Abstract: The present disclosure generally relates to alkylated aromatic compounds useful as basestocks and additives for high viscosity applications. In an embodiment is provided an alkylated aromatic compound. In another embodiment is provided a lubricant formulation that includes an alkylated aromatic compound. In another embodiment is provided a lubricant formulation that includes an alkylated aromatic compound, an additive, and optionally, a Group III basestock, Group IV basestock, Group V basestock, or a combination thereof, the Group V basestock being different than the alkylated aromatic compound. In another embodiment is provided a method of forming a lubricant formulation that includes introducing a mPAO, an aromatic compound, and an acid catalyst to a reactor under reactor conditions to form an alkylated aromatic compound; and introducing the alkylated aromatic compound to an additive to form a lubricant formulation.

Abstract: The present disclosure generally relates to processes to produce alpha-olefin oligomers and poly alpha-olefins. In an embodiment, a process to produce a poly alpha-olefin (PAO) includes introducing a first alpha-olefin and a first catalyst system comprising a metallocene compound into a continuous stirred tank reactor or a continuous tubular reactor under first reactor conditions to form a first reactor effluent. The alpha-olefin is introduced to the reactor at a flow rate of about 100 g/hr or more. The first reactor effluent includes PAO dimer comprising at least 96 mol % of vinylidene and 4 mol % or less of trisubstituted vinylene and disubstituted vinylene, based on total moles of vinylidene, trisubstituted vinylene, and disubstituted vinylene. The method includes introducing the first reactor effluent, a second alpha-olefin and a second catalyst composition comprising an acid catalyst into a second reactor under second reactor conditions to form a second reactor effluent comprising PAO trimer.

Abstract: The present disclosure provides processes and apparatus for producing poly alpha olefins. In at least one embodiment, a process to produce a poly alpha olefin includes introducing a first olefin monomer to a first catalyst and an activator in a first reactor to form a first reactor effluent comprising an olefin dimer and an olefin trimer. The process includes introducing the first reactor effluent to a filtration unit to form a filtration effluent, and introducing the filtration effluent to a first distillation unit to form a first distillation effluent. The process includes introducing the first distillation effluent (or a second distillation effluent) to a second catalyst in a second reactor to form a second reactor effluent comprising the olefin trimer. The process includes removing a sample at any stage of the process and introducing the sample to a gas chromatograph.

Abstract: The present disclosure provides processes and apparatus for producing poly alpha olefins. In at least one embodiment, a process to produce a poly alpha olefin includes introducing a first olefin monomer to a first catalyst and an activator in a first reactor to form a first reactor effluent comprising olefin dimers and olefin timers. The process includes heating the first reactor effluent to form an isomerized product and introducing the isomerized product to a filtration unit to form a filtration effluent. The process may include introducing the filtration effluent to a first distillation unit to form a first distillation effluent. The process may include introducing the first distillation effluent to a second distillation unit to form a second distillation effluent. The process includes introducing the first distillation effluent and/or the second distillation effluent to a second catalyst in a second reactor to form a second reactor effluent comprising the olefin timers.

Abstract: The present disclosure generally relates to processes to produce alpha-olefin oligomers and poly alpha-olefins. In an embodiment, a process to produce a poly alpha-olefin (PAO) includes introducing a first alpha-olefin and a first catalyst system comprising a metallocene compound into a continuous stirred tank reactor or a continuous tubular reactor under first reactor conditions to form a first reactor effluent. The alpha-olefin is introduced to the reactor at a flow rate of about 100 g/hr or more. The first reactor effluent includes PAO dimer comprising at least 96 mol % of vinylidene and 4 mol % or less of trisubstituted vinylene and disubstituted vinylene, based on total moles of vinylidene, trisubstituted vinylene, and disubstituted vinylene. The method includes introducing the first reactor effluent, a second alpha-olefin and a second catalyst composition comprising an acid catalyst into a second reactor under second reactor conditions to form a second reactor effluent comprising PAO trimer.

Abstract: Processes are described for separating 3,4?- and 4,4?-dimethylbiphenyl from a mixture comprising at least 3,3?-, 3,4?- and 4,4?-dimethylbiphenyl. In the processes, the mixture is cooled to produce a crystallization product comprising at least of the 4,4?-dimethylbiphenyl from the feed mixture and a first mother liquor product. The first mother liquor product is distilled to produce a bottoms stream enriched in 4,4?-dimethylbiphenyl as compared with the first mother liquor product and an overhead stream deficient in 4,4?-dimethylbiphenyl as compared with the first mother liquor product. The overhead stream is then cooled to produce a second crystallization product comprising at least part of the 3,4?-dimethylbiphenyl from the overhead stream and a second mother liquor product.

Abstract: Processes are described for purifying a biphenyldicarboxylic acid product containing one or more impurities, particularly at least formylbiphenylcarboxylic acid. In the processes, a mixture comprising the biphenyldicarboxylic acid product is contacted with hydrogen in the presence of a hydrogenation catalyst under conditions to selectively reduce at least part of the formylbiphenylcarboxylic acid to produce a hydrogenation effluent comprising (i) hydroxymethylbiphenylcarboxylic acid and/or methylbiphenylcarboxylic acid, and (ii) biphenylcarboxylic acid. At least a portion of the biphenyldicarboxylic acid is then separated from the hydrogenation effluent. Advantageously, a polyester product may be produced from the separated biphenyldicarboxylic acid.

Abstract: The present disclosure generally relates to processes to produce alpha-olefin oligomers and poly alpha-olefins. In an embodiment, a process to produce a poly alpha-olefin (PAO) includes introducing a first alpha-olefin and a first catalyst system comprising a metallocene compound into a continuous stirred tank reactor or a continuous tubular reactor under first reactor conditions to form a first reactor effluent. The alpha-olefin is introduced to the reactor at a flow rate of about 100 g/hr or more. The first reactor effluent includes PAO dimer comprising at least 96 mol % of vinylidene and 4 mol % or less of trisubstituted vinylene and disubstituted vinylene, based on total moles of vinylidene, trisubstituted vinylene, and disubstituted vinylene. The method includes introducing the first reactor effluent, a second alpha-olefin and a second catalyst composition comprising an acid catalyst into a second reactor under second reactor conditions to form a second reactor effluent comprising PAO trimer.

Abstract: Processes are described for separating 3,4?- and 4,4?-dimethylbiphenyl from a mixture comprising at least 3,3?-, 3,4?- and 4,4?-dimethylbiphenyl. In the processes, the mixture is cooled to produce a crystallization product comprising at least of the 4,4?-dimethylbiphenyl from the feed mixture and a first mother liquor product. The first mother liquor product is distilled to produce a bottoms stream enriched in 4,4?-dimethylbiphenyl as compared with the first mother liquor product and an overhead stream deficient in 4,4?-dimethylbiphenyl as compared with the first mother liquor product. The overhead stream is then cooled to produce a second crystallization product comprising at least part of the 3,4?-dimethylbiphenyl from the overhead stream and a second mother liquor product.

Abstract: Processes are described for purifying a biphenyldicarboxylic acid product containing one or more impurities, particularly at least formylbiphenylcarboxylic acid. In the processes, a mixture comprising the biphenyldicarboxylic acid product is contacted with hydrogen in the presence of a hydrogenation catalyst under conditions to selectively reduce at least part of the formylbiphenylcarboxylic acid to produce a hydrogenation effluent comprising (i) hydroxymethylbiphenylcarboxylic acid and/or methylbiphenylcarboxylic acid, and (ii) biphenylcarboxylic acid. At least a portion of the biphenyldicarboxylic acid is then separated from the hydrogenation effluent. Advantageously, a polyester product may be produced from the separated biphenyldicarboxylic acid.

Abstract: Processes are described for purifying a biphenyldicarboxylic acid product containing one or more impurities, particularly at least formylbiphenylcarboxylic acid. In the processes, at least a portion of the biphenyldicarboxylic acid product is contacted with an alcohol under conditions effective to esterify at least part of the biphenyldicarboxylic acid and at least part of the formylbiphenylcarboxylic acid and produce an esterification effluent containing biphenyldicarboxylic acid diester and formylbiphenylcarboxylic acid ester. At least part of the biphenyldicarboxylic acid diester is then separated from the esterification effluent by crystallization. Advantageously, a polyester product may be produced from the separated biphenyldicarboxylic acid diester.

Abstract: The present disclosure generally relates to processes to produce alpha-olefin oligomers and poly alpha-olefins. In an embodiment, a process to produce a poly alpha-olefin (PAO) includes introducing a first alpha-olefin and a first catalyst system comprising a metallocene compound into a continuous stirred tank reactor or a continuous tubular reactor under first reactor conditions to form a first reactor effluent. The alpha-olefin is introduced to the reactor at a flow rate of about 100 g/hr or more. The first reactor effluent includes PAO dimer comprising at least 96 mol % of vinylidene and 4 mol % or less of trisubstituted vinylene and disubstituted vinylene, based on total moles of vinylidene, trisubstituted vinylene, and disubstituted vinylene. The method includes introducing the first reactor effluent, a second alpha-olefin and a second catalyst composition comprising an acid catalyst into a second reactor under second reactor conditions to form a second reactor effluent comprising PAO trimer.

Abstract: The invention relates to processes for oxygenate synthesis and homologation, to equipment and materials useful in such processes, and to the use of such oxygenate for producing olefin and polyolefin.

Abstract: The invention relates to processes for oxygenate synthesis and homologation, to equipment and materials useful in such processes, and to the use of such oxygenate for producing olefin and polyolefin.