Methods and systems for solution polymerization. The method can include forming a first mixture stream consisting essentially of at least one catalyst and a process solvent, and forming a second mixture stream consisting essentially of at least one activator and the process solvent. The first mixture stream and the second mixture stream can be fed separately to at least one reaction zone comprising one or more monomers dissolved in the process solvent where the at least one monomers can be polymerized within the at least one reaction zone in the presence of the catalyst, activator and process solvent to produce a polymer product.

The present disclosure relates to Lewis base catalysts. Catalysts, catalyst systems, and processes of the present disclosure can provide high temperature ethylene polymerization, propylene polymerization, or copolymerization as the Lewis base catalysts can be stable at high polymerization temperatures and have good activity at the high polymerization temperatures. The stable catalysts with good activity can provide formation of polymers having high melting points, high isotacticity, and controllable molecular weights, and the ability to make an increased amount of polymer in a given reactor, as compared to conventional catalysts. Hence, the present disclosure demonstrates highly active catalysts capable of operating at high reactor temperatures while producing polymers with controlled molecular weights and or robust isotacticity.

The present disclosure relates to Lewis base catalysts. Catalysts, catalyst systems, and processes of the present disclosure can provide high temperature ethylene polymerization, propylene polymerization, or copolymerization as the Lewis base catalysts can be stable at high polymerization temperatures and have good activity at the high polymerization temperatures. The stable catalysts with good activity can provide formation of polymers having high melting points, high isotacticity, and controllable molecular weights, and the ability to make an increased amount of polymer in a given reactor, as compared to conventional catalysts. Hence, the present disclosure demonstrates highly active catalysts capable of operating at high reactor temperatures while producing polymers with controlled molecular weights and or robust isotacticity.

The present disclosure provides base stocks and or diesel fuel, and processes for producing such base stocks and or diesel fuel by polymerizing alpha-olefins and internal olefins. The present disclosure further provides polyolefin products useful as base stocks and or diesel fuel. In at least one embodiment, a process includes: i) introducing, neat or in the presence of a solvent, a feed comprising a branched C.sub.5-C.sub.30 internal olefin, with a catalyst compound comprising a group 8, 9, 10, or 11 transition metal and at least one heteroatom; and ii) obtaining a C.sub.6-C.sub.100 polyolefin product having one olefin, a methylene content of from about 1 wt. % to about 98 wt. %, and or a methyl content of from about 1 wt. % to about 75 wt. %. The feed may further include a linear C.sub.4-C.sub.30 internal olefin, a C.sub.2-C.sub.30 alpha-olefin, or a mixture thereof.

The present disclosure provides base stocks and or diesel fuel, and processes for producing such base stocks and or diesel fuel by polymerizing alpha-olefins and internal olefins. The present disclosure further provides polyolefin products useful as base stocks and or diesel fuel. In at least one embodiment, a process includes: i) introducing, neat or in the presence of a solvent, a feed comprising a branched C.sub.5-C.sub.30 internal olefin, with a catalyst compound comprising a group 8, 9, 10, or 11 transition metal and at least one heteroatom; and ii) obtaining a C.sub.6-C.sub.100 polyolefin product having one olefin, a methylene content of from about 1 wt. % to about 98 wt. %, and or a methyl content of from about 1 wt. % to about 75 wt. %. The feed may further include a linear C.sub.4-C.sub.30 internal olefin, a C.sub.2-C.sub.30 alpha-olefin, or a mixture thereof.

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.

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.

A block copolymer composition is disclosed herein. In some embodiments, a block copolymer composition has a weight average molecular weight (M.sub.w) of 70,000 g/mol to 120,000 g/mol, a polydispersity index (PDI) of 1.0 to 2.0, a glass transition temperature (T.sub.g) of −55° C. to −30° C., and a melt index (MI), measured at 230° C. and a loading condition of 5 kg, of 0.2 g/10 minutes to 3.0 g/10 minutes. The block copolymer composition has excellent processability.

A block copolymer composition is disclosed herein. In some embodiments, a block copolymer composition has a weight average molecular weight (M.sub.w) of 70,000 g/mol to 120,000 g/mol, a polydispersity index (PDI) of 1.0 to 2.0, a glass transition temperature (T.sub.g) of −55° C. to −30° C., and a melt index (MI), measured at 230° C. and a loading condition of 5 kg, of 0.2 g/10 minutes to 3.0 g/10 minutes. The block copolymer composition has excellent processability.

A method for producing a block copolymer composition including a diblock copolymer and a triblock copolymer each containing a polyolefin-based block and a polystyrene-based block is disclosed herein. In some embodiments, the method includes reacting an organic zinc compound with one or more kinds of olefin-based monomers in the presence of a transition metal catalyst to form an intermediate having an olefin-based polymer block, reacting the intermediate styrene-based monomer in the presence of an alkyllithium compound to form a product having a styrene-based polymer block, and reacting the product with water, oxygen, or an organic acid to form a block copolymer wherein the number of moles of the alkyllithium compound used to form the product is larger than the number of moles of the organic zinc compound used to form the intermediate.