Abstract: This disclosure describes polymerization processes and processes for quenching polymerization reactions using reactive particulates, such as amorphous silica, as quenching agents, typically in solution or bulk polymerization processes.

Abstract: In an embodiment, a heat-seal film includes 10-90 wt % of a first polymer component and 10-90 wt % of a second polymer component, based on a total weight of the first polymer component and the second polymer component, wherein: the first polymer component includes propylene, and optionally, up to 18 wt % of a C2 and/or a C4-C20 ?-olefin based on a total weight of the first polymer component; and the second polymer component includes 91-99.9 wt % of propylene and 0.1-9 wt % of ethylene based on a total weight of the second polymer component, the second copolymer component having a melt flow rate of 2-60 g/10 min. In another embodiment, a multi-layer film structure includes a heat-seal layer including a heat-seal film described herein; and an unoriented, an uniaxially oriented, or a biaxially oriented base layer including polypropylene homopolymer, a polypropylene random copolymer, or a combination thereof.

Abstract: Polymer compositions and films are provided. The polymer compositions include (A) 10-50 wt % heterogeneously branched Ziegler-Natta-catalyzed LLDPE polymer having a composition distribution breadth index (CBDI) <50.0%; and (B) 90-50 wt % metallocene-catalyzed LLDPE polymer having melt index 0.5 g/10 min to 5.0 g/10 min; melt index ratio from 20 to 40; weight average molecular weight (Mw) of from 20,000 to 200,000 g/mol; a molecular weight distribution (Mw/Mn) from 2.0 to 4.5; density 0.910 to 0.925 g/cm3; CDBI less than 35.0%; and comonomer distribution such that a first peak and a second peak in a comonomer distribution analysis, wherein the first peak has a maximum at a log(Mw) value of 4.3 to 4.7 and a TREF elution temperature of 85.0° C. to 95.0° C. and the second peak has a maximum at a log(Mw) value of 5.1 to 5.6 and a TREF elution temperature of 60.0° C. to 70.0° C.

Abstract: Although polyolefin elastomers are widely employed commodity polymers, there are shortcomings of this class of polymers for certain applications. For example, the rheological properties of some polyolefin elastomers may be insufficient to provide the green strength or low shear viscosity necessary to form stable foams, or to provide sufficient viscosity modification effects when present in a solvent. Cationomeric modification of polyolefin elastomers may alleviate these difficulties. Such polyolefin elastomers may feature a random cationomeric polyolefin copolymer comprising at least a first monomer and a second monomer, in which the first monomer is a neutral monomer and the second monomer has a side chain bearing a cationic moiety. The polyolefin elastomers may be present in foamed polyolefin compositions comprising a gas component and/or in liquid compositions comprising a solvent in which the polyolefin elastomer is dissolved.

Abstract: Provided herein are polymer compositions comprising a polymer and polymer processing aid (PPA) comprising a blend of at least two of: (i) a polyethylene glycol; (ii) a surfactant comprising a sorbitan ester or a polysorbate; and (iii) a metal salt of a fatty acid. The polymer can be a C2-C6 olefin homopolymer or a copolymer of two or more C2-C20 ?-olefins, and the polymer composition can take the form of polymer pellets; a polymer melt; reactor-grade polymer granules and/or polymer slurries; or other form of polymer composition containing the PPA and optionally one or more other additives. The polymer composition is preferably free or substantially free of fluorine, including fluoropolymer-based PPAs.

Abstract: A catalyst comprising a microporous crystalline metallosilicate having a Constraint Index of 12, or 10, or 8, or 6 or less, a binder, a Group 1 alkali metal or a compound thereof and/or a Group 2 alkaline earth metal or a compound thereof, a Group 10 metal or a compound thereof, and, optionally, a Group 11 metal or a compound thereof; wherein the catalyst is calcined in a first calcining step before the addition of the Group 10 metal or compound thereof and optionally the Group 11 metal or compound thereof; and wherein the first calcining step includes heating the catalyst to first temperatures of greater than 500° C.; and wherein the catalyst is calcined in a second calcining step after the addition of the Group 10 metal or compound thereof and optionally the Group 11 metal or compound thereof wherein the second calcining step includes heating the catalyst to temperatures of greater than 400° C.

Abstract: This disclosure provides an improved process for converting benzene/toluene via methylation with methanol/dimethyl ether for producing, e.g., p-xylene, comprising separating and recycling dimethyl ether from the methylation reaction product mixture effluent to the methylation reactor. High selectivity toward p-xylene, among others, can be achieved.

Abstract: Disclosed are multilayer films with at least one MDO substrate.

Abstract: A process for making a poly alpha-olefin (PAO) having a relatively high vinylidene content (or combined vinylidene and tri-substituted vinylene content) and a relatively low vinyl and/or di-substituted vinylene content, as well as a relatively low molecular weight. The process includes: contacting a feed containing a C2-C32 alpha-olefin with a catalyst system comprising activator and a bis-cyclopentadienyl metallocene compound, typically a cyclopentadienyl-benzindenyl group 4 transition metal compound.

Abstract: The present disclosure provides processes for producing polyethylene resins. In at least one embodiment, a polyethylene has: a density of from about 0.91 g/cm3 to about 0.94 g/cm3; a value of Mz of about 1,500,000 g/mol or greater; and a ratio of Mz to Mw of about 7 or greater. A process includes introducing a first feed stream having ethylene monomer and a first free radical initiator to a first inlet of a first reaction zone, where the first reaction zone has a first inlet temperature. The process further includes introducing a second feed stream having ethylene monomer and a second free radical initiator to a second inlet of a second reaction zone, where the second reaction zone has a second inlet temperature that is the same or different than the first inlet temperature.

Abstract: Processes for upgrading a hydrocarbon. The process can include (I) contacting a hydrocarbon-containing feed with a catalyst that can include a Group 8-10 element or a compound thereof disposed on a support to effect one or more of dehydrogenation, dehydroaromatization, and dehydrocyclization of at least a portion of the hydrocarbon-containing feed to produce a coked catalyst and an effluent. The process can also include (II) contacting at least a portion of the coked catalyst with an oxidant to effect combustion of at least a portion of the coke to produce a regenerated catalyst. The process can also include (III) contacting an additional quantity of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst. A cycle time from the contacting the hydrocarbon-containing feed with the catalyst in step (I) to the contacting the additional hydrocarbon-containing feed with the regenerated catalyst in step (III) can be ?5 hours.

Abstract: A process and system for separating paraxylene from a mixture of paraxylene, metaxylene, orthoxylene, and ethylbenzene in a simulated moving bed apparatus using a membrane to separate non-aromatics from a desorbent stream. The lower nonaromatics content in the desorbent improves paraxylene product purity, increases paraxylene production at the same desorbent rate, reduces the desorbent rate, and/or reduces energy consumption in the product tower.

Abstract: A process is described for producing paraxylene, in which an aromatic hydrocarbon feedstock comprising benzene and/or toluene is contacted with an alkylating reagent comprising methanol and/or dimethyl ether in an alkylation reaction zone under alkylation conditions in the presence of an alkylation catalyst to produce an alkylated aromatic product comprising xylenes. The alkylation catalyst comprises a molecular sieve having a Constraint Index?5, and the alkylation conditions comprise a temperature less than 500° C. The alkylation catalyst may be selectivated to produce a higher than equilibrium amount of paraxylene by using a molar ratio of alkylating agent to aromatic of at least 1:4.

Abstract: Processes for preparing a low particulate liquid hydrocarbon product are provided and includes blending a tar stream containing particles with a fluid to produce a fluid-feed mixture containing tar, the particles, and the fluid, and centrifuging the fluid-feed mixture at a temperature of greater than 60° C. to produce a higher density portion and a lower density portion, where the lower density portion contains no more than 25 wt % of the particles in the fluid-feed mixture.

Abstract: A process is described for producing paraxylene, in which an aromatic hydrocarbon feedstock comprising benzene and/or toluene is contacted with an alkylating reagent comprising methanol and/or dimethyl ether in an alkylation reaction zone under alkylation conditions in the presence of an alkylation catalyst to produce an alkylated aromatic product comprising xylenes. The alkylation catalyst comprises a molecular sieve having a Constraint Index?5, and the alkylation conditions comprise a temperature less than 500° C. Paraxylene may then be recovered from the alkylated aromatic product.

Abstract: Systems and methods are provided for co-processing of pyrolysis tar with pre-pyrolysis flash bottoms. In some aspects, the co-processing can correspond to solvent-assisted hydroprocessing. By combining pyrolysis tar and flash bottoms with a solvent, various difficulties associated with hydroprocessing of the fractions can be reduced or minimized, such as difficulties associated with hydroprocessing of high viscosity feeds and/or high sulfur feeds. Optionally, separate solvents and/or fluxes can be used for the pyrolysis tar and the flash bottoms. The resulting upgraded products can be suitable, for example, for inclusion in low sulfur fuel oils (LSFO).

Abstract: Sequential, double elastomer vulcanization method, system, and composition. First and second immiscible elastomers are mixed together with a first additive package. A first curative system is activated to vulcanize the first elastomer in a dispersed phase of the first elastomer to form a partially vulcanized mixture while maintaining melt flowability of the second elastomer in a continuous phase. Then, a second curative system is activated to vulcanize the second elastomer in the continuous phase. Since the partially vulcanized mixture is melt processable, a second additive package can be introduced to the mixture after activating the first curative system. Or, the second curative system can be activatable at a temperature which is higher than an activation temperature of the first curative system. In this manner, blends of dissimilar elastomers can be vulcanized with independent control of plasticizer, filler and curative distribution.

Abstract: A hydrocarbon fluid is disclosed that has a pour point of at most ?30° C., as measured by ASTM D5950, and that comprises at least 99 wt % of naphthenes and paraffins, based on the total weight of the hydrocarbon fluid, wherein the weight ratio of naphthenes to paraffins is at least 1, as measured by GC-MS, and wherein the paraffins consist essentially of isoparaffins, as determined by GC-FID. In addition, preferred uses of said hydrocarbon fluid are disclosed.

Abstract: The present disclosure generally relates to process to produce a poly alpha-olefin (PAO), comprising: a) introducing a first alpha-olefin to a first catalyst system comprising non-aromatic hydrocarbon soluble activator and a metallocene compound into a continuous stirred tank reactor or a continuous tubular reactor under first reactor conditions, wherein the first alpha-olefin is preferably introduced to the reactor at a flow rate of about 100 g/hr or more, to form a first reactor effluent comprising PAO (such as at least 60 wt % of PAO dimer and 40 wt % or less of higher oligomers, where the higher oligomers are oligomers that have a degree of polymerization of 3 or more); and b) introducing the first reactor effluent and a second alpha-olefin to a second catalyst composition comprising an acid catalyst, such as BF3, in a second reactor to form a second reactor effluent comprising PAO trimer.

Abstract: Catalyst composition which comprises a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m2/g is disclosed. These catalyst compositions are used to remove catalyst poisons from untreated feed streams having one or more impurities which cause deactivation of the downstream catalysts employed in hydrocarbon conversion processes, such as those that produce mono-alkylated aromatic compounds.