Process for the extrusion of low density polyethylene

Abstract: A process for extrusion comprising: (i) blending low density polyethylene having a density equal to or less than about 0.915 gram per cubic centimeter with a liquid hydrocarbon oil in an amount of about 5 to about 30 parts by weight of oil per 100 parts by weight of low density polyethylene; and (ii) extruding the blend.

Description: This invention relates to a process for the extrusion of polyethylene, which has a density equal to or less than about 0.915 gram per cubic centimetre (low density polyethylene). The low modulus of commercial rubbers such as ethylene/propylene copolymers (EPM) and plasticized polyvinyl chloride (PVC) make these rubbers very useful in such applications as hose and tubing. In addition, PVC finds extensive use in film and other applications in which compliance with Food & Drug Administration (FDA) requirements is necessary. Because of its higher modulus, polyethylene including low density polyethylene has found limited utility in the aforementioned applications even though it has other advantageous qualities such as toughness and chemical resistance. DE-A-3 630 682 discloses an extrusion process comprising blending low density polyethylene with an additive comprising corn oil, polybutene, stearate, petroleum resin and extruding the blend. The product may be used as an improved food wrapping film. An object of this invention, therefore, is to provide a process which will not only serf to extrude the polyethylene into, for example, hose, tubing, and film but will reduce its modulus to a level at which it will be competitive with its EPM and PVC counterparts. Other objects and advantages will become hereinafter. According to the present invention, there is provided an extrusion process comprising blending a copolymer of ethylene and a minor amount of one or more alpha-olefins having at least 4 carbon atoms, said copolymer having a density equal to or less than 0.915 gram per cubic centimetre; a molecular weight in the range of 150,000 to 300,000; and a melt index in the range of from 0.05 to 1.5 gram per 10 minutes as determined under ASTM D-1238, Condition E, with a liquid hydrocarbon oil having a viscosity of at least 2500 SUS (Saybolt Universal Seconds) at 37.8°C in an amount of 5 to 20 parts by weight of oil per 100 parts by weight of copolymer; and extruding the blend. The copolymer of ethylene and an alpha olefin having less than 4 carbon atoms is termed low density polyethylene herein. The copolymer comprises a minor amount of one or more alpha-olefins having at least 4 carbon atoms, and preferably having 4 to 8 carbon atoms. The low density polyethylene can be prepared by the process described in EP-A-No.0 120 501 published on October 3, 1984. The low density polyethylene can be in the form of porous granules or pellets. The porous granules of the low density polyethylene generally have a diameter in the range of about 25 micrometres to about 2500 micrometres. Regardless of its form, the low density polyethylene has a density equal to or less than about 0.915 gram per cubic centimetre, preferably in the range of 0.870 to 0.915 gram per cubic centimetre. If the low density polyethylene is in pallet form, the blending step is carried out with the polyethylene in the molten state. The molecular weight of the low density polyethylene can be in the range of 150,000 to 300,000 and is preferably in the range of 150,000 to 250,000. Thus, the melt index is preferably in the range of 0.1 to 1.5 grams per 10 minutes. Melt index is determined under ASTM D-1238, Condition E. It is measured at 190 o C and reported as grams per 10 minutes. The portion of the copolymer attributed to the alpha-olefin comonomers can be in the range of 5 to 50 percent by weight based on the weight of the copolymer and is preferably in the range of 10 to 30 percent by weight based on the weight of the copolymer. The balance of the copolymer is based on ethylene. The preferred comonomers are 1-butene, 1-hexene, and 1-octene. The liquid hydrocarbon oil is generally a petroleum derived processing oil commonly used in the compounding and extruding of rubber compositions. The major oil type present in any of these oils can be aromatic or aliphatic. Examples of these liquid hydrocarbon oils are paraffin oils, naphthenic oils, and mineral oils. Liquid polybutene can also be included among the examples. Mixtures of the various oils can be used, if desired. The oils can have preferably a viscosity upto 3000 SUS at 100°F (37.8°C). In the case of porous granular low density polyethylene, the oils are usually dry blended with the polyethylene prior to extrusion (preblending), but the oil and resin can be blended in the extruder itself, if desired. Preblending is preferable, however, since it shortens the mixing time and is a key factor in achieving uniform distribution of the oil in the resin. In the case of pelletized low density polyethylene, the low density polyethylene is in the molten state when the blending is initiated. The amount of oil introduced into the blend of is in the range of 5 to 20 parts by weight of oil per 100 parts by weight of low density polyethylene. The low density polyethylene mixes readily with the oil without the use of heat except, as noted, when it is in pelletized form. Mixers and extruders useful in carrying out the process of the invention are conventional off-the-shelf equipment. A typical extruder is described in US patent 4,857,600. Mixers, which can be used to blend the resin and the oil, are Banbury or other internal mixers, two roll mills, or Baker Perkins or similar sigma blade mixers, As noted, extruders can also be used to mix the resin and the oil. Advantages of the blend are improved processability in the extruder, e.g., a fractional melt index will display the extrusion behavior of a 1 to 2 melt index resin; avoidance of bleeding when oil is used in preferred amounts; extrusion can be conducted under less pressure and amperage without sacrificing production rates; hose and tubing made from the combination of high molecular weight low density polyethylene and oil, when compared to plasticized PVC, have a lower brittle point, a higher softening temperature, and better chemical and environmental resistance; and, with respect to extruded film, the oil modified low density polyethylene displays improved puncture dart drop and clarity. The production of film from the oil modified low density polyethylene is particularly useful in the preparation of products, which must meet FDA requirements. Thus, a low density polyethylene with, for example, a 0.910 g/cc density, which meets FDA requirements, can be blended with an oil, which also meets FDA requirements. The result is a product which has the properties of a low density polyethylene having a lower density than 0.910 g/cc and still meets the FDA requirements. Polyethylenes, in general, display poor compression set and resiliency. Compression set, which is determined under ASTM-D-395-85, is defined as the amount (in percent) by which a standard test piece fails to return to its original thickness after being subjected to a standard compression load for a fixed period of time. The better the compression set, i.e., the lower the percent, the more resilient the polymer. One more advantage of the oil modified low density polyethylene is its improved compression set relative to the unmodified low density polyethylene. The compression set is further improved by crosslinking the oil modified low density polyethylene. Crosslinking is accomplished by using conventional techniques. The oil modified low density polyethylene can be crosslinked by adding a crosslinking agent to the composition or by making the resin hydrolyzable, which is accomplished by adding hydrolyzable groups, such as -Si(OR)₃ wherein R is a hydrocarbyl radical, to the resin structure through copolymerization or grafting. Suitable cross linking agents are organic peroxides such as dicumyl peroxide; 2,5-dimethyl-2,5-di(t-butylperoxy)hexane; t-butyl cumyl peroxide; and 2,5-dimethyl-2,5-di(t-butylperoxy)hexane-3. Dicumyl peroxide is preferred. Hydrolyzable groups can be added, for example, by copolymerizing ethylene with an ethylenically unsaturated compound having one or more -Si(OR)₃ groups such as vinyltrimethoxysilane, vinyltriethoxysilane, and gammamethacryloxypropyl-trimethoxysilane or by grafting these silane compounds to the resin in the presence of the aforementioned organic peroxides. The hydrolyzable resins are then crosslinked by moisture in the presence of a silanol condensation catalyst such as dibutyltin dilaurate, dibutyltin dlacetate, stannous acetate, lead naphthenane, and zinc caprylate. Dibutyltin dilaurate is preferred. Conventional additives can be added to the oil modified low density polyethylene during the preblending step and/or the extrusion step. The amount of additive is usually in the range of 0.01 to 60 percent by weight based on the weight of the resin. Useful additives are antioxidants, ultraviolet absorbers, antistatic agents, pigments, dyes, fillers, slip agents, fire retardants, plasticizers, processing aids, lubricants, stabilizers, smoke inhibitors, viscosity control agents, vulcanizing agents, crosslinking agents, crosslinking catalysts, and crosslinking boosters. The invention is illustrated by the following examples. Examples 1 to 4 Porous granular low density polyethylene having a density of 0.910 gram per cubic centimeter and prepared using the catalyst and process described in European Patent Application 0 120 501, referred to above, is used in the examples. The comonomer is 1-hexene. The oil is a paraffin oil having a viscosity of 2540 SUS at 37.8°C (100°F). The low density polyethylene and the oil are mixed in a ribbon blender for 15 minutes. The mixture is then pelletized, and the pellets are extruded in an extruder to provide a film having a thickness of 0.025mm (0.001 inch). The extruder operates at 60 revolutions per minute, the die gap (or die diameter) in the extruder is 0.025mm (0.001 inch); and the BUR is 2:1. The BUR is the blow-up ratio. This is the ratio of die diameter to bubble diameter. The bubble diameter is 2 X layflat/pi. The "layflat" refers to the width of the flattened bubble. It is found that the modulus of the oil modified low density polyethylene is approximately the same as otherwise equivalent commercial EPM's and PVC's. Variables and conditions are set forth in the Table:

Claims: An extrusion process comprising: (i) blending a copolymer of ethylene and a minor amount of one or more alpha-olefins having at least 4 carbon atoms, said copolymer having a density equal to or less than 0.915 gram per cubic centimetre; a molecular weight in the range of 150,000 to 300,000; and a melt index in the range of from 0.05 to 1.5 grams per 10 minutes as determined under ASTM D-1238, Condition E, with a liquid hydrocarbon oil having a viscosity of at least 2500 SUS (Saybolt Universal Seconds) at 37.8°C in an amount of 5 to 20 parts by weight of oil per 100 parts by weight of copolymer; and (ii) extruding the blend. A process as claimed in claim 1 wherein the copolymer is in a porous granular form. A process as claimed in claim 1 or claim 2 wherein the blending is conducted with the copolymer in the molten state. A process as claimed in any one of the preceding claims wherein the density of the copolymer is above about 0.870 gram per cubic centimetre. A process as claimed in any one of the preceding claims wherein the molecular weight is in the range of from 150,000 to 250,000. A process as claimed in any one of the preceding claims wherein the melt index of the copolymer is in the range of from 0.1 to 1.5 grams per 10 minutes. A process as claimed in any one of the preceding claims wherein the oil is a paraffin oil, a naphthenic oil, a mineral oil, polybutene, or a mixture of two or more of such oils. A process as claimed in any one of the preceding claims wherein the copolymer and the oil are blended in an extruder. A process as claimed in any one of the preceding claims wherein a cross linking agent is blended with the copolymer or incorporated into the mixture of copolymer and oil during extrusion, and cross linking of the copolymer is effected either during or after extrusion. Process as claimed in any one of the preceding claims for producing an extruded product in the form of a hose, tubing or film.

Inventors: RIFI MAHMOUD RASHAD, RIFI, MAHMOUD RASHAD
Applicants: UNION CARBIDE CHEM PLASTIC, UNION CARBIDE CHEMICALS AND PLASTICS COMPANY, INC.
Application year: 1991
Main classification: C08L23
IPC codes: C08L91, C08J5, C08L23, C08K5, B29C47, B29C35, B29L7, B29K105, B29K23