A PROCESS FOR CONTROLLING WATER TREES

Abstract: A process for controlling the length of water trees in a copolymer of ethylene and one or more alpha-olefins having 3 to 12 carbon atoms, which will be exposed to moisture, comprising selecting a copolymer with (1) a density in the range of 0.860 to 0.930 gram per cubic centimeter and (2) a melt flow ratio having at least about a value determined by the following formula: 2.7183 to the power of {[(6.184 times the density selected from the range set forth above) minus 5.21] divided by 0.08898}.

Description: A PROCESS FOR CONTROLLING WATER TREES Technical Field This invention relates to a process for controlling water trees in a power cable. Background Information A typical electric power cable generally comprises one or more conductors, which form a cable core that is surrounded by several layers of polymeric material including a first semiconducting shield layer, an insulating layer, a second semiconducting shield layer, a metallic tape or wire shield, and a jacket. These insulated cables are known to suffer from shortened life when installed in an environment where the insulation is exposed to water, e.g., underground or locations of high humidity. The shortened life has been attributed to the formation of water trees, which occur when an organic polymeric material is subjected to an electrical field over a long period of time in the presence of water in liquid or vapor form. The net result is a reduction in the dielectric properties of the insulation. Many solutions have been proposed for increasing the resistance of organic insulating materials used in cables to degradation by water treeing, i.e., controlling the length of water trees. One solution involves the addition of polyethylene glycol (PEG), as a water tree growth inhibitor, to a heterogeneous low density polyethylene such as described in United States Patents 4,305,849; 4,612,139; and 4,812, 505. The addition of PEG to polyethylene, however, presents certain problems, particularly in the area of long term heat stability and in compatibility with the host polymer. The latter is addressed by selecting a PEG of a particular molecular weight (weight average molecular weight); however, compounding conditions may still produce a low molecular weight fraction. The former requires the addition of a high level of certain heat stabilizers, which cause staining of the composition. The color (or stain) produced and the reduction in crosslinking, both due to the high level of heat stabilizer, lead to some commercial difficulties. The optimum would be a cable containing a polymer which exhibits commercially acceptable water tree retardance without the need for water tree retardant additives. Industry has not, however, found cables, which meet this criteria. Disclosure of the Invention An object of this invention, therefore, is to provide a process for improving the water tree retardance of a polymer, which is used to insulate power cable, without the use of tree retardant additives. Other objects and advantages will become apparent hereinafter. According to the invention, a process for controlling the length of water trees in a copolymer of ethylene and one or more alpha-olefins having 3 to 12 carbon atoms, which will be exposed to moisture, has been discovered which meets the above object. The process comprises selecting a copolymer with (1) a density in the range of 0.860 to 0.930 gram per cubic centimeter and (2) a melt flow ratio having at least about a value determined by the following formula: 2.7183 to the power of {[(6.184 times the density selected from the range set forth above) minus 5.21] divided by 0.08898}. Description of the Preferred Embodiment (s) Polyethylene, as that term is used herein, is a copolymer of ethylene and a minor proportion of one or more alpha-olefins having 3 to 12 carbon atoms, and preferably 4 to 8 carbon atoms, and, optionally, a diene, or a mixture of such copolymers. The mixture can be a mechanical blend or an in situ blend. Examples of the alpha- olefins are propylene, 1-butene, 1-hexene, 4-methyl-l-pentene, and 1- octene. The polyethylene can be homogeneous or heterogeneous, and can have long chain branching. The homogeneous polyethylenes usually have a polydispersity (Mw/Mn) in the range of about 1.5 to about 3.5 and an essentially uniform comonomer distribution, and are characterized by single and relatively low DSC melting points. The heterogeneous polyethylenes, on the other hand, have a polydispersity (Mw/Mn) greater than 3.5 and do not have a uniform comonomer distribution. Mw is defined as weight average molecular weight and Mn is defined as number average molecular weight. The polyethylenes of interest here can have a density in the range of 0.860 to 0.930 gram per cubic centimeter, and preferably have a density in the range of 0.880 to 0.920 gram per cubic centimeter. Once the density is selected the melt flow ratio is determined according to the formula set forth above, i.e., a melt flow ratio having at least about a value determined by the following formula: 2.7183 to the power of {[(6.184 times a density selected from the range set forth above) minus 5.21] divided by 0.08898}. The preferred minimum for metallocene catalyst systems is at least about 10 percent higher than for other transition metal catalyst systems such as Ziegler-Natta catalyst systems. It will be understood that the desired melt flow ratio provides the improved water tree resistance. The melt index can be in the range of about 0.1 to about 30 grams per 10 minutes, and is preferably in the range of about 0.5 to about 10 grams per 10 minutes. The polyethylenes can be produced by low pressure processes. They are preferably produced in the gas phase, but they can also be produced in the liquid phase in solutions or slurries by conventional techniques. Low pressure processes are typically run at pressures below 1000 psi. Typical transition metal catalyst systems, which can be used to prepare these polyethylenes, are magnesium/titanium based catalyst systems, which can be exemplified by the catalyst system described in United States patent 4,302,565 (heterogeneous polyethylenes); vanadium based catalyst systems such as those described in United States patents 4,508,842 (heterogeneous polyethylenes) and 5,332,793; 5,342,907; and 5,410,003 (homogeneous polyethylenes); a chromium based catalyst system such as that described in United States patent 4,101,445; a metallocene catalyst system such as that described in United States patents 4,937,299 and 5,317,036 (homogeneous polyethylenes); or other transition metal catalyst systems. Many of these catalyst systems are often referred to as Ziegler-Natta catalyst systems. Catalyst systems, which use chromium or molybdenum oxides on silica-alumina supports, are also useful. Typical processes for preparing the polyethylenes are also described in the aforementioned patents. The various polyethylenes can include linear low density polyethylenes, very low density polyethylenes, and medium density polyethylenes. Thus, the copolymer having the desired density and melt flow ratio is prepared by conventional processes or selected from commercial polyethylenes, both in accordance with the formula set forth above. Density is measured by producing a plaque in accordance with ASTM D-1928, procedure C, and then testing "as is" via ASTM D-1505. The density is reported in gram per cubic centimeter. Melt Index (g/10 min) is determined under ASTM D-1238, Condition E. It is measured at 190 degrees C and reported as grams per 10 minutes. Flow Index is determined under ASTM D-1238, Condition F. It is measured at 190 degrees C at 10 times the weight used in the melt index test above. Melt flow ratio is the ratio of flow index to melt index. Conventional additives, which can be introduced into the polyethylene composition, are exemplified by antioxidants, coupling agents, ultraviolet absorbers or stabilizers, antistatic agents, pigments, dyes, nucleating agents, reinforcing fillers or polymer additives, slip agents, plasticizers, processing aids, lubricants, viscosity control agents, tackifiers, anti-blocking agents, surfactants, extender oils, metal deactivators, voltage stabilizers, flame retardant fillers and additives, crosslinking agents, boosters, and catalysts, and smoke suppressants. Fillers and additives can be added in amounts ranging from less than about OJ to more than about 200 parts by weight for each 100 parts by weight of the base resin, in this case, polyethylene. The use of carbon black in semiconductive layers is mentioned in United States Patent 4,857,232. Examples of antioxidants are: hindered phenols such as tetrakis[methylene(3,5-di-tert- butyl-4-hydroxyhydrocinnamate)]- methane, bis[(beta-(3,5-ditert-butyl-4-hydroxybenzyl)- methylcarboxyethyl)] sulphide, 4,4-thiobis(2-methyl-6-tert- butylphenol), 4,4-thiobis(2-tert-butyl-5-methylphenol), 2,2-thiobis(4- methyl-6-tert-butylphenol), and thiodiethylene bis(3,5-di-tert-butyl-4- hydroxy)hydrocinnamate; phosphites and phosphonites such as tris(2,4-di-tert-butylphenyl)phosphite and di-tert-butylphen l- phosphonite; thio compounds such as dilaurylthiodipropionate, dimyristylthiodipropionate, and distearylthiodipropionate; various siloxanes; and various amines such as polymerized 2,2,4-trimethyl-l,2- dihydroquinoline. Antioxidants can be used in amounts of about 0.1 to about 5 parts by weight per 100 parts by weight of polyethylene. The resins in the composition 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. They can also be crosslinked by irradiation. Suitable crosslinking 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 and comonomer(s) with an ethylenically unsaturated compound having one or more -Si(OR)o groups such as vinyl trimethoxysilane, vinyltriethoxysilane, and gamma- methacryloxypropyltrimethoxysilane or grafting these silane compounds to the either 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, dioctyltin maleate, dibutyltin diacetate, stannous acetate, lead naphthenate, and zinc caprylate. Dibutyltin dilaurate is preferred. Examples of hydrolyzable copolymers and hydrolyzable grafted copolymers are ethylene/comonomer/ vinyltrimethoxy silane copolymer, ethylene/comonomer/gamma- methacryloxypropyltrimethoxy silane copolymer, vinyltrimethoxy silane grafted ethylene/comonomer copolymer, vinyltrimethoxy silane grafted linear low density ethylene/1-butene copolymer, and vinyltrimethoxy silane grafted low density polyethylene. Cables using the copolymer provided by this invention can be prepared in various types of extruders, e.g., single or twin screw types. Compounding can be effected in the extruder or prior to extrusion in a conventional mixer such as a Brabender™ mixer ; a Banbury™ mixer; or the twin screw extruder. A description of a conventional extruder can be found in United States patent 4,857,600. A typical extruder has a hopper at its upstream end and a die at its downstream end. The hopper feeds into a barrel, which contains a screw. At the downstream end, between the end of the screw and the die, is a screen pack and a breaker plate. The screw portion of the extruder is considered to be divided up into three sections, the feed section, the compression section, and the metering section, and two zones, the back heat zone and the front heat zone, the sections and zones running from upstream to downstream. In the alternative, there can be multiple heating zones (more than two) along the axis running from upstream to downstream. If it has more than one barrel, the barrels are connected in series. The length to diameter ratio of each barrel is in the range of about 15:1 to about 30:1. In wire coating, where the material is crosslinked after extrusion, the die of the crosshead feeds directly into a heating zone, and this zone can be maintained at a temperature in the range of about 100 degrees C to about 260 degrees C, and preferably in the range of about 120 degrees C to about 220 degrees C. The advantages of the process of the invention lies in the much improved water tree growth rate of the insulating or semiconducting layer in which the copolymer is used, i.e., matching water tree growth rates of tree retardant additive containing compositions, and the freedom from tree retardant additives. The composition, which includes the copolymer, is useful in low, medium, and high voltage applications. The term "surrounded" as it applies to a substrate being surrounded by an insulating composition, jacketing material, or other cable layer is considered to include extruding around the substrate; coating the substrate; or wrapping around the substrate as is well known by those skilled in the art. The substrate can include, for example, a core including a conductor or a bundle of conductors, or various underlying cable layers as noted above. All molecular weights mentioned in this specification are weight average molecular weights unless otherwise designated. The patents and patent application mentioned in this specification are incorporated by reference herein. The invention is illustrated by the following examples. Examples 1 to 8 The resins of examples 1, 3, 5, 6, and 7 are made with a spray dried magnesium/titanium based catalyst as described in United States patent 5,290,745. The resin of example 2 is a compounded mixture of the resins made by a conventional Ziegler-Natta catalyst and a resin made by a metallocene catalyst. The resin of example 5 is made with a chromium based catalyst as described in United States patent application serial number 928,734 filed on September 12, 1997. A density is selected and the minimum melt flow ratio are determined in accordance with the formulas set forth above. Polymerization conditions are set to obtain the density and minimum melt flow ratio. The resin of example 8 is a crosslinked low density polyethylene made by a high pressure process. It is combined with a water tree retardant additive and an antioxidant to provide a high pressure low density polyethylene (HP-LDPE) composition. The 8 resins are tested for water tree retardance under ASTM D-6097-97 at 5 kiloVolts and 1 kiloHerz for 30 days under 0.01 Normal salt (sodium chloride) water. The water tree retardance is assessed by determining the average water tree length in millimeters; the shorter tree length indicates the better tree retardance. The standard deviation of tree measurement is about 0.05 millimeter. Density is measured by a density column in accordance with ASTM D-792. The standard deviation of density measurement is 0.003 gram per cubic centimeter. Melt index and melt flow ratio are defined above. The standard deviations of melt index and melt flow ratio are 10 percent and 20 percent, respectively. Variables and result are reported in Table I: - li ¬ lt will be observed that examples 1 and 2 meet the MFR criteria at a given density. Thus, the water tree lengths are substantially lower than those of examples 3 to 7, and better than the crosslinked HP- LDPE composition of example 8, which contains a water tree retardant additive. Table II provides a calculated minimum melt flow ratio for each density to achieve good tree retardancy Table II density minimum (g/cc) MFR 0.860 3.6 0.865 5.0 0.870 7.1 0.875 10J 0.880 14.3 0.885 20.2 0.890 28.7 0.895 40.6 0.900 57.5 0.905 81.4 0.910 115.2 0.915 163.1 0.920 231.0 0.925 327.0 0.930 463.0

Claims: Claims 1. A process for controlling the length of water trees in a copolymer of ethylene and one or more alpha-olefins having 3 to 12 carbon atoms, which will be exposed to moisture, comprising selecting a copolymer with (1) a density in the range of 0.860 to 0.930 gram per cubic centimeter and (2) a melt flow ratio having at least about a value determined by the following formula: 2.7183 to the power of {[(6.184 times the density selected from the range set forth above) minus 5.21] divided by 0.08898}. 2. The process defined in claim 1 wherein the density is selected from the range of 0.880 to 0.920 gram per cubic centimeter. 3. The process defined in claim 1 wherein the alpha-olefin has 4 to 8 carbon atoms. 4. The process defined in claim 1 wherein the alpha-olefin is 1-butene, 1-hexene, or 1-octene. 5. The process defined in claim 1 wherein the alpha-olefin is a mixture of 1- butene and 1-hexene or 1-butene and 1-octene. 6. The process defined in claim 1 wherein the selected copolymer is extruded around an electrical conductor or a core of electrical conductors to form a cable. 7. A process for controlling the length of water trees in a cable, which will be exposed to moisture comprising selecting a copolymer of ethylene and one or more alpha-olefins having 4 to 8 carbon atoms with (1) a density in the range of 0.880 to 0.920 gram per cubic centimeter and (2) a melt flow ratio having at least about a value determined by the following formula: 2.7183 to the power of {[(6.184 times the density selected from the range set forth above) minus 5.21] divided by 0.08898} and extruding the selected copolymer around an electrical conductor or a core of electrical conductors to form a cable. 8. The process defined in claim 7 wherein the alpha-olefin is 1-butene, 1-hexene, or 1-octene. 9. The process defined in claim7 wherein the alpha-olefin is a mixture of 1- butene and 1-hexene or 1-butene and 1-octene.

Inventors: JOW JINDER, JOW, JINDER
Applicants: UNION CARBIDE CHEM PLASTIC, UNION CARBIDE CHEMICALS & PLASTICS TECHNOLOGY CORPORATION
Application year: 1999
Main classification: H01B7
IPC codes: C08L23, H01B7