A heavy load vortex internal apparatus is provided having a vibration channel for receiving plastic granular material. The vibration channel has a channel floor and two side walls opposite each other, where the length of the vibration channel is greater in the longitudinal direction than the maximum height and width of a channel cross section perpendicular to the longitudinal direction. At least two vibration generators are provided for generating a vibration excitation having a transverse component perpendicular to a vertical plane in the longitudinal direction. At least two channel carriers are spaced apart from each other in the longitudinal direction, each supporting the channel floor and the side walls from the outside and bridging the vibration channel opposite the channel floor. One of the vibration generators in each case is fastened to at least two of the channel carriers. Also provided is a method for crystallization of plastic granular material.

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 10.sup.5 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 10.sup.5 centipoise.

The invention relates to a nontacky film-forming polymer composition (cover material), and tacky hot melt adhesives in the form of pellets which are coated with the polymer composition and producible by coextruding the hot melt adhesive and the cover material. The film-forming composition comprises 5 to 40% by weight of at least one Fischer-Tropsch wax having a melting point of >95° C. and 30 to 70% by weight of at least one metallocene-catalyzed polyolefin having a softening point of >95° C. and a melt flow index (MFI) (230° C., 2.16 kg) of ≦1000 and ≧300 g/10 minutes. The invention further relates to suitable uses for such hot melt adhesives, methods for their use, and products containing these adhesives.

The present invention provides a resin pellet that enables the molding of a molded product exhibiting a tensile breaking strength at the same level as that of a tensile breaking strength of a resin contained in the resin pellet, a manufacturing method for a resin pellet, a molded product, an automobile part, an electronic apparatus part, and a fiber. The resin pellet of the present invention contains a microcapsule encompassing a heat storage material and a thermoplastic resin, in which a content of the heat storage material is 70% by mass or less with respect to a total mass of the resin pellet, and a capsule wall of the microcapsule contains at least one resin selected from the group consisting of polyurethane urea, polyurethane, and polyurea.

A granulation apparatus for granulating a plastic material is provided. The granulation apparatus has a fixed support extending along a vertical axis, a rotating support, connected in a rotatable manner to the fixed support, and actuatable in rotation about a first direction parallel or coincident with the vertical axis, a die connected to an extruder, a cutting assembly suitable for facing the die and constrained to the rotating support so that, by rotating the rotating support around the first direction, the cutting assembly also rotates around that first direction. In one embodiment the cutting assembly is slidably constrained relative to the rotating support. In a further embodiment the cutting assembly is supported in a cantilevered manner by the rotating support. A maintenance method for the granulation apparatus and a granulation method for a molten plastic material are also provided.

A granulation apparatus for granulating a plastic material is provided. The granulation apparatus has a fixed support extending along a vertical axis, a rotating support, connected in a rotatable manner to the fixed support, and actuatable in rotation about a first direction parallel or coincident with the vertical axis, a die connected to an extruder, a cutting assembly suitable for facing the die and constrained to the rotating support so that, by rotating the rotating support around the first direction, the cutting assembly also rotates around that first direction. In one embodiment the cutting assembly is slidably constrained relative to the rotating support. In a further embodiment the cutting assembly is supported in a cantilevered manner by the rotating support. A maintenance method for the granulation apparatus and a granulation method for a molten plastic material are also provided.

The present invention relates to a melt processable thermoplastic polyurethane-urea composition formed by a continuous bulk process without the presence of solvent using a polyol component, an isocyanate component, and chain extender component comprising a hindered aromatic diamine.

The present invention is directed to a method of manufacturing a fibre-reinforced polymer composition comprising the steps of providing at least one multifilament strand comprising a plurality of continuous fibre filaments, applying an impregnating agent to said strand to form an impregnated continuous multifilament strand, and embedding the impregnated continuous multifilament strand in a thermoplastic polymer material for providing said fibre reinforced polymer composition, wherein said impregnating agent has a low viscosity at application temperature and is applied by jetting said impregnating agent onto the at least one continuous multifilament strand. The invention is further directed to a device for use in such a method.

The present application relates to a process for producing a multimodal polyethylene composition comprising the steps of polymerizing a polyethylene fraction (A-1) having a weight average molecular weight Mw of equal to or more than 500 kg/mol to equal to or less than 10,000 kg/mol and a density of equal to or more than 915 kg/m.sup.3 to equal to or less than 960 kg/m.sup.3 in one reaction step and polymerizing a polyethylene fraction (A-2) having a lower weight average molecular weight Mw as polyethylene fraction (A-1) and a density of equal to or more than 910 kg/m.sup.3 to equal to or less than 975 kg/m.sup.3 in a second reaction step of a sequential multistage process wherein one of said polyethylene fractions is polymerized in the presence of the other of said polyethylene fractions to form a first polyethylene resin (A) having a weight average molecular weight Mw of equal to or more than 150 kg/mol to equal to or less than 1,500 kg/mol, and a density of equal to or more than 910 kg/m.sup.3 to equal to or less than 975 kg/m.sup.3, wherein the weight average molecular weight Mw of the first polyethylene resin (A) is lower than the weight average molecular weight Mw of the polyethylene fraction (A-1), blending the first polyethylene resin (A) with a second polyethylene resin (B) having a weight average molecular weight Mw of equal to or more than 50 kg/mol to less than 500 kg/mol, and a density of equal to or more than 910 kg/m.sup.3 to equal to or less than 970 kg/m.sup.3 to form said multimodal polyethylene composition, wherein the multimodal polyethylene composition a melt flow rate MFR.sub.5 (190° C., 5 kg) of 0.01 to 10 g/10 min and a density of equal to or more than 910 kg/m.sup.3 to equal to or less than 970 kg/m.sup.3 a polyethylene composition obtainable by said process and the polyethylene resin of said first polymerization step.

The present invention is directed to a process for producing a modified olefin polymer in an extruder having a feed zone, a melting zone, optionally a mixing zone and optionally a die zone, (A) introducing a stream of an olefin polymer into the feed zone of the extruder; (B) introducing a stream of a free radical generator directly into the feed zone or the melting zone or the mixing zone, if present, of the extruder; (C) introducing a stream of a functionally unsaturated compound directly into the feed zone or the melting zone or the mixing zone, if present, of the extruder; (D) extruding the mixture in the extruder at a temperature which is greater than the decomposition temperature of the free radical generator and the melting temperature of the olefin polymer but less than the decomposition temperature of the olefin polymer thereby producing the modified olefin polymer in the extruder; and, optionally, (G) passing the melt of the modified olefin polymer through the die zone to a pelletiser.