Abstract: Processes for activating chromium polymerization catalysts, which can use lower maximum activation temperatures and shorter activation times than conventional activation methods, and provide polyethylenes with high melt indices, broader molecular weight distributions, and lower long chain branching content. The activation process can comprise heating a supported chromium catalyst in an inert atmosphere to a first temperature (T1) for a first hold time (tH1), followed by allowing the chromium catalyst to attain a second temperature (T2) in the inert atmosphere, then contacting the chromium catalyst with an oxidative atmosphere for a second hold time (tH2), in which T2 can be less than or equal to T1. Additional activation treatments and conditioning steps are disclosed which can be used to enhance the melt index potential of Phillips (Cr/silica) catalysts.

Abstract: Polymerization processes and reactor systems for producing multimodal ethylene polymers are disclosed in which at least one loop reactor and at least one fluidized bed reactor are utilized. Configurations include a loop reactor in series with a fluidized bed reactor and two loop reactors in series with a fluidized bed reactor.

Abstract: A cassette for use in an auto injector for administering a medicament, the cassette comprises a syringe compartment containing the medicament; a hollow needle in fluid connection with the syringe compartment; a rigid needle shield connected to the syringe compartment and covering the hollow needle; a stopper movable inside the syringe compartment; a syringe holder extending around at least part of the syringe compartment; a rigid needle shield holder having a first part positioned between the rigid needle shield and the proximal end of the syringe compartment, and a cassette skin sensor. Also disclosed is the auto injector.

Abstract: A system comprising a pretreated hydrocarbon feedstock supply, wherein said pretreated hydrocarbon feedstock supply comprises at least hydrocarbon feedstock and dissolved salts; a wash water supply, wherein said wash water supply comprises at least water; an alkalinity modifier supply, wherein said alkalinity modifier supply comprises at least one alkalinity modifier or solutions thereof; a desalting vessel; a desalted crude outlet, wherein said desalted crude outlet comprises hydrocarbon feedstock with less dissolved salts by weight than the hydrocarbon feedstock in the pretreated hydrocarbon feedstock supply; and a wash water brine outlet, wherein said wash water brine outlet comprises water with more dissolved salts by weight than the water in the wash water supply.

Abstract: Polymer compositions containing an ethylene polymer, 50-1500 ppm by weight of a glycerol stearate, and 250-7500 ppm by weight of an antioxidant selected from a phenolic antioxidant, a phosphite antioxidant, a thioester antioxidant, or any combination thereof, are described. These polymer compositions have improved initial color, improved color after long-term aging, or improved color after multi-pass extrusion processing.

Abstract: Disclosed is a process for operating a flashline heater and a flashline separation system. In the process and system, heat is supplied to the flashline heater by a first steam stage followed by a second steam stage. The steam pressure is controlled by a steam control system such that the pressure in the first steam stage is not equal to the pressure in the second steam stage. Also disclosed is a process for retrofitting a steam control system in a flashline separation system of an olefin polymerization system at least by changing the number of steam stages in the flashline separation system to include a first steam stage followed by a second steam stage, and changing the stream pressure control scheme such that the pressure in the first steam stage is independently controlled to be not equal to the pressure in the second steam stage.

Abstract: A pyrolysis oil fractionation system for treating a pyrolysis oil feed includes a fractionation column, at least one treatment catalyst bed, and a plurality of distillation trays. The system further includes a condenser to receive a light fraction and produce a condensed gasoline product and a vapor, a receiver coupled to the condenser, a knockout drum, and a distillate stripper coupled to the fractionation column. A method for treating a pyrolysis oil feed includes, in a fractionating column, dehydrohalogenating, decontaminating, and/or dehydrating a pyrolysis oil feed in at least one treatment catalyst bed, and distilling the treated pyrolysis oil feed into a light fraction, a middle fraction, a heavy fraction, and a bottom fraction. The method further includes condensing the light fraction and producing a condensed gasoline product and a vapor, separating a fuel gas product from the vapor, and stripping the middle fraction to produce a distillate product.

Abstract: Catalysts and catalytic processes for the synthesis of acrylic acid and other ?,?-unsaturated carboxylic acids and their salts, which are carried out in a diluent or in the absence of a diluent. In an aspect, ethylene and CO2 can be contacted with a Group 8-11 transition metal precursor compound or a Group 8-11 transition metal metalalactone compound in the presence of a metal-treated chemically-modified solid oxide (MT-CMSO) or a metal-treated solid oxide (MT-SO), to form a metal acrylate. As the catalytic activity wanes in either the presence or absence of a diluent, pressure cycling—that is, pressurizing the reaction system with CO2 and an olefin such as ethylene for a time period, releasing the pressure, then re-pressurizing with CO2 and ethylene—can rejuvenate the catalyst and restore its declining catalytic activity.

Abstract: Methods for synthesizing a water-soluble titanium-silicon complex are disclosed herein. The titanium-silicon complex can be utilized to produce titanated solid oxide supports and titanated chromium supported catalysts. The titanated chromium supported catalysts subsequently can be used to polymerize olefins to produce, for example, ethylene based homopolymer and copolymers.

Abstract: An auto injector for delivery of administering a medicament comprising: a housing; an electrical motor adapted to move a piston between proximal and distal positions in a longitudinal direction of the auto injector; a syringe holder extending from a proximal to a distal end and configured to receive a syringe, a first spring adapted for moving the syringe holder with the syringe proximally for insertion of the needle; wherein the electrical motor is the only motor in the auto injector.

Abstract: Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650° C. to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m2/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Abstract: A process to produce 1-octene and 1-decene includes (a) separating a composition containing an oligomer product—which contains 15 to 80 mol % C6 olefins, 20 to 80 mol % C8 olefins, and 5 to 20 mol % C10+ olefins—into a first oligomer composition containing C6 alkanes and at least 85 mol % C6 olefins (e.g., 1-hexene), a second oligomer composition containing at least 20 mol % C8 olefins (e.g., 1-octene), and a heavies stream containing C10+ olefins, then (b) contacting a metathesis catalyst system with the first oligomer composition to form a first composition comprising C10 linear internal olefins, (c) contacting the C10 linear internal olefins with a catalytic isomerization catalyst system in the presence of photochemical irradiation to form a second composition comprising 1-decene, and (d) purifying the second composition to isolate a third composition comprising at least 90 mol % 1-decene.

Abstract: Pyrolysis processes comprise contacting a waste polyolefin with a solid catalyst at a pyrolysis temperature to form a pyrolysis product containing C1-C10 hydrocarbons. In some instances, the solid catalyst can be a silica-coated alumina, a fluorided silica-coated alumina, or a sulfated alumina, while in other instances, the solid catalyst can be any suitable solid oxide or chemically-treated solid oxide that is characterized by a d50 average particle size from 5 to 12 ?m and a particle size span from 0.7 to 1.7. Hydrocarbon compositions are formed from the pyrolysis of waste polyolefins with specific amounts of methane and higher carbon number hydrocarbons.

Abstract: A purge system for a polymerization system may include a purge column including a stripping zone and a stripping fluid distributor below the stripping zone for injecting a stripping fluid including one or more light olefins. A first displacement zone is below the distributor. A second displacement zone is below the first displacement zone. A nitrogen distributor introduces nitrogen in the second displacement zone. Another purge system for a polymerization system may include a fluidized bed separator and a purge column. The fluidized bed separator includes a separator inlet, a stripping fluid inlet, a first stripped fluid outlet, and a separator outlet. The purge column includes a flake inlet, a stripping zone, a stripping fluid distributor below the stripping zone, a stripped flake outlet, and a second stripped fluid outlet for a second stripped fluid from the purge column.

Abstract: Processes for using pyrolysis gas as a feedstock or a co-feedstock for making a variety of chemicals, for example, circular ethylene, circular ethylene polymers and copolymers, and other circular products. In these processes, pyrolysis reactor conditions can be selected to increase or optimized the production of pyrolysis gas over pyrolysis oil, and the pyrolysis gas which is usually used as fuel or flared can be fed downstream of the steam cracker furnace for economic use to form circular chemicals. Operating parameters of the pyrolysis unit may be adjusted to increase or decrease the proportion of pyrolysis gas relative to pyrolysis liquid as a function of their relative economic values.

Abstract: Fluorided silica-coated alumina activator-supports have a bulk density from 0.15 to 0.37 g/mL, a total pore volume from 0.85 to 2 mL/g, a BET surface area from 200 to 500 m2/g, an average pore diameter from 10 to 25 nm, and from 80 to 99% of pore volume in pores with diameters of greater than 6 nm. Methods of making the fluorided silica-coated alumina activator-supports and using the fluorided silica-coated aluminas in catalyst compositions and olefin polymerization processes also are described. Representative ethylene-based polymers produced using the compositions and processes have a melt index of 0.1 to 10 g/10 min and a density of 0.91 to 0.96 g/cm3, and contain from 70 to 270 ppm solid oxide and from 2 to 18 ppm fluorine.

Abstract: Processes for converting methane into methanol are disclosed in which methane, water, and a supported chromium (VI) catalyst are contacted with a light beam at a wavelength in the UV-visible spectrum in an oxidizing atmosphere in a single reactor to form a reaction product comprising methanol, followed by discharging a reactor effluent containing the reaction product from the single reactor, and then separating methanol from the reaction product. Processes to produce methanol using additional reactors also are described, as well as related methanol production systems.

Abstract: A method of operating a polyethylene reactor system includes feeding ethylene, an optional first comonomer, a diluent, and a chromium-based catalyst to a first polymerization reactor. The method further includes contacting ethylene and the comonomer with the catalyst in the first polymerization reactor to form a first product including a first polyethylene. The method further includes feeding the first product from the first polymerization reactor to a second polymerization reactor. The method further includes contacting ethylene and a second optional comonomer with catalyst from the first reactor in the second polymerization reactor to form a second product including the first polyethylene and a second polyethylene. The method further includes controlling one or both of a molecular weight or a breadth of molecular weight distribution of the second product by adjusting a rate of hydrogen fed to one or both of the first polymerization reactor or the second polymerization reactor.

Abstract: Methods for controlling the long chain branch content of ethylene homopolymers and copolymers produced in a polymerization process include the steps of contacting a metallocene compound, an organoaluminum compound, a high LCB activator-support, and a low LCB activator-support to form a catalyst composition, contacting the catalyst composition with ethylene and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an ethylene polymer having a LCB content, and controlling the relative amount of the high LCB activator-support and the low LCB activator-support in the catalyst composition to adjust the LCB content of the ethylene polymer.

Abstract: According to some embodiments of the present disclosure, there is provided a first connector configured to be connected to an electrical cable, the first connector including an electrical connector configured to mate with and electrically connect to the electrical cable, and a body having a first end carrying a plurality of electrical terminals and having a second end coupled to an end of the electrical connector, the body including a sleeve extending from the first end to the second end, the sleeve being molded over and extending around the end of the electrical connector, and a flange axially extending outwardly from the first end of the body.