Abstract: Processes for upgrading a hydrocarbon. In some embodiments, the process can include contacting a hydrocarbon-containing feed with a first catalyst that can include a Group 8-10 element disposed on a support within a first conversion zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of a portion of the feed to produce first conversion zone effluent that includes one or more upgraded hydrocarbons, molecular hydrogen, and unconverted feed. The process can also include contacting the first conversion zone effluent with a second catalyst that can include a Group 8-10 element disposed on a support within a second conversion zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of at least a portion of the unconverted feed to produce a second conversion zone effluent that includes an additional quantity of upgraded hydrocarbon(s) and molecular hydrogen.

Abstract: A hydrocarbon conversion process comprises pyrolysing at a temperature ?700° C. a feedstock comprising hydrocarbon to produce a pyrolysis effluent comprising at least one C2 to C4 olefin and C5+ aliphatic and aromatic hydrocarbons. The pyrolysis effluent is contacted with an oleaginous quench stream to reduce the temperature of the pyrolysis effluent to ?400° C. At least first and second streams are separated from the cooled effluent. The first stream comprises at least one C2 to C4 olefin, and the second stream comprises a quench oil having an average boiling point at atmospheric pressure of at least 120° C. At least a portion of the second stream is catalytically hydroprocessed to produce a hydroprocessed stream, which is combined with at least a portion of any remainder of the second stream to form the quench stream.

Abstract: Processes for upgrading a hydrocarbon. In some embodiments, the process can include contacting a hydrocarbon-containing feed with a first catalyst that can include a Group 8-10 element disposed on a support within a first conversion zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of a portion of the feed to produce first conversion zone effluent that includes one or more upgraded hydrocarbons, molecular hydrogen, and unconverted feed. The process can also include contacting the first conversion zone effluent with a second catalyst that can include a Group 8-10 element disposed on a support within a second conversion zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of at least a portion of the unconverted feed to produce a second conversion zone effluent that includes an additional quantity of upgraded hydrocarbon(s) and molecular hydrogen.

Abstract: A process for endothermic dehydrogenation including contacting a catalyst material in a moving bed reactor having at least one reaction zone, the moving bed reactor comprising a heat exchanger containing a heating medium, wherein the catalyst material and the heating medium do not contact one another, and wherein at least 50% of the delta enthalpy of the at least one reaction zone is provided by the heat exchanger; and contacting a feedstock comprising hydrocarbons with the catalyst material in the at least one reaction zone of the moving bed reactor under reaction conditions to convert at least a portion of the hydrocarbons to a first effluent comprising a product comprising alkenes, alkynes, cyclic hydrocarbons, and/or aromatics.

Abstract: Processes are described for isomerizing one or more C14-C24 alpha olefins to produce an isomerization mixture comprising one or more C14-C24 internal olefins comprising contacting an olefinic feed comprising the one or more C14-C24 alpha olefins with a catalyst under isomerization conditions, wherein the catalyst comprises a microporous crystalline aluminosilicate having an MWW framework. The resulting isomerization mixture typically exhibits a low pour point with maintained biodegradability properties as compared to the olefinic feed, and is particularly useful in drilling fluid and paper sizing compositions.

Abstract: Processes and systems for upgrading a hydrocarbon feed. The process can include feeding a hydrocarbon feed, catalyst particles, and molecular hydrogen (H2) into a separation zone. The hydrocarbon feed and H2 can be contacted in the presence of the catalyst particles under hydrotreating conditions in the separation zone that can include contacting under a total pressure of less than 3,500 kilopascals-gauge. The H2 can be fed into the separation zone at a rate of no greater than 270 cubic meters of H2 per cubic meter of the hydrocarbon feed, where the volume of H2 and hydrocarbon feed are based on a temperature of 25 C and a pressure of 101 kilopascals-absolute. A vapor phase hydrocarbon stream and a liquid phase hydrocarbon stream can be obtained from the separation zone. At least a portion of the vapor phase hydrocarbon stream can be fed into a pyrolysis reaction zone to produce a pyrolysis effluent.

Abstract: A process including contacting one or more monomers, at least one catalyst system, and at least two condensing agents under polymerizable conditions to produce a polyolefin polymer is provided where the vapor pressure of the condensing agents is ±4 bara of the optimum vapor pressure given by the formula: optimum vapor pressure=614?716*D+2.338*P+3.603*ln(MI), where the optimum vapor pressure has units (bara), D is the polyolefin polymer density with units (g/cc), P is the polymerization condition pressure with units (barg), and MI is the polyolefin polymer melt index with units (g/10 min). The invention also relates to a process where at least three condensing agents are used.

Abstract: In an embodiment, a method for decreasing reactor fouling in a steam cracking process is provided. The method includes steam cracking a hydrocarbon feed to obtain a quench oil composition comprising a concentration of donatable hydrogen of 0.5 wt. % or more based on a total weight percent of the quench oil composition; exposing a steam cracker effluent flowing from a pyrolysis furnace to the quench oil composition to form a mixture; and fractionating the mixture in a separation apparatus to obtain a steam cracker tar. In another embodiment, a hydrocarbon mixture is provided. The hydrocarbon mixture includes a mid-cut composition.

Abstract: The invention relates to approach temperatures and approach temperature ranges that are beneficial in operating a pyrolysis reactor, to pyrolysis reactors exhibiting a beneficial approach temperature, to processes for carrying out hydrocarbon pyrolysis in a pyrolysis reactor having a beneficial approach temperature. The pyrolysis reactor can be, e.g., a reverse-flow pyrolysis reactor, such as a regenerative reverse-flow pyrolysis reactor.

Abstract: Processes and systems for upgrading a hydrocarbon feed. The process can include feeding a hydrocarbon feed, catalyst particles, and molecular hydrogen (H2) into a separation zone. The hydrocarbon feed and H2 can be contacted in the presence of the catalyst particles under hydrotreating conditions in the separation zone that can include contacting under a total pressure of less than 3,500 kilopascals-gauge. The H2 can be fed into the separation zone at a rate of no greater than 270 cubic meters of H2 per cubic meter of the hydrocarbon feed, where the volume of H2 and hydrocarbon feed are based on a temperature of 25 C and a pressure of 101 kilopascals-absolute. A vapor phase hydrocarbon stream and a liquid phase hydrocarbon stream can be obtained from the separation zone. At least a portion of the vapor phase hydrocarbon stream can be fed into a pyrolysis reaction zone to produce a pyrolysis effluent.

Abstract: The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes oligomerizing an olefin in the presence of a catalyst and a process solvent in at least one reactor, quenching the reactor effluent, and subjecting the quenched effluent to separation steps to obtain a stream enriched in one or more linear alpha olefins.

Abstract: A process for endothermic dehydrogenation including contacting a catalyst material in a moving bed reactor having at least one reaction zone, the moving bed reactor comprising a heat exchanger containing a heating medium, wherein the catalyst material and the heating medium do not contact one another, and wherein at least 50% of the delta enthalpy of the at least one reaction zone is provided by the heat exchanger; and contacting a feedstock comprising hydrocarbons with the catalyst material in the at least one reaction zone of the moving bed reactor under reaction conditions to convert at least a portion of the hydrocarbons to a first effluent comprising a product comprising alkenes, alkynes, cyclic hydrocarbons, and/or aromatics.

Abstract: Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

Abstract: A hydrocarbon conversion process comprises pyrolysing at a temperature ?700° C. a feedstock comprising hydrocarbon to produce a pyrolysis effluent comprising at least one C2 to C4 olefin and C5+ aliphatic and aromatic hydrocarbons. The pyrolysis effluent is contacted with an oleaginous quench stream to reduce the temperature of the pyrolysis effluent to ?400° C. At least first and second streams are separated from the cooled effluent. The first stream comprises at least one C2 to C4 olefin, and the second stream comprises a quench oil having an average boiling point at atmospheric pressure of at least 120° C. At least a portion of the second stream is catalytically hydroprocessed to produce a hydroprocessed stream, which is combined with at least a portion of any remainder of the second stream to form the quench stream.

Abstract: Processes are described for isomerizing one or more C14-C24 alpha olefins to produce an isomerization mixture comprising one or more C14-C24 internal olefins comprising contacting an olefinic feed comprising the one or more C14-C24 alpha olefins with a catalyst under isomerization conditions, wherein the catalyst comprises a microporous crystalline aluminosilicate having an MWW framework. The resulting isomerization mixture typically exhibits a low pour point with maintained biodegradability properties as compared to the olefinic feed, and is particularly useful in drilling fluid and paper sizing compositions.

Abstract: Methods of transforming a hydrocarbon feedstream into an aromatization product in a multi-stage reverse flow reactor (RFR) apparatus are disclosed. The methods include at least two reaction stages in series, at least one being a pyrolysis stage and at least another being a catalytic aromatization stage. Using a highly saturated hydrocarbon feedstream the pyrolysis stage focuses on desaturation, while the catalytic aromatization stage focuses on aromatization. The catalytic aromatization stage contains a aromatization catalyst that can include substantially no magnesium, scandium, yttrium, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron, ruthenium, cobalt, rhodium, nickel, palladium, platinum, copper, silver, gold, gallium, indium, tin, lanthanides, or actinides, or, in some cases, substantially no added active metals at all.

Abstract: This disclosure relates to naphthalene-1,8-dicarboxylate ester compounds, lubricating oil base stocks comprising naphthalene-1,8-dicarboxylate ester compounds, lubricating oil compositions comprising such base stocks, and method of making such base stocks. The lubricating oil base stocks comprising naphthalene-1,8-dicarboxylate ester compounds exhibit desirable lubricating properties such as polarity.

Abstract: The invention relates to hydrocarbon pyrolysis, to equipment and materials useful for hydrocarbon pyrolysis, to processes for carrying out hydrocarbon pyrolysis, and to the use of hydrocarbon pyrolysis for, e.g., hydrocarbon upgrading.

Abstract: Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating diisobutylene to produce neopentane. The diisobutylene may be provided by the dimerization of isobutylene.

Abstract: Processes for producing neopentane are disclosed herein. Processes comprise demethylating a C6-C8 alkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.