Abstract: Processes for making and using slurry catalyst mixtures. In some embodiments, the process for making the slurry catalyst mixture can include introducing a mineral oil into a vessel. The mineral oil can be heated to a temperature of about 60° C. to about 80° C. to produce a heated mineral oil. A moisture concentration of the heated mineral oil can be reduced to produce a dried mineral oil. Catalyst particles can be introduced into the dried mineral oil to produce a mixture. The mixture can be agitated for at least 2 hours to remove at least a portion of any gas present within pores of the catalyst particles to produce the slurry catalyst mixture. The slurry catalyst mixture can be free of or include ?1 wt % of any wax having a melting point, at atmospheric pressure, of ?25° C., based on a total weight of the slurry catalyst mixture.

Abstract: Polymerization processes. In some embodiments, the polymerization process can include introducing a carrier fluid, an olefin, and a catalyst feed into a polymerization reactor, wherein the catalyst feed comprises one or more catalysts, a carrier liquid and optionally an induced condensing agent. In some embodiments, a combined amount of the carrier liquid and any induced condensing agent in the catalyst feed is ?350 kg per mole of the one or more catalysts introduced into the polymerization reactor. The process can also include polymerizing the olefin in the presence of the catalyst within the polymerization reactor to produce a polymer product.

Abstract: Systems and methods useful in determining the superficial gas velocity in fluidized bed reactors may utilize a pressure drop across a portion of the system but not associated with a flowmeter. For example, method may comprise: obtaining a pressure for each of two different locations within a fluidized bed reactor system that comprises a reactor capable of containing a fluidized bed and a cycle gas loop, wherein one or both of the two different locations is not at a flowmeter; calculating a pressure drop based on the two pressures; calculating a first superficial gas velocity (SGValt) for the fluidized bed based on the pressure drop; and operating the fluidized bed reactor system based at least in part on the SGValt.

Abstract: Gas phase polymerization processes include contacting an input stream comprising a monomer and an induced condensing agent in the presence of an inert gas with a catalyst in a fluidized bed reactor to produce a polymer, unreacted monomer, and an output gas; recycling a recycle stream of the unreacted monomer from the reactor to the input stream; venting at least a portion of the output gas from the reactor; and maintaining a partial pressure of the inert gas in the reactor above a reference inert gas pressure to decrease losses of the recycle stream with the vented output gas. The processes may include controlling the inert gas partial pressure to vary the total reactor pressure up to the maximum safe pressure, without causing carry-over of product polymer.

Abstract: Methods for scale-up from a pilot plant to full production of a bimodal polymer product having a density, melt index, and a melt index ratio are provided herein. The methods provide for adjusting reactor conditions and catalyst ratio of a bimodal catalyst system to optimize the transition from single catalyst to bimodal polymer compositions on a full-scale process plant consistent with pilot plant development.

Abstract: Methods for scale-up from a pilot plant to a larger production facility of a bimodal polymer product having a density, a melt index and melt index ratio are provided herein.

Abstract: The present disclosure relates to processes for production of polyolefins from olefin monomer(s) in a gas phase reactor using condensing agent(s) (CAs), and in particular relates to controlling condensed phase cooling in a gas phase reactor used to polymerize olefin monomer(s). The method may include introducing first and second condensing agent(s) into the reactor at ratio(s) determined by ascertaining a stick limit for the first condensing agent, calculating an equivalence factor relating the first and second condensing agents, ascertaining total allowable condensing agent, and calculating amount of the first condensing agent removed and replaced by the second condensing agent. The method may further include calculating the dew point limit of a gas phase composition including olefin monomer(s) as well as the first and second condensing agents; and determining if introducing a mixture comprising the olefin monomer(s) and the condensing agent composition would exceed the calculated dew point limit.

Abstract: This disclosure relates to processes for producing polyolefins in a gas phase reactor using condensing agent(s) (CAs), and real-time calculation of the ratio of one type of CA to another CA within a CA composition. This disclosure provides methods for controlling condensed phase cooling in a gas phase reactor used to polymerize olefins. The polymerization may employ one or more polymerization catalysts to polymerize one or more olefin monomers, and may include introducing a first condensing agent and a second condensing agent in a ratio of first condensing agent to second condensing agent, which ratio is calculated by ascertaining a stick limit for a first condensing agent, calculating an equivalence factor relating the first condensing agent and a second condensing agent, ascertaining a total allowable condensing agent, and calculating a first amount of the first condensing agent removed and replaced by a second amount of the second condensing agent.

Abstract: Gas phase polymerization processes include contacting an input stream comprising a monomer and an induced condensing agent in the presence of an inert gas with a catalyst in a fluidized bed reactor to produce a polymer, unreacted monomer, and an output gas; recycling a recycle stream of the unreacted monomer from the reactor to the input stream; venting at least a portion of the output gas from the reactor; and maintaining a partial pressure of the inert gas in the reactor above a reference inert gas pressure to decrease losses of the recycle stream with the vented output gas. The processes may include controlling the inert gas partial pressure to vary the total reactor pressure up to the maximum safe pressure, without causing carry-over of product polymer.

Abstract: Films produced with polyethylene blends having improved stiffness and heat sealing are provided herein. The films may have an average MD/TD 1% secant modulus greater than or equal to about 3300 psi. The films may also have a heat seal initiation temperature at 5 N of less than or equal to about 95° C. or a hot tack seal initiation temperature at 1 N of less than or equal to about 95° C.

Abstract: The present disclosure provides processes for polymerizing olefin(s). Methods can include contacting a first composition and a second composition in a line to form a third composition. The first composition can include a contact product of a first catalyst, a second catalyst, a support, a first activator, a mineral oil. The second composition can include a contact product of an activator, a diluent, and the first catalyst or the second catalyst. Methods can include introducing the third composition from the line into a gas-phase fluidized bed reactor, introducing a condensing agent to the line and/or the reactor, exposing the third composition to polymerization conditions, and/or obtaining a polyolefin.

Abstract: In a gas phase fluidized bed polymerization process for the production of polyolefin polymers, such as polyethylene polymers or polypropylene polymers, loss of ethylene or propylene accompanying inert gas purging is reduced by passing an ethylene- or propylene-containing purge stream through a vent column to contact a hydrocarbon liquid flowing through the vent column contercurrent to the purge stream whereby unreacted ethylene or propylene in the purge stream portion is dissolved in the hydrocarbon liquid to produce an ethylene- or propylene-enriched liquid stream and an ethylene- or propylene-depleted gaseous stream. The ethylene- or propylene-enriched liquid stream is then recycled to the fluidized bed reactor, while at least part of the ethylene- or propylene-depleted gaseous stream is purged.

Abstract: In a gas phase fluidized bed polymerization process for the production of polyolefin polymers, such as polyethylene polymers or polypropylene polymers, loss of ethylene or propylene accompanying inert gas purging is reduced by passing an ethylene- or propylene-containing purge stream through a vent column to contact a hydrocarbon liquid flowing through the vent column contercurrent to the purge stream whereby unreacted ethylene or propylene in the purge stream portion is dissolved in the hydrocarbon liquid to produce an ethylene- or propylene-enriched liquid stream and an ethylene- or propylene-depleted gaseous stream. The ethylene- or propylene-enriched liquid stream is then recycled to the fluidized bed reactor, while at least part of the ethylene- or propylene-depleted gaseous stream is purged.

Abstract: Methods for scale-up from a pilot plant to a larger production facility of a bimodal polymer product having a density, a melt index and melt index ration are provided herein.

Abstract: Polyethylene compositions including at least 65 wt % ethylene derived units and from 0 to 35 wt % of C3-C12 olefin comonomer derived units, based upon the total weight of the polyethylene composition are provided. The polyethylene compositions have a) an RCI,m of 100 kg/mol or greater and one or both of: b) a Tw1-Tw2 value of from ?16 to ?38° C.; and c) an Mw1/Mw2 value of at least 0.9. The polyethylene compositions may be used to manufacture articles such as films.

Abstract: Polyethylene compositions including at least 65 wt % ethylene derived units and from 0 to 35 wt % of C3-C12 olefin comonomer derived units, based upon the total weight of the polyethylene composition are provided. The polyethylene compositions have a) an RCI,m of 100 kg/mol or greater and one or both of: b) a Tw1-Tw2 value of from ?16 to ?38° C.; and c) an Mw1/Mw2 value of at least 0.9. The polyethylene compositions may be used to manufacture articles such as films.

Abstract: Methods for scale-up from a pilot plant to full production of a bimodal polymer product having a density, melt index, and a melt index ratio are provided herein. The methods provide for adjusting reactor conditions and catalyst ratio of a bimodal catalyst system to optimize the transition from single catalyst to bimodal polymer compositions on a full-scale process plant consistent with pilot plant development.

Abstract: The present disclosure provides processes for polymerizing olefin(s). Methods can include contacting a first composition and a second composition in a line to form a third composition. The first composition can include a contact product of a first catalyst, a second catalyst, a support, a first activator, a mineral oil. The second composition can include a contact product of an activator, a diluent, and the first catalyst or the second catalyst. Methods can include introducing the third composition from the line into a gas-phase fluidized bed reactor, introducing a condensing agent to the line and/or the reactor, exposing the third composition to polymerization conditions, and/or obtaining a polyolefin. Polyethylene compositions including at least 65 wt % ethylene derived units, based upon the total weight of the polyethylene composition, are provided.

Abstract: The present disclosure provides processes for polymerizing olefin(s). Methods can include contacting a first composition and a second composition in a line to form a third composition. The first composition can include a contact product of a first catalyst, a second catalyst, a support, a first activator, a mineral oil. The second composition can include a contact product of an activator, a diluent, and the first catalyst or the second catalyst. Methods can include introducing the third composition from the line into a gas-phase fluidized bed reactor, introducing a condensing agent to the line and/or the reactor, exposing the third composition to polymerization conditions, and/or obtaining a polyolefin. Polyethylene compositions including at least 65 wt % ethylene derived units, based upon the total weight of the polyethylene composition, are provided.

Abstract: A polymerization catalyst supply system is provided. The polymerization catalyst supply system can be used to prepare polyolefin polymers with multimodal or broad molecular weight distribution, or to prepare polyolefins having broad compositional distribution. A process for preparing polyolefin polymers using the polymerization catalyst supply system is also provided.