Abstract: A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

Abstract: Processes and systems for recovery of a dilute ethylene stream are illustrated and described. More specifically, embodiments disclosed herein relate to processes and systems for separation of a dilute ethylene stream from an offgas or other vapor streams, where the ultra-low temperature refrigeration for the desired separations is provided by the offgas itself, and only moderately-low temperature externally supplied propylene refrigerants (for example, at ?40° C. to 15° C.) are necessary.

Abstract: Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor.

Abstract: Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system.

Abstract: A catalyst comprising NiO, a metal mixture comprising at least one of MoO3 or WO3, a mixture comprising at least one of SiO2 and Al2O3, and P2O5. In this embodiment the metal sites on the catalyst are sulfided and the catalyst is capable of removing tar from a synthesis gas while performing methanation and water gas shift reactions at a temperature range from 300° C. to 600° C.

Abstract: A process for upgrading residuum hydrocarbons and decreasing tendency of the resulting products toward asphaltenic sediment formation in downstream processes is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a hydroconversion catalyst in a hydrocracking reaction zone to convert at least a portion of the residuum hydrocarbon fraction to lighter hydrocarbons; recovering an effluent from the hydrocracking reaction zone; contacting hydrogen and at least a portion of the effluent with a resid hydrotreating catalyst; and separating the effluent to recover two or more hydrocarbon fractions.

Abstract: Processes and systems for producing olefins, including: dehydrogenating a first n-alkane to produce a first effluent; and dehydrogenating at least one of a first isoalkane or a second n-alkane to produce a second effluent. The first and second effluents may be compressed and fed to a common separation train to separate the effluents into two or more fractions. In some embodiments, each of the first and second dehydrogenation reaction zones may include two reactors, one reactor in each of the reaction zones operating in a dehydrogenation cycle, one operating in a regeneration cycle, and one operating in a purge or evacuation/reduction cycle. Operation of the reactors in the dehydrogenation cycle is staggered, such that the purge cycle, regeneration cycle, or evacuation/reduction cycle of the reactors may not overlap.

Abstract: A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

Abstract: A fluid catalytic cracking apparatus and process is disclosed, providing for efficient conversion of heavy hydrocarbon feeds to light olefins, aromatics, and gasoline. A countercurrent flow reactor operating in bubbling or turbulent fluidization regimes is integrated with a fluid catalytic cracking riser reactor. A heavy hydrocarbon feed is catalytically cracked to naphtha and light olefins in the riser reactor, a co-current flow reactor. To enhance the yields and selectivity to light olefins, cracked hydrocarbon products from the riser reactor, such as C4 and naphtha range hydrocarbons, may be recycled and processed in the countercurrent flow reactor. The integration of the countercurrent flow reactor with a conventional FCC riser reactor and catalyst regeneration system may overcome heat balance issues commonly associated with two-stage cracking processes, may substantially increase the overall conversion and light olefins yield, and/or may increases the capability to process heavier feedstocks.

Abstract: A butadiene extraction processes designed for flexible operations, with or without a compressor, is disclosed. The ability to run at both high and low pressures provides added process flexibility.

Abstract: A process for recovering butadiene from a C4 fraction is disclosed. The process may include: contacting a mixed C4 stream comprising butane, butene, and butadiene, with a solvent comprising an organic solvent and water in a butadiene pre-absorber column to recover an overheads fraction comprising at least a portion of the butane, butene, and water, and a first bottoms fraction comprising the organic solvent, butadiene, and at least a portion of the butene; and feeding the first bottoms fraction to a butadiene extraction unit to recover a butene fraction, a crude butadiene fraction, and a solvent fraction.

Abstract: A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a hydrocarbon stream including olefins with a ?-alumina-titania isomerization catalyst to convert at least a portion of the olefin to its positional isomer. The ?-alumina-titanic isomerization catalysts disclosed herein may also have the activity to convert alcohol into additional olefins, while having increased resistance to oxygenate poisons.

Abstract: A process for recovering butadiene from a C4 fraction is disclosed. The process may include: contacting a mixed C4 stream comprising butane, butene, and butadiene, with a solvent comprising an organic solvent and water in a butadiene pre-absorber column to recover an overheads fraction comprising at least a portion of the butane, butene, and water, and a first bottoms fraction comprising the organic solvent, butadiene, and at least a portion of the butene; and feeding the first bottoms fraction to a butadiene extraction unit to recover a butene fraction, a crude butadiene fraction, and a solvent fraction.

Abstract: Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system.

Abstract: A process for the production of jet and other heavy fuels from alcohols and mixture of alcohols is disclosed. The process may include contacting in a reaction zone at least one C2 to C11 alcohol with a solid catalyst having activity for the simultaneous dehydration of the alcohols to form olefins, isomerization of the olefins to form internal olefins, and oligomerization of the olefins produced in situ via the dehydration reaction to form an effluent comprising mono-olefinic hydrocarbons. Preferably, the alcohol feed is a mixture of alcohols, such as C2 to C7 alcohols or C4 and C6 alcohols, enabling the production of a mixture of branched hydrocarbons that may be used directly as a jet fuel without blending.

Abstract: Processes and systems for producing olefins, including: dehydrogenating a first n-alkane to produce a first effluent; and dehydrogenating at least one of a first isoalkane or a second n-alkane to produce a second effluent. The first and second effluents may be compressed and fed to a common separation train to separate the effluents into two or more fractions. In some embodiments, each of the first and second dehydrogenation reaction zones may include two reactors, one reactor in each of the reaction zones operating in a dehydrogenation cycle, one operating in a regeneration cycle, and one operating in a purge or evacuation/reduction cycle. Operation of the reactors in the dehydrogenation cycle is staggered, such that the purge cycle, regeneration cycle, or evacuation/reduction cycle of the reactors may not overlap.

Abstract: Systems and processes for efficiently cracking of hydrocarbon mixtures, such as mixtures including compounds having a normal boiling temperature of greater than 450° C., 500° C., or even greater than 550° C., such as whole crudes for example, are disclosed.

Abstract: Olefins may be recovered from a methanol to olefins reactor effluent by initially feeding the effluent to an absorber demethanizer to contact the effluent with an absorbent to recover an overheads including methane and ethylene and a bottoms including the absorbent, ethylene, and ethane. The bottoms are separated to recover an ethylene fraction and an ethane fraction. The overheads are cooled and partially condensed in a first heat exchanger to a temperature of ?40° C. or greater. The resulting stream, or a portion thereof, may be further cooled and condensed via indirect heat exchange with a mixed refrigerant to a temperature of less than ?40° C. The non-condensed vapors are separated from the condensed liquids to form a liquid fraction and a methane fraction. The liquid fraction is fed to the absorber demethanizer as reflux, and the methane and ethane fractions combined to form the mixed refrigerant.

Abstract: Producing C5 olefins from steam cracker C5 reeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a traction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system.

Abstract: Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system.