Abstract: A naphtha cracking feed stream is taken, heated and passed to a cracking reactor. Hydrogen is added to the cracking reactor to mitigate catalyst deactivation. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked effluent stream comprising aromatic compounds and cracked olefins.

Abstract: A process utilizing a micro-emulsion is described. The micro-emulsion formed by contacting an ionic liquid, a co-solvent, a hydrocarbon, an optional surfactant, and an optional catalyst promoter to form the micro-emulsion. The micro-emulsion comprises a hydrocarbon component comprising the hydrocarbon and an ionic liquid component comprising the ionic liquid. The ionic liquid comprises a halometallate anion and a cation. The co-solvent has a polarity greater than a polarity of the hydrocarbon. The ionic liquid is present in an amount of 0.05 wt % to 40 wt % of the micro-emulsion. A product mixture comprising a product is produced in a process zone containing the micro-emulsion.

Abstract: A catalyst composition comprising a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50. A first hydrogenation metal comprising platinum, a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum and an optional third metal from Group IA of the Periodic Table may be deposited on the support. The ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support may be between about 15 and about 75.

Abstract: A process and apparatus for making aromatics are described. The process includes reforming a naphtha stream in a reforming zone to form a reformer effluent comprising aromatic compounds and non-aromatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups. The reformer effluent is heated and passed directly to an acid cracking reaction zone. The non-aromatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of an acid cracking catalyst to form a cracked reformer effluent comprising the aromatic compounds and cracked olefins.

Abstract: A process and apparatus for making olefins and aromatics are described. The process includes reforming a naphtha stream in a reforming unit to produce a reformer effluent stream comprising aromatic compounds and aliphatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups. A cracking feed stream is taken from the reformer effluent stream, heated and passed to a cracking reactor. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked reformer effluent stream comprising aromatic compounds and cracked olefins.

Abstract: A naphtha cracking feed stream is taken, heated and passed to a cracking reactor. Hydrogen is added to the cracking reactor to mitigate catalyst deactivation. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked effluent stream comprising aromatic compounds and cracked olefins.

Abstract: Processes and apparatuses for the production of propylene are provided. In an embodiment, a process is provided for production of propylene from an oxygenate feed comprising passing the oxygenate feed to an oxygenate-to-olefin reactor to contact the oxygenate feed with a catalyst to provide an effluent stream comprising olefins comprising ethylene, propylene and butylene. The effluent stream is separated in a product separation zone to generate a propylene product stream, an ethylene stream and a C4+ stream. The ethylene stream is reacted in an ethylene dimerization or oligomerization reactor in presence of a dimerization or oligomerization catalyst to provide a first process stream. The C4+ stream and the first process stream are cracked in a cracking reactor under cracking conditions to provide a cracked stream comprising additional amounts of ethylene and propylene. Finally, the cracked stream is passed to the product separation zone to recover additional amounts of propylene.

Abstract: A micro-emulsion and a method of making the micro-emulsion are described. The micro-emulsion composition includes more than about 50 vol % of an oil phase and polar structures. The oil phase comprises a hydrocarbon component and a co-solvent, and the polar structures comprise an ionic liquid. The ionic liquid comprises a halometallate anion and a cation which is at least slightly soluble in the hydrocarbon component or in the co-solvent. The micro-emulsion can optionally include a surfactant, and a catalyst promoter. The co-solvent has a polarity greater than the polarity of the hydrocarbon, and the co-solvent is miscible in the hydrocarbon.

Abstract: Processes and apparatuses for the production of propylene are provided. In an embodiment, a process is provided for production of propylene from an oxygenate feed comprising passing the oxygenate feed to an oxygenate-to-olefin reactor to contact the oxygenate feed with a catalyst to provide an effluent stream comprising olefins comprising ethylene, propylene and butylene. The effluent stream is separated in a product separation zone to generate a propylene product stream, an ethylene stream and a C4+ stream. The ethylene stream is reacted in an ethylene dimerization or oligomerization reactor in presence of a dimerization or oligomerization catalyst to provide a first process stream. The C4+ stream and the first process stream are cracked in a cracking reactor under cracking conditions to provide a cracked stream comprising additional amounts of ethylene and propylene. Finally, the cracked stream is passed to the product separation zone to recover additional amounts of propylene.

Abstract: A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C4 and C7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

Abstract: A process of making terephthalic acid or a derivative of terephthalic acid is described. The process includes reacting a derivative of 2,5-dimethylfuran, with a dienophile containing an unsaturated 2-carbon unit, in the presence of a catalyst having Brönsted acidity to form a para-xylene derivative; and optionally reacting the para-xylene derivative to terephthalic acid.

Abstract: A process for refining naphtha and upgrading butanes is described. The process involves separating a hydrotreated heavy naphtha feed into a C7-rich fraction and a C8+-rich fraction in a separation zone and then reacting the C7-rich fraction with C4 paraffins to form to a low aromatic gasoline blendstock. The C8+-rich fraction is sent to a reforming zone to form a reformed product with higher octane and lower RVP than a reformed product derived from heavy naphtha.

Abstract: A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C4 and C7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

Abstract: A reverse disproportionation reaction of two hydrocarbon feeds allows production of a reaction mixture containing products with intermediate carbon numbers. The amount of at least one of the products with intermediate carbon numbers is equal to or greater than the amount formed from disproportionation of the hydrocarbon alone. A reverse disproportionation reaction mixture is also described.

Abstract: A reverse disproportionation reaction of two hydrocarbon feeds allows production of a reaction mixture containing products with intermediate carbon numbers. The amount of at least one of the products with intermediate carbon numbers is equal to or greater than the amount formed from disproportionation of the hydrocarbon alone. A reverse disproportionation reaction mixture is also described.

Abstract: The present invention comprises a hydrocarbon-conversion process using an improved MgMxAPSO-31 molecular sieve which demonstrates a favorable combination of conversion and selectivity in aromatics conversion. The sieve comprises at least two divalent elements with narrow specific concentration limits in the framework structure having defined crystal characteristics. The element Mx may comprise one or more of manganese, cobalt, nickel, iron and zinc.

Abstract: A process for forming a zeolite beta dielectric layer onto a substrate such as a silicon wafer has been developed. The zeolite beta is characterized in that it has an aluminum concentration from about 0.1 to about 2.0 wt. %, and has crystallites from about 5 to about 40 nanometers. The process involves first dealuminating a starting zeolite beta, then preparing a slurry of the dealuminated zeolite beta followed by coating a substrate, e.g. silicon wafer with the slurry, heating to form a zeolite beta film and treating the zeolite beta with a silylating agent.

Abstract: The present invention comprises a hydrocarbon-conversion process using an improved MgAPSO-31 molecular sieve which demonstrates a favorable combination of conversion and selectivity in aromatics conversion. The sieve has a specific combination of crystal configuration, being limited in diameter and length, specified crystallinity as measured by an X-Ray Diffraction Index (XRDI), and a narrow range of magnesium content.

Abstract: A process is presented for the selective catalytic cracking of naphtha to light olefins. The process includes contacting a naphtha feedstream with a mixture of catalysts to reduce the amount of recycle, and especially the recycle of light paraffins. The mixture of catalysts includes a first molecular sieve made up from a small pore zeolite having a pore index between 13 and 26, and a second molecular sieve made up from an intermediate pore zeolite having a pore index between 26 and 30.

Abstract: The present invention comprises a hydrocarbon-conversion process using an improved MgAPSO-31 molecular sieve which demonstrates a favorable combination of conversion and selectivity in aromatics conversion. The sieve has a specific combination of crystal configuration, being limited in diameter and length, specified crystallinity as measured by an X-Ray Diffraction Index (XRDI), and a narrow range of magnesium content.