At least about 70% by weight of catalyst is abruptly separated from at least about 80% of the cracked products at the end of the reactor chamber.

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: A process for isomerizing olefins to more highly branched olefins with certain alumina isomerization catalysts wherein coke formation is reduced by regenerating the catalysts with a wet regenerating gas.

Abstract: A process which comprises recracking a cracked naphtha feed containing up to about 60 percent, suitably from about 20 to about 40 percent olefins, over a crystalline aluminosilicate zeolite catalyst to further crack the naphtha and saturate at least about 50 percent of the olefins, preferably from about 90 percent to about 100 percent of the olefins, based on the weight of said cracked naphtha feed. In a preferred combination a gas oil is catalytically cracked in a first stage to produce a cat cracked naphtha product of high olefin content, and an intermediate boiling component thereof is recracked as a feed in a second stage over a zeolite catalyst to saturate the olefins, and hydrodenitrogenate and hydrodesulfurize said cat cracked naphtha. The recracked cat cracked naphtha is then hydrotreated at low to mild severities and then catalytically reformed (hydroformed) to produce high octane gasoline.

Abstract: Ethane is converted to LPG and gasoline and/or aromatics concentrate in a combination process which comprises directly passing olefin effluent from the thermal cracking of ethane over a special crystalline aluminosilicate zeolite of the ZSM-5 type and recovering aromatics and C.sub.3 + hydrocarbons. For best yields, the thermal cracking step is conducted under more severe conditions than are used when ethylene production is optimized. The second, olefin conversion step is carried out at either the same pressure as the cracking step or higher. The process is of particular interest where low cost ethane is available.

Abstract: A combination operation is described comprising gas oil cracking in the presence of a large and smaller pore size crystalline zeolite dual component cracking catalyst in which combination C.sub.6 minus products are separated and catalytically upgraded under selected conditions providing cyclization and/or carbon chain growth as by oligmerization and polymerization. Conversion of C.sub.6 and lower boiling hydrocarbons is particularly accomplished with the smaller pore crystalline zeolite of the dual component catalyst.

Abstract: A process combination is described for upgrading a gasoline product of fluid cracking by treatment with a ZSM-5 catalyst wherein the cracking operation is performed under conditions to provide a depentanized gasoline product of cracking containing not more than 15 wt.% olefins before ZSM-5 treatment thereof for octane improvement.