The instant disclosure relates to saponified pellets of an ethylene-vinyl ester based copolymer as well as a film and a multilayer structure formed therefrom. The saponified pellets of an ethylene-vinyl ester based copolymer has an ethylene content of 24-35 mole %, and the pellets have a turbidity of less than 300 NTU when dissolved in a 60% (w/w) methanol aqueous solution; or the pellet has an ethylene content of 36-48 mole %, and the pellets have a turbidity of less than 200 NTU when dissolved in a 80% (w/w) methanol aqueous solution. The present invention controls the amount of aggregates by controlling the turbidity of the saponified pellets of an ethylene-vinyl ester based copolymer dissolved in methanol aqueous to reduce the amount of gel produced after film formation.

A raw material quantity is supplied by a supply unit along a trajectory through a supply opening into the production machine. The trajectory of the raw material quantity is changeable. A supply unit for supplying a raw material quantity into a production machine comprises a supply channel portion having an exit opening and a feed hopper. The supply unit has at least one actuating unit, by which an actuating movement of the supply channel portion and/or of the feed hopper can be generated, so that the supply channel portion can be displaced relative to the feed hopper. A raw material mixture is supplied to the extrusion machine by the moved supply unit. In this way it is possible to supply the raw material mixture into the extrusion machine in a particularly uniform manner so that the raw material mixture can be processed by means of the extrusion machine.

A hopper charged with a powder material, a screw arranged below the hopper and exposed at a supply port formed at the bottom of the hopper, and a rolling element in contact with the screw at the supply port are provided. The rolling element is larger than a space between end portions of the supply port and a screw groove of the screw.

A planetary extruder for producing and processing polymers includes a degassing section. The extruder includes a housing and a bushing arranged therein. The bushing has an internal toothing with a pitch diameter and a root circle. An externally toothed central spindle is arranged within the housing. Planetary spindles rotate about the central spindle between the central spindle and the bushing. A heat transfer fluid is guided through fluid channels which extend helically along an outer surface of the bushing and guide the heat transfer fluid axially. A degassing opening is provided to which a negative pressure is applied for degassing. A minimum radial thickness (t) of the bushing between the root circle of the internal toothing on an inside of the bushing and a bottom of the fluid channels on an outside of the bushing is selected based on the pitch diameter (d) of the internal toothing.

A composition that includes: (a) from 65 to 85% by weight of polypropylene homopolymer in powder form, the average particle size of which is micrometric, (b) from 14 to 30% by weight, preferably 14 to 25% by weight, of natural fibers less than or equal to 2 mm in length, and (c) from 1 to 3% by weight of compatibilizer, its uses for the preparation of a composite material by extrusion, wherein this composite material is useful for preparing a part by injection, in particular a vehicle part whose rigidity is improved.

A planetary roller extruder section forms a feed part of an extruder. The planetary roller extruder has an internally toothed housing and an externally toothed central spindle disposed centrally within and at a distance from the housing. Planetary spindles are arranged to rotate in a void between the central spindle and the housing. Each planetary spindle has an external toothing meshing with both the housing and the central spindle. At least one planetary spindle has two axially spaced areas with less than a full set of teeth. Those axially spaced areas include a first area having a first number of teeth and a second area having a second number of teeth. The second number of teeth is less than a full set of teeth and more than the first number of teeth.

The present invention relates to a method for continuously manufacturing UHMWPE products comprising:—providing a counter-rotating twin-screw extruder;—feeding UHMWPE powder into a hopper of said counter-rotating twin-screw extruder;—transporting said UHMWPE powder from said hopper through said counter-rotating twin-screw extruder to an outlet of said counter-rotating twin-screw extruder;—further transporting said UHMWPE powder from said outlet of said counter-rotating twin-screw extruder to an entrance of a heat-controlled tooling system for defining the shape of UHMWPE products;—withdrawing said UHMWPE products from an outlet of said heat-controlled tooling system.

Disclosed are cable types, including a type THHN cable, the cable types having a reduced surface coefficient of friction, and the method of manufacture thereof, in which the central conductor core and insulating layer are surrounded by a material containing nylon or thermosetting resin. A silicone based pulling lubricant for said cable, or alternatively, erucamide or stearyl erucamide for small cable gauge wire, is incorporated, by alternate methods, with the resin material from which the outer sheath is extruded, and is effective to reduce the required pulling force between the formed cable and a conduit during installation.

Low permeation fuel hose is provided comprising an outer cover layer prepared from a composition comprising a polyvinyl chloride (PVC), a thermoplastic copolyester elastomer and, optionally, a thermoplastic polyurethane (TPU), wherein the hose exhibits improved low and high temperature performance compared to conventional fuel hoses having an outer layer consisting of industrial grade PVC.

Methods for startup of an extruder include (a) initiating feed of a polymer resin to the extruder using a volumetric feeder such that, where the melt index of the polymer resin is less than 10 g/10 min (ASTM D1238 at 230° C., 2.16 kg), the volumetric feeder is operated at a first volumetric feeder speed; or (b) initiating feed of a polymer resin to the extruder using the volumetric feeder such that, where the melt index of the polymer resin is 10 g/10 min or greater, the volumetric feeder is operated at a second volumetric feeder speed greater than the first. The first volumetric feeder speed can range from about 20% to about 25% of the volumetric feeder max speed; and the second volumetric feeder speed can range from about 30% to about 35% of the volumetric feeder max speed.