Abstract: Embodiments are directed towards methods for purifying a reclaimed polymer.

Abstract: Embodiments are directed towards methods for purifying a reclaimed polymer.

Abstract: Disclosed herein too is a method comprising charging to a reactor system a feed stream comprising a catalyst, a monomer and a solvent; reacting the monomer to form a polymer; where the polymer is contained in a single phase polymer solution; transporting the polymer solution to a pre-heater to increase the temperature of the polymer solution; charging the polymer solution to a liquid-liquid separator; reducing a pressure of the polymer solution in the liquid-liquid separator and separating a polymer-rich phase from a solvent-rich phase in the liquid-liquid separator; transporting the polymer-rich phase to a plurality of devolatilization vessels located downstream of the liquid-liquid separator, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and separating the polymer from volatiles present in the polymer rich phase.

Abstract: An apparatus to batch or continuously form solid polymer particles, the apparatus comprising the following components: A) at least one pastillation unit comprising a pastillation head, said unit used to form discrete molten polymer particles from a polymer melt; B) a moving belt to receive and transfer the discrete molten polymer particles from the pastillation head; C) a means to transfer water onto the moving belt, such that the water comes into contact with the discrete molten polymer particles on the moving belt to form the solid polymer particles; and wherein the water of component C is sprayed onto the discrete molten polymer particles, such that the ratio of “the rate of water spray” to “the discharge rate” is ?3.0; and wherein the belt residence time is ?50 seconds.

Abstract: Methods of propylene polymerization incorporate bis biphenyl-phenoxy procatalysts favoring polypropylene isotacticity at elevated reactor temperatures. The methods include polymerizing propylene in the presence of a catalyst system to produce a propylene-based polymer. The catalyst system includes a metal-ligand complex selected from bis-biphenyl-phenoxy procatalysts. Polymerization reactions result in polypropylenes having greater than 90% isotacticity, as measured by percentages of isotactic triads, at reaction temperatures from 110° C. to 190 ° C. or from 160 ° C. to 190 ° C.

Abstract: A method of producing bimodal ethylene-based polymer includes reacting ethylene monomer and C3-C12 ?-olefin comonomer in the presence of a first catalyst in an agitated reactor to produce a first polymer fraction, and outputting effluent from the agitated reactor. A second catalyst is added to the effluent downstream of the agitated reactor and upstream from a non-agitated reactor, the second catalyst facilitates production of a second polymer fraction having a density and melt index (I2) different from the first polymer fraction. The second catalyst and effluent are mixed in at least one mixer. The second catalyst, second polymer fraction, and the first polymer fraction are passed to the non-agitated reactor; and additional ethylene monomer, additional C3-C12 ?-olefin comonomer, and solvent are passed to the non-agitated reactor to produce more second polymer fraction and thereby the bimodal ethylene-based polymer.

Abstract: Polyethylene compositions are disclosed that may have a density of 0.910 g/cm3 to 0.924 g/cm3 and a melt index (I2) In of 0.1 g/10 minutes to 0.5 g/10 minutes and include a first polyethylene fraction area in the temperature range from 45° C. to 80° C. of an elution profile via improved comonomer composition distribution (iCCD) analysis method; a second polyethylene fraction area in the temperature range from 80° C. to 95° C. of the elution profile, and a third polyethylene fraction area in the temperature range from 95° C. to 110° C. of the elution profile. The second polyethylene fraction area may include at least 5% of the total area of the elution profile. The third polyethylene fraction area may include at least 25% of the total area of the elution profile. A ratio of the first polyethylene fraction area to the second polyethylene fraction area may be from 6 to 15.

Abstract: Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive a monomer and to react the monomer to form a polymer; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and a heat exchanger disposed between two devolatilization vessels and in fluid communication with them, where the heat exchanger has an inlet port temperature of 100° C. to 230° C., an outlet port temperature of 200° C. to 300° C., an inlet port pressure of 35 to 250 kgf/cm2 and an outlet port pressure of 20 to 200 kgf/cm2; and wherein the polymer solution remains in a single phase during its residence in the heat exchanger.

Abstract: Disclosed herein too is a method comprising charging to a reactor system a feed stream comprising a catalyst, a monomer and a solvent; reacting the monomer to form a polymer; where the polymer is contained in a single phase polymer solution; transporting the polymer solution to a pre-heater to increase the temperature of the polymer solution; charging the polymer solution to a liquid-liquid separator; reducing a pressure of the polymer solution in the liquid-liquid separator and separating a polymer-rich phase from a solvent-rich phase in the liquid-liquid separator; transporting the polymer-rich phase to a plurality of devolatilization vessels located downstream of the liquid-liquid separator, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and separating the polymer from volatiles present in the polymer rich phase.

Abstract: Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive an anti-solvent, a monomer, and a solvent, and to react the monomer to form a polymer; where the anti-solvent is not a solvent for the polymer and is operative to reduce the lower critical solution temperature; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel and wherein the plurality of devolatilization vessels receives a polymer solution from the reactor system; and a liquid-liquid separator that is operative to receive a polymer solution from the reactor system and to facilitate a separation between the polymer and volatiles by reducing the pressure and temperature of the polymer solution in the liquid-liquid separator.

Abstract: A method of producing bimodal ethylene-based polymer includes reacting ethylene monomer and C3-C12 ?-olefin comonomer in the presence of a first catalyst in an agitated reactor to produce a first polymer fraction, and outputting effluent from the agitated reactor. A second catalyst is added to the effluent downstream of the agitated reactor and upstream from a non-agitated reactor, the second catalyst facilitates production of a second polymer fraction having a density and melt index (I2) different from the first polymer fraction. The second catalyst and effluent are mixed in at least one mixer. The second catalyst, second polymer fraction, and the first polymer fraction are passed to the non-agitated reactor; and additional ethylene monomer, additional C3-C12 ?-olefin comonomer, and solvent are passed to the non-agitated reactor to produce more second polymer fraction and thereby the bimodal ethylene-based polymer.

Abstract: Disclosed herein is a system comprising a first pump; a pelletization system that comprises an underwater pelletizer; where the pelletization system is located downstream of the first pump and is in fluid communication with it; a direct line that is located downstream of the first pump and upstream of the pelletization system; where the direct line does not contain a pump or a heat exchanger; and a bypass line that is located downstream of the first pump and upstream of the pelletization system; where the bypass line comprises a second pump; where the first pump is operative to discharge the polymer to the pelletization system via the direct line when the polymer has a melt viscosity greater than 105 centipoise; and where the first pump is operative to discharge the polymer to the pelletization system via the bypass line when the polymer has a melt viscosity less than 105 centipoise.

Abstract: Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive a monomer and to react the monomer to form a polymer; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and a heat exchanger disposed between two devolatilization vessels and in fluid communication with them, where the heat exchanger has an inlet port temperature of 100° C. to 230° C., an outlet port temperature of 200° C. to 300° C., an inlet port pressure of 35 to 250 kgf/cm2 and an outlet port pressure of 20 to 200 kgf/cm2; and wherein the polymer solution remains in a single phase during its residence in the heat exchanger.

Abstract: A process to form an olefin-based polymer, said process comprising at least the following steps: a) polymerizing a reaction mixture comprising an olefin, in at least one reactor, in a solution polymerization, to form a polymer solution; b) feeding at least a portion of the polymer solution through at least one devolatilizer, to form the olefin-based polymer, in melt form; c) feeding at least a portion of the olefin-based polymer, in melt, form through a heat exchanger, and then into a pastillation apparatus to form polymer particles.

Abstract: The invention provides a method, and apparatus, for determining the degree of separation (DOS) of a polymer solution into a polymer-rich stream and a solvent-rich stream, said method comprising the following: adding to a liquid-liquid separation vessel the polymer solution, which comprises a polymer, a solvent and an anti-solvent; separating the polymer solution into a polymer-rich stream and a solvent-rich stream; removing at least some the polymer-rich stream from at least one outlet P on the vessel, and measuring the actual solution density of this polymer-rich stream using at least one flow meter; removing at least some of the solvent-rich stream from at least one other outlet S on the vessel, and measuring the actual density of the solvent-rich stream using at least one flow meter; and wherein the degree of separation (DOS) is determined by the following equation (Eqn.

Abstract: The instant invention provides an improved process for producing pelletized polymer compositions, and pelletized polymer compositions. The process for producing a pelletized polymer composition according to the present invention comprises: (1) polymerizing one or more alpha-olefins in one or more solution reactors thereby producing a molten polymer composition comprising one or more solvents; (2) removing at least a portion of said one or more solvents thereby forming a polymer composition having a low solvent content (typically less than 1,000 parts of solvent per million of polymer on a weight basis); (3) removing heat from said polymer composition having low solvent content to a temperature in the range of equal to or greater than the crystallization point of the polymer composition having low solvent content to less than or equal to a temperature in the range of from (the crystallization point of the polymer composition having low solvent content+20° C.

Abstract: A process to form an olefin-based polymer, said process comprising at least the following steps: a) polymerizing a reaction mixture comprising an olefin, in at least one reactor, in a solution polymerization, to form a polymer solution; b) feeding at least a portion of the polymer solution through at least one devolatilizer, to form the olefin-based polymer, in melt form; c) feeding at least a portion of the olefin-based polymer, in melt, form through a heat exchanger, and then into a pastillation apparatus to form polymer particles.

Abstract: The invention provides a method, and apparatus, for determining the degree of separation (DOS) of a polymer solution into a polymer-rich stream and a solvent-rich stream, said method comprising the following: adding to a liquid-liquid separation vessel the polymer solution, which comprises a polymer, a solvent and an anti-solvent; separating the polymer solution into a polymer-rich stream and a solvent-rich stream; removing at least some the polymer-rich stream from at least one outlet P on the vessel, and measuring the actual solution density of this polymer-rich stream using at least one flow meter; removing at least some of the solvent-rich stream from at least one other outlet S on the vessel, and measuring the actual density of the solvent-rich stream using at least one flow meter; and wherein the degree of separation (DOS) is determined by the following equation (Eqn.

Abstract: The invention provides a method, and apparatus, for determining the degree of separation (DOS) of a polymer solution into a polymer-rich stream and a solvent-rich stream, said method comprising the following: adding to a liquid-liquid separation vessel the polymer solution, which comprises a polymer, a solvent and an anti-solvent; separating the polymer solution into a polymer-rich stream and a solvent-rich stream; removing at least some the polymer-rich stream from at least one outlet P on the vessel, and measuring the actual solution density of this polymer-rich stream using at least one flow meter; removing at least some of the solvent-rich stream from at least one other outlet S on the vessel, and measuring the actual density of the solvent-rich stream using at least one flow meter; and wherein the degree of separation (DOS) is determined by the following equation (Eqn.

Abstract: Disclosed herein is a system comprising a first pump; a pelletization system that comprises an underwater pelletizer; where the pelletization system is located downstream of the first pump and is in fluid communication with it; a direct line that is located downstream of the first pump and upstream of the pelletization system; where the direct line does not contain a pump or a heat exchanger; and a bypass line that is located downstream of the first pump and upstream of the pelletization system; where the bypass line comprises a second pump; where the first pump is operative to discharge the polymer to the pelletization system via the direct line when the polymer has a melt viscosity greater than 105 centipoise; and where the first pump is operative to discharge the polymer to the pelletization system via the bypass line when the polymer has a melt viscosity less than 105 centipoise.